CN111544909A - Evaporation concentration system - Google Patents
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- CN111544909A CN111544909A CN202010346284.5A CN202010346284A CN111544909A CN 111544909 A CN111544909 A CN 111544909A CN 202010346284 A CN202010346284 A CN 202010346284A CN 111544909 A CN111544909 A CN 111544909A
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Abstract
The embodiment of the invention discloses an evaporation concentration system, which aims to improve the energy utilization rate of an original system. An evaporative concentration system for evaporative concentration of a feed solution containing an organic solvent, the evaporative concentration system comprising: steam jet, first heat exchanger, evaporimeter and the second heat exchanger that communicates in proper order, wherein: the steam ejector is communicated with the raw steam pipeline and communicated with the first heat exchanger through a steam injection pipeline; the first heat exchanger is communicated with the evaporator through a first liquid circulation pipeline and a second liquid circulation pipeline; the evaporator is communicated with the second heat exchanger through a secondary steam pipeline; the second heat exchanger is communicated with the cold water pipeline and is communicated with the steam ejector through a tertiary steam pipeline.
Description
Technical Field
The invention relates to the technical field of evaporation equipment, in particular to an evaporation concentration system.
Background
The evaporation concentration is a very typical chemical unit operation in industrial production, and is widely applied to industrial production processes of chemical industry, light industry, food, pharmacy, seawater desalination, sewage treatment and the like.
The material which is often evaporated in industrial production is an aqueous solution. Saturated steam is commonly used as a heating source, and the 'secondary steam' evaporated from the solution is not beneficial to transportation due to low pressure and low quality, so that the gas using condition is basically not achieved. Therefore, the secondary steam is directly discharged to the atmosphere, condensed by a cooling system or used in some low-pressure steam equipment, so that pollution and energy waste are caused.
Currently, there are three main processes in the field of evaporative concentration: conventional Multiple Effect Evaporation (MEE), Thermal Vapor Recompression (TVR), Mechanical Vapor Recompression (MVR). The multiple-effect evaporation process needs to spend an external heat source to provide heat, the materials are heated, so that secondary organic solvent steam generated by the evaporation of the previous effect is used as a heating source of the next effect, and devices such as a cooling tower and the like are used for producing cooling water to cool the secondary organic solvent steam of the last effect evaporation. And the thermal steam recompression is additionally provided with an injection pump on the basis of the traditional process, a part of external heat sources are spent to inject part of secondary organic solvent steam generated by the materials, and the steam is used as a heat source for heating the materials after temperature rise and pressure rise.
At present, the traditional Chinese medicine is concentrated by a thermal steam recompression process, and an ejector is needed to eject the organic solvent in the traditional Chinese medicine by raw steam in the concentration process, so that the concentration and quality of the organic solvent can be reduced, and the organic solvent is not favorably recycled.
Disclosure of Invention
The embodiment of the invention aims to provide an evaporation concentration system so as to improve the energy utilization rate of the system.
The embodiment of the invention provides an evaporation concentration system, which is used for evaporating and concentrating raw material liquid containing organic solvent, and comprises: steam jet, first heat exchanger, evaporimeter and the second heat exchanger that communicates in proper order, wherein:
the steam ejector is communicated with the raw steam pipeline and the first heat exchanger through a steam ejection pipeline; the first heat exchanger is communicated with the evaporator through a first liquid circulation pipeline and a second liquid circulation pipeline; the evaporator is communicated with the second heat exchanger through a secondary steam pipeline; the second heat exchanger is communicated with the cold water pipeline and communicated with the steam ejector through a tertiary steam pipeline.
In any embodiment of this technical solution, optionally, the evaporation concentration system further includes an organic solvent extraction line in communication with the second heat exchanger.
In this embodiment, optionally, there is one steam ejector, one first heat exchanger, one evaporator, and one second heat exchanger;
the first heat exchanger comprises a first raw material liquid inlet and a first raw material liquid outlet, and the evaporator comprises a second raw material liquid inlet, a third raw material liquid inlet and a second raw material liquid outlet; first raw material liquid import passes through first liquid circulation pipeline with the export intercommunication of second raw material liquid, first raw material liquid export with the import of third raw material liquid passes through the second liquid circulation pipeline intercommunication contains the import of organic solvent raw material liquid and gets into through the import of second raw material liquid the evaporimeter.
