CN205635427U - Continuous negative pressure of acetonitrile distillation extraction device - Google Patents
Continuous negative pressure of acetonitrile distillation extraction device Download PDFInfo
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- CN205635427U CN205635427U CN201620403476.4U CN201620403476U CN205635427U CN 205635427 U CN205635427 U CN 205635427U CN 201620403476 U CN201620403476 U CN 201620403476U CN 205635427 U CN205635427 U CN 205635427U
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Abstract
The utility model relates to a continuous negative pressure of acetonitrile distillation extraction device, it includes acetonitrile dehydration column, extraction rectifying column and glycol dehydration tower, the acetonitrile dehydration column is connected with waste liquid recycling pump and waste liquid reboiler, the acetonitrile dehydration column is connected with high enriched acetonitrile one -level condenser and high enriched acetonitrile second grade condenser, and high enriched acetonitrile second grade condenser is connected with high enriched acetonitrile return tank, and high enriched acetonitrile return tank is connected with high enriched acetonitrile circulating pump, extraction rectifying tower connected has 99% acetonitrile one -level condenser and 99% acetonitrile second grade condenser, and 99% acetonitrile second grade condenser is connected with 99% acetonitrile return tank and acetonitrile vacuum pump, extraction rectifying tower connected has ethylene glycol circulating pump A, and ethylene glycol circulating pump A is connected with the ethylene glycol pre -heater, and the ethylene glycol pre -heater is connected with acetonitrile tower reboiler, the glycol dehydration tower is connected with ethylene glycol circulating pump B, ethylene glycol reboiler and the interim groove of ethylene glycol, and the interim groove of ethylene glycol is connected with the ethylene glycol vacuum pump, the utility model has the advantages of the energy can be saved, purification degree height.
Description
Technical field
This utility model relates to a kind of distilling and extracting device, belongs to acetonitrile and purifies field, is specially a kind of acetonitrile continuous negative pressure distilling and extracting device.
Background technology
During producing acetonitrile, use in " glacial acetic acid+liquefied ammonia " synthesis crude acetonitrile containing acetonitrile 52%, water 47%, ammonium sulfate 1% and a small amount of acetone, propionitrile, tar etc.；In order to obtain the pure acetonitrile of content more than 99%, needing to purify the crude acetonitrile of synthesis, during purifying acetonitrile, crude acetonitrile dehydration is obtained water content is 30% high concentration acetonitrile；In common acetonitrile distilling and extracting device, extractive distillation column is added after first aqueous high concentration acetonitrile being heated to 80 DEG C, 180 DEG C will be heated to without water glycol simultaneously and add extractive distillation column, in extractive distillation column, carry out heat exchange and sleep is changed, the water of high concentration acetonitrile seizes without water glycol in being extracted rectifying column, high concentration acetonitrile absorbs without being vaporizated into pure acetonitrile after the heat of water glycol, the pure acetonitrile obtained enters acetonitrile after extractive distillation column is drawn up after condenser is cooled to liquid and receives tank, go out from the bottom of extractive distillation column after obtaining water without water glycol, recirculate after glycol dehydration column distillation is dehydrated and use；But such acetonitrile extraction distillation process, the high concentration acetonitrile needing aqueous 30% adds extractive distillation column after being heated to 80 DEG C, extractive distillation column is added after requiring heat to 180 DEG C without water glycol, during this, consumed energy is bigger, will necessarily cause serious energy waste and economic loss for manufacturing enterprise.
Summary of the invention
This utility model provide for overcoming the deficiencies in the prior art a kind of save the energy, cost-effective, flow process is stable, easy operation, acetonitrile continuous negative pressure distilling and extracting device that purification degree is high.
