Continuous production equipment for bis (chlorosulfonyl) imide

Abstract

The invention discloses continuous production equipment for bis (chlorosulfonyl) imide, and belongs to the technical field of chemical equipment, the continuous production equipment comprises a feeding process, a synthesis process, a purification process and a tail gas treatment process, a feeding system of the feeding process realizes feeding of thionyl chloride, chlorosulfonic acid and sulfamic acid, a continuous reaction device of the synthesis process can synthesize bis (chlorosulfonyl) imide, and the tail gas treatment process is performed. The distillation device in the purification process can separate out thionyl chloride and chlorosulfonic acid in the material and purify bis (chlorosulfonyl) imide, and the tail gas treatment system in the tail gas treatment process can purify tail gas discharged by the continuous reaction device and the distillation device and recover hydrogen chloride and sulfur dioxide in the tail gas, so that standard emission of the tail gas is realized. By adopting the method, the continuous production of the bis (chlorosulfonyl) imide can be realized, the production efficiency and the production capacity are improved, the waste of raw materials is reduced, and the production cost is reduced.

Description

Technical Field

[0001] The invention belongs to the technical field of chemical equipment, and in particular relates to a continuous production device for bischlorosulfonyl imide. Background Art

[0002] Bischlorosulfonyl imide is a common organic synthesis intermediate, widely used in pesticides, medicines, dyes and other fields, and has high economic value. Bischlorosulfonyl imide is synthesized using thionyl chloride, chlorosulfonic acid and aminosulfonic acid as raw materials. The reaction process is as follows: 2SOCl2+ClSO3H+NH2SO3H Cl2HNO4S2+2SO2 +3HCl .

[0003] In the production process of bischlorosulfonyl imide, thionyl chloride, aminosulfonic acid and chlorosulfonic acid need to be mixed and reacted at a suitable temperature to obtain bischlorosulfonyl imide.

[0004] The existing processes are mostly produced in batches, the material turnover is cumbersome and discontinuous, and the exhaust gas emitted by each process cannot be treated in time and is discharged into the atmosphere, causing environmental pollution; the intermediate products cannot be fully recycled and reused, resulting in a waste of resources. This production method cannot form continuous production and has the defects of many production steps, high production costs, low production efficiency and production volume. Summary of the invention

[0005] In order to solve the above problems, the present invention provides a continuous production device for bischlorosulfonyl imide.

[0006] To achieve the above purpose, the technical solution adopted by the present invention is as follows: A bischlorosulfonyl imide continuous production device comprises a feeding process, a synthesis process, a purification process and a tail gas treatment process, wherein the feeding system of the feeding process is used to realize the feeding of thionyl chloride, chlorosulfonic acid and aminosulfonic acid, the continuous reaction device of the synthesis process is used to synthesize bischlorosulfonyl imide, the distillation device of the purification process is used to separate thionyl chloride and chlorosulfonic acid in the material and purify bischlorosulfonyl imide, the tail gas treatment system of the tail gas treatment process is used to purify the tail gas discharged from the continuous reaction device and the distillation device, the feeding system is used to continuously feed into a reaction tank of the continuous reaction device, the material discharged from the continuous reaction device enters the distillation device through a conveying component to complete the distillation purification of bischlorosulfonyl imide, and the tail gas treatment system can recover hydrogen chloride and sulfur dioxide in the tail gas.

[0007] Furthermore, the feeding system includes a thionyl chloride storage tank, a chlorosulfonic acid storage tank, a batching tank and a chemical tank. The thionyl chloride in the thionyl chloride storage tank is transported to the batching tank through a conveying component. A hanger is provided above the batching tank. The hanger is used to lift the aminosulfonic acid packaging bag to the top of the batching tank and add aminosulfonic acid into the batching tank; the top of the batching tank is connected to a compressed air pipe, and the compressed air in the compressed air pipe can continuously press the mixed liquid in the batching tank into the chemical tank through a discharge pipe; the chemical tank is connected to the reaction tank of the synthesis process through the discharge pipe, and the chlorosulfonic acid storage tank is connected to different areas in the reaction tank through a distribution and conveying pipeline, which is used to drip chlorosulfonic acid into the reaction tank in different areas; agitators are provided in the batching tank and the chemical tank, and exhaust pipes are provided on the tops of the chemical tank and the reaction tank, and heating layers are provided on the outer walls.

[0008] Furthermore, the distribution and delivery pipeline includes a feed main pipe and multiple feed branches connected in parallel therewith, the feed branches are provided with a flow meter and a control valve connected to the central console, and the outlets of the multiple feed branches are sequentially connected to the chlorosulfonic acid feed ports on the top wall of each area in the reaction tank; the feed main pipe is connected to the bottom outlet of the chlorosulfonic acid storage tank through a magnetic pump.

[0009] Furthermore, the continuous reaction device includes a horizontally placed reaction tank and an insulation tank, the feed port of the reaction tank is connected to the discharge pipe of the material tank outlet, and the discharge port of the reaction tank is connected to the insulation tank through a conveying component; the reaction tank and the insulation tank are sequentially divided into a plurality of interconnected areas, each area is provided with an agitator, the top of each area of ​​the reaction tank is provided with a chlorosulfonic acid feed port, and the outer walls of the reaction tank and the insulation tank are provided with a heating layer; the discharge port of the insulation tank is connected to the distillation device of the purification process; the tops of the reaction tank and the insulation tank are provided with an exhaust pipe and a condensation reflux component.

[0010] Furthermore, the chemical tank, reaction tank and insulation tank are all horizontal tank bodies with a heating layer, and a plurality of baffles and a plurality of deflectors are arranged at intervals along the length direction of the chemical tank. The baffles and the baffles are arranged in a staggered manner, and the upper end of the baffle is connected to the top wall of the chemical tank, and the lower end is provided with a gap with the bottom of the chemical tank, and the lower end of the baffle is connected to the bottom of the chemical tank, and the upper end is provided with a gap with the top wall of the chemical tank; the chemical tank is divided into several areas by baffles and baffles, each area is provided with a thermometer and an agitator, and the top of each area is provided with an exhaust pipe; the internal structure of the reaction tank and the insulation tank is the same as the internal structure of the chemical tank, and the top of each area of ​​the reaction tank is provided with a chlorosulfonic acid feed port, and the bottom of the chemical tank, the reaction tank and the insulation tank are provided with a discharge pipe.

[0011] Furthermore, the condensation reflux component includes a condenser and a low-temperature heat exchanger, the multiple exhaust pipes on the top of the reaction tank and the insulation tank are respectively connected to the multiple condensers, the bottom discharge pipes of the multiple condensers are respectively connected to the top of the reaction tank and the insulation tank, the top air outlet of the condenser is connected to the exhaust main pipe; the exhaust main pipe is connected to the lower feed port of the low-temperature heat exchanger, the bottom outlet of the low-temperature heat exchanger is connected to the top of the reaction tank, and the top air outlet of the low-temperature heat exchanger is connected to the tail gas pipe; the top air outlets of the condenser and the low-temperature heat exchanger are both provided with thermometers.