In any embodiment of this technical solution, optionally, the number of the steam ejector is one, the number of the first heat exchangers is at least two, the number of the evaporators is the same as that of the first heat exchangers, and the first heat exchangers and the evaporators are alternately arranged, wherein:
the steam ejector is communicated with the first heat exchanger at the head end through a steam ejection pipeline, and the second heat exchanger is communicated with the second heat exchanger through a tertiary steam pipeline.
In this embodiment, optionally, the first heat exchanger includes a first raw material liquid inlet and a first raw material liquid outlet, and the evaporator includes a second raw material liquid inlet, a third raw material liquid inlet and a second raw material liquid outlet;
the first heat exchanger and the evaporator which are communicated in sequence are evaporation concentration groups, for each evaporation concentration group, the first raw material liquid inlet is communicated with the second raw material liquid outlet through the first liquid circulation pipeline, the first raw material liquid outlet is communicated with the third raw material liquid inlet through the second liquid circulation pipeline, and the organic solvent-containing raw material liquid enters the evaporator through the second raw material liquid inlet.
In any embodiment of this technical solution, optionally, the number of the steam ejector is one, the number of the second heat exchanger is one, the number of the first heat exchangers is at least two, the number of the evaporators is the same as that of the first heat exchangers, and the first heat exchangers and the evaporators are alternately arranged, wherein:
the steam ejector is communicated with the first heat exchanger at the head end through a steam ejection pipeline, and the second heat exchanger is communicated with the second heat exchanger through a tertiary steam pipeline;
the evaporative concentration system further includes an organic solvent extraction conduit in communication with the terminal evaporator.
In this embodiment, optionally, the first heat exchanger includes a first raw material liquid inlet and a first raw material liquid outlet, and the evaporator includes a second raw material liquid inlet, a third raw material liquid inlet and a second raw material liquid outlet;
the first heat exchanger and the evaporator which are communicated in sequence are evaporation concentration groups, for each evaporation concentration group, the first raw material liquid inlet is communicated with the second raw material liquid outlet through the first liquid circulation pipeline, the first raw material liquid outlet is communicated with the third raw material liquid inlet through the second liquid circulation pipeline, and the organic solvent-containing raw material liquid enters the evaporator through the second raw material liquid inlet.
In any embodiment of the present disclosure, optionally, the second raw material liquid outlet is communicated with the raw material liquid collecting pipeline.
In this embodiment, optionally, the evaporation concentration system further includes a concentration detection device disposed in the evaporator, and the concentration detection device is configured to detect a concentration of the raw material liquid at the second raw material liquid outlet.
In this embodiment, optionally, the evaporation concentration system further includes a condensed water collecting pipe communicated with the first heat exchanger.
According to the evaporation concentration system adopting the technical scheme, firstly, raw steam enters a first heat exchanger through a raw steam pipeline and a steam ejector, organic solvent-containing raw material liquid enters an evaporator through a raw material liquid input pipeline to form secondary organic solvent steam, the organic solvent raw material liquid in the evaporator flows back to the first heat exchanger through a first liquid circulation pipeline, and the raw steam and the organic solvent-containing raw material liquid exchange heat in the first heat exchanger to form condensed water and first concentrated liquid; then, cold water enters a second heat exchanger through a cold water pipeline, the first concentrated solution flows back to an evaporator through a second liquid circulation pipeline, and secondary organic solvent steam in the second heat exchanger exchanges heat with the cold water to form water vapor; finally, the water vapor enters the steam ejector through the tertiary steam pipeline, and the generated steam is guided to the first heat exchanger.
In the evaporation concentration system of the technical scheme, the secondary organic solvent steam is injected by the raw steam, so that the waste of the secondary organic solvent steam is avoided, and the energy utilization rate of the evaporation concentration system is effectively improved.
Based on the same inventive concept, the present technical solution further provides a method for preparing a concentrated solution by using the evaporation concentration system as described above, the method comprising:
feeding the raw material liquid into an evaporator to generate a first concentrated liquid and organic solvent steam;
the organic solvent steam enters a second heat exchanger through a secondary steam pipeline;
the first concentrated solution flows back to the first heat exchanger for heat exchange to generate a second concentrated solution and condensed water;
cold water enters a second heat exchanger through a cold water pipeline to exchange heat with organic solvent steam to generate water vapor, the organic solvent steam is condensed into organic solvent solution, and the organic solvent solution enters an organic solvent extraction pipeline;
raw steam enters an ejector to inject water vapor into a first heat exchanger;
and the second concentrated solution flows back to the evaporator for repeated evaporation and concentration, and is collected when the concentration meets the requirement.
