CN106431836A - Technology for separating ethyl alcohol-water system by means of extractive distillation and flash coupling - Google Patents
Technology for separating ethyl alcohol-water system by means of extractive distillation and flash coupling Download PDFInfo
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- CN106431836A CN106431836A CN201610829622.4A CN201610829622A CN106431836A CN 106431836 A CN106431836 A CN 106431836A CN 201610829622 A CN201610829622 A CN 201610829622A CN 106431836 A CN106431836 A CN 106431836A
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- extractive distillation
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- 238000000895 extractive distillation Methods 0.000 title claims abstract description 33
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 title claims abstract description 10
- 238000005516 engineering process Methods 0.000 title abstract description 4
- 230000008878 coupling Effects 0.000 title abstract 3
- 238000010168 coupling process Methods 0.000 title abstract 3
- 238000005859 coupling reaction Methods 0.000 title abstract 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000002608 ionic liquid Substances 0.000 claims abstract description 47
- -1 1-ethyl-3-methylimidazolium tetrafluoroborate Chemical compound 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 24
- 239000002904 solvent Substances 0.000 claims abstract description 7
- 239000000203 mixture Substances 0.000 claims description 26
- 238000000926 separation method Methods 0.000 claims description 16
- 239000007788 liquid Substances 0.000 claims description 15
- 238000010992 reflux Methods 0.000 claims description 15
- 238000007701 flash-distillation Methods 0.000 claims description 8
- IBZJNLWLRUHZIX-UHFFFAOYSA-N 1-ethyl-3-methyl-2h-imidazole Chemical compound CCN1CN(C)C=C1 IBZJNLWLRUHZIX-UHFFFAOYSA-N 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 5
- 230000005494 condensation Effects 0.000 claims description 5
- 230000006837 decompression Effects 0.000 claims description 2
- 239000008214 highly purified water Substances 0.000 claims description 2
- 239000003795 chemical substances by application Substances 0.000 abstract description 4
- 235000019441 ethanol Nutrition 0.000 abstract 4
- MKHFCTXNDRMIDR-UHFFFAOYSA-N cyanoiminomethylideneazanide;1-ethyl-3-methylimidazol-3-ium Chemical compound [N-]=C=NC#N.CCN1C=C[N+](C)=C1 MKHFCTXNDRMIDR-UHFFFAOYSA-N 0.000 abstract 1
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 238000000605 extraction Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 150000002500 ions Chemical class 0.000 description 3
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 229910017053 inorganic salt Inorganic materials 0.000 description 2
- 238000002955 isolation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 238000001577 simple distillation Methods 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- MCTWTZJPVLRJOU-UHFFFAOYSA-N 1-methyl-1H-imidazole Chemical compound CN1C=CN=C1 MCTWTZJPVLRJOU-UHFFFAOYSA-N 0.000 description 1
- BTBUEUYNUDRHOZ-UHFFFAOYSA-N Borate Chemical compound [O-]B([O-])[O-] BTBUEUYNUDRHOZ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000001944 continuous distillation Methods 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
- C07C29/84—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation by extractive distillation
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a technology for separating an ethyl alcohol-water system by means of extractive distillation and flash coupling. The technology comprises the steps that ionic liquid is adopted as an extracting agent, the relative volatility of ethyl alcohol for water can be improved, and the separating efficiency can be improved to obtain an ethyl alcohol product, wherein the ionic liquid is 1-ethyl-3-methylimidazolium tetrafluoroborate and 1-ethyl-3-methylimidazolium dicyanamide. The adopted ionic liquid extracting agent can improve the relative volatility of ethyl alcohol in the ethyl alcohol-water system, and the solvent ratio is decreased. The ethyl alcohol with the purity larger than 99.9% is obtained. According to the technological process for separating ethyl alcohol-water by means of extractive distillation and flash coupling, the stable and continuous ionic liquid can be recycled.
