Continuous production system of electrolyte
The continuous electrolyte production system with a tubular reactor and temperature control addresses slow dissolution issues by optimizing solvent temperature for rapid additive mixing, enhancing production efficiency and quality.
Patent Information
- Application Number
- CN202420783149.0
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-04-16
- Publication Date
- 2024-12-20
- Estimated Expiration
- 2034-04-16
Smart Images
Figure CN222196739U_ABST
Abstract
Description
Technical Field
[0001] The utility model relates to the technical field of lithium ion batteries, in particular to a continuous production system of electrolyte. Background Art
[0002] In the production of electrolyte, additives are generally added. Additives are divided into high-temperature additives and low-temperature additives. High-temperature additives include vinylene carbonate and fluoroethylene carbonate; low-temperature additives include vinyl sulfate, etc. When adding high-temperature additives to the solvent, the solvent temperature needs to be kept high to help the high-temperature additives dissolve in the solvent in a shorter time; when adding low-temperature additives to the solvent, the solvent temperature needs to be kept low to prevent the low-temperature additives from deteriorating.
[0003] The existing electrolyte production process mainly uses a kettle configuration device, which needs to be heated up before adding a high-temperature additive, then cooled down after the high-temperature additive is fully dissolved, and then lithium salt is added and mixed evenly, and then cooled down again and a low-temperature additive is added. Taking the electrolyte configured in a 10T reactor as an example, it contains lithium hexafluorophosphate, vinylene carbonate, fluoroethylene carbonate, and vinyl sulfate, wherein the concentration of lithium hexafluorophosphate is 12.5wt%, vinylene carbonate, fluoroethylene carbonate, and vinyl sulfate each account for 1% of the total weight of the electrolyte, and the solvent is a mixture of vinyl carbonate, ethyl methyl carbonate, and diethyl carbonate in a mass ratio of 1:2:2; the total planned production weight of the electrolyte is 8 tons, which is divided into 3 steps. The first step is to add all the solvents to a 10 cubic meter reactor, heat it to 60°C, add vinylene carbonate and fluoroethylene carbonate, keep stirring, and stir for 0.5h to completely dissolve vinylene carbonate and fluoroethylene carbonate; then it takes 1h to cool down to 40°C, add lithium salt, stir for 0.5h, cool down to 15°C, add vinyl sulfate, stir for 0.5h, and cool down to 5°C. The entire production process takes up to 2.5h. And it requires 3 workers to operate together.
[0004] The traditional operation has the following problems: the dissolution time of the high-temperature additive is too long, which makes the overall process too time-consuming;
[0005] In the prior art, CN219849280U discloses a device for mixing lithium-ion electrolyte based on a star mixer, which discloses using a star mixer and a tubular reactor to mix materials to prepare electrolyte; the star mixer has nearly a thousand interlaced mixing sheets inside, which is suitable for premixing two liquid materials. The premixed materials cannot contain solid particles, nor can they generate solid particles after contact;
[0006] The problem with this solution is that the star-shaped mixer cannot process solids, resulting in the inability to dissolve solid high-temperature additives. If the solid high-temperature additives and electrolytes are added to the tubular reactor at the same time, either the dissolution time of the high-temperature additives will be prolonged, or the temperature will be raised to the dissolution temperature, causing the electrolyte to deteriorate. Utility Model Content
[0007] In order to solve the above technical problems, the utility model provides a continuous production system for electrolyte, which adopts a combination of a tubular reactor and a temperature regulating device. The temperature regulating device adjusts the solvent in the tubular reactor so that the solute can be dissolved at an appropriate temperature. Combined with the highly mixed characteristics of the tubular reactor, the solute dissolution rate can be increased, thereby reducing the overall production time of the electrolyte production.
[0008] The technical solution of the utility model is:
[0009] A continuous production system for electrolyte, comprising a solvent supply unit, a mixing unit, and an electrolyte collection unit;
[0010] The mixing unit includes a tubular reactor, a temperature regulating device for controlling the temperature of the solvent in the tubular reactor, and a feeding module for adding solutes into the tubular reactor; the solvent in the tubular reactor comes from a solvent supply unit; and the material of the tubular reactor is output to an electrolyte collection unit.
[0011] The core of this case is to control the temperature of the tubular reactor so that the solute can be dissolved at a suitable temperature, thereby improving the production effect of the electrolyte.