By adopting the method for preparing the concentrated solution in the technical scheme, the organic solvent-containing raw material solution is evaporated and concentrated, and on the basis of meeting the concentration requirement, the waste of secondary organic solvent steam is avoided, so that the energy utilization rate of an evaporation and concentration system is effectively improved; in addition, an organic solvent solution with higher concentration and better quality can be obtained, and the recovery rate of the organic solvent is improved.
Drawings
FIG. 1 is a schematic diagram of an evaporative concentration system according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of an evaporative concentration system according to another embodiment of the present invention;
FIG. 3 is a schematic diagram of an evaporative concentration system according to yet another embodiment of the present invention;
FIG. 4 is a flow chart of a method of preparing a concentrate according to an embodiment of the present invention.
Reference numerals:
1-a steam ejector;
2-a first heat exchanger;
201-a head end first heat exchanger;
202-secondary first heat exchanger;
203-first feedstock liquid inlet;
204-a first feedstock liquid outlet;
3-an evaporator;
301-head end evaporator;
302-end evaporator;
303-a second feed solution inlet;
304-a third feed solution inlet;
305-a second feedstock liquid outlet;
4-a second heat exchanger;
5-a raw steam pipeline;
6-steam injection pipeline;
7-a first liquid circulation conduit;
8-a second liquid circulation conduit;
9-a cold water pipeline;
10-secondary steam piping;
11-tertiary steam line;
12-evaporation concentration group;
13-organic solvent extraction line; 14-a raw material liquid collecting pipeline;
15-condensed water collecting pipe.
Detailed Description
In order to improve the recovery utilization rate of ethyl acetate and the energy utilization rate of the system, the embodiment of the invention provides an evaporation concentration system. In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail by referring to the following examples.
As shown in fig. 1 to 3, an embodiment of the present invention provides an evaporation concentration system for evaporation concentration of a raw material liquid containing ethyl acetate, the evaporation concentration system including: steam ejector 1, first heat exchanger 2, evaporimeter 3 and the second heat exchanger 4 that communicate in proper order, wherein:
the steam ejector 1 is communicated with a raw steam pipeline 5 and is communicated with the first heat exchanger 2 through a steam ejection pipeline 6; the first heat exchanger 2 is communicated with the evaporator 3 through a first liquid circulating pipeline 7 and a second liquid circulating pipeline 8; the evaporator 3 is communicated with the second heat exchanger 4 through a secondary steam pipeline 10; the second heat exchanger 4 is in communication with the cold water conduit 9 and with the steam ejector 1 via a tertiary steam conduit 11.
According to the evaporation concentration system adopting the technical scheme, firstly, raw steam enters a first heat exchanger 2 through a raw steam pipeline 5 and a steam ejector 1, raw material liquid containing ethyl acetate enters an evaporator 3 through a raw material liquid input pipeline to form secondary ethyl acetate steam, the ethyl acetate raw material liquid in the evaporator 3 flows back to the first heat exchanger 2 through a first liquid circulation pipeline 7, and thus the raw steam and the raw material liquid containing ethyl acetate exchange heat in the first heat exchanger 2 to form condensed water and a first concentrated solution; then, cold water enters the second heat exchanger 4 through a cold water pipeline 9, the first concentrated solution flows back to the evaporator 3 through a second liquid circulating pipeline 8, and secondary ethyl acetate steam in the second heat exchanger 4 exchanges heat with the cold water to form water vapor; finally, the water vapor enters the steam injector 1 through the tertiary steam pipe 11, and is introduced into the first heat exchanger 2 by the raw steam.
In the evaporation concentration system of the technical scheme, secondary ethyl acetate steam is injected through raw steam, so that waste of the secondary ethyl acetate steam is avoided, and the energy utilization rate of the evaporation concentration system is effectively improved.
As shown in fig. 1, in one embodiment of the present disclosure, there are one steam ejector 1, one first heat exchanger 2, one evaporator 3, and one second heat exchanger 4;
the first heat exchanger 2 comprises a first raw material liquid inlet 203 and a first raw material liquid outlet 204, and the evaporator 3 comprises a second raw material liquid inlet 303, a third raw material liquid inlet 304 and a second raw material liquid outlet 305; the first raw material liquid inlet 203 is communicated with a second raw material liquid outlet 305 through a first liquid circulation pipeline 7, the first raw material liquid outlet 204 is communicated with a third raw material liquid inlet 302 through a second liquid circulation pipeline 8, and the ethyl acetate-containing raw material liquid enters the evaporator through a second raw material liquid inlet 303.
