CN220159255U - Device for recovering acetonitrile through rough steaming, extraction, dehydration, concentration and concentration - Google Patents
Device for recovering acetonitrile through rough steaming, extraction, dehydration, concentration and concentration Download PDFInfo
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- CN220159255U CN220159255U CN202321613846.3U CN202321613846U CN220159255U CN 220159255 U CN220159255 U CN 220159255U CN 202321613846 U CN202321613846 U CN 202321613846U CN 220159255 U CN220159255 U CN 220159255U
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- WEVYAHXRMPXWCK-UHFFFAOYSA-N Acetonitrile Chemical compound CC#N WEVYAHXRMPXWCK-UHFFFAOYSA-N 0.000 title claims abstract description 153
- 238000000605 extraction Methods 0.000 title claims abstract description 93
- 230000018044 dehydration Effects 0.000 title claims abstract description 52
- 238000006297 dehydration reaction Methods 0.000 title claims abstract description 52
- 238000010025 steaming Methods 0.000 title claims description 7
- 239000007788 liquid Substances 0.000 claims abstract description 91
- 238000010992 reflux Methods 0.000 claims abstract description 74
- 238000004821 distillation Methods 0.000 claims abstract description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000002351 wastewater Substances 0.000 claims abstract description 32
- 238000003756 stirring Methods 0.000 claims abstract description 23
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 239000002994 raw material Substances 0.000 claims abstract description 18
- 238000003860 storage Methods 0.000 claims abstract description 15
- 239000000523 sample Substances 0.000 claims description 56
- 239000012071 phase Substances 0.000 claims description 32
- 239000000498 cooling water Substances 0.000 claims description 26
- 239000007791 liquid phase Substances 0.000 claims description 16
- 239000012808 vapor phase Substances 0.000 claims description 7
- 239000000243 solution Substances 0.000 abstract description 11
- 239000007864 aqueous solution Substances 0.000 abstract description 8
- 238000000034 method Methods 0.000 abstract description 5
- 238000001704 evaporation Methods 0.000 abstract 1
- 230000008020 evaporation Effects 0.000 abstract 1
- 208000005156 Dehydration Diseases 0.000 description 38
- 238000004064 recycling Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000012544 monitoring process Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000012824 chemical production Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The utility model provides a device for recovering acetonitrile through crude evaporation, extraction, dehydration, concentration and concentration. The device is equipped with raw materials on the head tank and advances the pipe, and the head tank is linked together with charge pump, stirring reboiler, crude distillation tower, residual liquid pump, no. two coolers, raffinate storage tank with the pipeline, and crude distillation tower top is linked together with condenser No. one, crude distillation reflux drum, reflux pump, extraction tower with pipeline and extraction tower solution pot, no. two reboilers, extraction tower solution pot are linked together, and extraction tower top is linked together with condenser No. two, extraction reflux drum, product reflux pump, product pot, extractant pump, no. one reboiler, dehydration tower, no. one cooler, no. three condensers, vacuum pump, overhead water reflux pot, waste water pump, waste water storage tank with the pipeline. The device carries out concentration recovery on the low-concentration acetonitrile aqueous solution through the organic combination of equipment, adopts extraction rectification to ensure that acetonitrile and water are easier to separate, and has simple process route, equipment investment saving and high automation degree and working efficiency.
Description
Technical Field
The utility model relates to the technical field of chemical equipment and wastewater treatment, in particular to a device for recovering acetonitrile through rough steaming, extraction, dehydration, concentration and recovery.
