CN212492267U - Organic solvent recovery device for drying carrier gas treatment and tail gas treatment device - Google Patents
Organic solvent recovery device for drying carrier gas treatment and tail gas treatment device Download PDFInfo
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- CN212492267U CN212492267U CN202021044419.4U CN202021044419U CN212492267U CN 212492267 U CN212492267 U CN 212492267U CN 202021044419 U CN202021044419 U CN 202021044419U CN 212492267 U CN212492267 U CN 212492267U
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Abstract
The application discloses an organic solvent recovery unit and tail gas processing apparatus for dry carrier gas handles belongs to lithium-ion battery pole piece coating drying field. An organic solvent recovery device for dry carrier gas treatment, comprising: the liquefying device is used for liquefying the organic solvent in the dry carrier gas to obtain a crude liquid organic solvent and residual carrier gas; the intensified mixing unit is used for premixing at least part of the residual carrier gas and at least part of the new absorbent to obtain mixed gas; the absorption device is used for absorbing the organic solvent in the mixed gas to obtain clean carrier gas and an absorbent rich in the organic solvent; and the refining and regenerating device is used for refining and regenerating the absorbent rich in the organic solvent and the crude liquid organic solvent to obtain a refined organic solvent and a regenerated absorbent. The organic solvent is liquefied, premixed, absorbed, refined and regenerated, so that the organic solvent is additionally recycled while the emission of the organic solvent is reduced, and meanwhile, the environmental protection requirement and economic benefit are realized.
Description
Technical Field
The application relates to the field of coating and drying of battery pole pieces, in particular to an organic solvent recovery device and a tail gas treatment device for drying and carrier gas treatment.
Background
In general, in the manufacture of a lithium battery, a positive electrode active material, a binder, and a conductive agent of the battery are mixed with an organic solvent, N-methylpyrrolidone (NMP), in a ratio to form a positive electrode slurry. And (3) uniformly applying the slurry onto a current collector by a coating process, and then evaporating and separating the solvent from the pole piece by a subsequent drying process to obtain a finished pole piece.
NMP has many advantages such as high flash point, good safety, etc., and is widely used as an organic solvent in the lithium battery manufacturing industry. However, during the drying process, the NMP is entirely converted to gas and discharged with the fan. NMP is a chemical substance that can pollute air, and if directly discharged into the air, it will cause serious environmental pollution. And is a waste of raw materials.
SUMMERY OF THE UTILITY MODEL
The application aims to provide an organic solvent recovery device and a tail gas treatment device for drying carrier gas treatment in an electrode coating and drying process. The organic solvent in the dry carrier gas is liquefied, premixed, absorbed, refined and regenerated, so that the emission of the organic solvent is reduced, the organic solvent is recycled, and meanwhile, the environmental protection requirement and economic benefit are realized.
According to a first aspect of the present application, there is provided an organic solvent recovery apparatus for dry carrier gas treatment, comprising: the liquefying device is used for liquefying the organic solvent in the dry carrier gas to obtain a crude liquid organic solvent and residual carrier gas; the intensified mixing unit is used for premixing at least part of the residual carrier gas and at least part of the new absorbent to obtain mixed gas; the absorption device is used for absorbing the organic solvent in the mixed gas to obtain clean carrier gas and an absorbent rich in the organic solvent; and the refining and regenerating device is used for refining and regenerating the absorbent rich in the organic solvent and the crude liquid organic solvent to obtain a refined organic solvent and a regenerated absorbent. Thereby realizing the recovery of the organic solvent in the dry carrier gas and leading the content of the organic solvent in the discharged gas to meet the requirement of environmental protection. According to different emission requirements of different solvents, the organic solvent recovery device can further comprise an adsorption device for adsorbing residual carrier gas volatile organic compounds so as to reduce the dosage of the absorbent and obtain better environmental protection benefits.
According to some embodiments, the organic solvent recovery apparatus further comprises a heat exchange device disposed upstream of the liquefaction device, and performing waste heat recovery on the dry carrier gas. Thereby fully recovering the waste heat and reducing the energy consumption.
Further, the heat exchange device comprises one of a shell-and-tube heat exchanger, a heat pipe heat exchanger, a runner heat exchanger or a plate heat exchanger.