The technical solution of the utility model is: a kind of acetonitrile continuous negative pressure distilling and extracting device, it includes acetonitrile dehydrating tower, extractive distillation column and glycol dehydration tower, the middle part of described acetonitrile dehydrating tower connects crude acetonitrile water input duct, connected by pipeline bottom acetonitrile dehydrating tower and have waste liquid circulation pump, connecting at described waste liquid circulation delivery side of pump and have waste liquid discharge line and waste liquid reboiler, described waste liquid reboiler is connected bottom acetonitrile dehydrating tower by pipeline；The top of acetonitrile dehydrating tower is connected with highly concentrated acetonitrile first-stage condenser and highly concentrated acetonitrile secondary condenser in turn by pipeline, described highly concentrated acetonitrile secondary condenser is connected by pipeline highly concentrated acetonitrile return tank, described highly concentrated acetonitrile return tank is connected by pipeline highly concentrated acetonitrile circulating pump, one pipeline of the outlet of described highly concentrated acetonitrile circulating pump is connected with the top of acetonitrile dehydrating tower, and another pipeline of the outlet of highly concentrated acetonitrile circulating pump is connected with the middle part inlet of extractive distillation column；The top of described extractive distillation column is connected with 99% acetonitrile first-stage condenser and 99% acetonitrile secondary condenser in turn by pipeline, 99% described acetonitrile secondary condenser is connected by pipeline 99% acetonitrile return tank, the top of 99% described acetonitrile return tank is connected by pipeline acetonitrile vacuum pump, the bottom of 99% acetonitrile return tank is connected by pipeline acetonitrile circulating pump, one pipeline in the exit of described acetonitrile circulating pump is connected with the top of extractive distillation column, another pipeline in the exit of acetonitrile circulating pump connects pure acetonitrile circulating pump, described pure acetonitrile circulation delivery side of pump is connected by pipeline high-boiling components dashpot, described high-boiling components dashpot is connected by pipeline 99% acetonitrile dashpot；The top of extractive distillation column connects ethylene glycol water influent pipeline, the bottom of extractive distillation column is connected by pipeline glycol circulation pump A, one pipeline in the exit of described glycol circulation pump A connects ethylene glycol preheater, described ethylene glycol preheater is connected by pipeline acetonitrile tower reboiler, described acetonitrile tower reboiler is connected with the bottom of extractive distillation column by pipeline, and another pipeline in the exit of glycol circulation pump A is connected with the middle part of glycol dehydration tower；The top of described glycol dehydration tower is connected by pipeline tower top distilled water collecting tank, the bottom of glycol dehydration tower is connected by pipeline glycol circulation pump B, the exit of described glycol circulation pump B is connected by pipeline ethylene glycol reboiler and the interim groove of ethylene glycol, described ethylene glycol reboiler is connected in the middle part of glycol dehydration tower by pipeline, and the top of the interim groove of described ethylene glycol is connected by pipeline ethylene vacuum pump.
The exit of described glycol circulation pump B is connected with ethylene glycol preheater by pipeline.
It is connected by pipeline between described glycol dehydration tower with tower top distilled water collecting tank and has distiller condenser.
Being provided with two sector hole mellapak packings in described acetonitrile dehydrating tower, be provided above the liquid distribution trough A, described liquid distribution trough A of described every sector hole mellapak packing are connected with crude acetonitrile input duct.
Being provided with three sections of wire packing A in described extractive distillation column, every section of described wire packing A is provided above liquid distribution trough B.
Being provided with two sections of wire packing B in described glycol dehydration tower, every section of described wire packing B is provided above liquid distribution trough C.