[0012] Furthermore, the distillation device includes a crude product tank I, a primary distillation and separation component, a crude product tank II and a secondary distillation and separation component. The crude product tank I is connected to the outlet of the insulation tank and is used to accommodate materials discharged from the synthesis process; the discharge port of the crude product tank I is connected to the feed port of the primary distillation and separation component through a primary conveying component, and the primary distillation and separation component is used to separate the thionyl chloride and chlorosulfonic acid in the material in sequence and store them in the thionyl chloride turnover tank and the chlorosulfonic acid turnover tank; the material of the primary distillation and separation component enters the crude product tank II, and the crude product tank II is connected to the secondary distillation and separation component through a secondary conveying component, and the secondary distillation and separation component is used to separate the finished product bischlorosulfonyl imide and store it in the finished product tank.

[0013] Furthermore, the primary distillation and separation component includes a primary distiller, a primary separator and a primary distillation heat exchanger, the top of the primary distiller is connected to the bottom of the primary separator, the top side of the primary distiller is provided with a material inlet connected to the primary conveying component, and the bottom is provided with a discharge port connected to the magnetic pump, the outlet of the magnetic pump is respectively connected to the reflux pipe and the feed pipe, the feed pipe is connected to the crude product II tank, and the other end of the reflux pipe is connected to the top of the primary separator; the lower part of the primary separator is connected to the bottom of the primary distillation heat exchanger, the top air outlet of the primary distillation heat exchanger is connected to the condenser, the bottom discharge port of the condenser is connected to the thionyl chloride turnover tank, the bottom discharge pipe of the condenser is connected to the chlorosulfonic acid turnover tank through a bypass pipe, and the air outlet of the condenser is connected to the tail gas pipe.

[0014] Furthermore, the secondary distillation separation component includes a secondary distiller, a secondary separator and a secondary distillation heat exchanger. The top of the secondary distiller is provided with a connection to the bottom of the secondary separator, the top side of the secondary distiller is provided with a material inlet connected to the secondary conveying component, and the bottom is provided with a discharge port connected to the magnetic pump, and the outlet of the magnetic pump is connected to the top of the secondary separator through a circulation pipe; the lower part of the secondary separator is connected to the bottom of the secondary distillation heat exchanger, the top air outlet of the secondary distillation heat exchanger is connected to the top air inlet pipe of the condenser III, and the air inlet pipe is provided with a thermometer and a pressure sensor; the bottom discharge port of the condenser III is connected to the finished product tank, and the exhaust port of the finished product tank is connected to the vacuum pump II.

[0015] Furthermore, the exhaust gas treatment system includes a buffer tank for accommodating exhaust gas, a discharge valve is provided at the bottom of the buffer tank, an upper air outlet of the buffer tank is connected to the top air inlet of the falling film absorber through an exhaust pipe, the bottom outlet of the falling film absorber is connected to a circulation tank for accommodating hydrochloric acid, the circulation tank is respectively connected to the upper liquid inlet of the falling film absorber and the hydrochloric acid tank through a circulation pump, and the lower air outlet of the falling film absorber is connected to the lower part of the packing tower; the bottom of the packing tower is connected to the circulation tank, the top exhaust port of the packing tower is connected to the lower air inlet of the drying tower, and the top exhaust port of the drying tower is connected to the subsequent sulfur dioxide conversion tower; the absorption medium in the falling film absorber and the packing tower is water, and the drying medium in the drying tower is concentrated sulfuric acid.

[0016] Compared with the prior art, the present invention has the following technical advances: The present invention has a feeding process, a synthesis process and a purification process connected in sequence through pipelines, realizes continuous feeding of thionyl chloride, chlorosulfonic acid and aminosulfonic acid through a feeding system, synthesizes bischlorosulfonyl imide in a continuous reaction device, separates thionyl chloride and chlorosulfonic acid in the material through a distillation device for recycling and reusing, and realizes purification of bischlorosulfonyl imide; finally, the tail gas discharged from the continuous reaction device and the distillation device is purified through a tail gas treatment system to achieve standard emission of tail gas. The present invention can realize continuous production of bischlorosulfonyl imide, improve production efficiency and production volume, reduce raw material waste, and reduce production cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] The accompanying drawings are used to provide further understanding of the present invention and constitute a part of the specification. They are used to explain the present invention together with the embodiments of the present invention and do not constitute a limitation of the present invention.

[0018] In the attached picture: Figure 1 A flow chart of a continuous production device for bis(chlorosulfonyl)imide provided in an embodiment of the present invention; Figure 2It is a structural schematic diagram of a feeding system in an embodiment of the present invention; Figure 3 This is a diagram of the internal structure of the chemical tank in an embodiment of the present invention; Figure 4 This is a schematic diagram of the structure of a continuous reaction device in an embodiment of the present invention; Figure 5 It is a structural schematic diagram of a distillation apparatus in an embodiment of the present invention; Figure 6 A schematic diagram of the structure of an exhaust gas treatment system in an embodiment of the present invention; In the figure: 1-magnetic pump; 2-condenser; 3-low temperature heat exchanger; 4-exhaust main pipe; 5-baffle; 6-baffle; 7-discharge pipe; 8-exhaust pipe; 9-control valve; 10-pressure sensor; 11-thermometer; 12-agitator; 13-liquid level meter; 14-flow meter; 101-sulfoxide chloride storage tank, 102-chlorosulfonic acid storage tank, 103-dosing tank, 104-chemical tank, 105-hanging device, 106-compressed air pipe, 107-gas phase condenser, 108-transport pump, 109-intermediate tank, 110-feed main pipe, 111-feed branch pipe; 201-reaction tank; 202-insulation tank; 301-crude product tank I; 302-crude product tank II; 303-thionyl chloride turnover tank; 304-chlorosulfonic acid turnover tank; 305-finished product tank; 307-primary separator; 308-primary distillation heat exchanger; 309-reflux pipe; 310-discharge pipe; 311-vacuum pump I; 312-bypass pipe; 313-secondary distiller; 314-secondary separator; 315-secondary distillation heat exchanger, 316-circulation pipe; 317-vacuum pump II; 21-condenser I; 22-condenser II; 23-condenser III; 401-buffer tank; 402-circulation pump; 403-hydrochloric acid tank; 404-drying tower; 405-return section; 406-water seal box; 407-primary alkali absorption tower; 408-secondary alkali absorption tower; 409-induced draft fan; 413-sulphuric acid tank; 414-heat exchanger; 415-fan; 416-hydrochloric acid pump; 410-falling film absorber, 411-first-stage falling film absorber, 412-second-stage falling film absorber; 420-circulation tank, 421-first-stage circulation tank, 422-second-stage circulation tank; 430-packed tower, 431-first-stage packed tower, 432-second-stage packed tower, 433-first-stage cache tank, 434-second-stage cache tank. DETAILED DESCRIPTION

[0019] The following specific embodiments may be combined with each other, and the same or similar concepts or processes may not be described in detail in some embodiments. The embodiments of the present invention will be described below in conjunction with the accompanying drawings.