Background
Acetonitrile is a raw materials commonly used in the chemical industry field and widely used, in the production process of chemical industry, can retrieve high concentration acetonitrile solution from low concentrated acetonitrile aqueous solution, if directly discharge low concentrated acetonitrile aqueous solution, can produce very big pollution to the environment, still can produce very big waste to the raw materials simultaneously, consequently the chemical industry enterprise all can concentrate recovery to low concentrated acetonitrile aqueous solution. In the prior art, the operation mode of recovering acetonitrile by using multiple pressure swing towers is generally adopted, namely, an ordinary pressure acetonitrile crude distillation tower, an acetonitrile pressure reduction rectifying tower and an acetonitrile normal pressure rectifying tower are adopted to recover acetonitrile. The specific operation mode is as follows: (1) Firstly, removing heavy component residual liquid in mixed raw material liquid from the bottom of a tower by using a normal-pressure acetonitrile crude distillation tower; (2) The water vapor phase of the crude distilled acetonitrile enters an acetonitrile vacuum tower for rectification, water is separated from the bottom of the tower, and the top of the tower is an azeotrope of acetonitrile and water; (3) The azeotrope of acetonitrile and water enters an atmospheric tower again for rectification, a high-concentration acetonitrile product is obtained at the bottom of the tower, an acetonitrile aqueous solution higher than the azeotropic composition of acetonitrile and water is obtained at the top of the tower, and the aqueous solution at the top of the tower is added at the top of an acetonitrile vacuum tower for rectification. The prior art has the following defects: 1. the acetonitrile recovery process is complex, and the energy consumption of a recovery system is high; 2. the operation and running of the system are relatively unstable; 3. the recovery equipment adopted is more, the pipeline connection is complex, and the equipment investment cost is high. Because of the particularities of the chemical production process and the limitations of the equipment used, it is highly desirable to design a device for acetonitrile recovery.
Disclosure of Invention
The utility model aims to provide a device for recovering acetonitrile through rough steaming, extraction, dehydration, concentration and concentration. The technical problems to be solved by the utility model are as follows: the technical problems of complex acetonitrile concentration recovery process, high investment cost, high energy consumption, unstable operation and the like are solved through the organic combination of an acetonitrile crude distillation tower, an acetonitrile extraction tower, an extractant dehydration tower, a reboiler, a condenser, a cooler, various pumps and pipelines.
In order to achieve the above purpose, the technical scheme of the utility model is as follows:
an apparatus for recovering acetonitrile by rough steaming, extracting, dewatering, concentrating and recovering, comprising: the device is provided with a raw material inlet pipe on the raw material tank, the raw material tank is communicated with an inlet of the feed pump by a pipeline, the outlet of the feed pump is communicated with the stirring reboiler by a pipeline, the bottom of the stirring reboiler is communicated with the crude distillation tower by a pipeline, the lower part of the crude distillation tower is provided with the first temperature probe and the first liquid level probe, the crude distillation tower bottom is respectively communicated with an inlet of the residual liquid pump, the second liquid level probe is communicated with the reboiler of the stirring bottom and the residual liquid pump by a pipeline, the first liquid level probe is communicated with the reflux tank by a pipeline, the first liquid inlet of the crude distillation tower is communicated with the reflux tank by a pipeline, the first liquid phase inlet of the crude distillation tower is communicated with the reflux tank by a pipeline, the first liquid level probe is communicated with the reflux tank by a pipeline, the crude distillation tower is communicated with the crude distillation liquid phase inlet of the crude distillation tower by a pipeline, the crude distillation tower is communicated with the crude distillation tower by a pipeline, the extraction tower solution tank is communicated with the dehydration tower through a pipeline, the top of the extraction tower is communicated with the second condenser through an extraction gas phase pipe, the second condenser is communicated with the extraction reflux tank through a condensate pipe, the extraction reflux tank is communicated with the inlet of a product reflux pump through a pipeline, the outlet of the product reflux pump is communicated with the upper part of the extraction tower through a product reflux pipe, the product reflux tank is simultaneously communicated with the product tank through a pipeline, the second temperature probe and the second liquid level probe are installed on the lower part of the dehydration tower, the bottom of the dehydration tower is respectively communicated with the inlet of an extractant inlet pipe and an inlet of the extractant pump through a dehydration liquid phase pipe, the first reboiler is communicated with the dehydration tower through a reboiling gas phase pipe, the outlet of the extractant pump is communicated with the extraction tower through an extraction liquid inlet pipe, the first condenser is installed on the extraction liquid inlet pipe, the top of the dehydration tower is communicated with a third condenser through a dehydration gas phase pipe, the third condenser is respectively installed on the third condenser and is communicated with the vacuum pump through a drain pipe, the third condenser is communicated with the top of the wastewater reflux tank through a condensate pipe, and the wastewater outlet of the wastewater reflux tank is communicated with the top of the wastewater tank.