The beneficial effects of the utility model are: this utility model is realized in, first crude acetonitrile is preheated to 70-80 DEG C of addition acetonitrile dehydrating tower and carries out rectification separation, acetonitrile dehydration tower top obtains the steam of acetonitrile and water, acetonitrile enters highly concentrated acetonitrile return tank with the steam of water after highly concentrated acetonitrile first-stage condenser and highly concentrated acetonitrile secondary condenser liquefy, highly concentrated acetonitrile in highly concentrated acetonitrile return tank is back to acetonitrile dehydrating tower through the extraction of highly concentrated acetonitrile circulating pump, water and the impurity taken off at the bottom of tower are drawn into waste liquid reboiler through waste liquid circulation pump, finally enter acetonitrile dehydrating tower to be circulated；nullWhen at the bottom of tower, waste liquid can't detect acetonitrile，Waste liquid at the bottom of tower is got by waste liquid circulation pump and is reclaimed，Highly concentrated acetonitrile in the most highly concentrated acetonitrile return tank sends into extractive distillation column by highly concentrated acetonitrile circulating pump，Added in extractive distillation column containing without water glycol, highly concentrated acetonitrile being carried out extractive distillation purification by ethylene glycol water influent pipeline simultaneously，Detection continual to extracting rectifying tower bottom liquid during purifying，When the ethane nitrile content of extracting rectifying tower bottom liquid is more than 0.2%，The acetonitrile steam of extracting rectifying tower top enters 99% acetonitrile return tank after 99% acetonitrile first-stage condenser and 99% acetonitrile secondary condenser liquefy，Pure acetonitrile in 99% acetonitrile return tank is circulated rectification and purification in extractive distillation column squeezed into by pure acetonitrile circulating pump，Extracting rectifying tower bottom liquid squeezes into ethylene glycol preheater through glycol circulation pump A，Through ethylene glycol reboiler backflow such as extractive distillation column, the acetonitrile in tower bottom liquid is purified further again；When the ethane nitrile content of extracting rectifying tower bottom liquid is less than 0.2%, pure acetonitrile in 99% acetonitrile return tank is squeezed in high-boiling components dashpot through pure acetonitrile circulating pump, final pure acetonitrile enters in 99% acetonitrile dashpot, extracting rectifying tower bottom liquid carries out dehydration purification in glycol circulation pump A squeezes into glycol dehydration tower simultaneously, when the water content of glycol dehydration tower bottom liquid is less than 0.2%, glycol dehydration tower bottom liquid is squeezed into extractive distillation column by glycol circulation pump B and is circulated use, it is also possible to squeezes into the interim groove of ethylene glycol and stores；Acetonitrile vacuum pump is had owing to 99% acetonitrile return tank connects, the interim groove of ethylene glycol connects ethylene vacuum pump, and 99% acetonitrile return tank connect with extractive distillation column, the interim groove of ethylene glycol connects with glycol dehydration tower, thus realizing extractive distillation column and glycol dehydration tower is negative pressure state；In this utility model, acetonitrile dehydrating tower is that normal pressure, extractive distillation column and glycol dehydration tower are negative pressure, thus greatly reduce the energy consumption in acetonitrile purification process, and improve the purification rate of acetonitrile；This utility model have save the energy, cost-effective, flow process is stable, easy operation, advantage that purification degree is high.
Accompanying drawing explanation
Fig. 1 is the structural representation of this utility model a kind of acetonitrile continuous negative pressure distilling and extracting device.
nullIn figure: 1、Acetonitrile dehydrating tower 2、Extractive distillation column 3、Glycol dehydration tower 4、Crude acetonitrile water input duct 5、Waste liquid circulation pump 6、Waste liquid discharge line 7、Waste liquid reboiler 8、Highly concentrated acetonitrile first-stage condenser 9、Highly concentrated acetonitrile secondary condenser 10、Highly concentrated acetonitrile return tank 11、Highly concentrated acetonitrile circulating pump 12、99% acetonitrile first-stage condenser 13、99% acetonitrile secondary condenser 14、99% acetonitrile return tank 15、Acetonitrile vacuum pump 16、Acetonitrile circulating pump 17、Pure acetonitrile circulating pump 18、High-boiling components dashpot 19、99% acetonitrile dashpot 20、Ethylene glycol water influent pipeline 21、Glycol circulation pump A 22、Ethylene glycol preheater 23、Acetonitrile tower reboiler 24、Tower top distilled water collecting tank 25、Glycol circulation pump B 26、Ethylene glycol reboiler 27、The interim groove of ethylene glycol 28、Ethylene vacuum pump 29、Distiller condenser 30、Perforated plate corrugated filler 31、Liquid distribution trough A 32、Wire packing A 33、Liquid distribution trough B 34、Wire packing B 35、Liquid distribution trough C.