In addition, the heat exchange device is also used for heating the fresh air of the drying process and/or part of the residual carrier gas serving as the internal circulation carrier gas, recycling the recovered waste heat and improving the utilization rate of energy.
According to some embodiments, the liquefaction unit comprises a chilled water unit or a booster unit and a common cooling water unit. When the freezing water is abundant, the freezing water device is used for low-temperature condensation liquefaction. Under the condition of no freezing water, the aim of liquefying with the same quality is achieved by pressurizing the carrier gas and matching with common cooling water for cooling, and the energy consumption is reduced.
According to some embodiments, the organic solvent comprises one or more of N-methylpyrrolidone, amides and derivatives thereof, furan and derivatives thereof, morpholine and derivatives thereof, other pyrrolidone derivatives, dimethylsulfoxide, wherein,
the amide and derivatives thereof include dimethylacetamide;
the furan and derivatives thereof include tetrahydrofuran and the like;
the morpholine and derivatives thereof include N-formyl morpholine;
the other pyrrolidone derivatives include N-ethyl pyrrolidone.
According to some embodiments, the intensive mixing unit comprises a venturi nozzle or an atomizer.
According to some embodiments, the intensive mixing unit is contained within the absorption device.
According to some embodiments, the absorbing means is provided with a mass transfer enhancing material.
Further, the mass transfer enhancing material comprises one or any combination of trays, irregular packing and structured packing.
According to some embodiments, the absorption means comprise spraying means and/or liquid phase redistribution means. And the spraying device is used for continuously or intermittently spraying the mixed regenerated absorbent and new absorbent into the absorption device or respectively spraying the mixed regenerated absorbent and new absorbent into the absorption device from different positions.
According to other embodiments, the organic solvent recovery apparatus further comprises an adsorption device for performing a re-adsorption process on the organic solvent-containing carrier gas.
Further, the re-adsorption device is provided with an adsorption material. The adsorbing material comprises one or any combination of activated carbon, zeolite molecular sieve, carbon molecular sieve, silica gel and alumina.
According to other embodiments, the refining and regenerating device is also used for refining and regenerating the liquefied organic solvent, so that the recovery rate of the organic solvent is improved.
According to other embodiments, the organic solvent recovery apparatus further comprises a storage device for storing the crude organic solvent after liquefaction and the refined organic solvent after refining.
According to other embodiments, the organic solvent recovery apparatus may be operated in a continuous, semi-continuous, or discontinuous batch process to accommodate different energy production requirements and energy supplies.
According to a second aspect of the present application, there is provided an exhaust gas treatment device comprising the above organic solvent recovery device.
It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive of the application.
Drawings
In order to more clearly illustrate the technical solutions in the embodiments of the present application, the drawings needed to be used in the description of the embodiments will be briefly introduced below, and it is apparent that the drawings in the following description are only some embodiments of the present application.
Fig. 1 shows a block diagram of the composition of an organic solvent recovery apparatus according to an exemplary embodiment of the present application.
Fig. 2 illustrates a flow diagram of an organic solvent recovery method according to an example embodiment of the present application.
Fig. 3 shows a first schematic diagram of an organic solvent recovery process according to an example embodiment of the present application.
Fig. 4 shows a second schematic diagram of an organic solvent recovery process according to an example embodiment of the present application.
Fig. 5 shows a third schematic diagram of an organic solvent recovery process according to an example embodiment of the present application.
Detailed Description
Example embodiments will now be described more fully with reference to the accompanying drawings. Example embodiments may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein. These embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the concept of example embodiments to those skilled in the art. The same reference numerals denote the same or similar parts in the drawings, and thus, a repetitive description thereof will be omitted.
Furthermore, the described features, structures, or characteristics may be combined in any suitable manner in one or more embodiments. In the following description, numerous specific details are provided to give a thorough understanding of embodiments of the application. One skilled in the relevant art will recognize, however, that the subject matter of the present application can be practiced without one or more of the specific details, or with other methods, components, devices, steps, and so forth. In other instances, well-known methods, devices, implementations, or operations have not been shown or described in detail to avoid obscuring aspects of the application.
