CN216725831U

CN216725831U - NMP high purity recovery unit

Info

Publication number: CN216725831U
Application number: CN202122836718.2U
Authority: CN
Inventors: 张新党; 王毅; 朱承浪; 龚丽芳
Original assignee: Jiangsu Sangui Resource Regeneration Co ltd
Current assignee: Jiangsu Sangui Resource Regeneration Co ltd
Priority date: 2021-11-18
Filing date: 2021-11-18
Publication date: 2022-06-14
Anticipated expiration: 2031-11-18

Abstract

The utility model belongs to the technical field of mixed solution recovery, and particularly relates to an NMP high-purity recovery device which comprises a primary rectifying tower and a secondary rectifying tower, wherein the number of theoretical plates of the primary rectifying tower is 10 larger than that of the theoretical plates of the secondary rectifying tower, a feed inlet of the primary rectifying tower is connected with a waste liquid input pipe, a recombination and fractionation outlet of the primary rectifying tower is connected with a feed inlet of the secondary rectifying tower, and a recombination and fractionation outlet of the secondary rectifying tower is communicated with the waste liquid input pipe. According to the utility model, the theoretical plate number of the first-stage rectifying tower is greatly increased, so that the dehydration efficiency is improved, water is completely removed to 60PPM, the purity of the recovered NMP is more than 99.9% through further purification treatment of the second-stage rectifying tower, the recovered waste materials can be combined with the waste liquid pipe to be extracted circularly, and the operation is simplified by replacing three towers with two towers, so that the whole recovery process is convenient to control, and the occupied area is reduced.

Description

NMP high purity recovery unit

Technical Field

The utility model belongs to the technical field of mixed solution recovery, and particularly relates to a NMP high-purity recovery device.

Background

N-methylpyrrolidone (NMP) was a colorless, transparent oily liquid with a slight amine odor. Low volatility, good thermal stability and chemical stability, and can be volatilized with water vapor. Because of its good performance, it is widely used in lithium battery and semiconductor industry. In the lithium battery and semiconductor manufacturing industry, NMP is discharged from production equipment in the form of waste gas, and if the waste gas is directly discharged into the environment without being recycled, on one hand, environmental pollution is caused, and on the other hand, great resource waste is caused. Therefore, it is necessary to recover and treat the exhaust gas. The prior commonly used NMP recovery process is tower-type spray recovery, and a normal NMP recovery device is realized by three-tower combined transportation, so that the device has large investment, high energy consumption and complex operation.

SUMMERY OF THE UTILITY MODEL

Aiming at the defects of the prior art, the utility model provides a high-purity NMP recovery device, and aims to solve the technical problems that the conventional NMP recovery process is tower-type spray recovery, a normal NMP recovery device is realized by three-tower combined transportation, the investment is large, the energy consumption is high, and the operation is complex.

The utility model provides a NMP high-purity recovery device, which has the following specific technical scheme:

NMP high purity recovery unit, including one-level rectifying column and second grade rectifying column, the theoretical plate number of one-level rectifying column is than the theoretical plate number of second grade rectifying column is 10 big, the waste liquid input tube is connected to the feed inlet of one-level rectifying column, the heavy fraction extraction of one-level rectifying column export with the feed inlet of second grade rectifying column is connected, the heavy fraction extraction of second grade rectifying column export and waste liquid input tube intercommunication, the light fraction extraction mouth of second grade rectifying column is connected with finished product output pipeline.

In certain embodiments, the device further comprises a first buffer tank and a first output pump, wherein a feed inlet of the first buffer tank is communicated with a light component extraction outlet of the first-stage rectifying tower, a discharge outlet of the first buffer tank is communicated with the top of the first-stage rectifying tower through the first output pump, and the first output pump is further connected with a liquid outlet pipeline.

In certain embodiments, the system further comprises a first condenser disposed between the first buffer tank and the first output pump.

In certain embodiments, the system further comprises a second buffer tank and a second output pump, wherein a feed inlet of the second buffer tank is communicated with a light component extraction outlet of the secondary rectification tower, a discharge outlet of the second buffer tank is communicated with the top of the secondary rectification tower through the second output pump, and the second output pump is further communicated with the finished product output pipeline.

Further, still include the second condenser, the second condenser is located between the second buffer tank and the second delivery pump.

In some embodiments, the first rectification column has an overhead temperature of 42 ℃, a bottoms temperature of 112 ℃, and a reflux ratio of 2.0.