Detailed description of the invention
Embodiment 1
As Figure 1-4, a kind of acetonitrile continuous negative pressure distilling and extracting device, it includes acetonitrile dehydrating tower 1, extractive distillation column 2 and glycol dehydration tower 3, the middle part of described acetonitrile dehydrating tower 1 connects crude acetonitrile water input duct 4, connected by pipeline bottom acetonitrile dehydrating tower 1 and have waste liquid circulation pump 5, the exit of described waste liquid circulation pump 5 connects waste liquid discharge line 6 and waste liquid reboiler 7, and described waste liquid reboiler 7 is connected with at the bottom of acetonitrile dehydrating tower 1 by pipeline；The top of acetonitrile dehydrating tower 1 is connected with highly concentrated acetonitrile first-stage condenser 8 and highly concentrated acetonitrile secondary condenser 9 in turn by pipeline, described highly concentrated acetonitrile secondary condenser 9 is connected by pipeline highly concentrated acetonitrile return tank 10, described highly concentrated acetonitrile return tank 10 is connected by pipeline highly concentrated acetonitrile circulating pump 11, one pipeline of the outlet of described highly concentrated acetonitrile circulating pump 11 is connected with the top of acetonitrile dehydrating tower 1, and another pipeline of the outlet of highly concentrated acetonitrile circulating pump 11 is connected with the middle part inlet of extractive distillation column 2；nullThe top of described extractive distillation column 2 is connected with 99% acetonitrile first-stage condenser 12 and 99% acetonitrile secondary condenser 13 in turn by pipeline，99% described acetonitrile secondary condenser 13 is connected by pipeline 99% acetonitrile return tank 14，The top of 99% described acetonitrile return tank 14 is connected by pipeline acetonitrile vacuum pump 15，The bottom of 99% acetonitrile return tank 14 is connected by pipeline acetonitrile circulating pump 16，One pipeline in the exit of described acetonitrile circulating pump 16 is connected with the top of extractive distillation column 2，Another pipeline in the exit of acetonitrile circulating pump 16 connects pure acetonitrile circulating pump 17，The outlet of described pure acetonitrile circulating pump 17 is connected by pipeline high-boiling components dashpot 18，Described high-boiling components dashpot 18 is connected by pipeline 99% acetonitrile dashpot 19；The top of extractive distillation column 2 connects ethylene glycol water influent pipeline 20, the bottom of extractive distillation column 2 is connected by pipeline glycol circulation pump A21, one pipeline in the exit of described glycol circulation pump A21 connects ethylene glycol preheater 22, described ethylene glycol preheater 22 is connected by pipeline acetonitrile tower reboiler 23, described acetonitrile tower reboiler 23 is connected with the bottom of extractive distillation column 2 by pipeline, and another pipeline in the exit of glycol circulation pump A21 is connected with the middle part of glycol dehydration tower 3；The top of described glycol dehydration tower 3 is connected by pipeline tower top distilled water collecting tank 24, the bottom of glycol dehydration tower 3 is connected by pipeline glycol circulation pump B25, the exit of described glycol circulation pump B25 is connected by pipeline ethylene glycol reboiler 26 and the interim groove of ethylene glycol 27, described ethylene glycol reboiler 26 is connected in the middle part of glycol dehydration tower 3 by pipeline, and the top of the interim groove of described ethylene glycol 27 is connected by pipeline ethylene vacuum pump 28.
This utility model is realized in, first crude acetonitrile is preheated to 70-80 DEG C of addition acetonitrile dehydrating tower and carries out rectification separation, acetonitrile dehydration tower top obtains the steam of acetonitrile and water, acetonitrile enters highly concentrated acetonitrile return tank with the steam of water after highly concentrated acetonitrile first-stage condenser and highly concentrated acetonitrile secondary condenser liquefy, highly concentrated acetonitrile in highly concentrated acetonitrile return tank is back to acetonitrile dehydrating tower through the extraction of highly concentrated acetonitrile circulating pump, water and the impurity taken off at the bottom of tower are drawn into waste liquid reboiler through waste liquid circulation pump, finally enter acetonitrile dehydrating tower and are circulated；nullWhen at the bottom of tower, waste liquid can't detect acetonitrile，Waste liquid at the bottom of tower is got by waste liquid circulation pump and is reclaimed，Highly concentrated acetonitrile in the most highly concentrated acetonitrile return tank sends into extractive distillation column by highly concentrated acetonitrile circulating pump，Added in extractive distillation column containing without water glycol, highly concentrated acetonitrile being carried out extractive distillation purification by ethylene glycol water influent pipeline simultaneously，Detection continual to extracting rectifying tower bottom liquid during purifying，When the ethane nitrile content of extracting rectifying tower bottom liquid is more than 0.2%，The acetonitrile steam of extracting rectifying tower top enters 99% acetonitrile return tank after 99% acetonitrile first-stage condenser and 99% acetonitrile secondary condenser liquefy，Pure acetonitrile in 99% acetonitrile return tank is circulated rectification and purification in extractive distillation column squeezed into by pure acetonitrile circulating pump，Extracting rectifying tower bottom liquid squeezes into ethylene glycol preheater through glycol circulation pump A，Through ethylene glycol reboiler backflow such as extractive distillation column, the acetonitrile in tower bottom liquid is purified further again；When the ethane nitrile content of extracting rectifying tower bottom liquid is less than 0.2%, pure acetonitrile in 99% acetonitrile return tank is squeezed in high-boiling components dashpot through pure acetonitrile circulating pump, final pure acetonitrile enters in 99% acetonitrile dashpot, extracting rectifying tower bottom liquid carries out dehydration purification in glycol circulation pump A squeezes into glycol dehydration tower simultaneously, when the water content of glycol dehydration tower bottom liquid is less than 0.2%, glycol dehydration tower bottom liquid is squeezed into extractive distillation column by glycol circulation pump B and is circulated use, it is also possible to squeezes into the interim groove of ethylene glycol and stores；Acetonitrile vacuum pump is had owing to 99% acetonitrile return tank connects, the interim groove of ethylene glycol connects ethylene vacuum pump, and 99% acetonitrile return tank connect with extractive distillation column, the interim groove of ethylene glycol connects with glycol dehydration tower, thus realizing extractive distillation column and glycol dehydration tower is negative pressure state；In this utility model, acetonitrile dehydrating tower is that normal pressure, extractive distillation column and glycol dehydration tower are negative pressure, thus greatly reduce the energy consumption in acetonitrile purification process, and improve the purification rate of acetonitrile；This utility model have save the energy, cost-effective, flow process is stable, easy operation, advantage that purification degree is high.