In this embodiment, the evaporative concentration system optionally further comprises an organic solvent extraction line 13 in communication with the second heat exchanger 4.
In this embodiment, the second raw material liquid outlet 305 is optionally in communication with the raw material liquid collecting conduit 14.
Further, in this embodiment, optionally, the evaporation concentration system further includes a concentration detection device (not shown in the figure) disposed in the evaporator 3, and the concentration detection device is configured to detect the concentration of the raw material liquid at the second raw material liquid outlet 305.
Furthermore, in this embodiment, optionally, the evaporation concentration system further comprises a condensed water collecting conduit 15 communicating with the first heat exchanger 2.
In the embodiment of the technical scheme, firstly, raw steam enters the first heat exchanger 2 through the raw steam pipeline 5 and the steam ejector 1, ethyl acetate-containing raw material liquid enters the evaporator 3 through the raw material liquid input pipeline to form ethyl diacetate steam, and the ethyl acetate raw material liquid in the evaporator 3 flows back to the first heat exchanger 2 through the first liquid circulation pipeline 7, so that the raw steam and the ethyl acetate-containing raw material liquid exchange heat in the first heat exchanger 2 to form condensed water and a first concentrated solution.
Then, the secondary ethyl acetate steam enters a second heat exchanger 4 through a secondary steam pipeline 10, cold water enters the second heat exchanger 4 through a cold water pipeline 9, the secondary ethyl acetate steam in the second heat exchanger 4 exchanges heat with the cold water to form water steam and ethyl acetate condensate, the water steam enters a steam ejector 1 through a tertiary steam pipeline 11, and the generated steam is introduced into a first heat exchanger 2; the ethyl acetate condensate enters the organic solvent extraction system through an organic solvent extraction line 13.
Finally, the first concentrated solution flows back to the evaporator 3 through the second liquid circulating pipeline 8 to continue evaporation concentration.
In the later stage of evaporation and concentration, the ethyl acetate in the raw material liquid is evaporated, the temperature of the first heat exchanger 2 is raised under continuous heating, and the water in the raw material liquid is evaporated and cooled to form condensed water, and the condensed water flows into the waste liquid collecting system through a condensed water collecting pipeline 15 communicated with the first heat exchanger 2. The concentrated raw material liquid in the evaporator 3 is returned to the first heat exchanger 2 and is repeatedly evaporated and concentrated, and when the concentration detection means provided in the evaporator 3 detects that the concentration of the raw material liquid at the second raw material liquid outlet 305 of the evaporator 3 reaches a predetermined value, the concentrated raw material liquid can be discharged and collected through the raw material liquid collection pipe 14 communicating with the second raw material liquid outlet 305, and at this time, the evaporation and concentration process is completed.
By adopting the evaporation concentration system of the embodiment of the technical scheme, the energy utilization rate of the evaporation concentration system can be effectively improved. And moreover, the extraction process of the organic solvent of the ethyl acetate water condensate can be simplified, and the ethyl acetate in the ethyl acetate water condensate has high concentration, so that the ethyl acetate after the organic solvent is extracted has high quality and can be continuously used, and therefore, the evaporation concentration system adopting the technical scheme can effectively improve the recovery utilization rate of the ethyl acetate.
As shown in fig. 2, in another embodiment of the present invention, there are one steam ejector 1, one second heat exchanger 4, at least two first heat exchangers 2, the same number of evaporators 3 as the first heat exchangers 2, and the first heat exchangers 2 and the evaporators 3 are alternately arranged, wherein:
the steam injector 1 is communicated with the first heat exchanger 201 at the head end through a steam injection pipeline 6, and the second heat exchanger 202 is communicated with the second heat exchanger 4 through a tertiary steam pipeline 11.
In this embodiment, the evaporative concentration system optionally further comprises an organic solvent extraction line 13 in communication with the second heat exchanger 4.
In this embodiment, optionally, the first heat exchanger 2 includes a first raw material liquid inlet 203 and a first raw material liquid outlet 204, and the evaporator 3 includes a second raw material liquid inlet 303, a third raw material liquid inlet 304 and a second raw material liquid outlet 305;
the first heat exchanger 2 and the evaporator 3 which are sequentially communicated are an evaporation concentration group 12, for each evaporation concentration group 12, the first raw material liquid inlet 203 is communicated with the second raw material liquid outlet 305 through a first liquid circulation pipeline 7, the first raw material liquid outlet 204 is communicated with the third raw material liquid inlet 304 through a second liquid circulation pipeline 8, and the raw material liquid containing ethyl acetate enters the evaporator 3 through the second raw material liquid inlet 303.