Those skilled in the art will appreciate that the drawings are merely schematic representations of exemplary embodiments, which may not be to scale. The blocks or flows in the drawings are not necessarily required to practice the present application and therefore should not be used to limit the scope of the present application.
Currently, manufacturers have begun to recover NMP. The more common methods are a rotating wheel method and an absorption method. When the rotary wheel method is adopted for adsorption, the problems that the rotary wheel is easy to block and is difficult to clean, the recovery rate is low, the equipment is difficult to seal, leakage pollution is easy to cause and the like exist. In patent document CN101543683B, NMP is recovered by a combination of condensation and absorption water columns. However, this process does not take into account secondary environmental pollution caused by NMP-rich solvents. And with the increase of NMP content in the absorbent, the absorption efficiency is gradually reduced, and the increasingly strict environmental protection requirements cannot be met, especially the international market does not have strong competitiveness.
Accordingly, the present application provides an organic solvent recovery device for electrode coating dry carrier gas treatment, comprising: the liquefying device is used for liquefying the organic solvent in the dry carrier gas to obtain a liquid organic solvent and residual carrier gas; the intensified mixing unit is used for premixing at least part of the residual carrier gas and at least part of the new absorbent to obtain mixed gas; the absorption device is used for absorbing the organic solvent in the mixed gas to obtain clean carrier gas and an absorbent rich in the organic solvent; and the refining and regenerating device is used for refining and regenerating the solvent to obtain a refined organic solvent and a regenerated absorbent. The organic solvent used in the electrode coating and drying process is N-methyl pyrrolidone, and the organic solvent recovery device can reduce the discharge of the N-methyl pyrrolidone and recover the N-methyl pyrrolidone, and meanwhile, the environmental protection requirement and the economic benefit are realized.
The technical solution of the present application will be described in detail below with reference to the accompanying drawings. Although the following description illustrates the examples of the present application with respect to NMP recovery, it will be readily understood by those skilled in the art that the examples of the present application can also be applied to the recovery of other similar solvents, such as amides and derivatives thereof, furans and derivatives thereof, morpholines and derivatives thereof, other pyrrolidone derivatives, dimethylsulfoxide, etc. Wherein the amide and derivatives thereof comprise dimethylacetamide; the furan and derivatives thereof include tetrahydrofuran and the like; the morpholine and derivatives thereof include N-formyl morpholine; the other pyrrolidone derivatives include N-ethyl pyrrolidone.
Fig. 1 shows a block diagram of the composition of an organic solvent recovery apparatus according to an exemplary embodiment of the present application.
As shown in fig. 1, the organic solvent recovery apparatus includes: a liquefaction apparatus 200, an intensive mixing unit 300, an absorption apparatus 400, and a refining regeneration apparatus 600.
The liquefaction device 200 is used for liquefying the organic solvent in the dry carrier gas to obtain a crude liquid organic solvent and a residual carrier gas.
According to some embodiments, liquefaction plant 200 may include a chilled water plant. According to other embodiments, liquefaction plant 200 may also include a pressurization plant and a common cooling water plant. When the freezing water is abundant, the freezing water device is used for low-temperature condensation liquefaction. Under the condition of no freezing water, the temperature is reduced by pressurizing the carrier gas and matching with common cooling water. Compared with the traditional condensation mode, the method achieves the liquefaction purpose with the same quality and reduces the energy consumption.
The intensive mixing unit 300 is configured to premix at least a part of the remaining carrier gas with at least a part of the fresh absorbent to obtain a mixed gas. NMP is miscible with a variety of absorbents such as, but not limited to, water, ethanol, and acetone. The intensified mixing unit 300 may include a venturi nozzle, an atomizer, and other devices that can intensify gas-liquid mass transfer mixing, but is not limited thereto.
The absorption device 400 is used for absorbing the organic solvent in the mixed gas to obtain the clean carrier gas and the absorbent rich in the organic solvent. The absorption device 400 may be located below the intensive mixing unit 300, which may also be included within the absorption device 400. The absorption unit 400 can be configured with mass transfer enhancement materials. The material includes, but is not limited to, trays, irregular packing, structured packing, or combinations thereof. The absorption apparatus 400 may further include a spraying apparatus for spraying the regenerated solvent mixed with the new solvent into the absorption apparatus at one time or from different positions. According to other embodiments of the present application, the absorption unit 400 may further comprise a liquid phase redistribution device to meet the requirements of different capacities for the transport effect.