[0020] like Figure 1 As shown, a continuous production equipment for bischlorosulfonyl imide includes a feeding process, a synthesis process, a purification process and a tail gas treatment process, wherein the feeding system of the feeding process is used to realize the feeding of thionyl chloride, chlorosulfonic acid and aminosulfonic acid, the continuous reaction device of the synthesis process is used to synthesize bischlorosulfonyl imide, the distillation device of the purification process is used to separate thionyl chloride and chlorosulfonic acid in the material and purify bischlorosulfonyl imide, the tail gas treatment system of the tail gas treatment process is used to purify the tail gas discharged from the continuous reaction device and the distillation device, the feeding system is used to continuously feed into the reaction tank of the continuous reaction device, the material discharged from the continuous reaction device enters the distillation device through the conveying component to complete the distillation and purification of bischlorosulfonyl imide, and the tail gas treatment system can recover hydrogen chloride and sulfur dioxide in the tail gas, the hydrogen chloride and water generate hydrochloric acid for standby use, and the sulfur dioxide is dried and reused later.

[0021] In a specific embodiment of the present invention, Figure 2 As shown, the feeding system includes a thionyl chloride storage tank 101, a chlorosulfonic acid storage tank 102, a batching tank 103 and a chemical tank 104. The thionyl chloride in the thionyl chloride storage tank 101 is transported to the batching tank 103 through a conveying assembly. A hanger 105 is provided above the batching tank 103. The hanger 105 is used to lift the aminosulfonic acid packaging bag to the top of the batching tank 103 and add aminosulfonic acid into the batching tank 103. The top of the batching tank 103 is connected to a compressed air pipe 106, and the compressed air pipe 106 is connected to the compressed air pipe 107. The compressed air in 6 can continuously press the mixed liquid in the batching tank 103 into the material tank 104 through the discharge pipe; the material tank 104 is connected to the reaction tank 201 of the synthesis process through the discharge pipe, and the chlorosulfonic acid storage tank 102 is connected to different areas in the reaction tank 201 through the distribution and delivery pipeline, which is used to drop chlorosulfonic acid into the reaction tank 201 in different areas; the batching tank 103 and the material tank 104 are both provided with a stirrer, and the tops of the material tank 104 and the reaction tank 201 are both provided with exhaust pipes, and the outer walls are both provided with heating layers.

[0022] During specific production, the outside of the thionyl chloride storage tank 101 is provided with a heat preservation sunscreen layer, the top exhaust pipe of the thionyl chloride storage tank 101 is connected to a gas phase condenser 107, and the gas phase condenser 107 is connected to a delivery pump 108, and the thionyl chloride storage tank 101 is fed by the delivery pump 108 and a feed pipe, and the outlet end of the feed pipe is close to the bottom of the thionyl chloride storage tank, and the delivery pump 108 can be connected to the discharge port of the tanker, which is convenient for unloading; the top of the thionyl chloride storage tank 101 is provided with a pressure sensor and a pressure relief valve linked thereto, and the thionyl chloride storage tank 101 and the gas phase condenser 107 outside thereof are provided with a liquid level gauge. The outer wall of the gas phase condenser is provided with a cooling medium inlet and outlet at the same time, and the thionyl chloride gas passing through can be cooled down and cooled. In view of the fact that thionyl chloride is a volatile liquid, the volatilized thionyl chloride can be cooled down and condensed by a gas phase condenser to avoid waste caused by volatilization.

[0023] The conveying assembly includes a magnetic pump 1 and a conveying pipe, the inlet of the magnetic pump 1 is connected to the bottom outlet of the thionyl chloride storage tank 101, and the magnetic pump 1 is connected to the batching tank 103 through the conveying pipe. The magnetic pump is started to transport the thionyl chloride to the batching tank, and the aminosulfonic acid is hoisted into the batching tank and stirred with the thionyl chloride to be fully mixed.

[0024] Chlorosulfonic acid also has certain volatility at the same time, and the top exhaust pipe of chlorosulfonic acid storage tank 102 is connected to gas phase condenser 107, and described gas phase condenser 107 is connected to delivery pump 108, and feeds into chlorosulfonic acid storage tank 102 by delivery pump 108 and feed pipe; described chlorosulfonic acid storage tank 102 and the gas phase condenser 107 outside thereof are provided with liquid level gauge, and described chlorosulfonic acid storage tank 102 is provided with pressure sensor; The bottom of described chlorosulfonic acid storage tank 102 is connected to reactor 201 by magnetic pump 1 and delivery pipe and distribution delivery pipeline. Similarly, cooling medium import and export are provided on the outer wall of gas phase condenser at the same time, and the chlorosulfonic acid gas passed through can be cooled down and cooled down. Utilize gas phase condenser to cool down and condense the chlorosulfonic acid that volatilizes, avoid volatilization and cause waste.

[0025] As a preferred structure, an intermediate tank 109 is provided between the batching tank 103 and the chemical tank 104, the inlet end of the discharge pipe of the batching tank 103 extends downward close to the bottom of the batching tank 103, and the outlet end of the discharge pipe is connected to the top of the intermediate tank 109, the inlet end of the discharge pipe of the intermediate tank 109 extends downward close to the bottom of the intermediate tank 109, and the outlet end of the discharge pipe extends into the chemical tank 104 and close to the bottom of the chemical tank 104; the discharge pipe between the batching tank 103 and the intermediate tank 109, and the discharge pipe between the intermediate tank 109 and the chemical tank 104 are inclined downward along the flow direction of the feed liquid to avoid the material from being retained in the discharge pipe. After the aminosulfonic acid and thionyl chloride are mixed in the batching tank, they enter the intermediate tank for stirring again, which can achieve full mixing of the two raw materials.

[0026] In the specific design, the bottom discharge pipe of the chemical tank 104 is connected to the upper feed port of the reaction tank 201, and the middle discharge port of the chemical tank 104 is connected to the lower feed port of the reaction tank 201 to achieve sufficient mixing of the materials; the discharge port of the reaction tank 201 is provided with a delivery pump 108 for delivering the liquid to the distillation device of the distillation process for distillation.

