CN212378581U - Wet process lithium battery diaphragm waste heat utilization system - Google Patents
Wet process lithium battery diaphragm waste heat utilization system Download PDFInfo
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- CN212378581U CN212378581U CN202022151016.6U CN202022151016U CN212378581U CN 212378581 U CN212378581 U CN 212378581U CN 202022151016 U CN202022151016 U CN 202022151016U CN 212378581 U CN212378581 U CN 212378581U
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- heat exchanger
- dichloromethane
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Abstract
The utility model relates to a wet process lithium cell diaphragm waste heat utilization system, including header tank, circulating pump, heater, first heat exchanger and second heat exchanger. The water collecting tank is used for collecting waste heat, the heater is used for liquid heating, the circulating pump is used for connecting water collecting tank and heater, first heat exchanger sets up in dichloromethane liquid recovery stage, provides the required heat of dichloromethane liquid recovery stage rectification, and the second heat exchanger sets up in the gaseous recovery stage of dichloromethane, provides the required comdenstion water of the gaseous recovery stage of dichloromethane. The utility model discloses to the waste heat make full use of in the diaphragm production process, for dichloromethane liquid recovery device provides the heat source, reduce the use amount of high temperature steam, reduce the cooling water quantity in the gaseous recovery process of dichloromethane simultaneously to reach energy saving and consumption reduction's purpose, reduce the diaphragm cost, improve product competitiveness.
Description
Technical Field
The utility model belongs to wet process lithium battery diaphragm waste heat recovery utilizes the field, specifically relates to a waste heat utilization system in wet process lithium battery diaphragm extract recovery process.
Background
The wet-process lithium battery diaphragm production process mainly comprises the working procedures of feeding, extruding, sheet casting, double-drawing, extracting, transverse-drawing, rolling and the like. After the cast sheet is stretched synchronously in two directions, the polyolefin molecular chain of the diaphragm material is stretched in different degrees in the longitudinal direction and the transverse direction, and white oil is used as a pore-forming agent and is uniformly distributed in the molecular chain. In the extraction process, dichloromethane is used as an extracting agent to extract the white oil, so that the separation of polyolefin and the white oil in the diaphragm is realized, and the diaphragm forms a compact and uniform microporous structure.
The heat source input in the existing wet-method lithium battery diaphragm production process is mainly high-temperature water vapor, a large amount of waste heat is generated after heat exchange of the high-temperature water vapor, if the waste heat is not fully utilized, energy waste can be caused, and the production cost of the product is improved. The extraction liquid can be changed into mixed liquid of white oil and dichloromethane after the diaphragm extraction process, and the dichloromethane solution is separated from the mixed liquid of white oil and dichloromethane at present and is convenient to recycle. The separation and recovery principle of the mixed liquid of the white oil and the dichloromethane at the present stage is to carry out rectification according to the difference of the boiling points of the two substances. The rectification process needs heat, and if the waste heat generated in the diaphragm production process is applied to dichloromethane liquid recovery, the cost is reduced. The extracted diaphragm can be attached with partial dichloromethane liquid, and a large amount of dichloromethane gas can be generated when the extraction liquid is dried and removed in the transverse pulling stage. The dichloromethane gas recovery method mainly comprises the steps of carbon fiber adsorption, desorption by using steam, and direct condensation by using cooling water after desorption. If the temperature-reduced aqueous solution after the dichloromethane liquid recovery stage is applied to the condensation stage of dichloromethane gas recovery, the cost is reduced.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, the utility model provides a wet process lithium battery diaphragm waste heat utilization system to the waste heat make full use of that produces in the wet process lithium battery diaphragm production technology, can reduce the quantity of heat use in dichloromethane liquid recovery stage and the quantity of dichloromethane gas recovery stage cooling water, reduces product manufacturing cost.
The utility model provides a technical problem can adopt following technical scheme to realize:
a wet-process lithium battery diaphragm waste heat utilization system comprises a water collecting tank, a circulating pump, a heater, a first heat exchanger and a second heat exchanger. The water collecting tank is used for collecting waste heat, the heater is used for liquid heating, the circulating pump is used for connecting water collecting tank and heater, first heat exchanger sets up in dichloromethane liquid recovery stage, provides the required heat of dichloromethane liquid recovery stage rectification, and the second heat exchanger sets up in the gaseous recovery stage of dichloromethane, provides the required comdenstion water of the gaseous recovery stage of dichloromethane. The water collecting tank, the circulating pump, the heater, the first heat exchanger and the second heat exchanger are sequentially connected through pipelines.
The waste heat comes from any one of the procedures of double-pulling, transverse-pulling and methylene dichloride steam desorption.
As a preferred scheme of the utility model, the first heat exchanger is a falling film evaporator, the heat exchange area is 80-150 square meters, and the material is stainless steel.
