CN107382915B - Energy-saving process for separating tetrahydrofuran-methanol by heat integration extraction rectification - Google Patents
Energy-saving process for separating tetrahydrofuran-methanol by heat integration extraction rectification Download PDFInfo
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- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/007—Energy recuperation; Heat pumps
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
- B01D3/322—Reboiler specifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/04—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having no double bonds between ring members or between ring members and non-ring members
- C07D307/06—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having no double bonds between ring members or between ring members and non-ring members with only hydrogen atoms or radicals containing only hydrogen and carbon atoms, directly attached to ring carbon atoms
- C07D307/08—Preparation of tetrahydrofuran
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
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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
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Abstract
The invention relates to an energy-saving process for separating tetrahydrofuran-methanol by heat integration extraction rectification, belonging to the technical field of chemical separation. According to the process, dimethyl sulfoxide is selected as an extracting agent, the tetrahydrofuran and the methanol are separated by extractive distillation through a side line extraction process and an intermediate reboiler process flow, the material extracted from the side line of an extractive distillation tower enters a solvent recovery tower, and the hot material flow at the bottom of the solvent recovery tower is used as a heat source, so that the heat integration of the intermediate reboiler and the extractive distillation tower reboiler is realized, and the energy consumption is greatly reduced. The mass fraction of the product of the invention is more than 99.9%. The invention has the advantages of energy saving, environmental protection, high purity of separated products, cost saving and the like.
Description
[ technical field ] A method for producing a semiconductor device
The invention belongs to the field of rectification and purification in the chemical industry, and particularly relates to an energy-saving process for separating tetrahydrofuran-methanol by heat integration extraction rectification.
[ background of the invention ]
Tetrahydrofuran is an important organic synthetic raw material and is a solvent with excellent performance, the most important purpose is to produce polytetrahydrofuran, which is particularly suitable for dissolving PVC, polyvinylidene chloride and butylaniline, and is widely used as a solvent for surface coating, anticorrosive coating, printing ink, magnetic tape and film coating, and also used as a reaction solvent, and the thickness and brightness of an aluminum layer can be arbitrarily controlled when the tetrahydrofuran is used for electroplating aluminum liquid. Methanol is one of basic organic raw materials, is mainly used for manufacturing various organic products such as formaldehyde, acetic acid, methyl chloride, methylamine, dimethyl sulfate and the like, is also one of raw materials of pesticides (insecticides, acaricides), medicines (sulfonamides, synomycin and the like), and is one of raw materials for synthesizing dimethyl terephthalate, methyl methacrylate and methyl acrylate.
At present, certain pharmaceutical enterprises generate tetrahydrofuran-methanol-containing waste liquid in the synthesis process of pharmaceutical and pesticide intermediates, and the waste liquid is required to be recycled from the aspects of environmental protection and economy. Due to the formation of the lowest azeotrope, the separation is difficult to realize by the common rectification method, and a special rectification method needs to be considered. The special rectification methods researched and developed by academia and industry at present comprise catalytic rectification, membrane rectification, adsorption rectification, pressure swing rectification, azeotropic rectification, salt effect rectification, extractive rectification and the like.
The patent (CN102911139A) discloses a solvent recovery and separation method containing a tetrahydrofuran-methanol system, which uses ethylene glycol as an extractant to recover a waste liquid solvent containing the tetrahydrofuran and methanol system, so as to obtain tetrahydrofuran and methanol products with purity of 98-99.5%. Because the process is complex and heat integration is not realized, the energy consumption is greatly increased.
The patent (CN206188692U) discloses a device for recovering tetrahydrofuran by extractive distillation, which uses dimethyl sulfoxide as an extracting agent, and because the device uses a double-tower process, only tetrahydrofuran can be recovered, and separation of methanol and water is not achieved.
The patent (CN104447636A) discloses a method for extracting and separating tetrahydrofuran-ethanol by using a dividing wall rectifying tower, 1, 4-butanediol is used as an extracting agent, a tetrahydrofuran-ethanol system is separated by a single tower, the operation of the process is relatively complex, and the tetrahydrofuran-methanol system is not involved.