[0027] like Figure 2 As shown, the distribution and delivery pipeline includes a feed main pipe 110 and a plurality of feed branches 111 connected in parallel therewith, the feed branches 111 are provided with a flow meter and a control valve connected to the central control console, and the outlets of the plurality of feed branches 111 are sequentially connected to the chlorosulfonic acid feed ports on the top wall of each area in the reaction tank 201; the feed main pipe 110 is connected to the bottom outlet of the chlorosulfonic acid storage tank 102 through a magnetic pump 1. The multi-stage control valve can be controlled by the central control console to start dripping chlorosulfonic acid, and the dripping speed is controlled according to the discharge speed of the material tank; and the amount of gas released from the reaction tank is recorded during the dripping process.

[0028] In a specific embodiment of the present invention, Figure 4 As shown, the continuous reaction device includes a horizontally placed reaction tank 201 and an insulation tank 202, the feed port of the reaction tank 201 is connected to the discharge pipe of the outlet of the material tank 104, and the discharge port of the reaction tank 201 is connected to the insulation tank 202 through a conveying component; the reaction tank 201 and the insulation tank 202 are sequentially divided into a plurality of interconnected areas, each area is provided with an agitator, the top of each area of ​​the reaction tank 201 is provided with a chlorosulfonic acid feed port, and the outer walls of the reaction tank 201 and the insulation tank 202 are provided with a heating layer; the discharge port of the insulation tank 202 is connected to the distillation device of the purification process; the tops of the reaction tank and the insulation tank are provided with exhaust pipes and condensation reflux components. The mixture of thionyl chloride and aminosulfonic acid reacts with chlorosulfonic acid added at multiple points in a reaction tank in a zoned manner; as the materials in the reaction tank react, the generated hydrogen chloride and sulfur dioxide are discharged from the exhaust pipe, and the thionyl chloride gas can be cooled by a condensation reflux component to flow back into the reaction tank to participate in the reaction again.

[0029] As a preferred structure, Figure 2-4As shown, the chemical tank 104, the reaction tank 201 and the insulation tank 202 are all horizontal tanks with a heating layer. The chemical tank 104 is provided with a plurality of baffles 5 and a plurality of baffles 6 at intervals along its length direction. The baffles 5 and the baffles 6 are arranged alternately. The upper end of the baffle 6 is connected to the top wall of the chemical tank 104, and the lower end is provided with a gap with the bottom of the chemical tank 104. The lower end of the baffle 5 is connected to the bottom of the chemical tank 104, and the upper end is provided with a gap with the top wall of the chemical tank 104. The chemical tank 104 is divided into several There are several areas, each of which is provided with a thermometer 11 and an agitator 12, and the exhaust pipes at the top of each area are connected in parallel with the main pipe 8, and the main pipe 8 is provided with a control valve 9 and a pressure sensor 10 linked thereto, and the pressure sensor 10 is used to detect the pressure in the chemical tank 104; the internal structure of the reaction tank 201 and the insulation tank 202 is the same as that of the chemical tank 104, and the top of each area of ​​the reaction tank 201 is provided with a chlorosulfonic acid feed port, and the bottom of the chemical tank 104, the reaction tank 201 and the insulation tank 202 are provided with a discharge pipe 7. Among them, the heating layer is a jacket arranged on the outer wall of the tank body, and steam is passed through the jacket.

[0030] exist Figure 3 In the specific embodiment shown, the inner cavity between the internal inlet and outlet of the chemical tank 104 is sequentially arranged with a baffle 5, a baffle 6, a baffle 5, and a baffle 6, which is used to divide its inner cavity into 5 areas; the interior of the reaction tank 201 is the same as that of the chemical tank, and the inner cavity between the internal inlet and outlet of the insulation tank 202 is sequentially arranged with a baffle 6, a baffle 5, a baffle 6, and a baffle 5. There are two reaction tanks 201 and insulation tanks 202, which are respectively connected in series, such as Figure 2 , 4 As shown; there are 10 branch pipes, and the 10 branch pipes correspond to the areas in the two reaction tanks 201. The multi-stage control valves on the multiple feed branch pipes on the top of the reaction tank can be controlled by the central console to start dripping chlorosulfonic acid, and the dripping speed is controlled according to the discharge speed of the material tank; at the same time, the amount of gas released by the reaction tank is recorded during the dripping process.

[0031] The mixture of aminosulfonic acid and thionyl chloride enters the material tank 104 for preheating, and the material temperature can be raised to 70-75 degrees, and kept warm for 6 hours; then the mixed material enters the reaction tank 201, and chlorosulfonic acid is added to the reaction tank in sections through multiple feed branches, so that the material can react while being heated in the reaction tank, thereby improving the reaction efficiency. As the material in the reaction tank reacts, the generated hydrogen chloride and sulfur dioxide will be discharged from the exhaust pipe, and the gas release of the reaction tank will gradually slow down within 8 hours after the addition of chlorosulfonic acid; then the material enters the insulation tank and continues to be heated to 85-90 degrees to ensure that the material reacts fully.

[0032] The following is a feeding process of the reaction tank in a specific embodiment: First, turn on the agitator in the reaction tank, open the steam valve of the reaction tank, and introduce steam into the jacket of the reaction tank to maintain the temperature between 68-72°C; turn on the circulating water of the condenser and start the tail gas treatment system; Start feeding: start the compressed air in the intermediate tank to press the material in the chemical tank into the first reaction tank to the upper edge of the first baffle inside; open the control valve of the main feed pipe, slowly open the 1# chlorosulfonic acid valve on the first feed branch pipe, control the flow rate at 40-60kg / h, open the 2# chlorosulfonic acid valve on the second feed branch pipe two hours later, control the flow rate at 100-120kg / h, and stabilize the reaction for 2 hours; Continue to feed into the first reaction tank, control the feed flow rate at 2.6-2.7m³ / h, open the 3# chlorosulfonic acid valve after 2 hours, control the flow rate at 100-120kg / h; open the 4# chlorosulfonic acid valve after 2 hours, control the flow rate at 100-120kg / h; When the material reaches the upper edge of the second baffle, open the 5# chlorosulfonic acid valve 2 hours later and control the flow rate at 100-120kg / h; Then the material enters the second reactor. After 2 hours, the 6# chlorosulfonic acid valve is opened to control the flow rate at 100-120kg / h. After 2 hours, the 7# chlorosulfonic acid valve is opened to control the flow rate at 100-120kg / h. When the material reaches the upper edge of the first baffle of the second reactor, open the 8# chlorosulfonic acid valve 2 hours later and control the flow rate at 100-120kg / h; open the 9# chlorosulfonic acid valve 2 hours later and control the flow rate at 100-120kg / h. When the material reaches the upper edge of the second baffle of the second reactor, start sampling from the last section of the reactor 2 hours later to test the chlorosulfonic acid content. Open the 10# chlorosulfonic acid valve appropriately according to the test results and control the flow rate at 40-60kg / h; Then feed the material into the first insulation tank, open the steam valve of the jacket on the insulation tank, and control the temperature at 80-85°C; when the material reaches the second insulation tank, open the steam valve of the jacket on the insulation tank, and control the temperature at 85-90°C.