As a preferred scheme of the utility model, circulating pump flow is 10-30m dry labor/h.
As a preferred scheme of the utility model, the heating mode of the heater is steam heating, and the heating temperature range is 60-100 ℃.
As a preferred embodiment of the present invention, the heater control mode is a programmable logic controller control.
As a preferred scheme of the utility model, the heat exchange area of the second heat exchanger is 80-120 square meters and the material is stainless steel.
The utility model has the advantages that: the waste heat make full use of to producing in the lithium cell diaphragm production process provides the heat source for dichloromethane liquid recovery unit, provides the cooling water for dichloromethane gaseous state recovery unit simultaneously, has reduced the quantity of high temperature steam and comdenstion water. Realizes energy saving and consumption reduction, and reduces the production cost of products.
Drawings
Fig. 1 is the utility model relates to a wet process lithium battery diaphragm waste heat utilization system schematic diagram.
Fig. 2 is a schematic diagram of a wet lithium battery separator production process.
FIG. 3 is a schematic diagram of a methylene chloride gas recovery process.
Detailed Description
The present invention will now be further described with reference to fig. 1.
As shown in figure 1, the utility model relates to a wet process lithium battery diaphragm waste heat utilization system includes header tank, circulating pump, heater, first heat exchanger and second heat exchanger. The water collecting tank is used for collecting waste heat, the heater is used for liquid heating, the circulating pump is used for connecting water collecting tank and heater, first heat exchanger sets up in dichloromethane liquid recovery stage, provides the required heat of dichloromethane liquid recovery stage rectification, and the second heat exchanger sets up in the gaseous recovery stage of dichloromethane, provides the required comdenstion water of the gaseous recovery stage of dichloromethane. The water collecting tank, the circulating pump, the heater, the first heat exchanger and the second heat exchanger are sequentially connected through pipelines.
The waste heat comes from any one of the procedures of double-pulling, transverse-pulling and methylene dichloride steam desorption.
The first heat exchanger is a falling film evaporator, the heat exchange area is 80-150 square meters, and the material is stainless steel.
And the flow rate of the circulating pump is 10-30 m/h.
The heating mode of the heater is steam heating, and the heating temperature range is 60-100 ℃.
The heater control mode is controlled by a programmable logic controller.
The heat exchange area of the second heat exchanger is 80-120 square meters and the material is stainless steel.
Example 1
As shown in figure 2, the diaphragm double-pulling process generates high-temperature steam waste heat, and condensed water with the temperature of 60-70 ℃ is formed. Then the mixture enters a water collecting tank shown in figure 1 for collection, and is sent to a first heat exchanger through a circulating pump and a heater, wherein the first heat exchanger is a falling film evaporator, the heat exchange area is 80 square meters, and the material is stainless steel. When the temperature of the circulating water is lower than 60 ℃, the heater is controlled by the programmable logic controller, and the control valve is started to heat the circulating water by high-temperature steam. And the mixed liquid of the white oil and the dichloromethane is rectified by the first heat exchanger, so that the dichloromethane liquid is recovered. Circulating water subjected to heat exchange by the first heat exchanger enters a second heat exchanger, the heat exchange area is 80 square meters, desorption gas in the dichloromethane gas recovery device is condensed, and gaseous dichloromethane is changed into liquid for recovery. Under the process temperature, the high-temperature steam is saved by the dichloromethane liquid recovery device by 1.2t/h, and the cooling water is saved by the dichloromethane gas recovery device by 100m for carrying out high-temperature steam production/h.
Example 2
As shown in figure 2, the diaphragm transverse drawing process generates high-temperature steam waste heat, and condensed water with the temperature of 70-75 ℃ is formed. Then the mixture enters a water collecting tank shown in figure 1 for collection, and is sent to a first heat exchanger through a circulating pump and a heater, wherein the first heat exchanger is a falling film evaporator, the heat exchange area is 120 square meters, and the material is stainless steel. When the temperature of the circulating water is lower than 60 ℃, the heater is controlled by the programmable logic controller, and the control valve is started to heat the circulating water by high-temperature steam. And the mixed liquid of the white oil and the dichloromethane is rectified by the first heat exchanger, so that the dichloromethane liquid is recovered. Circulating water subjected to heat exchange by the first heat exchanger enters a second heat exchanger, the heat exchange area is 100 square meters, desorption gas in the dichloromethane gas recovery device is condensed, and gaseous dichloromethane is changed into liquid for recovery. Under the process temperature, the high-temperature steam is saved by the dichloromethane liquid recovery device by 2t/h, and the cooling water is saved by the dichloromethane gas recovery device by 130m during the high-temperature vapor distillation.