The invention overcomes the defects of the patents, adopts a heat integration extraction rectification method, takes dimethyl sulfoxide as an extracting agent, separates out a high-purity tetrahydrofuran-methanol product, simultaneously utilizes a heat integration technology, takes a hot material flow at the bottom of a solvent recovery tower T2 as a heat source, realizes the heat integration of an intermediate reboiler R3 and an extraction rectification tower T1 reboiler R1, and greatly reduces the energy consumption.
[ summary of the invention ]
[ problem to be solved ]
The invention provides an energy-saving process for separating tetrahydrofuran-methanol by heat integration extractive distillation, which solves the problem that tetrahydrofuran-methanol mixture is difficult to separate due to azeotropy.
[ solution ]
The invention provides an energy-saving process for separating tetrahydrofuran-methanol by heat integration extractive distillation, aiming at the current situations of high separation energy consumption and complex process of a binary azeotropic mixture in the extractive distillation process. Dimethyl sulfoxide is used as an extracting agent, high-purity tetrahydrofuran-methanol products are separated, meanwhile, a heat integration technology is utilized, a hot material flow at the bottom of a solvent recovery tower T2 is used as a heat source, heat integration of an intermediate reboiler R3 and an extraction rectifying tower T1 reboiler R1 is realized, and energy consumption is greatly reduced.
The invention relates to an energy-saving process for separating tetrahydrofuran-methanol by heat integration extractive distillation, which comprises the following specific implementation steps:
(1) the tetrahydrofuran-methanol mixture enters an extractive distillation tower T1 through a pipeline 1 via a preheater E1, a part of materials at the bottom of an extractive distillation tower T1 enters a reboiler R1, the materials are vaporized and then return to the bottom of an extractive distillation tower T1, and the other part of materials at the bottom of the tower enter a mixer M1 through a pipeline 4; a tetrahydrofuran product is extracted from the tower top through a pipeline 2; the material is extracted from the side line of the pipeline 3 and enters a solvent recovery tower T2;
(2) a part of materials at the bottom of the solvent recovery tower T2 enter a reboiler R2, return to the bottom of the solvent recovery tower T2 after vaporization, and extract the other part of materials through a pipeline 8 to enter a separator S1; the methanol product is extracted from the tower top through a pipeline 5;
(3) the solvent recovery tower T2 enters an intermediate reboiler R3 through a side line drawn material of a pipeline 6, and returns to the solvent recovery tower T2 through a pipeline 7 after heat exchange;
(4) the stream in the line 8 is divided into two streams by a separator S1, and one stream enters a reboiler R3 through a line 9 to exchange heat and then enters a mixer M1; the other stream enters reboiler R1 via line 11 and enters mixer M1; make-up lost extractant via line 13;
(5) the material flow is mixed by a mixer M1 and then preheated by a preheater E1 and enters the top of the extractive distillation column T1;
(6) heat integration is respectively realized in an intermediate reboiler R3 and a reboiler R1, a hot material flow from the bottom of a solvent recovery tower T2 is divided into two material flows through a separator S1, one material flow enters the intermediate reboiler R3 through a pipeline 9 to exchange heat with a material extracted from the side line of the solvent recovery tower T2, and the material flows enter a mixer M1 through a pipeline 10 after heat exchange; one material flow enters a reboiler R1 through a pipeline 11 to exchange heat with the bottom material of the extractive distillation column T1, and enters a mixer M1 through a pipeline 12 after heat exchange. The operating pressure of the extractive distillation tower T1 is 0.1-0.3 atm; the number of theoretical plates of the extractive distillation column T1 is 45-55, the feeding position is 20-27, the feeding position of the extractant is 3-6, the lateral line extraction position is 40-45, and the reflux ratio of the extractive distillation column T1 is 1.8-2.2; the operating pressure of the solvent recovery tower T2 is normal pressure 1atm, the number of theoretical plates is 12-15, the position of a feeding plate is 7-10, and the reflux ratio of the solvent recovery tower T2 introduced into an intermediate reboiler is 4-7, and is 2.0-2.5; the temperature of the top of the extraction rectifying tower T1 is 23.09-33.42 ℃, the temperature of the bottom of the extraction rectifying tower T1 is 160.85-173.08 ℃, the temperature of the top of the solvent recovery tower T2 is 64.26-64.40 ℃, and the temperature of the bottom of the solvent recovery tower is 193.53-193.58 ℃.