[0012] Specifically, in actual production, the solutes can be graded according to the dissolution rate and / or the difficulty of dissolution; solutes of different solubility grades are introduced into a tubular reactor containing a solvent in batches for mixing and dissolution, thereby preparing the electrolyte; the classification can be performed according to the dissolution rate of the solute, or according to the difficulty of dissolution of the solute, or according to a comprehensive consideration of the dissolution rate and the difficulty of dissolution of the solute; the definition of dissolution rate refers to the dissolution time of the solute at the same temperature; the shorter the dissolution time, the faster the dissolution rate; the definition of dissolution difficulty refers to whether the solute is soluble, insoluble or partially soluble at the same temperature; if it is soluble, it has a low dissolution difficulty, if it is insoluble, it has a high dissolution difficulty, and if it is partially soluble, it has a medium dissolution difficulty; partially soluble generally refers to the saturated concentration in a certain volume of solvent at a set temperature; the larger the saturated concentration, the lower the dissolution difficulty of the partially soluble solute.
[0013] Therefore, the solutes can be classified by considering the dissolution rate and the difficulty of dissolution;
[0014] Taking electrolyte production as an example, under the condition of 20℃, vinylene carbonate has very poor solubility and its dissolution rate is very slow. Therefore, the solubility level of this additive can be defined as level 1. Even under the condition of 70℃, it takes a long time to dissolve. This article defines it as a high-temperature additive.
[0015] In the electrolyte production process, the factor that most affects the electrolyte production speed is that the high-temperature additive dissolves too slowly, and the solvent needs to be raised to a higher temperature to dissolve. The system of the utility model can dissolve the high-temperature additive at a temperature suitable for it, and combined with the highly mixed characteristics of the tubular reactor, mixing can be achieved within seconds. The dissolution of the high-temperature additive does not affect the dissolution of other lithium salts and additives that are easily deteriorated at room temperature or high temperature, thereby achieving an increase in the overall production speed.
[0016] The above scheme generally has three specific implementation forms:
[0017] Implementation form 1: There is one tubular reactor and one or more feeding modules.
[0018] If there are solutes with three solubility levels in the electrolyte, three feeding modules are required; the three feeding modules are located on the same tubular reactor. During the production process, the solvent is divided into three parts. When the first part of the solvent is input, the temperature is controlled at 70°C, and the solute with the highest solubility level (the most insoluble and slowest to dissolve) is added. Then the second part of the solvent is input, the temperature is controlled at 40°C, and the solute with a medium solubility level is added. Finally, the third part of the solvent is input, the remaining solutes are added, and the temperature is controlled at 10°C. The final electrolyte is a solvent mixed with three different solutes.
[0019] Implementation form 2: The tubular reactors are connected in parallel, and the inlet of each tubular reactor is connected to the solvent supply unit; the outlet of each tubular reactor is connected to the electrolyte collection unit.
[0020] Taking the above three solubility levels of solutes as an example, the solvent is also divided into three parts, which are respectively introduced into different tubular reactors, and the solutes of different solubility levels are added into the corresponding tubular reactors through the feeding module; finally, the solutions of different tubular reactors are combined to obtain the electrolyte.
[0021] Implementation form 3: The tubular reactors are connected in series, the inlet of the first tubular reactor is connected to the solvent supply unit; and the outlet of the last tubular reactor is connected to the electrolyte collection unit.
[0022] Taking the above three solubility levels of solutes as an example, the solvent does not need to be divided into several parts. The solvent is input from the first tubular reactor and passes through multiple tubular reactors in sequence. The solute with the highest solvent level is added to the first tubular reactor, and so on, to complete the addition of the solute to the solvent. In this process, the temperature is controlled by gradually lowering the temperature from the front to the back, so as to achieve the dissolution of solvents of different solubility levels and finally prepare an electrolyte.
[0023] In addition to the above three methods, a parallel-series hybrid method can also be used, and its specific principle is a combination of the above implementation forms 2 and 3.
[0024] It should be noted that the above scheme is not limited to three levels of solubility, and in practical applications, multiple levels can be used. For example, in general, depending on the solubility level of the solute, the number of tubular reactors can be 2-8;
[0025] In the above-mentioned continuous production system of electrolyte, a temperature regulating device is provided at the outlet of the tubular reactor directly connected to the electrolyte collecting unit.