The refining and regenerating device 600 is used for refining and regenerating the absorbent rich in organic solvent and the crude liquid organic solvent to obtain refined organic solvent and regenerated absorbent.
According to some embodiments, referring to fig. 1, the organic solvent recovery apparatus may further include a heat exchange apparatus 100 disposed upstream of the liquefying apparatus for performing waste heat recovery on the dry carrier gas. For example, the heat exchanger 100 has a small pressure loss, a high efficiency, a pressure loss of 50Kpa or less, and a temperature of the drying carrier gas is lowered by about 35 ℃. The heat exchange device 100 includes a conventional tube-and-shell heat exchanger, a heat pipe heat exchanger, a rotary heat exchanger, a plate heat exchanger, or the like, but is not limited thereto. When the temperature of the drying carrier gas is reduced, fresh air of the drying system or part of the rest carrier gas after liquefaction can be heated in the heat exchange device 100 and circularly used for coating and drying, and the temperature is raised by about 30 ℃ through heat recovery.
According to some embodiments, as shown in fig. 1, the organic solvent recovery device may further include an adsorption device 500 for performing an adsorption process on the organic solvent-containing carrier gas. The material used for the adsorption device 500 includes, but is not limited to, metal or non-metal adsorption material such as activated carbon, zeolite molecular sieve, carbon molecular sieve, silica gel, alumina, etc. After passing through the re-adsorption device 500, the clean carrier gas can meet any stringent environmental requirements.
Alternatively, as shown in fig. 1, the organic solvent recovery apparatus may further include a storage device 700 for storing the crude liquefied organic solvent and the refined organic solvent after refining.
According to other embodiments, lower emissions may be achieved by configuring a volatile organic rotating wheel device for the remaining carrier gas before the mixing unit and the absorption device for different emission requirements of different solvents.
Fig. 2 illustrates a flow diagram of an organic solvent recovery method according to an example embodiment of the present application.
As shown in fig. 2, at S1, the organic solvent in the dry carrier gas is liquefied to obtain a crude liquid organic solvent and a residual carrier gas.
As described above, the low-temperature condensation liquefaction may be performed using chilled water, or the condensation liquefaction may be performed using ordinary cooling water by pressurizing carrier gas. Thus, low-temperature condensation liquefaction is performed using the chilled water when the chilled water is abundant. Under the condition of no freezing water, no additional freezing water is needed to be prepared.
The organic solvent used in the lithium battery coating and drying process is NMP, the temperature of generated drying carrier gas is high, and the carrier gas is usually subjected to waste heat recovery before treatment so as to fully utilize energy. For example, after primary liquefaction by NMP, the NMP content of the carrier gas is greatly reduced, and most of the carrier gas serving as the internal circulation carrier gas can be reused for internal circulation of the drying equipment. And part of the residual carrier gas can be heated by utilizing the recovered waste heat and then reused for coating and drying, so that the energy utilization efficiency is improved, and the overall process energy consumption is reduced.
At S2, at least part of the remaining carrier gas is premixed with fresh absorbent to obtain a mixed gas.
In order to ensure the implementation of the subsequent process, the absorbent is premixed with a part of the remaining carrier gas as purge gas. As mentioned above, the premixing device includes but is not limited to Venturi nozzle, atomizer, etc. to enhance the mixing of gas and liquid.
At S3, the organic solvent in the mixed gas is absorbed to obtain a clean carrier gas and an absorbent rich in organic solvent.
According to example embodiments, the organic solvent in the mixed gas may be absorbed using a fresh absorbent and/or the regenerated absorbent. In addition, the mixed gas can be absorbed by adopting a mass transfer enhancing material. According to theoretical calculation, under the condition of mass transfer configuration of no more than 10 theoretical plates, the NMP content in the absorbed carrier gas can be less than 1mg/m3And the emission standard of China and most other countries is reached.
At S4, refining regeneration is performed on the organic solvent to obtain a refined organic solvent and a regenerated absorbent.
According to an exemplary embodiment, the NMP-rich absorbent may be regenerated using a regeneration and NMP refining apparatus to produce refined NMP and a regenerated absorbent.