A first condenser, a second condenser, a third condenser, a first cooler and a second cooler in the device are respectively provided with a cooling water inlet pipe and a cooling water outlet pipe, and the cooling water outlet pipe is communicated with a circulating cooling water system.
The device is characterized in that a stirring reboiler, a first reboiler and a second reboiler are respectively provided with a steam inlet pipe and a condensed water outlet pipe, and the condensed water outlet pipe is communicated with a condensed water recovery system.
The feeding pump, the vacuum pump, the waste water pump, the extraction pump, the product reflux pump, the residual liquid pump, the first temperature probe, the second temperature probe, the third temperature probe, the first liquid level probe, the second liquid level probe and the third liquid level probe in the device are respectively connected with a control unit in a control room by leads.
The crude liquid tank, the crude distillation tower, the crude distillation reflux tank, the extraction tower, the dehydration tower, the extraction reflux tank, the overhead water reflux tank, the waste water storage tank, the product tank, the extraction tower solution tank, the residual liquid storage tank, the condenser, the cooler, the reboiler, various conveying pumps and the vacuum pump in the device are all chemical unit devices in the prior art, wherein the crude distillation tower and the extraction tower are normal pressure rectification towers, and the dehydration tower is a reduced pressure rectification tower; the temperature probe and the liquid level probe are all monitoring components commonly used in chemical units in the prior art.
Compared with the prior art, the utility model has the following positive effects:
1. the device is characterized in that low-concentration acetonitrile aqueous solution is concentrated and recovered through an acetonitrile crude distillation tower, an acetonitrile extraction tower, an extractant dehydration tower, a reboiler, a condenser, a cooler and organic combinations of various pumps and pipelines;
2. the device adopts extraction rectification, so that acetonitrile and water are easier to separate, thus greatly reducing the number of theoretical plates of the tower required by rectification, reducing the tower height and saving equipment investment;
3. the device carries out concentration recovery on the low-concentration acetonitrile aqueous solution through extraction and rectification, so that the concentration of the recovered acetonitrile is higher;
4. the device adopts extraction and rectification, acetonitrile and water are easy to separate, so that the operation is more stable;
5. the device has the advantages of simple process route, stable and controllable production operation, high degree of automation and high operation elasticity;
6. the device has low overall investment cost, low production cost, high working efficiency and great market competitiveness.
Drawings
The drawings that are required to be used in the embodiments for more clearly explaining the technology of the present utility model are briefly described. The drawings in the following description are merely exemplary and other implementations drawings may be derived from the drawings provided without inventive effort for a person of ordinary skill in the art.
The drawings described in the present specification are only for the purpose of combining the disclosure of the present specification, and are not intended to limit the applicable limitations of the present utility model, but are intended to cover any modifications of the structure, the changes of the ratio, or the adjustment of the size of the present utility model, without affecting the efficacy and achievement of the present utility model.
FIG. 1 is a schematic structural diagram of an acetonitrile crude steaming extraction dehydration recovery device;
FIG. 2, feed pump, vacuum pump, waste water pump, extractant pump, product return pump, residual liquid pump, temperature probe, liquid level probe and control room connection block diagram.
