CN215439684U - Bis chlorosulfonyl imide continuous preparation system - Google Patents
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Abstract
The utility model relates to a continuous preparation system of bis (chlorosulfonyl) imide, which comprises a batching system, a conveying system, a reaction system and an exhaust system which are sequentially connected; the batching system comprises a batching tank, and a liquid raw material feeding pipeline, a solid raw material feeding pipeline, a weighing system, a cooling system and a stirring system which are arranged on the batching tank; the conveying system comprises a conveying pump and a flow control system which are connected in sequence; the reaction system comprises one or more pipeline reactors and a heat exchange system arranged outside the pipeline reactors; the exhaust system comprises a gas-liquid separator, a demister and a condenser which are arranged at the upper end of the gas-liquid separator, and a control system. The method can obtain high-quality and high-purity products, is economical and practical, and is suitable for industrial production.
Description
Technical Field
The utility model relates to the field of lithium batteries and lithium capacitors, in particular to a continuous preparation system of bis (chlorosulfonyl) imide.
Background
Lithium ion batteries are widely used in various fields such as mobile phones, notebook computers, small-sized charging systems, electric vehicles and the like because of their advantages of high energy density, high operating voltage, long cycle life and the like, and their application fields are still continuously expanding with the continuous development of society. The electrolyte in the existing lithium ion batteries is lithium hexafluorophosphate (LiPF)6) The product has the advantages of high conductivity and the like, but also has the defects of poor thermal stability, rigorous preparation process, poor high-temperature and low-temperature performances and the like. Therefore, researchers are also continuously developing new electrolytes for lithium ion batteries to improve the overall performance of the lithium ion batteries. The lithium bis (fluorosulfonyl) imide (LiFSI) is a novel electrolyte lithium salt used in lithium battery electrolyte, is environment-friendly, has good safety performance, and has basic conditions for industrial application. With conventional lithium salt LiPF6Compared with LiFSI, lithium ions are easier to dissociate, so that the lithium ion battery has higher conductivity; LiFSI decomposition temperature higher than 200
The thermal stability and the safety performance are obviously superior to those of LiPF6(ii) a In addition, the lithium ion battery electrolyte has unique effects on improving the performances of high-temperature storage, low-temperature discharge and the like, and has excellent characteristics of good compatibility with electrodes and the like, so that LiFSI is an electrolyte with good prospects in lithium ion batteries.
The synthesis process of lithium bis (fluorosulfonyl) imide generally requires three steps: (1) synthesizing bis (chlorosulfonyl) imide; (2) preparing bis (fluorosulfonyl) imide by bis (chlorosulfonyl) imide fluorination; (3) preparation of alkali metal salts of bis (fluorosulfonyl) imide, a key step in which is the synthesis of bis (chlorosulfonyl) imide.
CN106365132A discloses two processes for preparing bischlorosulfonimide. The first process comprises the following steps: urea and chlorosulfonic acid are used as raw materials, and after one-step reaction, dichlorosulfonic acid imine, ammonium bisulfate, hydrochloric acid and carbon dioxide are produced; the second process comprises the following steps: sulfamic acid and phosphorus pentachloride are used as raw materials to generate chlorosulfonyl phosphazene, and then the chlorosulfonyl phosphazene generates a dichlorosulfonimide product under the action of chlorosulfonic acid, wherein the adopted mode is that the product is obtained by batch reaction in a stirring kettle.
CN106241757A proposes that a bis-chlorosulfonyl imide product is prepared by taking sulfamic acid, thionyl chloride and chlorosulfonic acid as raw materials through high-temperature and high-pressure reaction. The preparation method has the advantages of high safety, easy control of the preparation process and the like, and is a preparation process widely adopted at present.
CN106365132A discloses a method for preparing imido dithioacyl compound in continuous reaction with chlorosulfonic acid and chlorosulfonic acid isocyanate as raw materials at high temperature, wherein the reaction temperature is 180 to 300 ℃, the pressure is 50 to 500bar, and the method is not suitable for industrial scale-up production due to high temperature and high pressure.