In certain embodiments, the secondary rectification column has a top temperature of 101 ℃, a bottom temperature of 105 ℃, and a reflux ratio of 1.5.

In some embodiments, the heavy fraction outlet of the first-stage rectification column is connected with the feed inlet of the second-stage rectification column through an extraction pump.

The utility model has the following beneficial effects: according to the NMP high-purity recovery device provided by the utility model, the theoretical plate number of the first-stage rectifying tower is greatly increased, so that the dehydration efficiency is improved, water is completely removed to 60PPM, the recovered NMP is further purified by the second-stage rectifying tower, the purity is over 99.9 percent, the water content is 60PPM, and the recovered waste materials can be combined with the waste liquid pipe so as to be extracted circularly. The utility model replaces three towers with double towers, thereby simplifying the operation, facilitating the control of the whole recovery process and reducing the occupied area.

Drawings

FIG. 1 is a schematic plan view of a high purity recovery apparatus for NMP according to the present invention.

Detailed Description

In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings 1 in conjunction with specific embodiments.

Example 1

NMP high purity recovery unit, including first order rectifying column 1 and second grade rectifying column 2, the theoretical plate number of first order rectifying column 1 is 10 great than the theoretical plate number of second grade rectifying column 2, waste liquid input tube 11 is connected to the feed inlet of first order rectifying column 1, the heavy component extraction mouth of first order rectifying column 1 is connected with the feed inlet of second grade rectifying column 2, the heavy component extraction mouth of second grade rectifying column 2 and waste liquid input tube 11 intercommunication, the light component extraction mouth of second grade rectifying column 2 is connected with finished product output pipeline 21. Industrial waste water gets into one-level rectifying column 1 from waste liquid input tube 11, and one-level rectifying column 1 carries out dehydration to the waste liquid, and the tower bottom product after handling gets into from the feed inlet of second grade rectifying column 2 and carries out recovery processing, only needs two rectifying columns just can retrieve high-purity NMP.

In this embodiment, still include first buffer tank 3 and first delivery pump 4, the feed inlet of first buffer tank 3 and the light component of one-level rectifying column 1 are adopted the export intercommunication, and the discharge gate of first buffer tank 3 is through the top of the tower intercommunication of first delivery pump 4 with one-level rectifying column 1, and first delivery pump 4 still is connected with out the liquid pipeline. First buffer tank 3 is used for storing the gathering with the feed liquid of the export is adopted to the light component of one-level rectifying column 1, and first buffer tank 3 guarantees overall system steady operation through reflux capacity and output.

In this embodiment, the first condenser 5 is further included, and the first condenser 5 is disposed between the first buffer tank 3 and the first output pump 4. The first condenser 5 liquefies part of the gas in the first buffer tank 3 and outputs the liquefied gas through the first output pump 4, and part of the liquefied gas is refluxed to the top of the first-stage rectifying tower 1 through the first output pump 4.

In this embodiment, still include second buffer tank 6 and second delivery pump 7, the feed inlet of second buffer tank 6 and the light component of second grade rectifying column 2 are adopted the export and are communicate, and the discharge gate of second buffer tank 6 passes through second delivery pump 7 and the top of the tower of second grade rectifying column 2 intercommunication, and second delivery pump 7 still communicates finished product output pipeline 21. The second buffer tank 6 is used for storing and gathering the feed liquid at the light component extraction outlet of the second-stage rectifying tower 2, and the second buffer tank 6 ensures that the liquid of the whole system flows and runs smoothly through reflux quantity and output quantity.

Further, a second condenser 8 is further included, and the second condenser 8 is arranged between the second buffer tank 6 and the second output pump 7. The second condenser 8 liquefies part of the gas in the second buffer tank 6, and outputs the liquefied part of the gas from the finished product output pipeline 21 through the second output pump 7, namely the concentration of the gas is up to more than 99.9%, and part of the gas reflows to the top of the second-stage rectifying tower 2 through the second output pump 7.

In this example, the top temperature of the first-stage rectification column 1 was 42 ℃, the bottom temperature was 112 ℃, and the reflux ratio was 2.0.

In this example, the top temperature of the secondary rectification column 2 was 101 ℃, the bottom temperature was 105 ℃, and the reflux ratio was 1.5.

In this embodiment, the heavy component extraction outlet of the first-stage rectification tower 1 is connected with the feed inlet of the second-stage rectification tower 2 through the liquid pump 9. The material output from the recombination and fractionation outlet of the first-stage rectifying tower 1 is pumped into the second-stage rectifying tower 2 through an extraction pump 9.