Description
【Technical field】
The invention belongs to chemical separating purification art is and in particular to a kind of extracting rectifying and flash separation alcohol-water thing system
Technique.
【Background technology】
In chemical industry and pharmaceutical industry, ethanol is important solvent and raw material, and demand is continuously increased.Return in the industrial production
Receipts utilize high purity ethanol, and this extremely has economic implications for enterprise.Because ethanol and water can form azeotropic mixture, azeotropic temperature is
78.15 DEG C, application conventional distillation method is difficult to it is efficiently separated.In recent years, because ionic liquid has extremely low steaming
Vapour pressure, low melting point, heat stability, the property that nontoxic, non-corrosiveness, designability etc. are excellent, for ionic liquid as extraction
The extracting rectifying of agent, expands research and practice.Species with ionic liquid gets more and more, and selects in whole production process
Favourable ionic liquid knows from experience the problems such as solution energy-conservation, environmental pollution, equipment investment.
Patent (CN103073388A) discloses a kind of composite extractant separating alcohol-water with ionic liquid and inorganic salt
Method, but the Solvent quantity of the method is big, and reflux ratio is larger, and energy consumption is higher, and because using inorganic salt, process units is had
Corrosivity.
Patent (CN103435445A) discloses a kind of double solventss with ionic liquid or ionic liquid and organic solvent
For the method for extractant separating alcohol-water thing system, reduce energy consumption and production cost, and obtained high purity ethanol, yield
More than 99.0%.Patent (CN103601618A) is related to a kind of method of separation of extractive distillation ethanol-water azeotropic thing, and the method is adopted
Spent glycol and chlorination 1- ethyl-3-methylimidazole carry out batch extracting rectified operation for mixed solvent, and its Application Example is tied
Really：Alcohol product purity reaches 99.5%.
For the extracting rectifying process using ionic liquid as extractant, the selection of ionic liquid is crucial.Above-mentioned existing
Isolation technics present in defect and deficiency be：Have ignored the properties such as viscosity, the heat stability of ionic liquid to production process
Impact；The cost of separation process is higher；And have impact on product quality to a certain extent；Technological process is complicated.With tradition
Organic solvent extraction separation process compare, ionic liquid is separated with water or Organic substance only need to need not using simple distillation
Complicated distillation process, and ionic liquid can be recycled, almost free of losses.
The green high-efficient isolation technics of exploitation ethanol-water mixture are significant, relevant separating alcohol-water mixture
Article and patent in there is not yet publish with ionic liquid 1- ethyl-3-methylimidazole tetrafluoroborate and 1- ethyl-
The technique that 3- Methylimidazole. dicyan amine salt carries out extracting rectifying and flash distillation integrated separation alcohol-water thing system as extractant.This
The ionic liquid of bright employing because under room temperature liquid condition, viscosity less and favourable to whole production process.
【Content of the invention】
It is an object of the invention to provide the apparatus and method of a kind of extracting rectifying and flash distillation integrated separation alcohol-water thing system,
By being isolated after ethanol using ion liquid abstraction rectification to alcohol-water thing system, by extractive distillation column tower reactor contain extractant and
Aqueous mixtures carry out vacuum flashing, reduce the energy consumption during production operation, and the equipment investment that the method adopts is few, operate bar
Part is easily controllable, and the purity of alcohol obtaining is higher.
The present invention is realized by the following technical programs.