The main production process of the dichlorosulfonimide is obtained by dropwise adding chlorosulfonic acid and chlorosulfonic acid isocyanate as raw materials into a reaction kettle and stirring for reaction, wherein the chlorosulfonic acid, chlorosulfonic acid isocyanate and the product dichlorosulfonimide are toxic and strongly corrosive substances, and the product is extremely easy to decompose after the temperature exceeds 170 ℃ and emits a large amount of decomposition heat, so that sufficient safety measures are required in intermittent production, the reaction temperature is not higher than 150 ℃ in the intermittent production process so as to avoid explosion hazard, a large amount of carbon dioxide gas is emitted in the reaction process, the dropwise adding speed cannot be too high in order to avoid material flushing in the reaction kettle, and the reaction time can reach 8 to 24 hours at a time due to the fact that the reaction temperature cannot be improved and is slow, the production efficiency is difficult to improve.
Therefore, a continuous preparation system of bis (chlorosulfonyl) imide is needed.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a continuous preparation system of bis (chlorosulfonyl) imide, aiming at the defects in the prior art.
In order to achieve the purpose, the utility model adopts the technical scheme that:
the utility model provides a continuous preparation system of bis (chlorosulfonyl) imide, which comprises a batching system, a conveying system, a reaction system and an exhaust system which are connected in sequence;
the batching system comprises a batching tank, and a liquid raw material feeding pipeline, a solid raw material feeding pipeline, a weighing system, a cooling system and a stirring system which are arranged on the batching tank, so that raw materials with various proportions can be accurately prepared under the normal temperature or low temperature condition, and the feeding speed can be monitored in real time;
the conveying system comprises a conveying pump and a flow control system which are connected in sequence;
the reaction system comprises one or more pipeline reactors and a heat exchange system arranged outside the pipeline reactors; a groove for forming plug flow is also arranged in the pipeline reactor; the heat exchange system can heat the pipeline reactor or remove heat from the pipeline reactor; the length and/or the number of the reactors can be increased or decreased according to the reaction requirements; the exhaust systems are arranged between every two pipeline reactors;
the exhaust system comprises a gas-liquid separator, a demister and a condenser which are arranged at the upper end of the gas-liquid separator, and a control system; the control system comprises a pressure sensor arranged on the gas-liquid separator and a pneumatic valve arranged between the gas-liquid separator and the demister; the pressure sensor is interlocked with the pneumatic valve, when the pressure in the gas-liquid separator exceeds the preset pressure, the pneumatic valve is opened to discharge carbon dioxide gas generated by reaction, the discharged gas firstly passes through the demister and then is cooled by the condenser, so that the gasified raw materials in the gas-liquid separator are recycled to the system as far as possible, and finally are uniformly and intensively treated; the pressure of the gas-liquid separator arranged at the front is higher than that of the gas-liquid separator arranged at the back, so that the liquid-phase reaction materials flow in the system by the pushing of the pressure difference, and subsequent devices such as a delivery pump and the like can be omitted.
Preferably, the delivery pump is a constant pressure delivery pump, and the fixed pressure is 0.5MPa-5 MPa.
Preferably, the constant pressure delivery pump is selected from one of a gear pump, a screw pump, a plunger pump or a diaphragm pump.
Preferably, the motor matched with the delivery pump is a variable frequency motor, so that the variable frequency motor can be adjusted in a variable frequency mode.
Preferably, a safety valve is further arranged at the outlet of the delivery pump.
Preferably, the material of the pipeline reactor is selected from one or more of hastelloy, nickel material, silicon carbide or enamel and other corrosion-resistant materials.
Preferably, the heat exchange medium or the heat exchange mode of the heat exchange system is selected from one of heat conduction oil, steam or electric heat exchange.
Preferably, the material of the gas-liquid separator, the pneumatic valve, the demister and the condenser is selected from one or more of hastelloy, nickel material, silicon carbide, enamel or graphite.
Preferably, the lower end of the pipeline reactor is also provided with a liquid storage area.
Preferably, the control system further comprises a liquid level sensor arranged in the liquid storage section, and the liquid level sensor is interlocked with the pneumatic valve.
Preferably, the control system further comprises a DCS control cabinet, and the pressure control and the liquid level control are carried out through the DCS control cabinet.