Embodiment 2
As Figure 1-4, a kind of acetonitrile continuous negative pressure distilling and extracting device, it includes acetonitrile dehydrating tower 1, extractive distillation column 2 and glycol dehydration tower 3, the middle part of described acetonitrile dehydrating tower 1 connects crude acetonitrile water input duct 4, connected by pipeline bottom acetonitrile dehydrating tower 1 and have waste liquid circulation pump 5, the exit of described waste liquid circulation pump 5 connects waste liquid discharge line 6 and waste liquid reboiler 7, and described waste liquid reboiler 7 is connected with at the bottom of acetonitrile dehydrating tower 1 by pipeline；The top of acetonitrile dehydrating tower 1 is connected with highly concentrated acetonitrile first-stage condenser 8 and highly concentrated acetonitrile secondary condenser 9 in turn by pipeline, described highly concentrated acetonitrile secondary condenser 9 is connected by pipeline highly concentrated acetonitrile return tank 10, described highly concentrated acetonitrile return tank 10 is connected by pipeline highly concentrated acetonitrile circulating pump 11, one pipeline of the outlet of described highly concentrated acetonitrile circulating pump 11 is connected with the top of acetonitrile dehydrating tower 1, and another pipeline of the outlet of highly concentrated acetonitrile circulating pump 11 is connected with the middle part inlet of extractive distillation column 2；nullThe top of described extractive distillation column 2 is connected with 99% acetonitrile first-stage condenser 12 and 99% acetonitrile secondary condenser 13 in turn by pipeline，99% described acetonitrile secondary condenser 13 is connected by pipeline 99% acetonitrile return tank 14，The top of 99% described acetonitrile return tank 14 is connected by pipeline acetonitrile vacuum pump 15，The bottom of 99% acetonitrile return tank 14 is connected by pipeline acetonitrile circulating pump 16，One pipeline in the exit of described acetonitrile circulating pump 16 is connected with the top of extractive distillation column 2，Another pipeline in the exit of acetonitrile circulating pump 16 connects pure acetonitrile circulating pump 17，The outlet of described pure acetonitrile circulating pump 17 is connected by pipeline high-boiling components dashpot 18，Described high-boiling components dashpot 18 is connected by pipeline 99% acetonitrile dashpot 19；The top of extractive distillation column 2 connects ethylene glycol water influent pipeline 20, the bottom of extractive distillation column 2 is connected by pipeline glycol circulation pump A21, one pipeline in the exit of described glycol circulation pump A21 connects ethylene glycol preheater 22, described ethylene glycol preheater 22 is connected by pipeline acetonitrile tower reboiler 23, described acetonitrile tower reboiler 23 is connected with the bottom of extractive distillation column 2 by pipeline, and another pipeline in the exit of glycol circulation pump A21 is connected with the middle part of glycol dehydration tower 3；The top of described glycol dehydration tower 3 is connected by pipeline tower top distilled water collecting tank 24, the bottom of glycol dehydration tower 3 is connected by pipeline glycol circulation pump B25, the exit of described glycol circulation pump B25 is connected by pipeline ethylene glycol reboiler 26 and the interim groove of ethylene glycol 27, described ethylene glycol reboiler 26 is connected in the middle part of glycol dehydration tower 3 by pipeline, and the top of the interim groove of described ethylene glycol 27 is connected by pipeline ethylene vacuum pump 28；The exit of described glycol circulation pump B25 is connected with ethylene glycol preheater 22 by pipeline；It is connected by pipeline between the 24 of described glycol dehydration tower 3 and tower top distilled water collecting tank and has distiller condenser 29；Being provided with two sector hole mellapak packings 30 in described acetonitrile dehydrating tower 1, be provided above the liquid distribution trough A31, described liquid distribution trough A31 of described every sector hole mellapak packing 30 are connected with crude acetonitrile input duct 4；Being provided with three sections of wire packing A32 in described extractive distillation column 2, every section of described wire packing A32 is provided above liquid distribution trough B33；Being provided with two sections of wire packing B34 in described glycol dehydration tower 3, every section of described wire packing B34 is provided above liquid distribution trough C35.