[0033] During the reaction of the materials in the reaction tank and the insulation tank, the pressure is controlled at 0.1 MPa. Firstly, it can increase the reaction temperature and promote a more thorough reaction of the materials; secondly, it maintains a positive pressure to increase the boiling point of thionyl chloride, reduce thionyl chloride in the tail gas, and make it easier to recover.

[0034] In a specific embodiment of the present invention, Figure 4As shown, the condensation reflux assembly includes a condenser 2 and a low-temperature heat exchanger 3, and the multiple exhaust pipes at the top of the reaction tank 201 and the insulation tank 202 are respectively connected to the multiple condensers 2, and the bottom discharge pipes of the multiple condensers 2 are respectively connected to the top of the reaction tank 201 and the insulation tank 202, and the top air outlet of the condenser 2 is connected to the exhaust manifold 4; the exhaust manifold 4 is connected to the lower feed port of the low-temperature heat exchanger 3, the bottom outlet of the low-temperature heat exchanger 3 is connected to the top of the reaction tank 201, and the top air outlet of the low-temperature heat exchanger 3 is connected to the tail gas pipe 8; the top air outlets of the condenser 2 and the low-temperature heat exchanger 3 are both provided with thermometers. Among them, the lower and upper parts of the outer wall of the condenser are provided with a cooling medium inlet and outlet, which can cool the gas passing through the inside. The thionyl chloride in the exhaust gas is cooled by the condenser and the low-temperature condenser, so that it condenses and refluxes into the reaction tank, thereby improving the material utilization rate. The hydrogen chloride and sulfur dioxide finally discharged converge into the tail gas pipe and enter the tail gas treatment system for purification.

[0035] At the same time, a control valve and a pressure sensor linked thereto are provided on the top outlet pipes of the condenser 2 and the low-temperature heat exchanger 3, and the pressure sensor is used to detect the outlet pressure of the condenser 2 and the low-temperature heat exchanger 3. The use of this structure can ensure the safe operation of the equipment.

[0036] In a specific embodiment of the present invention, Figure 5 As shown, the distillation device includes a crude product tank I 301, a primary distillation and separation component, a crude product tank II 302 and a secondary distillation and separation component. The crude product tank I 301 is connected to the outlet of the insulation tank 202 and is used to accommodate the material discharged from the synthesis process; the discharge port of the crude product tank I 301 is connected to the feed port of the primary distillation and separation component through a primary conveying component, and the primary distillation and separation component is used to separate the thionyl chloride and chlorosulfonic acid in the material in sequence and store them in the thionyl chloride turnover tank 303 and the chlorosulfonic acid turnover tank 304; the material of the primary distillation and separation component enters the crude product tank II 302, and the crude product tank II 302 is connected to the secondary distillation and separation component through a secondary conveying component, and the secondary distillation and separation component is used to separate the finished product bis(chlorosulfonyl)imide and store it in the finished product tank 305. The crude product tank I contains crude bischlorosulfonyl imide doped with chlorosulfonic acid and thionyl chloride. Chlorosulfonic acid and thionyl chloride can be distilled out separately through a primary distillation separation component, and then bischlorosulfonyl imide can be distilled out through a secondary distillation separation component.

[0037] As a preferred structure, the primary distillation separation component includes a primary distiller 306, a primary separator 307 and a primary distillation heat exchanger 308. The top of the primary distiller 306 is connected to the bottom of the primary separator 307. The top side of the primary distiller 306 is provided with a material inlet connected to the primary conveying component, and the bottom is provided with a discharge port connected to the magnetic pump 1. The outlet of the magnetic pump 1 is respectively connected to the reflux pipe 309 and the feed pipe 310. The feed pipe 310 is connected to the crude product. Ⅱ tank 302, the other end of the reflux pipe 309 is connected to the top of the primary separator 307; the lower part of the primary separator 307 is connected to the bottom of the primary distillation heat exchanger 308, the top air outlet of the primary distillation heat exchanger 308 is connected to the condenser 2, the bottom discharge port of the condenser 2 is connected to the thionyl chloride turnover tank 303, the bottom discharge pipe of the condenser 2 is connected to the chlorosulfonic acid turnover tank 304 through a bypass pipe, and the air outlet of the condenser 2 is connected to the tail gas pipe 8. Through the above-mentioned first-stage distillation and separation component, thionyl chloride is first distilled out at 125±2℃ (vacuum degree ≤20 kpa), condensed into thionyl chloride turnover tank 303 through a condenser, and then transferred from the turnover tank to a thionyl chloride storage tank for recycling and reuse; after distillation until no liquid is produced, the temperature is raised to 130±2℃ (vacuum degree ≤5kpa), chlorosulfonic acid begins to be distilled out, condensed into chlorosulfonic acid turnover tank 304 through a condenser, and then transferred from the turnover tank to a chlorosulfonic acid storage tank for recycling and reuse.

[0038] There are two condensers 2, namely condenser I21 and condenser II22. The top air inlet of condenser I21 is connected to the top air outlet of the primary distillation heat exchanger 308 through an air inlet pipe, and a thermometer and a pressure sensor are provided on the air inlet pipe; the lower discharge port of condenser I21 is connected to the lower feed port of condenser II22, the top exhaust pipe of condenser II22 is connected to the tail gas pipe 8 through a vacuum pump I311, and a thermometer is provided on the exhaust pipe; the bottom discharge ports of condenser I21 and condenser II22 are respectively connected to two thionyl chloride turnover tanks 303; the lower part of condenser I21 and condenser II22 is provided with a cooling medium inlet and the upper part is provided with a cooling medium outlet. According to the different boiling points of thionyl chloride and chlorosulfonic acid, thionyl chloride and chlorosulfonic acid are cooled and cooled respectively, and after condensation, they enter the thionyl chloride turnover tank 303 and the chlorosulfonic acid turnover tank 304 respectively.

[0039] In the specific design, the bottom discharge pipe of the condenser I 21 is provided with two bypass pipes 312, one bypass pipe 312 is connected to the chlorosulfonic acid turnover tank 304 to realize the recovery and reuse of chlorosulfonic acid; the other bypass pipe 312 is connected to the crude product I tank 301, so that the material discharged from the condenser I can be returned to the crude product I tank to continue to participate in the distillation, so as to increase the yield of bischlorosulfonyl imide.