The use method of the system for continuously preparing the bis (chlorosulfonyl) imide is further provided: firstly, opening the public works of all subsystems, and quantitatively adding reactants chlorosulfonic acid, chlorosulfonic acid isocyanate and a catalyst into a proportioning tank through a weighing system after the temperature and the pressure in the proportioning tank, a pipeline reactor and a gas-liquid separator reach preset values; secondly, starting a stirring system to uniformly mix the materials in the batching tank, simultaneously maintaining the temperature in the batching tank between-40 ℃ and 25 ℃, preferably between-40 ℃ and-5 ℃, starting a constant-pressure delivery pump after the raw materials are uniformly stirred and mixed, preferably setting the pressure of the outlet of the delivery pump between 1MPa and 3MPa, and enabling the fluid after the pressure is increased by the delivery pump to enter a pipeline reactor of a first section after passing through a flow control system, wherein the flow is 0.1-5m3A preferred flow rate is between 0.5 and 3m3The temperature of the pipeline reactor is set between 120 ℃ and 250 ℃, preferably between 150 ℃ and 200 ℃, and the pipe diameter of the pipeline reactor is DN10-DNBetween 50, preferably between DN15 and DN 32; the method comprises the following steps that reactants flow forwards while reacting in a pipeline reactor, then flow into a gas-liquid separator from the pipeline reactor of a first section, a large amount of carbon dioxide gas is generated in the reaction process, the gas quantity in a system is increased along with the reaction, the pressure of the system is increased, when the pressure in the gas-liquid separator is higher than a preset pressure value (the preset pressure value in the first stage gas-liquid separator is 4-5 MPa), a pneumatic valve is automatically opened to discharge gas products generated by the reaction, the discharged gas is firstly subjected to a demister to remove liquid drops, is cooled by a condenser, gasified raw materials are recycled into the system as far as possible, and finally are subjected to unified centralized treatment; because the preset pressure value of the gas-liquid separator in the latter section is lower than that of the gas-liquid separator in the former section, the reaction material is pushed by the pressure difference to enter the pipeline reactor in the second section, and the reaction material is circulated until the preset conversion rate is reached, and then enters the subsequent separation and refining section.
The reaction equation involved is as follows:
by adopting the technical scheme, compared with the prior art, the utility model has the following technical effects:
the utility model can accurately prepare materials, uniformly mix in the early stage, eliminate the influence of mass transfer, enable the reaction to be smooth, and simultaneously prepare materials at low temperature to prevent the raw materials from deteriorating and the possibility of reaction; the continuous pipeline type reaction has high automation degree, few artificial interference factors, stable product quality, improved production efficiency, less reaction liquid holdup and greatly improved safety in the production process; intermittent exhaust in the reaction process reduces the pressure of the system, promotes the reaction to move in the positive direction and improves the conversion rate of the reaction; the rear section of the system adopts pressure difference to push materials to flow forwards, thereby greatly reducing the investment of pumps and other dynamic equipment and improving the reliability of the system.
The method can obtain high-quality and high-purity products, is economical and practical, and is suitable for industrial production.
Drawings
FIG. 1 is a schematic structural view of a continuous bis (chlorosulfonyl) imide production system according to the present invention;
wherein the reference numerals include:
a dosing tank 1; a stirring system 11; a delivery pump 2; a flow control system 3; a pipeline reactor 4; a heat exchange system 5; a gas-liquid separator 6; a demister 61; a condenser 62; a pressure sensor 63; the air-operated valve 64; a level sensor 65.
Detailed Description
As shown in fig. 1, a continuous preparation system of bis (chlorosulfonyl) imide is provided, which comprises a batching system, a conveying system, a reaction system and an exhaust system which are connected in sequence;
the batching system comprises a batching tank 1, and a liquid raw material feeding pipeline, a solid raw material feeding pipeline, a weighing system, a cooling system and a stirring system 11 which are arranged on the batching tank 1, so that raw materials with various proportions can be accurately prepared under the condition of normal temperature or low temperature, and the feeding speed is monitored in real time;
the conveying system comprises a conveying pump 2 and a flow control system 3 which are connected in sequence;
the reaction system comprises one or more pipeline reactors 4 and a heat exchange system 5 arranged outside the pipeline reactors 4; a groove for forming plug flow is also arranged in the pipeline reactor 4; the heat exchange system 5 can heat the pipeline reactor 4 or remove heat from the pipeline reactor 4; the length and/or the number of the reactors can be increased or decreased according to the reaction requirements; the gas-liquid separators 6 are arranged between every two pipeline reactors 4;
the exhaust system comprises a gas-liquid separator 6, a demister 61 and a condenser 62 which are arranged at the upper end of the gas-liquid separator 6, and a control system; the control system comprises a pressure sensor 63 arranged on the gas-liquid separator 6 and an air-operated valve 64 arranged between the gas-liquid separator 6 and the demister 61; the pressure sensor 63 is interlocked with the pneumatic valve 64, when the pressure in the gas-liquid separator 6 exceeds the preset pressure, the pneumatic valve 64 is opened to discharge carbon dioxide gas generated by reaction, the discharged gas firstly passes through the demister 61 and then is cooled by the condenser 62, so that the gasified raw materials in the gas-liquid separator are recycled to the system as far as possible, and finally are uniformly and intensively processed; the pressure of the gas-liquid separator 6 arranged at the front is higher than that of the gas-liquid separator 6 arranged at the back, so that the liquid-phase reaction materials flow in the system by the pushing of the pressure difference, and subsequent devices such as a delivery pump 2 and the like can be omitted.