A kind of extracting rectifying and the method for flash separation alcohol-water thing system, the method adopts extracting rectifying device to implement even
Continuous distillation operation, described extracting rectifying device includes extractive distillation column, and extractive distillation column bottom of towe connects reboiler, and tower top connects
Condenser, connects after condenser and receives tank, and ionic liquid reclaims flash tank it is characterised in that including procedure below：Alcohol-water
Mixture enters in extractive distillation column by tower middle and lower part, and extractant is ion liquid solvent, is entered in tower by tower top；In extraction
In rectifying tower, after the condensation of overhead stream condensed device, a part of liquid returns reflux in tower, and a part of liquid is as high-purity
Alcohol product extraction；After tower base stream boils through reboiler again, a part returns in tower, is partly into flash tank；
Realize the separation of the mixture of extractant and water in flash tank, obtain highly purified water, warp in flash tank tower top
Directly produce after condensation；Obtain, in flash tank bottom, the ionic liquid that mass fraction is 0.2-0.4%, adopted by flash tank bottom
Go out, loop back extractive distillation column；Wherein said extractant adopts ionic liquid, specifically includes 1- ethyl-3-methylimidazole tetrafluoro
Borate and 1- ethyl-3-methylimidazole dicyan amine salt.
Described extractive distillation column internal diameter is Φ 400-500mm, and the number of plates is 35-45 block, and operating pressure is 1atm, ethanol-
Aqueous mixtures feed in 29-35 block column plate, and extractant feeds in 3-6 block column plate, and tower top temperature is 77.8-80 DEG C, bottom of towe
Temperature is 95-120 DEG C, and described flash tank adopts decompression operation, and operating pressure is 0.1-0.2atm absolute pressure, and temperature is 108-112
℃.
Described ion liquid solvent is preferably 1- ethyl-3-methylimidazole tetrafluoroborate and 1- ethyl -3- methyl miaow
Azoles dicyan amine salt.
Two kinds of composition arbitrary proportions in described ethanol-water mixture material.
In described alcohol-water thing system, two kinds of composition qualities are than preferably ethanol：Water=0.25-1.
Beneficial effects of the present invention are：Described ionic liquid physical ability improves the relative volatility of the ethanol in alcohol-water thing system,
Reduce solvent ratio.When the mass fraction of ionic liquid reaches 17%-50%, the azeotropic point of alcohol-water can be made to disappear.By should
Known with embodiment, when the mass ratio of ionic liquid and alcohol-water thing system is 1:When 3, you can carry out extracting rectifying well, obtain
Ethanol more than 99.5%.For alcohol-water thing system, ionic liquid 1- ethyl-3-methylimidazole tetrafluoroborate and 1- ethyl-
3- Methylimidazole. dicyan amine salt and water have preferable intersolubility, can be acted on water by chemical affinity, hydrogen bond force etc., improve second
Alcohol is for the relative volatility of water, thus ionic liquid addition is less, uses ionic liquid using simple Distillation recovery, fall
The low energy consumption of separation process and investment.
【Brief description】
Fig. 1：A kind of extracting rectifying of the present invention and the schematic flow sheet of flash distillation integrated separation alcohol-water thing system.
Wherein, T1 extractive distillation column；T2 flash tank；F1 extractive distillation column material inlet；F2 extractant feed mouth；
B1 extractive distillation column bottom of towe discharging opening；B2 cycling extraction agent exports；D1 alcohol product exports；D2 water out；1 reboiler；
2,3 condensers.
【Specific embodiment】
Embodiment 1：The internal diameter of extractive distillation column is Φ 500mm, number of theoretical plate is 40, operating pressure is 101.325kPa,
Operating reflux ratio be 1.8, tower top temperature control 77 DEG C, bottom temperature be 95 DEG C, 25 DEG C of ionic liquid 1- ethyl -3- methyl
Tetrafluoroborate is entered by the 6th block of plate, 25 DEG C of mass fraction be 20% ethanol -80% aqueous mixtures by the 34th block of plate with
The flow of 1000kg/h enters, and controls ionic liquid to be 1 with the mass ratio of alcohol-water:3, tower top upflowing vapor is entered by condenser
Row condensation.By the overhead reflux of extractive distillation column, Produced Liquid is the ethanol of mass fraction 99.5% to backflow.Extractive distillation column
Tower reactor is the mixture of 1- ethyl-3-methylimidazole tetrafluoroborate and water, and backflow returns after boiling in 126 DEG C through reboiler again
Stream, remaining enters flash tank, and operating pressure is 0.12atm, flash tank temperature control at 112 DEG C.The bottom of flash tank is quality
Fraction is the ionic liquid of 0.4% water.