[0026] In the above-mentioned continuous production system of electrolyte, the aspect ratio of the tubular reactor is 15-40, and the tube length is 40-900cm. In actual production, the specifications of the tubular reactor are designed according to the material characteristics to control the material to be dissolved in a shorter time, especially to enable the high-temperature additive to be dissolved in a shorter time; in the experimental verification process of the utility model, it is confirmed that the conventional high-temperature additives in the field can be well dissolved under the conditions of the aspect ratio of the tubular reactor used in 15-40 and the tube length of 70-400cm; technical personnel in this field should flexibly adjust the equipment parameters according to the actual situation.
[0027] In the above-mentioned continuous production system of electrolyte, the solvent supply unit includes a solvent storage tank and a pump which are connected in sequence, and the pump is connected to a temperature regulating device.
[0028] In the above-mentioned continuous production system of electrolyte, the temperature regulating device is one or more of a heat exchanger, a heater, and a refrigerator.
[0029] In the above-mentioned continuous production system of electrolyte, the feeding module is one or both of a pump and a powder feeder. In practical applications, the feeding drive of the powder feeder can be in the form of an auger, extrusion based on gas pressure, etc. It is preferred to feed by an auger to improve the feeding accuracy. The pump can be selected as a metering pump to improve the feeding accuracy.
[0030] One of the above technical solutions of the utility model has at least one of the following advantages or beneficial effects:
[0031] The system combines a tubular reactor with a temperature control device. The temperature control device is used to adjust the solvent in the tubular reactor so that the solute can be dissolved at an appropriate temperature. Combined with the highly mixed characteristics of the tubular reactor, the solute dissolution rate can be increased, thereby reducing the overall production time of the electrolyte production. BRIEF DESCRIPTION OF THE DRAWINGS
[0032] Figure 1This is a schematic diagram of the structure of Embodiment 1 of the present utility model;
[0033] Figure 2 This is a schematic diagram of the structure of Embodiment 2 of the present utility model;
[0034] Figure 3 This is a schematic diagram of the structure of Embodiment 3 of the present utility model;
[0035] Figure 4 This is a schematic diagram of the structure of Embodiment 4 of the present utility model;
[0036] Figure 5 This is a schematic diagram of the structure of Example 5 of the present utility model. DETAILED DESCRIPTION
[0037] The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments in the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.
[0038] Example 1
[0039] See also Figure 1 , a continuous production system for electrolyte, comprising a solvent storage tank 1, a pump 2, a heater 3, a feed pipe 4, a first tubular reactor 5, a first heat exchanger 6, a second tubular reactor 7, a second heat exchanger 8, a buffer tank 9, and a loading pump 10 connected in sequence;
[0040] The first additive (described in detail in the application examples) can be added to the feed pipe or to the first tubular reactor.
[0041] The relevant actual equipment parameters are described in detail in the subsequent embodiments;
[0042] Additional explanation: The tubular reactors involved in all embodiments of the present invention are empty tubes without fillers.
[0043] The feeding modules on the first tubular reactor 5 and the second tubular reactor 7 have different options due to the different states of additives in different formulations, which can be seen in the subsequent application examples 1-3.
[0044] Example 2
[0045] See also Figure 2, a continuous production system for electrolyte, comprising a solvent storage tank 1, a pump 2, a heater 3, a feed pipe 4, a first tubular reactor 5, a first heat exchanger 6, a second tubular reactor 7, a second heat exchanger 8, a third tubular reactor 9 and a third heat exchanger 10, a buffer tank 11, and a loading pump 12 connected in sequence;
[0046] The first additive (described in detail in the application examples) can be added to the feed pipe or to the first tubular reactor.
[0047] The relevant actual equipment parameters are described in detail in the subsequent embodiments.
[0048] The feeding modules on the first tubular reactor 5, the second tubular reactor 7 and the third tubular reactor 9 have different options due to the different states of additives in different formulations, which can be seen in the subsequent application examples 4-7 for details.