In this embodiment, the second raw material liquid outlet 305 is optionally in communication with the raw material liquid collecting conduit 14.
Further, in this embodiment, optionally, the evaporation concentration system further includes a concentration detection device disposed in the evaporator 3, and the concentration detection device is configured to detect the concentration of the raw material liquid at the second raw material liquid outlet 305.
Furthermore, in this embodiment, optionally, the evaporation concentration system further comprises a condensed water collecting conduit 15 communicating with the first heat exchanger 2.
The present embodiment will be described in detail by taking an example in which one steam ejector 1 is provided, one second heat exchanger 4 is provided, two first heat exchangers 2 are provided, and two evaporators 3 are provided, and the embodiment is similar to that in the case where a plurality of first heat exchangers 2 and evaporators 3 are provided.
In this embodiment, first, raw steam enters the first heat exchanger 201 at the head end through the raw steam pipeline 5 and the steam ejector 1, raw material liquid containing ethyl acetate enters each evaporator 3 through the raw material liquid input pipeline 14 to form ethyl acetate secondary steam, and the raw material liquid containing ethyl acetate in the evaporator 3 returns to the first heat exchanger 2 through the first liquid circulation pipeline 7, so that the raw steam and the raw material liquid containing ethyl acetate exchange heat in the first heat exchanger 2 to form condensed water and a first concentrated solution.
Then, the secondary ethyl acetate steam enters a second heat exchanger 4 through a secondary steam pipeline 10, cold water enters the second heat exchanger 4 through a cold water pipeline 9, the secondary ethyl acetate steam in the second heat exchanger 4 exchanges heat with the cold water to form water steam and ethyl acetate condensate, one part of the water steam enters a steam ejector 1 through a tertiary steam pipeline 11, the generated steam is introduced into a first heat exchanger 2, and the other part of the water steam enters a secondary first heat exchanger 202 through the tertiary steam pipeline 11 to exchange heat with the raw material liquid; the ethyl acetate condensate enters the organic solvent extraction system through an organic solvent extraction line 13.
Finally, the first concentrated solution flows back to the evaporator 3 through the second liquid circulating pipeline 8 to continue evaporation concentration.
In the later stage of evaporation and concentration, the ethyl acetate in the raw material liquid is evaporated, the temperature of the first heat exchanger 2 is raised under continuous heating, and the water in the raw material liquid is evaporated and cooled to form condensed water, and the condensed water flows into the waste liquid collecting system through a condensed water collecting pipeline 15 communicated with the first heat exchanger 2. The concentrated raw material liquid in the evaporator 3 is returned to the first heat exchanger 2 and is repeatedly evaporated and concentrated, and when the concentration detection means provided in the evaporator 3 detects that the concentration of the raw material liquid at the second raw material liquid outlet 305 of the evaporator 3 reaches a predetermined value, the concentrated raw material liquid can be discharged and collected through the raw material liquid collection pipe 14 communicating with the second raw material liquid outlet 305, and at this time, the evaporation and concentration process is completed.
By adopting the evaporation concentration system of the embodiment of the technical scheme, as the evaporation concentration system is provided with the first heat exchangers 2 and the evaporators 3, the secondary ethyl acetate steam can be more fully utilized, and the energy utilization rate of the evaporation concentration system is further improved. And moreover, the extraction process of the organic solvent of the ethyl acetate water condensate can be simplified, and the ethyl acetate in the ethyl acetate water condensate has high concentration, so that the ethyl acetate after the organic solvent is extracted has high quality and can be continuously used, and therefore, the evaporation concentration system adopting the technical scheme can effectively improve the recovery utilization rate of the ethyl acetate.
As shown in fig. 3, in another embodiment of the present invention, there are one steam ejector 1, one second heat exchanger 4, at least two first heat exchangers 2, the same number of evaporators 3 as the first heat exchangers 2, and the first heat exchangers 2 and the evaporators 3 arranged alternately, wherein:
the steam ejector 1 is communicated with the first heat exchanger 201 at the head end through a steam ejection pipeline 6, and the second first heat exchanger 202 is communicated with the second heat exchanger 4 through a tertiary steam pipeline 11;
the evaporative concentration system also includes an organic solvent extraction line in communication with the terminal evaporator 301.