Preferably, the delivery pump 2 is a constant pressure delivery pump 2, and the fixed pressure is 0.5MPa-5 MPa.
Preferably, the constant pressure delivery pump 2 is selected from one of a gear pump, a screw pump, a plunger pump or a diaphragm pump.
Preferably, the motor matched with the delivery pump 2 is a variable frequency motor, so that the variable frequency motor can be adjusted in a variable frequency mode.
Preferably, a safety valve is further arranged at the outlet of the delivery pump 2.
Preferably, the material of the pipe reactor 4 is selected from one or more of hastelloy, nickel material, silicon carbide or enamel and other corrosion-resistant materials.
Preferably, the heat exchange medium or the heat exchange mode of the heat exchange system 5 is selected from one of heat transfer oil, steam or electric heat exchange.
Preferably, the material of the gas-liquid separator 6, the pneumatic valve 64, the demister 61 and the condenser 62 is selected from one or more of hastelloy, nickel material, silicon carbide, enamel or graphite.
Preferably, the lower end of the pipeline reactor 4 is also provided with a liquid storage area.
Preferably, the control system further comprises a liquid level sensor 65 disposed within the liquid storage region, wherein the liquid level sensor 65 is interlocked with the pneumatic valve 64.
The use method of the system for continuously preparing the bis (chlorosulfonyl) imide is further provided: firstly, opening the public works of all subsystems, and quantitatively adding reactants chlorosulfonic acid, chlorosulfonic acid isocyanate and a catalyst into a proportioning tank through a weighing system after the temperature and the pressure in the proportioning tank, a pipeline reactor and a gas-liquid separator reach preset values; secondly, starting a stirring system to uniformly mix materials in the batching tank, simultaneously maintaining the temperature in the batching tank between-40 ℃ and 25 ℃, preferably between-40 ℃ and-5 ℃, starting a constant-pressure delivery pump after uniformly stirring and mixing the raw materials, enabling the pressure of the delivery pump to be between 1MPa and 3MPa, enabling the fluid after the pressure of the delivery pump is increased to enter a pipeline reactor of a first section after passing through a flow control system, wherein the flow is between 0.1 and 5m3/h, preferably between 0.5 and 3m3/h, setting the temperature of the pipeline reactor to be between 120 ℃ and 250 ℃, preferably between 150 ℃ and 200 ℃, setting the pipe diameter of the pipeline reactor to be between DN10 and DN50, preferably between DN15 and DN 32; the method comprises the following steps that reactants flow forwards while reacting in a pipeline reactor, then flow into a gas-liquid separator from the pipeline reactor of a first section, a large amount of carbon dioxide gas is generated in the reaction process, the gas quantity in a system is increased along with the reaction, the pressure of the system is increased, when the pressure in the gas-liquid separator is higher than a preset pressure value (the preset pressure value in the first stage gas-liquid separator is 4-5 MPa), a pneumatic valve is automatically opened to discharge gas products generated by the reaction, the discharged gas is firstly subjected to a demister to remove liquid drops, is cooled by a condenser, gasified raw materials are recycled into the system as far as possible, and finally are subjected to unified centralized treatment; because the preset pressure value of the gas-liquid separator in the latter section is lower than that of the gas-liquid separator in the former section, the reaction material is pushed by the pressure difference to enter the pipeline reactor in the second section, and the reaction material is circulated until the preset conversion rate is reached, and then enters the subsequent separation and refining section.
The reaction equation involved is as follows:
the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The utility model is further described with reference to the following drawings and specific examples, which are not intended to be limiting.