In the figure: 1. a raw material tank, 2, a raw material inlet pipe, 3, a feed pump, 4, a stirring reboiler, 5, a gas phase inlet pipe, 6, a temperature probe, 7, a liquid level probe, 8, a crude distillation column, 9, a return pipe, 10, a crude vapor phase pipe, 11, a condenser, 12, an evacuation pipe, 13, a crude distillation return tank, 14, a condensate pipe, 15, an extract inlet pipe, 16, an extraction column, 17, a product return pipe, 18, an extraction gas phase pipe, 19, a condenser No. two, 20, a cooling water outlet pipe, 21, a cooling water inlet pipe, 22, an extraction return tank, 23, a cooler No. one, 24, a dehydration tower, 25, a dehydration gas phase pipe, 26, a condenser No. three, 27, an exhaust pipe, 28, a vacuum pump, 29, a waste water return pipe, 30, overhead water reflux tank, 31, overhead water outlet pipe, 32, waste water storage tank, 33, waste water pump, 34, extractant inlet pipe, 35, no. two temperature probes, 36, no. two liquid level probes, 37, dehydration liquid phase pipe, 38, extraction pump, 39, reboiling liquid phase pipe, 40, product tank, 41, no. one reboiler, 42, reboiling gas phase pipe, 43, product reflux pump, 44, extraction tower solution tank, 45, no. three liquid level probes, 46, no. three temperature probes, 47, no. two reboiler, 48, condensate outlet pipe, 49, steam inlet pipe, 50, reflux liquid inlet pipe, 51, reflux pump, 52, crude vapor phase pipe, 53, raffinate pump, 54, no. two coolers, 55, raffinate storage tank, 56, vacuum pipe, 57, control room.
The direction indicated by the arrow in fig. 1 is the flow direction of the gas phase and the liquid phase in the pipeline.
Detailed Description
The technical scheme of the utility model is further clearly and completely described below with reference to the accompanying drawings.
Referring to fig. 1-2, the process parameters of the feed pump 3, vacuum pump 28, waste water pump 33, extraction pump 38, product return pump 43, return pump 51, residual pump 53, temperature probe 6, temperature probe 35, temperature probe 46, liquid level probe 7, liquid level probe 36, and liquid level probe 45 are respectively transmitted to the control unit of the control room 57 by the connection of the equipment and the pipelines and the input of the process parameters in the device.
The raw material inlet pipe 2 is arranged on the raw material tank 1, the raw material tank 1 is communicated with the inlet of the feeding pump 3 by a pipeline, the outlet of the feeding pump 3 is communicated with the stirring reboiler 4 by a pipeline, the bottom of the stirring reboiler 4 is communicated with the crude steam liquid phase pipe 52 by a pipeline, and the stirring reboiler 4 is communicated with the crude steam tower 8 by the gas phase inlet pipe 5. A first temperature probe 6 and a first liquid level probe 7 are arranged at the lower part of the crude distillation column 8, a crude distillation liquid phase pipe 52 is arranged at the bottom of the crude distillation column 8, the crude distillation liquid phase pipe 52 is respectively communicated with the bottom of the stirring reboiler 4 and the inlet of a residual liquid pump 53, the residual liquid pump 53 is communicated with a second cooler 54 by a pipeline, and the second cooler 54 is communicated with a residual liquid storage tank 55 by a pipeline. The top of the crude distillation column 8 is provided with a crude vapor phase pipe 10 which is communicated with a first condenser 11, the first condenser 11 is communicated with a crude distillation reflux drum 13 by a condensate pipe 14, the crude distillation reflux drum 13 is communicated with the inlet of a reflux pump 51 by a pipeline, the outlet of the reflux pump 51 is communicated with the upper part of the crude distillation column 8 by a reflux pipe 9, and the reflux liquid inlet pipe 50 is communicated with an extraction column 16. A third temperature probe 46 and a third liquid level probe 45 are arranged at the lower part of the extraction tower 16, the bottom of the extraction tower 16 is communicated with an extraction tower solution tank 44 by a pipeline, a reboiling liquid phase pipe 39 is communicated with a second reboiler 47, the reboiling gas phase pipe 42 is used for communicating the second reboiler 47 with the extraction tower 16, and the extraction tower solution tank 44 is communicated with a dehydration tower 24 by a pipeline. The top of the extraction tower 16 is connected with the second condenser 19 by an extraction gas phase pipe 18, the second condenser 19 is connected with the extraction reflux tank 22 by a condensate pipe 14, the extraction reflux tank 22 is connected with the inlet of a product reflux pump 43 by a pipeline, the outlet of the product reflux pump 