Embodiment 2：The internal diameter of extractive distillation column is Φ 400mm, number of theoretical plate is 35, operating pressure is 101.325kPa,
Operating reflux ratio be 2.1, tower top temperature control 77.8 DEG C, bottom temperature be 109 DEG C, 25 DEG C of ionic liquid 1- ethyl -3-
Methyl imidazolium tetrafluoroborate is entered by the 6th block of plate, and 25 DEG C of mass fraction is 30% ethanol -70% aqueous mixtures by the 29th piece
Plate is entered with the flow of 1000kg/h, controls ionic liquid to be 1 with the mass ratio of alcohol-water:2.5, tower top upflowing vapor is by cold
Condenser is condensed.By the overhead reflux of extractive distillation column, Produced Liquid is the ethanol of mass fraction 99.6% to backflow.Extraction essence
The tower reactor evaporating tower is the mixture of 1- ethyl-3-methylimidazole tetrafluoroborate and water, and backflow boils in 120 DEG C through reboiler again
After flow back, remaining enter flash tank, operating pressure be 0.15atm, flash tank temperature control at 109 DEG C.The bottom of flash tank is
Mass fraction is the ionic liquid of 0.3% water.
Embodiment 3：The internal diameter of extractive distillation column is Φ 400mm, number of theoretical plate is 35, operating pressure is 101.325kPa,
Operating reflux ratio be 2.6, tower top temperature control 77.8 DEG C, bottom temperature be 107 DEG C, 25 DEG C of ionic liquid 1- ethyl -3-
Methyl imidazolium tetrafluoroborate is entered by the 6th block of plate, and 25 DEG C of mass fraction is 40% ethanol -60% aqueous mixtures by the 30th piece
Plate is entered with the flow of 1000kg/h, controls ionic liquid to be 1 with the mass ratio of alcohol-water:2, tower top upflowing vapor is by condensing
Device is condensed.By the overhead reflux of extractive distillation column, Produced Liquid is the ethanol of mass fraction 99.6% to backflow.Extracting rectifying
The tower reactor of tower is the mixture of 1- ethyl-3-methylimidazole tetrafluoroborate and water, after backflow boils in 120 DEG C through reboiler again
Backflow, remaining flash tank, operating pressure is 0.18atm, flash tank temperature control at 110 DEG C.The bottom of flash tank is divided for quality
Number is the ionic liquid of 0.3% water.
Embodiment 4：The internal diameter of extractive distillation column is Φ 500mm, number of theoretical plate is 40, operating pressure is 101.325kPa,
Operating reflux ratio be 1.2, tower top temperature control 78.0 DEG C, bottom temperature be 119 DEG C, 25 DEG C of ionic liquid 1- ethyl -3-
Methylimidazole. dicyan amine salt is entered by the 5th block of plate, and 25 DEG C of mass fraction is 20% ethanol -80% aqueous mixtures by the 32nd block of plate
Entered with the flow of 1000kg/h, control ionic liquid to be 1 with the mass ratio of alcohol-water:4, tower top upflowing vapor is by condenser
Condensed.By the overhead reflux of extractive distillation column, Produced Liquid is the ethanol of mass fraction 99.8% to backflow.Extractive distillation column
Tower reactor be 1- ethyl-3-methylimidazole dicyan amine salt and water mixture, backflow returns after boiling in 127 DEG C through reboiler again
Stream, remaining enters flash tank, and operating pressure is 0.14atm, flash tank temperature control at 108 DEG C.The bottom of flash tank is quality
Fraction is the ionic liquid of 0.1% water.