This utility model is realized in, first crude acetonitrile is preheated to 70-80 DEG C of addition acetonitrile dehydrating tower and carries out rectification separation, acetonitrile dehydration tower top obtains the steam of acetonitrile and water, acetonitrile enters highly concentrated acetonitrile return tank with the steam of water after highly concentrated acetonitrile first-stage condenser and highly concentrated acetonitrile secondary condenser liquefy, highly concentrated acetonitrile in highly concentrated acetonitrile return tank is back to acetonitrile dehydrating tower through the extraction of highly concentrated acetonitrile circulating pump, water and the impurity taken off at the bottom of tower are drawn into waste liquid reboiler through waste liquid circulation pump, finally enter acetonitrile dehydrating tower and are circulated；nullWhen at the bottom of tower, waste liquid can't detect acetonitrile，Waste liquid at the bottom of tower is got by waste liquid circulation pump and is reclaimed，Highly concentrated acetonitrile in the most highly concentrated acetonitrile return tank sends into extractive distillation column by highly concentrated acetonitrile circulating pump，Added in extractive distillation column containing without water glycol, highly concentrated acetonitrile being carried out extractive distillation purification by ethylene glycol water influent pipeline simultaneously，Detection continual to extracting rectifying tower bottom liquid during purifying，When the ethane nitrile content of extracting rectifying tower bottom liquid is more than 0.2%，The acetonitrile steam of extracting rectifying tower top enters 99% acetonitrile return tank after 99% acetonitrile first-stage condenser and 99% acetonitrile secondary condenser liquefy，Pure acetonitrile in 99% acetonitrile return tank is circulated rectification and purification in extractive distillation column squeezed into by pure acetonitrile circulating pump，Extracting rectifying tower bottom liquid squeezes into ethylene glycol preheater through glycol circulation pump A，Through ethylene glycol reboiler backflow such as extractive distillation column, the acetonitrile in tower bottom liquid is purified further again；When the ethane nitrile content of extracting rectifying tower bottom liquid is less than 0.2%, pure acetonitrile in 99% acetonitrile return tank is squeezed in high-boiling components dashpot through pure acetonitrile circulating pump, final pure acetonitrile enters in 99% acetonitrile dashpot, extracting rectifying tower bottom liquid carries out dehydration purification in glycol circulation pump A squeezes into glycol dehydration tower simultaneously, when the water content of glycol dehydration tower bottom liquid is less than 0.2%, glycol dehydration tower bottom liquid is squeezed into extractive distillation column by glycol circulation pump B and is circulated use, it is also possible to squeezes into the interim groove of ethylene glycol and stores；Acetonitrile vacuum pump is had owing to 99% acetonitrile return tank connects, the interim groove of ethylene glycol connects ethylene vacuum pump, and 99% acetonitrile return tank connect with extractive distillation column, the interim groove of ethylene glycol connects with glycol dehydration tower, thus realizing extractive distillation column and glycol dehydration tower is negative pressure state；In this utility model, acetonitrile dehydrating tower is that normal pressure, extractive distillation column and glycol dehydration tower are negative pressure, thus greatly reduce the energy consumption in acetonitrile purification process, and improve the purification rate of acetonitrile；This utility model have save the energy, cost-effective, flow process is stable, easy operation, advantage that purification degree is high.