In this embodiment, optionally, the first heat exchanger 2 includes a first raw material liquid inlet 203 and a first raw material liquid outlet 204, and the evaporator 3 includes a second raw material liquid inlet 303, a third raw material liquid inlet 304 and a second raw material liquid outlet 305;
the first heat exchanger 2 and the evaporator 3 which are sequentially communicated are an evaporation concentration group 12, for each evaporation concentration group 12, the first raw material liquid inlet 203 is communicated with the second raw material liquid outlet 305 through a first liquid circulation pipeline 7, the first raw material liquid outlet 204 is communicated with the third raw material liquid inlet 304 through a second liquid circulation pipeline 8, and the raw material liquid containing ethyl acetate enters the evaporator 3 through the second raw material liquid inlet 303.
In this embodiment, the second raw material liquid outlet 305 is optionally in communication with the raw material liquid collecting conduit 14.
Further, in this embodiment, optionally, the evaporation concentration system further includes a concentration detection device disposed in the evaporator 3, and the concentration detection device is configured to detect the concentration of the raw material liquid at the second raw material liquid outlet 305.
Furthermore, in this embodiment, optionally, the evaporation concentration system further comprises a condensed water collecting conduit 15 communicating with the first heat exchanger 2.
The present embodiment will be described in detail by taking an example in which one steam ejector 1 is provided, one second heat exchanger 4 is provided, two first heat exchangers 2 are provided, and two evaporators 3 are provided, and the embodiment is similar to that in the case where a plurality of first heat exchangers 2 and evaporators 3 are provided.
In this embodiment, first, raw steam enters the first heat exchanger 301 at the head end through the raw steam pipeline 5 and the steam ejector 1, raw material liquid containing ethyl acetate enters each evaporator 3 through the raw material liquid input pipeline to form ethyl acetate twice steam, and the raw material liquid containing ethyl acetate in the evaporator 3 returns to the first heat exchanger 2 through the first liquid circulation pipeline 7, so that the raw steam and the raw material liquid containing ethyl acetate exchange heat in the first heat exchanger 2 to form condensed water and a first concentrated solution.
Then, the secondary ethyl acetate steam generated by the head-end evaporator 301 enters the second heat exchanger 4 through the secondary steam pipeline 10, the cold water enters the second heat exchanger 4 through the cold water pipeline 9, the secondary ethyl acetate steam in the second heat exchanger 4 exchanges heat with the cold water to form water vapor, a part of the water vapor enters the steam ejector 1 through the tertiary steam pipeline 11, is introduced into the first heat exchanger 2 by the generated steam, and the other part of the water vapor enters the secondary first heat exchanger 202 through the tertiary steam pipeline 11 to exchange heat with the raw material liquid; the vapor of ethyl diacetate produced by the end evaporator 302 enters the organic solvent extraction system through organic solvent extraction line 13.
Finally, the first concentrated solution flows back to the evaporator 3 through the second liquid circulating pipeline 8 to continue evaporation concentration.
In the later stage of evaporation and concentration, the ethyl acetate in the raw material liquid is evaporated, the temperature of the first heat exchanger 2 is raised under continuous heating, and the water in the raw material liquid is evaporated and cooled to form condensed water, and the condensed water flows into the waste liquid collecting system through a condensed water collecting pipeline 15 communicated with the first heat exchanger 2. The concentrated raw material liquid in the evaporator 3 is returned to the first heat exchanger 2 and is repeatedly evaporated and concentrated, and when the concentration detection means provided in the evaporator 3 detects that the concentration of the raw material liquid at the second raw material liquid outlet 305 of the evaporator 3 reaches a predetermined value, the concentrated raw material liquid can be discharged and collected through the raw material liquid collection pipe 14 communicating with the second raw material liquid outlet 305, and at this time, the evaporation and concentration process is completed.
By adopting the evaporation concentration system of the embodiment of the technical scheme, as the evaporation concentration system is provided with the first heat exchangers 2 and the evaporators 3, the secondary ethyl acetate steam can be more fully utilized, and the energy utilization rate of the evaporation concentration system is further improved. And moreover, the organic solvent extraction process of the secondary ethyl acetate steam can be simplified, and the ethyl acetate in the secondary ethyl acetate steam has high concentration, so that the quality of the ethyl acetate after the organic solvent extraction is high, and the ethyl acetate can be continuously used, and therefore, the evaporation concentration system adopting the technical scheme can effectively improve the recovery utilization rate of the ethyl acetate.