43 is connected with the upper part of the extraction tower 16 by a product reflux pipe 17, and the product reflux tank is connected with a product tank 40 by a pipeline. A temperature probe No. 35 and a liquid level probe No. 36 are installed at the lower part of the dehydration column 24, and a dehydration liquid phase pipe 37 is installed at the bottom of the dehydration column 24 and is respectively connected with inlets of the extractant inlet pipe 34 and the extractant pump 38. The reboiling liquid phase pipe 39 is connected with the first reboiler 41, the reboiling gas phase pipe 42 is connected with the dehydration tower 24, the outlet of the extractant pump 38 is connected with the extraction tower 16 through the extraction liquid inlet pipe 15, and the first cooler 23 is arranged on the extraction liquid inlet pipe 15. The top of the dehydration column 24 is connected to a third condenser 26 by a dehydration gas phase pipe 25, the evacuation pipe 12 is respectively installed on the first condenser 11 and the second condenser 19, the gas phase of the third condenser 26 is connected to a vacuum pump 28 by a vacuum pipe 56, and the evacuation pipe 27 is installed on the vacuum pump 28. The third condenser 26 is connected to the overhead water reflux drum 30 by the condensate pipe 14, the overhead water reflux drum 30 is connected to the inlet of the wastewater pump 33 by the overhead water outlet pipe 31, the outlet of the wastewater pump 33 is connected to the top of the dehydration column 24 by the wastewater reflux pipe 29, and the wastewater pump 33 is connected to the wastewater tank 32 by a pipeline.
The cooling water inlet pipe 21 and the cooling water outlet pipe 20 are respectively arranged on the first condenser 11, the second condenser 19, the third condenser 26, the first cooler 23 and the second cooler 54, and the cooling water outlet pipe 20 is communicated with a circulating cooling water system.
The steam inlet pipe 49 and the condensed water outlet pipe 48 are respectively arranged on the stirring reboiler 4, the first reboiler 41 and the second reboiler 47, and the condensed water outlet pipe 48 is communicated with a condensed water recovery system.
In use, the operator turns on the feed pump 3, vacuum pump 28, waste water pump 33, extraction pump 38, product return pump 43, return pump 51, and residual liquid pump 53 via the control unit in control room 57.
Raw material liquid enters the raw material tank 1 from the raw material inlet pipe 2, enters the feed pump 3 through a connecting pipeline, enters the stirring reboiler 4 from the feed pump 3 through the connecting pipeline for stirring reboiling treatment, steam enters the stirring reboiler 4 through the steam inlet pipe 49 for heating liquid, and steam condensate is discharged through the condensate outlet pipe 48 and conveyed to the condensate recovery system for recycling. After being treated by the stirring reboiler 4, the heavy liquid sinks to the lower part of the stirring reboiler 4, the light liquid enters the crude distillation column 8 through the gas phase inlet pipe 5 to be subjected to crude distillation treatment, after the light liquid is subjected to crude distillation treatment, the heavy liquid sinks to the lower part of the crude distillation column 8, the crude distillation column 8 and the heavy liquid in the stirring reboiler 4 are conveyed to the residual liquid pump 53 through the crude distillation liquid pipe 52, the residual liquid pump 53 conveys the residual liquid into the second cooler 54 through a connecting pipeline to be subjected to cooling treatment, and the cooled residual liquid is conveyed to the residual liquid storage tank 55 through a pipeline to be stored. The gas phase formed by the crude steam tower 8 enters the first condenser 11 through the crude steam phase pipe 10, cooling water enters the first condenser 11 through the cooling water inlet pipe 21, the entered gas is condensed, and the cooled cooling water is discharged through the cooling water outlet pipe 20 and enters the circulating water system for recycling. The liquid condensed in the first condenser 11 enters the crude distillation reflux tank 13 through the condensate pipe 14, the liquid in the crude distillation reflux tank 13 enters the reflux pump 51 through the connecting pipeline, the output of the reflux pump 51 is divided into two paths, one path is communicated with the crude distillation tower 8 through the reflux pipe 9, and the liquid flows back into the crude distillation tower 8 to maintain the balance of the crude distillation system in the tower; and the second is communicated with a reflux liquid inlet pipe 50, and liquid enters the extraction tower 16 for extraction treatment.