Example 3
As shown in fig. 3, the steam desorption stage of the dichloromethane gas recovery generates high-temperature steam waste heat, and the desorption gas temperature is 110-130 ℃. The high-temperature steam waste heat exchanges heat with circulating water, the circulating water enters a water collecting tank shown in figure 1 after heat exchange and is collected, the circulating water and a heater are used for feeding the circulating water into a first heat exchanger, the first heat exchanger is a falling film evaporator, the heat exchange area is 150 square meters, and the material is stainless steel. When the temperature of the circulating water is lower than 60 ℃, the heater is controlled by the programmable logic controller, and the control valve is started to heat the circulating water by high-temperature steam. And the mixed liquid of the white oil and the dichloromethane is rectified by the first heat exchanger, so that the dichloromethane liquid is recovered. Circulating water subjected to heat exchange by the first heat exchanger enters a second heat exchanger, the heat exchange area is 120 square meters, desorption gas in the dichloromethane gas recovery device is condensed, and gaseous dichloromethane is changed into liquid for recovery. Under the process temperature, the high-temperature steam is saved by the dichloromethane liquid recovery device by 2.5t/h, and the cooling water is saved by the dichloromethane gas recovery device by 150m for carrying out high-temperature steam production/h.
The following table 1 shows statistics of the high-temperature steam and cooling water saving amount after the wet lithium battery diaphragm waste heat utilization system is utilized.
TABLE 1 statistical table of high-temperature steam and cooling water saving
| Source of waste heat | Waste heat of double-drawing process | Residual heat of horizontal drawing process | Steam desorption waste heat |
| High temperature steam saving quantity (t/h) | 1.2 | 2 | 2.5 |
| Cooling water saving amount (m/h) | 100 | 130 | 150 |
From the table above, the utilization of the residual heat of the diaphragm in the double-pulling, transverse-pulling and dichloromethane gas recovery steam desorption stages saves the use amount of a large amount of high-temperature steam and cooling water in the diaphragm production process, reduces the production cost of the diaphragm and improves the competitiveness of the product.
The above embodiments are only specific examples for further detailed explanation of the technical solution of the present invention, and the present invention is not limited thereto. All modifications, equivalents, improvements and the like which are made within the scope of the present disclosure are intended to be included within the scope of the present disclosure.
Claims (6)
1. The utility model provides a wet process lithium cell diaphragm waste heat utilization system which characterized in that: the waste heat recovery device comprises a water collecting tank, a circulating pump, a heater, a first heat exchanger and a second heat exchanger, wherein the water collecting tank is used for collecting waste heat, the heater is used for heating liquid, and the circulating pump is used for connecting the water collecting tank and the heater; the first heat exchanger is arranged in a dichloromethane liquid recovery stage and provides heat required by rectification in the dichloromethane liquid recovery stage; the second heat exchanger is arranged in a dichloromethane gas recovery stage and provides condensed water required by the dichloromethane gas recovery stage; the water collecting tank, the circulating pump, the heater, the first heat exchanger and the second heat exchanger are sequentially connected through pipelines.
2. The wet process lithium battery diaphragm waste heat utilization system of claim 1, wherein the first heat exchanger is a falling film evaporator having a heat transfer area of 80 to 150 square meters and is made of stainless steel.
3. The wet lithium battery diaphragm waste heat utilization system of claim 1, wherein the circulation pump flow rate is 10-30 m/h.
4. The wet lithium battery diaphragm waste heat utilization system of claim 1, wherein the heater is heated by steam at a temperature ranging from 60 ℃ to 100 ℃.
5. The wet lithium battery diaphragm waste heat utilization system of claim 4, wherein the heater control mode is programmable logic controller control.
6. The wet process lithium battery diaphragm waste heat utilization system of claim 1, wherein the second heat exchanger has a heat exchange area of 80 to 120 square meters and is made of stainless steel.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2020211337630 | 2020-06-18 | ||
| CN202021133763 | 2020-06-18 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN212378581U true CN212378581U (en) | 2021-01-19 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202022151016.6U Active CN212378581U (en) | 2020-06-18 | 2020-09-27 | Wet process lithium battery diaphragm waste heat utilization system |
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| CN (1) | CN212378581U (en) |
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- 2020-09-27 CN CN202022151016.6U patent/CN212378581U/en active Active
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20230625 Address after: No. 14, Floor 8, B2 Administrative Office Building, Changjiang Industrial Park, Songjia Town, Sanjiang New District, Yibin City, Sichuan Province, 644004 Patentee after: Zhongcai Lithium Film (Yibin) Co.,Ltd. Address before: No. 368, Shunhe West Road, Tengzhou Economic Development Zone, Zaozhuang City, Shandong Province 277500 Patentee before: SINOMA LITHIUM FILM Co.,Ltd. |
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| TR01 | Transfer of patent right |