As shown in fig. 4, based on the same inventive concept, the present invention further provides a method for preparing a concentrated solution by using the evaporation concentration system, comprising:
step 001: feeding the raw material liquid into an evaporator to generate a first concentrated liquid and organic solvent steam;
step 002: the organic solvent steam enters a second heat exchanger through a secondary steam pipeline;
step 003: the first concentrated solution flows back to the first heat exchanger for heat exchange to generate a second concentrated solution and condensed water;
step 004: cold water enters a second heat exchanger through a liquid pipeline to exchange heat with organic solvent steam to generate water vapor, the organic solvent steam is condensed into organic solvent solution, and the organic solvent solution enters an organic solvent extraction pipeline;
step 005: raw steam enters an ejector to inject water vapor into a first heat exchanger;
step 006: and the second concentrated solution flows back to the evaporator for repeated evaporation and concentration, and is collected when the concentration meets the requirement.
By adopting the method for preparing the concentrated solution in the technical scheme, the organic solvent-containing raw material solution is evaporated and concentrated, and on the basis of meeting the concentration requirement, the waste of secondary organic solvent steam is avoided, so that the energy utilization rate of an evaporation and concentration system is effectively improved; in addition, an organic solvent solution with higher concentration and better quality can be obtained, and the recovery rate of the organic solvent is improved.
It will be apparent to those skilled in the art that various changes and modifications may be made in the present invention without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims of the present invention and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (11)
1. An evaporative concentration system for evaporative concentration of a feed solution containing an organic solvent, the evaporative concentration system comprising: steam jet, first heat exchanger, evaporimeter and the second heat exchanger that communicates in proper order, wherein:
the steam ejector is communicated with the raw steam pipeline and the first heat exchanger through a steam ejection pipeline; the first heat exchanger is communicated with the evaporator through a first liquid circulation pipeline and a second liquid circulation pipeline; the evaporator is communicated with the second heat exchanger through a secondary steam pipeline; the second heat exchanger is communicated with the cold water pipeline and communicated with the steam ejector through a tertiary steam pipeline.
2. The evaporative concentration system of claim 1, further comprising an organic solvent extraction conduit in communication with the second heat exchanger.
3. The evaporative concentration system of claim 2, wherein the steam ejector is one, the first heat exchanger is one, the evaporator is one, and the second heat exchanger is one;
the first heat exchanger comprises a first raw material liquid inlet and a first raw material liquid outlet, and the evaporator comprises a second raw material liquid inlet, a third raw material liquid inlet and a second raw material liquid outlet; first raw material liquid import passes through first liquid circulation pipeline with the export intercommunication of second raw material liquid, first raw material liquid export with the import of third raw material liquid passes through the second liquid circulation pipeline intercommunication contains the import of organic solvent raw material liquid and gets into through the import of second raw material liquid the evaporimeter.
4. The evaporative concentration system of claim 2, wherein the steam ejector is one, the second heat exchanger is one, the first heat exchanger is at least two, the number of evaporators is the same as the number of first heat exchangers, and the first heat exchangers are arranged alternately with the evaporators, wherein:
the steam ejector is communicated with the first heat exchanger at the head end through a steam ejection pipeline, and the second heat exchanger is communicated with the second heat exchanger through a tertiary steam pipeline.
5. The evaporative concentration system of claim 4, wherein the first heat exchanger includes a first feed solution inlet and a first feed solution outlet, and the evaporator includes a second feed solution inlet, a third feed solution inlet and a second feed solution outlet;
the first heat exchanger and the evaporator which are communicated in sequence are evaporation concentration groups, for each evaporation concentration group, the first raw material liquid inlet is communicated with the second raw material liquid outlet through the first liquid circulation pipeline, the first raw material liquid outlet is communicated with the third raw material liquid inlet through the second liquid circulation pipeline, and the organic solvent-containing raw material liquid enters the evaporator through the second raw material liquid inlet.
6. The evaporative concentration system of claim 1, wherein the steam ejector is one, the second heat exchanger is one, the first heat exchangers are at least two, the number of evaporators is the same as the number of first heat exchangers, the first heat exchangers are arranged alternately with the evaporators, wherein:
the steam ejector is communicated with the first heat exchanger at the head end through a steam ejection pipeline, and the second heat exchanger is communicated with the second heat exchanger through a tertiary steam pipeline;
the evaporative concentration system further includes an organic solvent extraction conduit in communication with the terminal evaporator.