[0049] Example 3
[0050] See also Figure 3 , a continuous production system of electrolyte, comprising a solvent storage tank 1, a pump 2, a heater 3, a first tubular reactor 5, a first heat exchanger 6, a buffer tank 7, and a loading pump 8 connected in sequence;
[0051] In addition, it also includes a second heat exchanger 9, a second tubular reactor 10, and a third heat exchanger 11 connected in sequence; and a fourth heat exchanger 12, a third tubular reactor 13, and a fifth heat exchanger 4 connected in sequence;
[0052] The outlet of the third heat exchanger 11 and the outlet of the fifth heat exchanger 4 are connected to the cache tank 7;
[0053] The inlet of the second heat exchanger 9 and the inlet of the fourth heat exchanger 12 are connected to the outlet of the pump 2 .
[0054] A first powder feeder 15 for adding solid high-temperature additives is arranged near the inlet of the first tubular reactor 5; a second powder feeder 16 for adding lithium salt powder is arranged near the inlet of the second tubular reactor 10; and a metering pump 17 for adding liquid low-temperature additives is arranged near the inlet of the third tubular reactor 13.
[0055] During the production process, if there are three solubility levels of solutes in the electrolyte (respectively, high-temperature additives, lithium salts, and low-temperature additives), during the production process, the solvent is divided into three parts, and the three parts of the solvent are simultaneously introduced into the first tubular reactor 5 (the solvent temperature is controlled to 70°C by the heater 3), the second tubular reactor 10 (the solvent temperature is controlled to 40°C by the second heat exchanger 9), and the third tubular reactor 13 (the solvent temperature is controlled to 10°C by the fourth heat exchanger 12) through a pump, and the high-temperature additive, lithium salt, and low-temperature additive are respectively added to the corresponding tubular reactor through the corresponding feeding modules. After the solute and the solvent are mixed, the output solvent is controlled to be 10°C through the first heat exchanger 6, the third heat exchanger 11, and the fifth heat exchanger 4, and is introduced into the buffer tank 7 to obtain the electrolyte.
[0056] Example 4
[0057] See also Figure 4 A continuous production system for electrolyte includes a solvent storage tank 1, a pump 2, a first heat exchanger 3, a tubular reactor 5, a second heat exchanger 6, a buffer tank 7, and a loading pump 8 connected in sequence; the tubular reactor 5 is provided with a first powder feeder 9 for adding solid high-temperature additives, a second powder feeder 10 for adding lithium salt powder, and a metering pump 4 for adding liquid low-temperature additives.
[0058] If there are three solutes with different solubility levels in the electrolyte (high-temperature additives, lithium salts, and low-temperature additives), the solvent is divided into three parts during the production process. When the first solvent is input, the first heat exchanger 3 controls the temperature of the solvent to 70°C, and adds a high-temperature additive with the highest solubility level (the most difficult to dissolve and the slowest to dissolve). At this time, the second heat exchanger 6 controls the solvent output temperature to 10°C. Then, the second solvent is input, the temperature is controlled to 40°C, and a lithium salt with a medium solubility level is added. At this time, the second heat exchanger 6 controls the solvent output temperature to 10°C. Finally, the third solvent is input, a low-temperature additive is added, and the temperature is controlled to 10°C. The electrolyte finally obtained is a solvent mixed with three different solutes.
[0059] Example 5
[0060] See also Figure 5 , a continuous production system for electrolyte, comprising a solvent storage tank 1, a pump 2, a heater 3, a feed pipe 4, a first tubular reactor 5, a first heat exchanger 6, a second tubular reactor 7, a second heat exchanger 8, a third tubular reactor 9, a third heat exchanger 10, a fourth tubular reactor 13, a fourth heat exchanger 14, a fifth tubular reactor 15, a fifth heat exchanger 16, a sixth tubular reactor 17, a sixth heat exchanger 18, a buffer tank 11, and a loading pump 12, which are connected in sequence; the first tubular reactor 5, the second tubular reactor 7, the third tubular reactor 9, the fourth tubular reactor 13, the fifth tubular reactor 15, and the sixth tubular reactor 17 are all connected with a feeding module;
[0061] The feed pipe 4 is connected to the inlets of the second tubular reactor 7, the third tubular reactor 9, the fourth tubular reactor 13, and the fifth tubular reactor 15 respectively through the first branch pipe 19;
[0062] The first heat exchanger 6 , the second heat exchanger 8 , the third heat exchanger 10 , the fourth heat exchanger 14 , and the fifth heat exchanger 16 are connected to the cache tank 11 through the second branch pipe 20 , respectively.