Embodiment 5：The internal diameter of extractive distillation column is Φ 500mm, number of theoretical plate is 45, operating pressure is 101.325kPa,
Operating reflux ratio is that 1.8, tower top temperature controls at 80 DEG C, and bottom temperature is 112 DEG C, 25 DEG C of ionic liquid 1- ethyl -3- first
Base imidazoles dicyan amine salt is entered by the 3rd block of plate, 25 DEG C of mass fraction be 30% ethanol -70% aqueous mixtures by the 31st block of plate with
The flow of 1000kg/h enters, and controls ionic liquid to be 1 with the mass ratio of alcohol-water:3, tower top upflowing vapor is entered by condenser
Row condensation.By the overhead reflux of extractive distillation column, Produced Liquid is the ethanol of mass fraction 99.9% to backflow.Extractive distillation column
Tower reactor is the mixture of 1- ethyl-3-methylimidazole dicyan amine salt and water, and backflow flows back after boiling in 126 DEG C through reboiler again,
Remaining enters flash tank, and operating pressure is 0.16atm, flash tank temperature control at 120 DEG C.The bottom of flash tank is mass fraction
Ionic liquid for 0.1% water.
Embodiment 6：The internal diameter of extractive distillation column is Φ 500mm, number of theoretical plate is 40, operating pressure is 101.325kPa,
Operating reflux ratio be 2.0, tower top temperature control 77.9 DEG C, bottom temperature be 120 DEG C, 25 DEG C of ionic liquid 1- ethyl -3-
Methylimidazole. dicyan amine salt is entered by the 4th block of plate, and 25 DEG C of mass fraction is 40% ethanol -60% aqueous mixtures by the 35th block of plate
Entered with the flow of 1000kg/h, control ionic liquid to be 1 with the mass ratio of alcohol-water:3, tower top upflowing vapor is by condenser
Condensed.By the overhead reflux of extractive distillation column, Produced Liquid is the ethanol of mass fraction 99.9% to backflow.Extractive distillation column
Tower reactor be 1- ethyl-3-methylimidazole dicyan amine salt and water mixture, backflow returns after boiling in 126 DEG C through reboiler again
Stream, remaining enters flash tank, and operating pressure is 0.2atm, flash tank temperature control at 112 DEG C.The bottom of steaming pot is mass fraction
Ionic liquid for 0.2% water.
Claims (4)
1. a kind of extracting rectifying and flash distillation integrated separation alcohol-water thing system technique it is characterised in that described technique include following
Step：
(1) ethanol-water mixture enters in extractive distillation column by tower middle and lower part, and extractant is ion liquid solvent, by tower top
Enter in tower；In extractive distillation column tower, after the condensation of overhead stream condensed device, a part of liquid return reflux in tower, one
Liquid is divided to produce as highly purified alcohol product；Tower base stream, after boiling through reboiler, a part returns in tower, a part again
Enter flash tank；
(2) realize the separation of the mixture of extractant and water in flash tank, obtain highly purified water in flash tank tower top, through cold
Directly produce after solidifying；Obtain, in flash tank bottom, the ionic liquid that mass fraction is 0.2-0.4%, produced by flash tank bottom,
Loop back extractive distillation column；
Wherein said extractant adopts ionic liquid, specifically includes 1- ethyl-3-methylimidazole tetrafluoroborate and 1- ethyl -3-
Methylimidazole. dicyan amine salt.
2. the technique of a kind of extracting rectifying according to claim 1 and flash distillation integrated separation alcohol-water thing system, its feature exists
It is Φ 400-500mm in described extractive distillation column internal diameter, the number of plates is 35-45 block, operating pressure is 1atm, alcohol-water mixes
Thing feeds in 29-35 block column plate, and extractant feeds in 3-6 block column plate, and tower top temperature is 77.8-80 DEG C, and column bottom temperature is
95-120 DEG C, described flash tank adopts decompression operation, and operating pressure is 0.1-0.2atm absolute pressure, and temperature is 108-112 DEG C.