7. The evaporative concentration system of claim 6, wherein the first heat exchanger includes a first feed solution inlet and a first feed solution outlet, and the evaporator includes a second feed solution inlet, a third feed solution inlet and a second feed solution outlet;
the first heat exchanger and the evaporator which are communicated in sequence are evaporation concentration groups, for each evaporation concentration group, the first raw material liquid inlet is communicated with the second raw material liquid outlet through the first liquid circulation pipeline, the first raw material liquid outlet is communicated with the third raw material liquid inlet through the second liquid circulation pipeline, and the organic solvent-containing raw material liquid enters the evaporator through the second raw material liquid inlet.
8. The evaporative concentration system of claim 3, 5 or 7, wherein the second feed solution outlet is in communication with a feed solution collection conduit.
9. The evaporative concentration system of claim 8, further comprising a concentration detection device disposed in the evaporator, the concentration detection device being configured to detect the concentration of the feed solution at the second feed solution outlet.
10. The evaporative concentration system of claim 1, further comprising a condensate collection conduit in communication with the first heat exchanger.
11. A method of preparing a concentrate using the evaporative concentration system of any one of claims 1 to 5, including a feed concentration process, the method comprising:
feeding the raw material liquid into an evaporator to generate a first concentrated liquid and organic solvent steam;
the organic solvent steam enters a second heat exchanger through a secondary steam pipeline;
the first concentrated solution flows back to the first heat exchanger for heat exchange to generate a second concentrated solution and condensed water;
cold water enters a second heat exchanger through a cold water pipeline to exchange heat with organic solvent steam to generate water vapor, the organic solvent steam is condensed into organic solvent solution, and the organic solvent solution enters an organic solvent extraction pipeline;
raw steam enters an ejector to inject water vapor into a first heat exchanger;
and the second concentrated solution flows back to the evaporator for repeated evaporation and concentration, and is collected when the concentration meets the requirement.
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| CN202010346284.5A CN111544909A (en) | 2020-04-27 | 2020-04-27 | Evaporation concentration system |
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| CN202010346284.5A CN111544909A (en) | 2020-04-27 | 2020-04-27 | Evaporation concentration system |
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| CN202010346284.5A Pending CN111544909A (en) | 2020-04-27 | 2020-04-27 | Evaporation concentration system |
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Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2948541A1 (en) * | 1979-12-03 | 1981-06-04 | Nukem Gmbh, 6450 Hanau | METHOD AND DEVICE FOR MULTI-STAGE EVAPORATION |
| CN1098959A (en) * | 1994-05-21 | 1995-02-22 | 陈启松 | Energy saving evaporating apparatus |
| CN101745241A (en) * | 2009-12-31 | 2010-06-23 | 南京航空航天大学 | Method and device for producing calcium chloride solution through concentration |
| CN202015502U (en) * | 2011-04-08 | 2011-10-26 | 魏仕英 | Jet enthalpy increasing heat return type evaporator |
| CN102698451A (en) * | 2012-07-05 | 2012-10-03 | 大连理工大学 | Heat pump type low-temperature evaporating device and method |
| CN208877938U (en) * | 2018-09-28 | 2019-05-21 | 上海新奥新能源技术有限公司 | A kind of multiple-effect evaporation concentration systems |
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2020
- 2020-04-27 CN CN202010346284.5A patent/CN111544909A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2948541A1 (en) * | 1979-12-03 | 1981-06-04 | Nukem Gmbh, 6450 Hanau | METHOD AND DEVICE FOR MULTI-STAGE EVAPORATION |
| CN1098959A (en) * | 1994-05-21 | 1995-02-22 | 陈启松 | Energy saving evaporating apparatus |
| CN101745241A (en) * | 2009-12-31 | 2010-06-23 | 南京航空航天大学 | Method and device for producing calcium chloride solution through concentration |
| CN202015502U (en) * | 2011-04-08 | 2011-10-26 | 魏仕英 | Jet enthalpy increasing heat return type evaporator |
| CN102698451A (en) * | 2012-07-05 | 2012-10-03 | 大连理工大学 | Heat pump type low-temperature evaporating device and method |
| CN208877938U (en) * | 2018-09-28 | 2019-05-21 | 上海新奥新能源技术有限公司 | A kind of multiple-effect evaporation concentration systems |
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Inventor after: Chen Feng Inventor after: Qian Jin Inventor after: Liu Hongtao Inventor before: Chen Feng Inventor before: Liu Hongtao |
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Application publication date: 20200818 |