[0063] The system has at least three switching modules (according to the direction of fluid flow):
[0064] Single system mode: solvent storage tank 1, pump 2, heater 3, feed pipe 4, first tubular reactor 5, first heat exchanger 6, second tubular reactor 7, second heat exchanger 8, third tubular reactor 9, third heat exchanger 10, fourth tubular reactor 13, fourth heat exchanger 14, fifth tubular reactor 15, fifth heat exchanger 16, sixth tubular reactor 17, sixth heat exchanger 18, buffer tank 11, loading pump 12;
[0065] Dual system mode: solvent storage tank 1, pump 2, heater 3, feed pipe 4, first tubular reactor 5, first heat exchanger 6, second tubular reactor 7, second heat exchanger 8, third tubular reactor 9, third heat exchanger 10, buffer tank 11, loading pump 12; (system 1)
[0066] Solvent storage tank 1, pump 2, heater 3, feed pipe 4, fourth tubular reactor 13, fourth heat exchanger 14, fifth tubular reactor 15, fifth heat exchanger 16, sixth tubular reactor 17, sixth heat exchanger 18, buffer tank 11, loading pump 12; (system 2)
[0067] Three-system mode: solvent storage tank 1, pump 2, heater 3, feed pipe 4, first tubular reactor 5, first heat exchanger 6, second tubular reactor 7, second heat exchanger 8, buffer tank 11, loading pump 12; (system 1)
[0068] Solvent storage tank 1, pump 2, heater 3, feed pipe 4, third tubular reactor 9, third heat exchanger 10, fourth tubular reactor 13, fourth heat exchanger 14, buffer tank 11, loading pump 12; (system 2)
[0069] Solvent storage tank 1, pump 2, heater 3, feed pipe 4, fifth tubular reactor 15, fifth heat exchanger 16, sixth tubular reactor 17, sixth heat exchanger 18, buffer tank 11, loading pump 12; (system 3)
[0070] The switching of the above modes is performed by correspondingly switching the first branch pipe 19 and the second branch pipe 20 .
[0071] Application Example 1
[0072] The formula of the electrolyte processed in this application example is:
[0073] The first additive: 1,3-propane sultone and fluoroethylene carbonate, each accounting for 1% of the total weight of the electrolyte;
[0074] Lithium salt: lithium hexafluorophosphate, accounting for 12.5% of the total mass of the electrolyte;
[0075] The rest is solvent, which is a mixture of ethylene carbonate, ethyl methyl carbonate and diethyl carbonate in a mass ratio of 1:2:2.
[0076] The system of Example 1 is used for production;
[0077] The hardware parameters and process of the system in Example 1 refer to Table 1;
[0078] Table 1 Hardware parameters and process table
[0079]
[0080] The whole system maintains a slight positive pressure of 5 bar; the liquid residence time in the first tubular reactor is 1.43 seconds; the lithium salt is pre-dispersed and dissolved in 40wt% of the solvent (lithium salt solution is the most common material in factory production. In most scenarios, it is prepared in large quantities and taken as needed); the remaining 60wt% of the solvent is injected through the first tubular reactor. 1,3-propane sultone is added through the inlet of the first tubular reactor using a powder feeder, and fluoroethylene carbonate is added through the inlet of the first tubular reactor by a metering pump.
[0081] The electrolyte produced in this embodiment was tested to have no visible solid impurities and all materials were mixed evenly.
[0082] The equipment of this embodiment has been further improved in production capacity to 10 T / h. The solvent is fully injected through the first tubular reactor, and the lithium salt is added to the second tubular reactor using a powder feeder. The liquid residence time in the first tubular reactor is 0.6 s. After testing, no solid impurities are visually visible, and the materials are mixed evenly.
[0083] Application Example 2
[0084] The formula of the electrolyte processed in this application example is:
[0085] The first additive: vinylene carbonate, which accounts for 2% of the total weight of the electrolyte;
[0086] Lithium salt: lithium hexafluorophosphate, accounting for 11% of the total mass of the electrolyte;
[0087] The rest is solvent, which is a mixture of ethylene carbonate, ethyl methyl carbonate and diethyl carbonate in a mass ratio of 1:2:4.