The extractant enters the extractant pump 38 through the extractant inlet tube 34, and the extractant is conveyed into the first cooler 23 through the extractant inlet tube 15 at the outlet of the extractant pump 38 for cooling, and then enters the extraction tower 16. The water in acetonitrile is extracted into the extractant by the extraction tower 16 to form heavy phase flow to the lower part of the extraction tower 16, part of liquid is conveyed into the extraction tower solution tank 44 by a pipeline through the bottom pipeline of the extraction tower 16, part of liquid enters the No. two reboiler 47 by the reboiling liquid phase pipe 39, steam enters the No. two reboiler 47 by the steam inlet pipe 49 to heat the liquid, and steam condensate is discharged and conveyed to the condensate recovery system by the condensate outlet pipe 48 for recycling. The gas phase formed in reboiler No. two 47 is fed into extraction column 16 via reboiling gas phase line 42. The acetonitrile gas phase formed after the water in the acetonitrile is extracted in the extraction tower 16 enters a second condenser 19 through an extraction gas phase pipe 18, cooling water enters a first condenser 11 through a cooling water inlet pipe 21, the entered gas is subjected to condensation treatment, and the cooled cooling water is discharged through a cooling water outlet pipe 20 and enters a circulating water system for recycling. The acetonitrile liquid condensed in the second condenser 19 enters the extraction reflux tank 22 through the condensate pipe 14, and the acetonitrile liquid in the extraction reflux tank 22 enters the product reflux pump 43 through a connecting pipeline. The output of the product reflux pump 43 is divided into two paths, one is communicated with the extraction tower 16 by the product reflux pipe 17, and acetonitrile liquid is refluxed into the extraction tower 16 to maintain the balance of an extraction system in the tower; the two-purpose pipeline is communicated with the product tank 40, and acetonitrile liquid enters the product tank 40 for storage.
The extractant solution in the extraction column solution tank 44 enters the dehydration column 24 through a connecting pipeline to carry out dehydration treatment, the liquid formed in the dehydration column 24 flows to the lower part of the dehydration column 24, enters the first reboiler 41 through a reboiling liquid phase pipe 39 of a tower bottom pipeline, steam enters the first reboiler 41 through a steam inlet pipe 49 to heat the liquid, and steam condensate is discharged through a condensate water outlet pipe 48 and conveyed to a condensate water recovery system for recycling. The gas phase formed in reboiler 41 is fed into dehydration column 24 through reboiling gas phase pipe 42. The gas phase formed in the dehydration tower 24 enters a third condenser 26 through a dehydration gas phase pipe 25, cooling water enters a first condenser 11 through a cooling water inlet pipe 21, the entered gas is subjected to condensation treatment, and the cooled cooling water is discharged through a cooling water outlet pipe 20 and enters a circulating water system for recycling. The shell side of the first condenser 11 and the second condenser 19 are operated at normal pressure, the non-condensable gas phase is directly discharged through the evacuation pipe 12, the non-condensable tail gas formed by the third condenser 26 enters the vacuum pump 28 through the vacuum pipe 56, and the non-condensable tail gas is discharged through the exhaust pipe 27 by the vacuum pump 28. The liquid condensed in the third condenser 26 enters the overhead water reflux drum 30 through a pipeline, and the overhead water in the overhead water reflux drum 30 enters the wastewater pump 33 through an overhead water outlet pipe 31. The output of the waste water pump 33 is divided into two paths, one is communicated with the dehydration tower 24 by a waste water return pipe 29, and the tower top water is returned into the dehydration tower 24 to maintain the balance of a dehydration system in the tower; the two pipelines are communicated with the waste water storage tank 32, and waste water enters the waste water storage tank 32 for storage and subsequent treatment.