[0040] As a preferred structure, the secondary distillation separation component includes a secondary distiller 313, a secondary separator 314 and a secondary distillation heat exchanger 315. The top of the secondary distiller 313 is connected to the bottom of the secondary separator 314. The top side of the secondary distiller 314 is provided with a material inlet connected to the secondary conveying component, and the bottom is provided with a discharge port connected to the magnetic pump 1. The outlet of the magnetic pump 1 is connected to the top of the secondary separator 314 through a circulation pipe 316; the lower part of the secondary separator 314 is connected to the bottom of the secondary distillation heat exchanger 315, and the top air outlet of the secondary distillation heat exchanger 315 is connected to the top air inlet pipe of the condenser III 23, and the air inlet pipe is provided with a thermometer and a pressure sensor; the bottom discharge port of the condenser III 23 is connected to the finished product tank 305, and the exhaust port of the finished product tank 305 is connected to the vacuum pump II 317. The lower part of the condenser III is provided with a cooling medium inlet, and the upper part is provided with a cooling medium outlet. The above-mentioned secondary distillation separation component can be used to distill out the bischlorosulfonyl imide in the residual material to obtain a bischlorosulfonyl imide finished product with higher purity.

[0041] In the specific design, a check valve is provided at the outlet of the vacuum pump II 317. The outlet of the finished product tank 305 is connected to the magnetic pump 1, and a check valve is installed at the outlet of the magnetic pump 1. By installing the check valve, air can be prevented from entering the finished product tank after the pump is stopped, causing pollution.

[0042] Meanwhile, the above-mentioned primary distiller, primary separator, primary distillation heat exchanger, secondary distiller, secondary separator and secondary distillation heat exchanger are all purchased equipment, and corresponding models can be selected according to actual production needs.

[0043] The structures of the primary conveying assembly and the secondary conveying assembly are the same, both of which include a magnetic pump 1 and a feed pipe, and the feed pipe is provided with a control valve that can be linked with the magnetic pump 1 to control the feed amount of the primary distillation separation assembly and the secondary distillation separation assembly. At the same time, the crude product tank I 301 and the crude product tank II 302 are both provided with insulation coils inside, which can pre-raise the material temperature to the process requirements, so as to reduce the heating time required during the distillation process, thereby improving production efficiency.

[0044] In the actual production process, the mass percentages of the components in the crude material in the crude product tank I are: 55-60% bischlorosulfonyl imide, 30-35% thionyl chloride, and 2-5% chlorosulfonic acid. After distillation by the primary distillation separation component, the crude material entering the crude product tank II is bischlorosulfonyl imide containing impurities. After distillation by the secondary distillation separation component, the remaining residue in the secondary distiller is the kettle residue.

[0045] In a specific embodiment of the present invention, Figure 6As shown, the tail gas treatment system includes a buffer tank 401 for accommodating tail gas, a discharge valve is provided at the bottom of the buffer tank 401, an upper gas outlet of the buffer tank 401 is connected to the top gas inlet of the falling film absorber 410 through an exhaust pipe, the bottom outlet of the falling film absorber 410 is connected to a circulation tank 420 for accommodating hydrochloric acid, the circulation tank 420 is respectively connected to the upper liquid inlet of the falling film absorber 410 and the hydrochloric acid tank 403 through a circulation pump 402, the lower gas outlet of the falling film absorber 410 is connected to the lower part of the packing tower 430; the bottom of the packing tower 430 is connected to the circulation tank 420, the top exhaust port of the packing tower 430 is connected to the lower gas inlet of the drying tower 404, and the top exhaust port of the drying tower 404 is connected to the subsequent sulfur dioxide conversion tower; the absorption medium in the falling film absorber 410 and the packing tower 430 is water, and the drying medium in the drying tower 404 is concentrated sulfuric acid. The materials carried in the exhaust gas can be retained in the buffer tank. The hydrogen chloride gas in the exhaust gas combines with water to form hydrochloric acid when passing through the falling film absorber and the packed tower and is stored in the hydrochloric acid tank; then it enters the drying tower and uses concentrated sulfuric acid to dry the wet sulfur dioxide, making it convenient to enter the subsequent sulfur dioxide conversion tower for reuse.

[0046] As a preferred structure, the falling film absorber 410 and the circulation tank 420 are both two, namely, a primary falling film absorber 411, a secondary falling film absorber 412, a primary circulation tank 421 and a secondary circulation tank 422. The buffer tank 401 is connected to the top air inlet of the primary falling film absorber 411 through an exhaust pipe, the bottom outlet of the primary falling film absorber 411 is connected to the primary circulation tank 421, and the primary circulation tank 421 is connected to the primary falling film absorber 411 through a circulation pump 402. The upper liquid inlet of the first falling film absorber 410 is connected to the feed port of the hydrochloric acid tank 403, the lower gas outlet of the first falling film absorber 411 is connected to the top gas inlet of the second falling film absorber 412; the bottom outlet of the second falling film absorber 412 is connected to the second circulation tank 422, and the second circulation tank 422 is respectively connected to the upper liquid inlet of the second falling film absorber 412 and the first circulation tank 421 through the circulation pump 402, and the lower gas outlet of the second falling film absorber 412 is connected to the lower part of the packed tower 430. The use of two sets of falling film absorbers 410 and circulation tanks 420 can increase the tail gas treatment capacity; the use of circulation tanks and circulation pumps can realize the circulation of materials, further improving the recovery rate of hydrogen chloride.

[0047] The above structure is further optimized, the bottom outlets of the primary falling film absorber 411 and the secondary falling film absorber 412 are connected to the primary circulation tank 421 and the secondary circulation tank 422 through the discharge pipe, respectively, the middle of the discharge pipe is provided with a return bend section 405, and the bottom of the return bend section 405 is provided with a thermometer 11, and the primary circulation tank 421 and the secondary circulation tank 422 are both provided with a liquid level gauge. The use of the return bend section can prevent the material from causing impact on the circulation tank and improve the safety factor.

[0048] Similarly, there are two packed towers 430, namely a first-level packed tower 431 and a second-level packed tower 432. The bottoms of the first-level packed tower 431 and the second-level packed tower 432 are respectively connected to the first-level cache tank 433 and the second-level cache tank 434 for containing hydrochloric acid, the air outlet of the second-level falling film absorber 412 is connected to the lower part of the first-level packed tower 431, and the circulation pump 402 in the first-level cache tank 433 is connected to the upper part of the first-level packed tower 431 and the second-level circulation tank 422 through the hydrochloric acid pipe; the top air outlet of the first-level packed tower 431 is connected to the lower part of the second-level packed tower 432 through the air outlet pipe, and the circulation pump in the second-level cache tank 434 is connected to the upper part of the second-level packed tower 432 and the first-level cache tank 433 through the hydrochloric acid pipe, and the first-level cache tank 433 and the second-level cache tank 434 are connected; the first-level cache tank 433 and the second-level cache tank 434 are both provided with a stirrer 12. Among them, both the first-level cache tank and the second-level cache tank are equipped with a liquid level meter (liquid level transmitter). The above structure can further increase the tail gas treatment capacity and further improve the recovery rate of hydrogen chloride.