[0088] The system of Example 1 is used for production;
[0089] The hardware parameters and process of the system in Example 1 refer to Table 2;
[0090] Table 2 Hardware parameters and process table
[0091]
[0092] The whole system maintains a slight positive pressure of 5 bar; the liquid residence time in the first tubular reactor is 0.89 s; the lithium salt is added to the second tubular reactor by a powder feeder; the solvent is injected through the first tubular reactor. The first additive is added through the inlet of the first tubular reactor by a metering pump.
[0093] The electrolyte produced in this embodiment was tested to have no visible solid impurities and all materials were mixed evenly.
[0094] Application Example 3
[0095] The formula of the electrolyte processed in this application example is:
[0096] The first additive: vinylene carbonate, which accounts for 1% of the total weight of the electrolyte;
[0097] Lithium salt: lithium hexafluorophosphate, accounting for 13% of the total mass of the electrolyte;
[0098] The rest is solvent, which is a mixture of ethylene carbonate and ethyl methyl carbonate in a mass ratio of 1:1.
[0099] The system of Example 1 is used for production;
[0100] The hardware parameters and process of the system in Example 1 refer to Table 3;
[0101] Table 3 Hardware parameters and process table
[0102]
[0103] The whole system is maintained at a slight positive pressure of 5 bar; the liquid residence time in the first tubular reactor is 1.8 s; the lithium salt is pre-dispersed and dissolved with 15 wt% of solvent; the remaining 85 wt% of solvent is injected through the first tubular reactor. The first additive is added through the inlet of the first tubular reactor using a metering pump.
[0104] The electrolyte produced in this embodiment was tested to have no visible solid impurities and all materials were mixed evenly.
[0105] Application Example 4
[0106] The formula of the electrolyte processed in this application example is:
[0107] The first additive: vinylene carbonate and 1,3-propane sultone, each accounting for 1% of the total weight of the electrolyte;
[0108] The second additive: vinyl sulfate, which accounts for 1% of the total weight of the electrolyte;
[0109] Lithium salt: lithium hexafluorophosphate, accounting for 12.5% of the total mass of the electrolyte;
[0110] The rest is solvent, which is a mixture of ethylene carbonate, ethyl methyl carbonate and diethyl carbonate in a mass ratio of 1:2:2.
[0111] The system of Example 2 is used for production;
[0112] The hardware parameters and process of the system in Example 2 refer to Table 4;
[0113] Table 4 Hardware parameters and process table
[0114]
[0115] The whole system is maintained at a slight positive pressure of 5 bar; the liquid residence time in the first tubular reactor is 1.85 seconds; the lithium salt is added to the second tubular reactor by a powder feeder; 95 wt% of the solvent is injected through the first tubular reactor. 1,3-propane sultone is added through the inlet of the first tubular reactor by a powder feeder, and vinylene carbonate is added through the inlet of the first tubular reactor by a metering pump. Vinyl sulfate is pre-dispersed and dissolved in 5 wt% of the solvent and then injected into the inlet of the third tubular reactor by a metering pump.
[0116] The electrolyte produced in this embodiment was tested to have no visible solid impurities and all materials were mixed evenly.
[0117] Application Example 5
[0118] The formula of the electrolyte processed in this application example is:
[0119] The first additive: vinylene carbonate and fluoroethylene carbonate, each accounting for 1.5% of the total weight of the electrolyte;
[0120] The second additive: methylene methane disulfonate, which accounts for 2% of the total weight of the electrolyte;
[0121] Lithium salt: lithium hexafluorophosphate, accounting for 12.5% of the total mass of the electrolyte;
[0122] The rest is a solvent, which is a mixture of ethylene carbonate, ethyl methyl carbonate and diethyl carbonate in a mass ratio of 1:1:1.
[0123] The system of Example 2 is used for production;
[0124] The hardware parameters and process of the system in Example 2 refer to Table 5;
[0125] Table 5 Hardware parameters and process table
[0126]
[0127] The whole system was maintained at a slight positive pressure of 5 bar; the liquid residence time in the first tubular reactor was 1.89 s; the lithium salt was added to the second tubular reactor using a powder feeder; the solvent was injected through the first tubular reactor. Vinylene carbonate and fluoroethylene carbonate were added through the inlet of the first tubular reactor by a metering pump. Methylene methane disulfonate was injected into the inlet of the third tubular reactor through a powder feeder.
[0128] The electrolyte produced in this embodiment was tested to have no visible solid impurities and all materials were mixed evenly.