A first temperature probe 6 and a first liquid level probe 7 which are arranged in the crude distillation tower 8 are used for monitoring the temperature and the liquid level of the liquid in the crude distillation tower 8; a second temperature probe 35 and a second liquid level probe 36 which are arranged in the dehydration tower 24 and are used for monitoring the temperature and the liquid level of the liquid in the dehydration tower 24; a third temperature probe 46 and a third liquid level probe 45 are provided in the extraction column 16 for monitoring the temperature and level of the liquid in the extraction column 16.
The above description is only a non-limiting embodiment of the utility model, but numerous examples can be derived, which can be made by a person skilled in the art without departing from the inventive concept and without inventive effort, and which fall within the scope of protection of the utility model.
Claims (4)
1. An apparatus for recovering acetonitrile by rough steaming, extracting, dewatering, concentrating and recovering, comprising: feed pump (3), stirring reboiler (4), crude distillation tower (8), condenser No. 11), crude distillation reflux drum (13), extraction tower (16), condenser No. two (19), extraction reflux drum (22), cooler No. one (23), dehydration tower (24), no. three (26), vacuum pump (28), overhead water reflux drum (30), waste water storage tank (32), waste water pump (33), extraction pump (38), product tank (40), reboiler No. 41), product reflux pump (43), extraction tower solution pot (44), reboiler No. two (47), reflux pump (51), residual liquid pump (53), no. two coolers (54), raffinate storage tank (55), control room (57), temperature probe No. 6) to No. three (46), liquid level probe No. 7) to No. three (45) and each connecting line, its characterized in that: the device is characterized in that a raw material inlet pipe (2) is arranged on a raw material tank (1), the raw material tank (1) is communicated with an inlet of a feed pump (3) through a pipeline, an outlet of the feed pump (3) is communicated with a stirring reboiler (4) through a pipeline, the bottom of the stirring reboiler (4) is communicated with a crude vapor phase pipe (52), a gas phase inlet pipe (5) of the stirring reboiler (4) is communicated with a crude vapor column (8), a first temperature probe (6) and a first liquid level probe (7) are arranged at the lower part of the crude vapor column (8), the crude vapor phase pipe (52) at the bottom of the crude vapor column (8) is respectively communicated with the bottom of the stirring reboiler (4) and an inlet of a residual liquid pump (53), the residual liquid pump (53) is communicated with a second cooler (54) through a pipeline, the top of the crude vapor column (8) is communicated with a first condenser (11) through a crude vapor phase pipe (10), the condensate liquid return pipe (14) at the bottom of the crude vapor column (8) is communicated with a reflux pump (13) through a reflux pipe (51), the reflux liquid return pipe (13) is communicated with the reflux pump (13) through a reflux pipe (51, a third temperature probe (46) and a third liquid level probe (45) are arranged at the lower part of the extraction tower (16), the bottom of the extraction tower (16) is communicated with an extraction tower solution tank (44) through a pipeline, a reboiling liquid phase pipe (39) is communicated with a second reboiler (47), the second reboiler (47) is communicated with the extraction tower (16) through a reboiling gas phase pipe (42), the extraction tower solution tank (44) is communicated with a dehydration tower (24) through a pipeline, an extraction gas phase pipe (18) is communicated with a second condenser (19) at the top of the extraction tower (16), the second condenser (19) is communicated with an extraction reflux tank (22) through a condensate pipe (14), the extraction reflux tank (22) is communicated with an inlet of a product reflux pump (43), an outlet of the product reflux pump (43) is communicated with the upper part of the extraction tower (16) through a pipeline, a