[0049] In the specific design, the top air outlet of the secondary packed tower 432 is connected to the water seal box 406 through a branch pipe, the exhaust pipe of the water seal box 406 is connected to the lower part of the primary alkali absorption tower 407, and a circulating pump 402 is provided in the storage tank at the bottom of the primary alkali absorption tower 407, which is used to transport the liquid in the storage tank to the upper part of the primary alkali absorption tower 407; the top air outlet of the primary alkali absorption tower 407 is connected to the lower part of the secondary alkali absorption tower 408 through an air outlet pipe, and the secondary alkali absorption tower 40 8. A circulating pump is provided in the storage tank at the bottom, which is used to transport the liquid in the storage tank to the upper part of the secondary alkali absorption tower 408 and the storage tank at the bottom of the primary alkali absorption tower 407. The top air outlet of the secondary alkali absorption tower 408 is connected to the induced draft fan 409. A stirrer 12 is provided in the bottom storage tanks of the primary alkali absorption tower 407 and the secondary alkali absorption tower 408. The absorption medium in the primary alkali absorption tower 407 and the secondary alkali absorption tower 408 is sodium hydroxide, which is used for neutralization reaction with hydrogen chloride gas. Among them, the bottom storage tanks of the primary alkali absorption tower 407 and the secondary alkali absorption tower 408 are both provided with a liquid level meter (liquid level transmitter). When the drying tower fails or is under maintenance, the alkali absorption method is used to remove sulfur dioxide in the tail gas. First, the tail gas enters the water seal and combines with the water therein, and then enters the primary alkali absorption tower and the secondary alkali absorption tower connected in series, so that sulfur dioxide can be neutralized with the internal sodium hydroxide to purify the tail gas.

[0050] In the specific design, a pressure sensor 10 is provided on the top outlet pipe of the secondary packing tower 432, and the pressure sensor 10 can be linked with the induced draft fan 409, the primary alkali absorption tower 407 and the circulating pump 402 in the bottom storage tank of the secondary alkali absorption tower 408. The use of this structure can ensure the safe operation of the equipment.

[0051] In a specific embodiment of the present invention, the bottom of the drying tower 404 is connected to the sulfuric acid tank 413, the sulfuric acid concentration in the sulfuric acid tank 403 is 93%, and the sulfuric acid tank 403 is provided with a stirrer 12; the concentrated sulfuric acid in the sulfuric acid tank 403 is transported to the upper part of the drying tower 404 by a circulating pump, and a heat exchanger 414 is provided on the discharge pipe of the circulating pump; the top outlet pipe of the drying tower 404 is connected to the fan 415, and the exhaust port of the fan 415 is connected to the sulfur dioxide conversion tower. Among them, a pressure sensor is provided on the outlet pipe of the drying tower 404, and a control valve 9 and a flow meter 14 are provided on the bottom air inlet pipe of the drying tower 404, and the fan can be linked with the pressure sensor and the control valve. When the sulfur dioxide in the tail gas passes through the drying tower, the concentrated sulfuric acid will absorb the moisture in the sulfur dioxide, thereby achieving the purpose of drying the sulfur dioxide.

[0052] In specific implementation, there are two hydrochloric acid tanks 403, and the feed pipes of the two hydrochloric acid tanks 403 are connected in parallel to the output pipe of the circulation tank 420; the bottom discharge ports of the two hydrochloric acid tanks 403 are connected to the hydrochloric acid pump 416, and a liquid level meter 13 (liquid level sensor) is provided on the hydrochloric acid tank 403.

[0053] In view of the corrosiveness of hydrogen chloride and sulfur dioxide, the pipes in the exhaust gas treatment system are made of FRP (fiber reinforced plastic) during production, and the corrosion resistance of FRP is used to increase the service life of the pipes.

[0054] In summary, the present invention has the advantages of reasonable structural design and good process continuity. The feeding system of the feeding process, the continuous reaction device of the synthesis process and the distillation device of the purification process are connected in sequence through pipelines. The feeding system can realize the mixing of thionyl chloride and aminosulfonic acid and the multi-point drop feeding of chlorosulfonic acid. The three raw materials are zoned in the continuous reaction device to synthesize bischlorosulfonyl imide and keep warm, so as to realize the full reaction of the material; then the thionyl chloride and chlorosulfonic acid in the material are separated by the distillation device for recycling and reuse, and the purification of bischlorosulfonyl imide is realized; finally, the tail gas discharged from the continuous reaction device and the distillation device is purified by the tail gas treatment system, and hydrochloric acid and sulfur dioxide are recovered to realize the standard emission of tail gas. The present invention can realize the continuous production of bischlorosulfonyl imide, improve the production efficiency and production volume, reduce the waste of raw materials, and reduce the production cost.

[0055] Finally, it should be noted that the above is only a preferred embodiment of the present invention and is not intended to limit the present invention. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art can still modify the technical solutions described in the aforementioned embodiments or replace some of the technical features therein with equivalents. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the scope of protection of the claims of the present invention.

Claims

1. A continuous production device for bis(chlorosulfonyl)imide, characterized in that: The invention comprises a feeding process, a synthesis process, a purification process and an exhaust gas treatment process. The feeding system of the feeding process is used to realize the feeding of thionyl chloride, chlorosulfonic acid and aminosulfonic acid. The continuous reaction device of the synthesis process is used to synthesize bischlorosulfonyl imide. The distillation device of the purification process is used to separate thionyl chloride and chlorosulfonic acid in the material and purify bischlorosulfonyl imide. The exhaust gas treatment system of the exhaust gas treatment process is used to purify the exhaust gas discharged from the continuous reaction device and the distillation device. The feeding system is used to continuously feed into the reaction tank of the continuous reaction device. The material discharged from the continuous reaction device enters the distillation device through a conveying component to complete the distillation and purification of bischlorosulfonyl imide. The exhaust gas treatment system can recover hydrogen chloride and sulfur dioxide in the exhaust gas.

2. A bis(chlorosulfonyl)imide continuous production equipment according to claim 1, characterized in that: The feeding system comprises a thionyl chloride storage tank, a chlorosulfonic acid storage tank, a batching tank and a chemical tank. The thionyl chloride in the thionyl chloride storage tank is transported to the batching tank through a conveying assembly. A sling is provided above the batching tank, and the sling is used to lift the aminosulfonic acid packaging bag to the top of the batching tank and add aminosulfonic acid into the batching tank; the top of the batching tank is connected to a compressed air pipe, and the compressed air in the compressed air pipe can continuously press the mixed liquid in the batching tank into the chemical tank through a discharge pipe; the chemical tank is connected to the reaction tank of the synthesis process through the discharge pipe, and the chlorosulfonic acid storage tank is connected to different areas in the reaction tank through a distribution and conveying pipeline, which is used to drop chlorosulfonic acid into the reaction tank in different areas; agitators are provided in the batching tank and the chemical tank, and exhaust pipes are provided on the tops of the chemical tank and the reaction tank, and heating layers are provided on the outer walls.