Example 1
The temperature of a batching tank is set to be 25 ℃ below zero, the temperature of a pipeline reactor is set to be 150 ℃, the pressure of a first-stage gas-liquid separator is set to be 1.5Mpa, the pressure of a second-stage gas-liquid separator is set to be 1.3Mpa, the pressure of a third-stage gas-liquid separator is set to be 1.1Mpa, 582.5 kilograms of chlorosulfonic acid, 778.3 kilograms of chlorosulfonic acid isocyanate, 5.8 kilograms of concentrated sulfuric acid are added into the batching tank, a stirring system in the batching tank is started, stirring is carried out for 20 minutes, a constant-pressure delivery pump is started, the pressure of a pump outlet is set to be 1.8Mpa, the flow rate is set to be 0.6m3And h, the temperature of a cooling medium of a condenser on the gas-liquid separator is-25 ℃, materials discharged from the three-stage pipeline reactor are collected and sampled, and the chlorosulfonic acid conversion rate is 70% and the yield is 97% by analysis.
Example 2
The temperature of a batching tank is set to be 25 ℃ below zero, the temperature of a pipeline reactor is set to be 180 ℃, the pressure of a first-stage gas-liquid separator is set to be 2Mpa, the pressure of a second-stage gas-liquid separator is set to be 1.8Mpa, the pressure of a third-stage gas-liquid separator is set to be 1.6Mpa, 582.5 kilograms of chlorosulfonic acid, 778.3 kilograms of chlorosulfonic acid isocyanate and 5.8 kilograms of concentrated sulfuric acid are added into the batching tank, a stirring system in the batching tank is started, stirring is carried out for 20 minutes, a constant-pressure delivery pump is started, the pressure of a pump outlet is set to be 2.3Mpa, and the flow is set to be 0.6m3The temperature of a cooling medium of a condenser on the gas-liquid separator is-25 ℃, and the cooling medium passes through a three-stage pipelineThe materials discharged from the reactor are collected and sampled, and the chlorosulfonic acid conversion rate is 90 percent and the yield is 95 percent by analysis.
Example 3
The temperature of a batching tank is set to be 25 ℃ below zero, the temperature of a pipeline reactor is set to be 150 ℃, the pressure of a first-stage gas-liquid separator is set to be 1.5Mpa, the pressure of a second-stage gas-liquid separator is set to be 1.3Mpa, the pressure of a third-stage gas-liquid separator is set to be 1.1Mpa, chlorosulfonic acid is added into the batching tank to be 582.5 kilograms, chlorosulfonic acid isocyanate is 778.3 kilograms, concentrated sulfuric acid is 5.8 kilograms, a stirring system in the batching tank is started, stirring is carried out for 20 minutes, a constant-pressure delivery pump is started, the pressure of an outlet of the pump is set to be 1.8Mpa, the flow is set to be 0.6m3And h, the temperature of a cooling medium of a condenser on the gas-liquid separator is-25 ℃, materials discharged from the three-stage pipeline reactor are collected and sampled, and the chlorosulfonic acid conversion rate is 92% and the yield is 96% through analysis.
Example 4
The batching tank is set at the temperature of-25 ℃, the pipeline reactor is set at the temperature of 180 ℃, the first-stage gas-liquid separator is set at the pressure of 2MPa, the second-stage gas-liquid separator is set at the pressure of 1.8MPa, the third-stage gas-liquid separator is set at the pressure of 1.6MPa, the fourth-stage gas-liquid separator is set at the pressure of 1.5MPa, chlorosulfonic acid is added into the batching tank of 582.5 kg, chlorosulfonic acid isocyanate is 778.3 kg, concentrated sulfuric acid is added into the batching tank of 5.8 kg, then a stirring system in the batching tank is started, stirring is carried out for 20 minutes, then a constant-pressure delivery pump is started, the pressure of the pump outlet is set at the pressure of 2.3MPa, the flow is set at 0.6m3And h, the temperature of a cooling medium of a condenser on the gas-liquid separator is-25 ℃, materials discharged from the three-stage pipeline reactor are collected and sampled, and the chlorosulfonic acid conversion rate is 100% and the yield is 95.1% by analysis.
The method can obtain high-quality and high-purity products, is economical and practical, and is suitable for industrial production.
While the utility model has been described with reference to a preferred embodiment, it will be understood by those skilled in the art that various changes in form and detail may be made therein without departing from the spirit and scope of the utility model.