second temperature probe (35) and a second liquid level probe (36) are arranged at the lower part of the dehydration tower (24), the bottom of the dehydration tower (24) is communicated with an inlet of the liquid phase pipe (37) through a condensate pipe (37) and the extraction reflux pump (41), a first reboiler (41) is communicated with a dehydration tower (24) through a reboiling gas phase pipe (42), an extraction liquid inlet pipe (15) for the outlet of an extraction pump (38) is communicated with the extraction tower (16), a first cooler (23) is arranged on the extraction liquid inlet pipe (15), the top of the dehydration tower (24) is communicated with a third condenser (26) through a dehydration gas phase pipe (25), an evacuation pipe (12) is respectively arranged on the first condenser (11) and the second condenser (19), a vacuum pipe (56) is arranged on the third condenser (26) and is communicated with a vacuum pump (28), an exhaust pipe (27) is arranged on the vacuum pump (28), the third condenser (26) is communicated with a top water reflux tank (30) through a condensate pipe (14), the top water reflux tank (30) is communicated with the inlet of a waste water pump (33) through a top water outlet pipe (31), the outlet of the waste water pump (33) is communicated with the top of the dehydration tower (24) through a waste water reflux pipe (29), and the waste water reflux pipe (32) is simultaneously communicated with a storage tank (32).
2. The device for recovering acetonitrile crude distillation, extraction, dehydration, concentration and recovery according to claim 1, wherein: a first condenser (11), a second condenser (19), a third condenser (26), a first cooler (23) and a second cooler (54) in the device are respectively provided with a cooling water inlet pipe (21) and a cooling water outlet pipe (20), and the cooling water outlet pipe (20) is communicated with a circulating cooling water system.
3. The device for recovering acetonitrile crude distillation, extraction, dehydration, concentration and recovery according to claim 1, wherein: the device is characterized in that a stirring reboiler (4), a first reboiler (41) and a second reboiler (47) are respectively provided with a steam inlet pipe (49) and a condensed water outlet pipe (48), and the condensed water outlet pipe (48) is communicated with a condensed water recovery system.
4. The device for recovering acetonitrile crude distillation, extraction, dehydration, concentration and recovery according to claim 1, wherein: the device comprises a feeding pump (3), a vacuum pump (28), a waste water pump (33), an extraction pump (38), a product reflux pump (43), a reflux pump (51), a residual liquid pump (53), a first temperature probe (6), a second temperature probe (35), a third temperature probe (46), a first liquid level probe (7), a second liquid level probe (36) and a third liquid level probe (45), wherein the third liquid level probe (45) is connected with a control unit in a control room (57) through leads.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321613846.3U CN220159255U (en) | 2023-06-25 | 2023-06-25 | Device for recovering acetonitrile through rough steaming, extraction, dehydration, concentration and concentration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321613846.3U CN220159255U (en) | 2023-06-25 | 2023-06-25 | Device for recovering acetonitrile through rough steaming, extraction, dehydration, concentration and concentration |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN220159255U true CN220159255U (en) | 2023-12-12 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321613846.3U Active CN220159255U (en) | 2023-06-25 | 2023-06-25 | Device for recovering acetonitrile through rough steaming, extraction, dehydration, concentration and concentration |
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| Country | Link |
|---|---|
| CN (1) | CN220159255U (en) |
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2023
- 2023-06-25 CN CN202321613846.3U patent/CN220159255U/en active Active
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