3. A bis(chlorosulfonyl)imide continuous production equipment according to claim 2, characterized in that: The distribution and delivery pipeline includes a feed main pipe and multiple feed branches connected in parallel therewith, the feed branches are provided with a flow meter and a control valve connected to the central console, the outlets of the multiple feed branches are sequentially connected to the chlorosulfonic acid feed ports on the top wall of each area in the reaction tank; the feed main pipe is connected to the bottom outlet of the chlorosulfonic acid storage tank through a magnetic pump.

4. A bis(chlorosulfonyl)imide continuous production equipment according to claim 3, characterized in that: The continuous reaction device comprises a horizontally placed reaction tank and an insulation tank, the feed port of the reaction tank is connected to the discharge pipe of the material tank outlet, and the discharge port of the reaction tank is connected to the insulation tank through a conveying component; the reaction tank and the insulation tank are sequentially divided into a plurality of interconnected areas, each area is provided with an agitator, the top of each area of ​​the reaction tank is provided with a chlorosulfonic acid feed port, and the outer walls of the reaction tank and the insulation tank are provided with a heating layer; the discharge port of the insulation tank is connected to the distillation device of the purification process; the tops of the reaction tank and the insulation tank are provided with an exhaust pipe and a condensation reflux component.

5. A bis(chlorosulfonyl)imide continuous production equipment according to claim 4, characterized in that: The chemical tank, reaction tank and insulation tank are all horizontal tank bodies with heating layers. A plurality of baffles and a plurality of deflectors are arranged at intervals along the length direction of the chemical tank. The baffles and the baffles are arranged alternately. The upper end of the baffle is connected to the top wall of the chemical tank, and a gap is provided between the lower end and the bottom of the chemical tank. The lower end of the baffle is connected to the bottom of the chemical tank, and a gap is provided between the upper end and the top wall of the chemical tank. The chemical tank is divided into several areas by the baffles and the baffles, each area is provided with a thermometer and an agitator, and the top of each area is provided with an exhaust pipe. The internal structure of the reaction tank and the insulation tank is the same as that of the chemical tank. A chlorosulfonic acid feed port is provided on the top of each area of ​​the reaction tank, and a discharge pipe is provided at the bottom of the chemical tank, the reaction tank and the insulation tank.

6. A bischlorosulfonyl imide continuous production equipment according to claim 4, characterized in that: The condensation reflux component includes a condenser and a low-temperature heat exchanger. The multiple exhaust pipes on the top of the reaction tank and the insulation tank are respectively connected to the multiple condensers, the bottom discharge pipes of the multiple condensers are respectively connected to the top of the reaction tank and the insulation tank, and the top air outlet of the condenser is connected to the exhaust main pipe; the exhaust main pipe is connected to the lower feed port of the low-temperature heat exchanger, the bottom outlet of the low-temperature heat exchanger is connected to the top of the reaction tank, and the top air outlet of the low-temperature heat exchanger is connected to the tail gas pipe; the top air outlets of the condenser and the low-temperature heat exchanger are both provided with thermometers.

7. A bischlorosulfonyl imide continuous production equipment according to claim 4, characterized in that: The distillation device comprises a crude product tank I, a primary distillation and separation component, a crude product tank II and a secondary distillation and separation component. The crude product tank I is connected to the outlet of the insulation tank and is used to accommodate materials discharged from the synthesis process; the discharge port of the crude product tank I is connected to the feed port of the primary distillation and separation component through a primary conveying component, and the primary distillation and separation component is used to separate thionyl chloride and chlorosulfonic acid from the materials in sequence and store them in thionyl chloride turnover tanks and chlorosulfonic acid turnover tanks; the materials of the primary distillation and separation component enter the crude product tank II, and the crude product tank II is connected to the secondary distillation and separation component through a secondary conveying component, and the secondary distillation and separation component is used to separate the finished product bischlorosulfonyl imide and store it in the finished product tank.

8. The continuous production equipment for bis(chlorosulfonyl)imide according to claim 7, characterized in that: The primary distillation separation component includes a primary distiller, a primary separator and a primary distillation heat exchanger. The top of the primary distiller is connected to the bottom of the primary separator. The top side of the primary distiller is provided with a material inlet connected to the primary conveying component, and the bottom is provided with a discharge port connected to the magnetic pump. The outlet of the magnetic pump is respectively connected to a reflux pipe and a feed pipe. The feed pipe is connected to a crude product II tank, and the other end of the reflux pipe is connected to the top of the primary separator; the lower part of the primary separator is connected to the bottom of the primary distillation heat exchanger, the top air outlet of the primary distillation heat exchanger is connected to a condenser, the bottom discharge port of the condenser is connected to a thionyl chloride turnover tank, the bottom discharge pipe of the condenser is connected to a chlorosulfonic acid turnover tank through a bypass pipe, and the air outlet of the condenser is connected to a tail gas pipe.

9. The continuous production equipment of bis(chlorosulfonyl)imide according to claim 7, characterized in that: The secondary distillation separation component includes a secondary distiller, a secondary separator and a secondary distillation heat exchanger. The top of the secondary distiller is provided with a connection to the bottom of the secondary separator, the top side of the secondary distiller is provided with a material inlet connected to the secondary conveying component, and the bottom is provided with a discharge port connected to the magnetic pump, and the outlet of the magnetic pump is connected to the top of the secondary separator through a circulation pipe; the lower part of the secondary separator is connected to the bottom of the secondary distillation heat exchanger, the top air outlet of the secondary distillation heat exchanger is connected to the top air inlet pipe of the condenser III, and the air inlet pipe is provided with a thermometer and a pressure sensor; the bottom discharge port of the condenser III is connected to the finished product tank, and the exhaust port of the finished product tank is connected to the vacuum pump II.

10. A bischlorosulfonyl imide continuous production equipment according to any one of claims 1 to 9, characterized in that: The tail gas treatment system includes a buffer tank for accommodating tail gas, a discharge valve is provided at the bottom of the buffer tank, an upper gas outlet of the buffer tank is connected to the top gas inlet of a falling film absorber through an exhaust pipe, the bottom outlet of the falling film absorber is connected to a circulation tank for accommodating hydrochloric acid, the circulation tank is respectively connected to the upper liquid inlet of the falling film absorber and the hydrochloric acid tank through a circulation pump, the lower gas outlet of the falling film absorber is connected to the lower part of a packing tower; the bottom of the packing tower is connected to the circulation tank, the top exhaust port of the packing tower is connected to the lower gas inlet of a drying tower, and the top exhaust port of the drying tower is connected to a subsequent sulfur dioxide conversion tower; the absorption medium in the falling film absorber and the packing tower is water, and the drying medium in the drying tower is concentrated sulfuric acid.

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