In addition, in the above method, the cleaning carrier gas after absorption may be subjected to a reabsorption treatment, thereby further reducing the amount of emissions.
Fig. 3, 4, and 5 respectively show schematic diagrams of organic solvent recovery processes according to example embodiments of the present application. The following will describe the recovery process of the organic solvent by combining FIGS. 3, 4 and 5.
As shown in fig. 3, the drying carrier gas 1 generated in the coating and drying process is subjected to waste heat recovery by the heat exchanger 100. And the cooled dry carrier gas 3 enters the liquefying device 200 for liquefaction to obtain crude organic solvent liquid 8, and the crude organic solvent liquid 8 is conveyed to the storage device 700 for storage. The liquefied remaining carrier gas 7 is premixed with a fresh absorbent 9 as a premixed solvent 9A by an intensive mixing unit 300. The premixed mixture 11 enters the absorption device 400. In the process, the regenerated absorbent 12 generated by the refining and regenerating device 600 is mixed with the new absorbent 9B and then continuously or intermittently sprayed into the absorption device 400 or sprayed from different positions, so that the gas-liquid mass transfer is enhanced. The absorbent 15 rich in organic solvent generated after absorption by the absorption apparatus 400 is sent to the refining and regeneration apparatus 600 for regeneration treatment, thereby obtaining the refined organic solvent 19 and the regenerated absorbent 12. The refined organic solvent 19 is mixed with the liquefied organic solvent liquid 8 to obtain the recovered organic solvent 20, and the recovered organic solvent 20 is stored in the storage device 700.
As shown in fig. 4, a part of the organic solvent liquid 8B liquefied by the liquefaction apparatus 200 may be transferred to the storage apparatus 700 via a pipeline. Part of the organic solvent liquid 8A may be passed to a refinery regeneration unit 600 for further refining. The clean carrier gas 14 generated after absorption by the absorption device 400 can be further processed by the absorption device 500 to obtain ultra-clean evacuation carrier gas 17.
As shown in fig. 5, the content of the organic solvent in the residual carrier gas 5 liquefied by the liquefying device 200 is greatly reduced, and most of the residual carrier gas 6 and the fresh air 22 pass through the heat exchanging device 100 to be heated to form the internal circulation air 23 for drying, and the internal circulation air is reused for the internal circulation of the drying equipment. The remaining carrier gas 6 may be directly mixed with the drying internal circulation wind 23 for internal circulation in the drying apparatus.
The process may be run as a continuous, semi-continuous or discontinuous batch process, depending on the projected capacity and energy supply. The regenerated solvent 12 may be sprayed into the absorption apparatus 400 again. The organic solvent concentration of the regenerated absorbent is extremely low, so that the absorption capacity of the regenerated absorbent can be ensured, and the quality of the cleaning carrier gas is ensured.
The present application further provides a tail gas treatment device, which may include any one of the organic solvent recovery devices described in the previous embodiments, and is not described herein again.
It should be noted that each of the embodiments described above with reference to the drawings is only for illustrating the present application and not for limiting the scope of the present application, and those skilled in the art should understand that modifications or equivalent substitutions made on the present application without departing from the spirit and scope of the present application should be covered by the present application. Furthermore, unless the context indicates otherwise, words that appear in the singular include the plural and vice versa. Additionally, all or a portion of any embodiment may be utilized with all or a portion of any other embodiment, unless stated otherwise.
Claims (21)
1. An organic solvent recovery device for dry carrier gas treatment, comprising:
the liquefying device is used for liquefying the organic solvent in the dry carrier gas to obtain a crude liquid organic solvent and residual carrier gas;
the intensified mixing unit is used for premixing at least part of the residual carrier gas and at least part of the new absorbent to obtain mixed gas;
the absorption device is used for absorbing the organic solvent in the mixed gas by using an absorbent to obtain a clean carrier gas and an absorbent rich in the organic solvent;
and the refining and regenerating device is used for refining and regenerating the absorbent rich in the organic solvent and the crude liquid organic solvent to obtain a refined organic solvent and a regenerated absorbent.