Claims (10)
1. A continuous preparation system of bis (chlorosulfonyl) imide is characterized by comprising a batching system, a conveying system, a reaction system and an exhaust system which are sequentially connected;
the batching system comprises a batching tank (1), and a liquid raw material feeding pipeline, a solid raw material feeding pipeline, a weighing system, a cooling system and a stirring system (11) which are arranged on the batching tank (1);
the conveying system comprises a conveying pump (2) and a flow control system (3) which are connected in sequence;
the reaction system comprises one or more pipeline reactors (4) and a heat exchange system (5) arranged outside the pipeline reactors (4); a groove for forming plug flow is also arranged in the pipeline reactor (4); the heat exchange system (5) can heat the pipeline reactor (4) or remove heat from the pipeline reactor (4); the exhaust systems are arranged between every two pipeline reactors (4);
the exhaust system comprises a gas-liquid separator (6), a demister (61) and a condenser (62) which are arranged at the upper end of the gas-liquid separator (6), and a control system; the control system comprises a pressure sensor (63) arranged on the gas-liquid separator (6) and an air-operated valve (64) arranged between the gas-liquid separator (6) and the demister (61); the pressure sensor (63) is interlocked with the pneumatic valve (64); the pressure of the gas-liquid separator (6) arranged at the front is higher than that of the gas-liquid separator (6) arranged at the rear.
2. The continuous bis-chlorosulfonyl imide production system according to claim 1, wherein said transfer pump (2) is a constant pressure transfer pump.
3. The continuous bis-chlorosulfonyl imide production system according to claim 2, wherein said constant pressure feed pump is one selected from a gear pump, a screw pump, a plunger pump and a diaphragm pump.
4. The continuous preparation system of bis-chlorosulfonyl imide according to claim 1, wherein the motor to which the transfer pump (2) is coupled is a variable frequency motor.
5. The continuous bis-chlorosulfonyl imide production system according to claim 1, wherein a safety valve is further provided at an outlet of the transfer pump (2).
6. The continuous bis (chlorosulfonyl) imide production system according to claim 1, wherein the material of the pipe reactor (4) is selected from one of hastelloy, nickel, silicon carbide, and enamel.
7. The continuous preparation system of bis (chlorosulfonyl) imide according to claim 1, wherein the heat exchange medium or the heat exchange means of the heat exchange system (5) is one selected from heat transfer oil, steam or electricity.
8. The continuous bis-chlorosulfonyl imide production system according to claim 1, wherein the material of the gas-liquid separator (6), the pneumatic valve (64), the demister (61), and the condenser (62) is selected from one of hastelloy, nickel, silicon carbide, enamel, and graphite.
9. The continuous bis (chlorosulfonyl) imide production system according to claim 1, wherein a reservoir is further provided at the lower end of the pipe reactor (4).
10. The continuous bis-chlorosulfonyl imide production system according to claim 9, wherein said control system further includes a level sensor (65) disposed within said reservoir, said level sensor (65) being interlocked with said pneumatic valve (64).
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115159480A (en) * | 2022-06-24 | 2022-10-11 | 森松（江苏）重工有限公司 | Production system of bis (chlorosulfonyl) imide |
| CN115304039A (en) * | 2022-10-10 | 2022-11-08 | 山东海科新源材料科技股份有限公司 | Purification device and method for bis (chlorosulfonyl) imide |
| CN115893337A (en) * | 2022-12-21 | 2023-04-04 | 浙江研一新能源科技有限公司 | Preparation method of lithium bis (fluorosulfonyl) imide |
-
2020
- 2020-11-25 CN CN202022772519.5U patent/CN215439684U/en active Active
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115159480A (en) * | 2022-06-24 | 2022-10-11 | 森松（江苏）重工有限公司 | Production system of bis (chlorosulfonyl) imide |
| CN115304039A (en) * | 2022-10-10 | 2022-11-08 | 山东海科新源材料科技股份有限公司 | Purification device and method for bis (chlorosulfonyl) imide |
| CN115304039B (en) * | 2022-10-10 | 2022-12-06 | 山东海科新源材料科技股份有限公司 | Purification device and method for bis (chlorosulfonyl) imide |
| CN115893337A (en) * | 2022-12-21 | 2023-04-04 | 浙江研一新能源科技有限公司 | Preparation method of lithium bis (fluorosulfonyl) imide |
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