The NMP high purity recovery apparatus provided in this example, the general implementation flow is as follows:

industrial waste water gets into one-level rectifying column 1 through the feed inlet of one-level rectifying column 1 by waste liquid input tube 11, one-level rectifying column 1 is to the dehydration of industrial waste water, the top of the tower product of one-level rectifying column 1 is water and light thing of boiling, export from the light component extraction outlet of one-level rectifying column 1, collect in first buffer tank 3, through the condensation of

first condenser

5, 4 parts of rethread first delivery pump are pumped back to the top of the tower of one-level rectifying column 1, the bottom of the tower product of one-level rectifying column 1 is the semi-pure product of NMP, export through drawing liquid pump suction secondary rectifying column 2 from the recombination branch of one-level rectifying column 1. Through the purification and recovery of the secondary rectifying tower 2, the tower top product of the secondary rectifying tower 2 is a 99.9% NMP pure product, the light component of the secondary rectifying tower 2 is output from the extraction port, collected in the second buffer tank 6, condensed by the second condenser 8, and then pumped back to the tower top of the primary rectifying tower 1 by the second output pump 7, and part of the light component is output, and the tower bottom product of the secondary rectifying tower 2 flows back to the primary rectifying tower 1 through the waste liquid input pipe 11 from the recombination and extraction port of the secondary rectifying tower 2 to be purified by NMP again.

In conclusion, the NMP high-purity recovery device provided by the utility model has the advantages that the theoretical plate number of the first-stage rectifying tower 1 is greatly increased, so that the dehydration efficiency is improved, water is completely removed to 60PPM, the NMP is further purified by the second-stage rectifying tower 2, the purity of the recovered NMP is more than 99.9 percent, the water content is 60PPM, and the recovered waste materials can be combined with the waste liquid pipe so as to be extracted circularly. The utility model replaces three towers with double towers, thereby simplifying the operation, facilitating the control of the whole recovery process and reducing the occupied area.

The above description is only for the purpose of illustrating preferred embodiments of the present invention and is not to be construed as limiting the utility model, and the present invention is not limited to the above examples, and those skilled in the art should also be able to make various changes, modifications, additions or substitutions within the spirit and scope of the present invention.

Claims

The NMP high-purity recovery device is characterized by comprising a first-stage rectifying tower and a second-stage rectifying tower, wherein the number of theoretical plates of the first-stage rectifying tower is 10 larger than that of the second-stage rectifying tower, a feed inlet of the first-stage rectifying tower is connected with a waste liquid input pipe, a heavy component extraction outlet of the first-stage rectifying tower is connected with the feed inlet of the second-stage rectifying tower, the heavy component extraction outlet of the second-stage rectifying tower is communicated with the waste liquid input pipe, and a light component extraction outlet of the second-stage rectifying tower is connected with a finished product output pipeline.
2. The NMP high-purity recovery device according to claim 1, further comprising a first buffer tank and a first output pump, wherein the feed inlet of the first buffer tank is communicated with the light component extraction outlet of the primary rectifying tower, the discharge outlet of the first buffer tank is communicated with the top of the primary rectifying tower through the first output pump, and the first output pump is further connected with a liquid outlet pipeline.
3. A high purity recovery apparatus for NMP as in claim 2 further comprising a first condenser disposed between said first buffer tank and said first output pump.
4. A high-purity NMP recovery device according to claim 1, further comprising a second buffer tank and a second output pump, wherein the feed inlet of the second buffer tank is communicated with the light component extraction outlet of the secondary rectification tower, the discharge outlet of the second buffer tank is communicated with the top of the secondary rectification tower through the second output pump, and the second output pump is further communicated with the finished product output pipeline.
5. A high purity recovery apparatus for NMP according to claim 4 further comprising a second condenser, said second condenser being disposed between said second buffer tank and said second output pump.
6. A high purity recovery apparatus for NMP as in claim 1 wherein the temperature at the top of the first rectification column is 42 ℃, the temperature at the bottom of the first rectification column is 112 ℃ and the reflux ratio is 2.0.
7. A high purity recovery apparatus for NMP as in claim 1 wherein the temperature at the top of the secondary distillation column is 101 ℃, the temperature at the bottom of the secondary distillation column is 105 ℃ and the reflux ratio is 1.5.
8. A high purity recovery apparatus for NMP according to claim 1, wherein the heavy fraction outlet of said primary distillation column is connected to the feed inlet of said secondary distillation column by an extraction pump.