2. The organic solvent recovery apparatus according to claim 1, further comprising:
and the heat exchange device is arranged at the upstream of the liquefying device and is used for recovering waste heat of the drying carrier gas.
3. The organic solvent recovery device of claim 2, wherein the heat exchange device comprises one of a shell-and-tube heat exchanger, a heat pipe heat exchanger, a rotary wheel heat exchanger, or a plate heat exchanger.
4. The organic solvent recovery device of claim 2, wherein the heat exchange device is further configured to heat the fresh air of the drying process and/or a portion of the residual carrier gas as an internal circulation carrier gas.
5. The organic solvent recovery device according to claim 1, wherein the liquefaction device comprises a chilled water device, or a pressurizing device and a normal cooling water device.
6. The organic solvent recovery apparatus of claim 1, wherein the organic solvent comprises one or more of N-methylpyrrolidone, amides and derivatives thereof, furan and derivatives thereof, morpholine and derivatives thereof, other pyrrolidone derivatives, and dimethylsulfoxide,
the amide and derivatives thereof include dimethylacetamide;
the furan and derivatives thereof include tetrahydrofuran and the like;
the morpholine and derivatives thereof include N-formyl morpholine;
the other pyrrolidone derivatives include N-ethyl pyrrolidone.
7. The organic solvent recovery device of claim 1, wherein the intensive mixing unit comprises a venturi nozzle or an atomizer.
8. The organic solvent recovery device according to claim 1, wherein the intensive mixing unit is contained within the absorption device.
9. The organic solvent recovery apparatus of claim 1, wherein the absorbing means is configured with mass transfer enhancing materials.
10. The organic solvent recovery device of claim 9, wherein the mass transfer enhancing material comprises one or any combination of trays, irregular packing, structured packing.
11. The organic solvent recovery apparatus according to claim 1, wherein the absorption device is provided with a spray device and/or a liquid phase redistribution device.
12. The organic solvent recovery apparatus of claim 11, wherein the spraying means is adapted to continuously or intermittently spray the mixed regenerated absorbent and fresh absorbent into the absorption apparatus.
13. The organic solvent recovery apparatus according to claim 11, wherein the spraying means is configured to spray the regenerated absorbent into the absorption apparatus from different positions with respect to a fresh absorbent.
14. The organic solvent recovery apparatus according to claim 1, further comprising:
and the adsorption device is used for carrying out adsorption treatment on the organic solvent-containing carrier gas.
15. The organic solvent recovery apparatus according to claim 14, wherein the adsorption apparatus is provided with an adsorbent.
16. The organic solvent recovery apparatus of claim 15, wherein the adsorption material comprises one of activated carbon, zeolite molecular sieve, carbon molecular sieve, silica gel, and alumina, and any combination thereof.
17. The organic solvent recovery apparatus according to claim 14, wherein the adsorption apparatus is disposed before the mixing unit or after the absorption apparatus according to different emission standards of different solvents.
18. The organic solvent recovery apparatus according to claim 1, wherein the refining and regenerating apparatus is configured to refine and regenerate the organic solvent-rich absorbent and the crude liquid organic solvent to obtain a refined organic solvent and a regenerated absorbent.
19. The organic solvent recovery apparatus according to claim 1, further comprising a storage device for storing the crude liquefied organic solvent and the refined organic solvent after refining.
20. The organic solvent recovery apparatus of claim 1, wherein the organic solvent recovery apparatus is operated in a continuous, semi-continuous or discontinuous batch process.
21. An exhaust gas treatment device comprising the organic solvent recovery device according to any one of claims 1 to 20.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113426250A (en) * | 2021-06-09 | 2021-09-24 | 厦门泽玥科技有限公司 | Remove formaldehyde system |
| WO2023032250A1 (en) * | 2021-09-02 | 2023-03-09 | 東レエンジニアリング株式会社 | Drying system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113426250A (en) * | 2021-06-09 | 2021-09-24 | 厦门泽玥科技有限公司 | Remove formaldehyde system |
| CN113426250B (en) * | 2021-06-09 | 2022-11-29 | 浙江悦峥环保科技有限公司 | Remove formaldehyde system |
| WO2023032250A1 (en) * | 2021-09-02 | 2023-03-09 | 東レエンジニアリング株式会社 | Drying system |
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