Claims (6)
1. an acetonitrile continuous negative pressure distilling and extracting device, it includes acetonitrile dehydrating tower, extractive distillation column and glycol dehydration tower, it is characterized in that: the middle part of described acetonitrile dehydrating tower connects crude acetonitrile water input duct, connected by pipeline bottom acetonitrile dehydrating tower and have waste liquid circulation pump, connecting at described waste liquid circulation delivery side of pump and have waste liquid discharge line and waste liquid reboiler, described waste liquid reboiler is connected bottom acetonitrile dehydrating tower by pipeline；The top of acetonitrile dehydrating tower is connected with highly concentrated acetonitrile first-stage condenser and highly concentrated acetonitrile secondary condenser in turn by pipeline, described highly concentrated acetonitrile secondary condenser is connected by pipeline highly concentrated acetonitrile return tank, described highly concentrated acetonitrile return tank is connected by pipeline highly concentrated acetonitrile circulating pump, one pipeline of the outlet of described highly concentrated acetonitrile circulating pump is connected with the top of acetonitrile dehydrating tower, and another pipeline of the outlet of highly concentrated acetonitrile circulating pump is connected with the middle part inlet of extractive distillation column；The top of described extractive distillation column is connected with 99% acetonitrile first-stage condenser and 99% acetonitrile secondary condenser in turn by pipeline, 99% described acetonitrile secondary condenser is connected by pipeline 99% acetonitrile return tank, the top of 99% described acetonitrile return tank is connected by pipeline acetonitrile vacuum pump, the bottom of 99% acetonitrile return tank is connected by pipeline acetonitrile circulating pump, one pipeline in the exit of described acetonitrile circulating pump is connected with the top of extractive distillation column, another pipeline in the exit of acetonitrile circulating pump connects pure acetonitrile circulating pump, described pure acetonitrile circulation delivery side of pump is connected by pipeline high-boiling components dashpot, described high-boiling components dashpot is connected by pipeline 99% acetonitrile dashpot；The top of extractive distillation column connects ethylene glycol water influent pipeline, the bottom of extractive distillation column is connected by pipeline glycol circulation pump A, one pipeline in the exit of described glycol circulation pump A connects ethylene glycol preheater, described ethylene glycol preheater is connected by pipeline acetonitrile tower reboiler, described acetonitrile tower reboiler is connected with the bottom of extractive distillation column by pipeline, and another pipeline in the exit of glycol circulation pump A is connected with the middle part of glycol dehydration tower；The top of described glycol dehydration tower is connected by pipeline tower top distilled water collecting tank, the bottom of glycol dehydration tower is connected by pipeline glycol circulation pump B, the exit of described glycol circulation pump B is connected by pipeline ethylene glycol reboiler and the interim groove of ethylene glycol, described ethylene glycol reboiler is connected in the middle part of glycol dehydration tower by pipeline, and the top of the interim groove of described ethylene glycol is connected by pipeline ethylene vacuum pump.
A kind of acetonitrile continuous negative pressure distilling and extracting device the most according to claim 1, it is characterised in that: the exit of described glycol circulation pump B is connected with ethylene glycol preheater by pipeline.
A kind of acetonitrile continuous negative pressure distilling and extracting device the most according to claim 1, it is characterised in that: it is connected by pipeline between described glycol dehydration tower with tower top distilled water collecting tank and has distiller condenser.
A kind of acetonitrile continuous negative pressure distilling and extracting device the most according to claim 1, it is characterized in that: in described acetonitrile dehydrating tower, be provided with two sector hole mellapak packings, be provided above the liquid distribution trough A, described liquid distribution trough A of described every sector hole mellapak packing are connected with crude acetonitrile input duct.
A kind of acetonitrile continuous negative pressure distilling and extracting device the most according to claim 1, it is characterised in that: being provided with three sections of wire packing A in described extractive distillation column, every section of described wire packing A is provided above liquid distribution trough B.
A kind of acetonitrile continuous negative pressure distilling and extracting device the most according to claim 1, it is characterised in that: being provided with two sections of wire packing B in described glycol dehydration tower, every section of described wire packing B is provided above liquid distribution trough C.
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| CN201620403476.4U CN205635427U (en) | 2016-05-06 | 2016-05-06 | Continuous negative pressure of acetonitrile distillation extraction device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112851550A (en) * | 2021-01-20 | 2021-05-28 | 山东亿盛实业股份有限公司 | Method and equipment for continuously extracting and separating acetonitrile water azeotrope |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112851550A (en) * | 2021-01-20 | 2021-05-28 | 山东亿盛实业股份有限公司 | Method and equipment for continuously extracting and separating acetonitrile water azeotrope |
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