[0129] Application Example 6
[0130] The same as in Application Example 5, except for the differences shown in Table 6;
[0131] Table 6 Hardware parameters and process table
[0132]
[0133] The whole system is maintained at a slight positive pressure of 5 bar; the liquid residence time in the first tubular reactor is 1.2 seconds; the lithium salt is added to the second tubular reactor using a powder feeder; the solvent is injected through the first tubular reactor. Vinylene carbonate and fluoroethylene carbonate are added through the inlet of the first tubular reactor by a metering pump. Methylene methane disulfonate is injected into the inlet of the third tubular reactor through a powder feeder.
[0134] The electrolyte produced in this embodiment was tested to have no visible solid impurities and all materials were mixed evenly.
[0135] Application Example 7
[0136] The same as in Application Example 5, except for the differences shown in Table 7;
[0137] Table 7 Hardware parameters and process table
[0138]
[0139] The whole system is maintained at a slight positive pressure of 5 bar; the liquid residence time in the first tubular reactor is 2.8 seconds; the lithium salt is added to the second tubular reactor by a powder feeder; the solvent is injected through the first tubular reactor. Vinylene carbonate and fluoroethylene carbonate are added through the inlet of the first tubular reactor by a metering pump. Methylene methane disulfonate is injected into the inlet of the third tubular reactor through a powder feeder.
[0140] The electrolyte produced in this embodiment was tested to have no visible solid impurities and all materials were mixed evenly.
[0141] Through the above-mentioned embodiments and application examples, it can be seen that the production efficiency is significantly improved by using the system and process of the utility model, and the dissolution time of the first additive is effectively shortened. At the same time, the multi-stage series / parallel tubular reactor and multi-stage cooling method can ensure the full dissolution of the material without causing the material to deteriorate. The system and process will hardly produce dripping, and the waste gas generated is also very small, reducing the number of production workers from 3 to 1.
[0142] Although the embodiments of the present invention have been shown and described, those skilled in the art will appreciate that various changes, modifications, substitutions and variations may be made to the embodiments without departing from the principles and spirit of the present invention, and that the scope of the present invention is defined by the claims and their equivalents.
Claims
1. A continuous production system for electrolyte, characterized in that: It includes a solvent supply unit, a mixing unit, and an electrolyte collection unit; The mixing unit includes a tubular reactor, a temperature regulating device for controlling the temperature of the solvent in the tubular reactor, and a feeding module for adding solutes into the tubular reactor; the solvent in the tubular reactor comes from a solvent supply unit; and the material of the tubular reactor is output to an electrolyte collection unit.
2. The continuous production system of electrolyte according to claim 1, characterized in that: The number of the tubular reactor is one, and the number of the feeding modules is one or more.
3. The continuous production system of electrolyte according to claim 1, characterized in that: The number of the tubular reactors is not less than 2; the tubular reactors are connected in parallel or in series, or the tubular reactors are arranged in a mixed manner of parallel and series.
4. The continuous production system of electrolyte according to claim 3, characterized in that: The tubular reactors are connected in parallel, and the inlet of each tubular reactor is connected to the solvent supply unit; and the outlet of each tubular reactor is connected to the electrolyte collection unit.
5. The continuous production system of electrolyte according to claim 3, characterized in that: The tubular reactors are connected in series, with the inlet of the first tubular reactor connected to the solvent supply unit; and the outlet of the last tubular reactor connected to the electrolyte collection unit.
6. The continuous production system of electrolyte according to any one of claims 3 to 5, characterized in that: The outlet of the tubular reactor directly connected to the electrolyte collection unit is provided with a temperature regulating device.
7. The continuous production system of electrolyte according to claim 1, characterized in that: The aspect ratio of the tubular reactor is 15-40, and the tube length is 40-900 cm.
8. The continuous production system of electrolyte according to claim 1, characterized in that: The solvent supply unit comprises a solvent storage tank and a pump which are connected in sequence, and the pump is connected to a temperature regulating device.
9. The continuous production system of electrolyte according to claim 1, characterized in that: The number of the tubular reactors is 2 to 8.
10. The continuous production system of electrolyte according to claim 1, characterized in that: The temperature regulating device is one or more of a heat exchanger, a heater, and a refrigerator; The feeding module is one or both of a pump and a powder feeder.