3. the technique of a kind of extracting rectifying according to claim 1 and flash distillation integrated separation alcohol-water thing system, its feature exists
It is arbitrarily ratio charging in described ethanol-water mixture, extractant and ethanol-water mixture charge-mass ratio are 0.25-1.
4. the technique of a kind of extracting rectifying according to claim 1 and flash distillation integrated separation alcohol-water thing system, its feature exists
Product purity of alcohol after this technique separates is 99.5-99.9wt%, and the purity of water is 99.6-99.9wt%.
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| CN201610829622.4A CN106431836B (en) | 2016-09-19 | 2016-09-19 | A kind of technique of extracting rectifying and flash distillation integrated separation alcohol-water object system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110028388A (en) * | 2019-05-23 | 2019-07-19 | 山东科技大学 | A method of with hydrophilic ionic-liquid separation of extractive distillation tetrafluoropropanol and water azeotropic mixture |
| CN112795397A (en) * | 2019-11-14 | 2021-05-14 | 中国石油天然气股份有限公司 | Composite solvent for separating cyclane and aromatic hydrocarbon from naphtha |
| CN113248378A (en) * | 2021-05-31 | 2021-08-13 | 鹤壁腾飞清洁能源有限公司 | System for extracting and rectifying methyl acetate and ethanol and using method thereof |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3152968A (en) * | 1958-06-27 | 1964-10-13 | Celanese Corp | Recovery of methylene chloride from a mixed solvent system by extractive distillation with water |
| CN103073388A (en) * | 2013-01-28 | 2013-05-01 | 北京化工大学 | Method for separating alcohol from water through ion liquid extraction and rectification |
| CN103435445A (en) * | 2013-08-20 | 2013-12-11 | 天津科林泰克科技有限公司 | Method for separating mixture of ethanol alcohol and water |
| CN103601618A (en) * | 2013-11-22 | 2014-02-26 | 天津大学 | Method for extracting, rectifying and separating alcohol-water azeotropic mixture |
-
2016
- 2016-09-19 CN CN201610829622.4A patent/CN106431836B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3152968A (en) * | 1958-06-27 | 1964-10-13 | Celanese Corp | Recovery of methylene chloride from a mixed solvent system by extractive distillation with water |
| CN103073388A (en) * | 2013-01-28 | 2013-05-01 | 北京化工大学 | Method for separating alcohol from water through ion liquid extraction and rectification |
| CN103435445A (en) * | 2013-08-20 | 2013-12-11 | 天津科林泰克科技有限公司 | Method for separating mixture of ethanol alcohol and water |
| CN103601618A (en) * | 2013-11-22 | 2014-02-26 | 天津大学 | Method for extracting, rectifying and separating alcohol-water azeotropic mixture |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110028388A (en) * | 2019-05-23 | 2019-07-19 | 山东科技大学 | A method of with hydrophilic ionic-liquid separation of extractive distillation tetrafluoropropanol and water azeotropic mixture |
| CN110028388B (en) * | 2019-05-23 | 2023-01-17 | 山东科技大学 | Method for separating tetrafluoropropanol and water azeotrope by using hydrophilic ionic liquid extraction and rectification |
| CN112795397A (en) * | 2019-11-14 | 2021-05-14 | 中国石油天然气股份有限公司 | Composite solvent for separating cyclane and aromatic hydrocarbon from naphtha |
| CN112795397B (en) * | 2019-11-14 | 2023-02-07 | 中国石油天然气股份有限公司 | Composite solvent for separating cyclane and aromatic hydrocarbon from naphtha |
| CN113248378A (en) * | 2021-05-31 | 2021-08-13 | 鹤壁腾飞清洁能源有限公司 | System for extracting and rectifying methyl acetate and ethanol and using method thereof |
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