An energy-saving process for separating tetrahydrofuran and methanol by heat integration extraction rectification is characterized in that the mass fraction of tetrahydrofuran obtained from the top of an extraction rectification tower T1 is more than 99.90%, the recovery rate of tetrahydrofuran is more than 99.90%, the mass fraction of methanol obtained from the top of a solvent recovery tower T2 is more than 99.90%, and the recovery rate of methanol is more than 99.90%.
The energy-saving process for separating tetrahydrofuran-methanol by heat integration extractive distillation is specifically described as follows:
the method comprises the following steps of (1) enabling a tetrahydrofuran-methanol mixture to enter a preheater E1 through a pipeline 1, providing a heat source of the preheater through a pipeline 14 heat flow, enabling a preheated mixed solution to enter an extraction and rectification tower T1 with absolute pressure of 0.1-0.3 atm and 45-55 tower plates, enabling the feeding position to be 20-27, enabling the side line extraction position to be 40-45 tower plates, extracting a tetrahydrofuran product from the top of the extraction and rectification tower T1 through a pipeline 2, enabling a tower bottom liquid to enter a mixer M1 through a pipeline 4, enabling the temperature of the top of the extraction and rectification tower T1 to be 23.09-33.42 ℃, and enabling the temperature of the bottom of the extraction and rectification tower T to be 160.85-173.08 ℃; the feed liquid extracted from the side line is conveyed to a solvent recovery tower T2 with the normal pressure of 1atm and the tower plate number of 12-15 through a pipeline 3, the feeding position is 7-10, the position where the side line is extracted and enters an intermediate reboiler R3 is 4-7, a methanol product is extracted from the top of a solvent recovery tower T2 through a pipeline 5, an extracting agent at the bottom of the tower enters a separator S1 through a pipeline 8, the temperature of the top of the solvent recovery tower is 64.26-64.40 ℃, and the temperature of the bottom of the tower is 193.53-193.58 ℃;
heat integration is respectively realized in an intermediate reboiler R3 and a reboiler R1, a hot material flow from the bottom of a solvent recovery tower T2 is divided into two material flows through a separator S1, one material flow enters the intermediate reboiler R3 through a pipeline 9 to exchange heat with a material extracted from the side line of the solvent recovery tower T2, and the material flows enter a mixer M1 through a pipeline 10 after heat exchange; one material flow enters a reboiler R1 through a pipeline 11 to exchange heat with the material at the bottom of the extractive distillation column T1, and enters a mixer M1 through a pipeline 12 after heat exchange; the mixed material flow enters a preheater E1 through a pipeline 14 to exchange heat with the feed material flow of the pipeline 1, and enters an extractive distillation tower T1 after heat exchange, wherein the feed position is 3-6 trays.
[ advantageous effects ]
The invention has the following beneficial effects:
(1) the tetrahydrofuran-methanol binary mixture is successfully separated to obtain two high-purity products, and the problem of difficult azeotropic separation of the tetrahydrofuran-methanol is solved.
(2) The process realizes heat integration, takes the hot material flow at the bottom of the solvent recovery tower as a heat source, realizes the heat integration of an intermediate reboiler and an extraction rectifying tower reboiler, and greatly reduces the energy consumption.
(3) Has the advantages of simple process, convenient operation, safety, no pollution, low equipment investment cost and the like.
[ description of the drawings ]
FIG. 1 is a schematic diagram of an energy-saving process for separating tetrahydrofuran-methanol by heat integration extractive distillation.
The invention is further described below with reference to fig. 1 and the detailed description, but the invention is not limited to the figures and examples.
In the figure: t1-extractive distillation column; t2-solvent recovery column; d1, D2-reflux drum; e1-preheater; c1-condenser; c2-condenser; r1, R2-reboiler; r3-intermediate reboiler; m1-mixer; s1-a separator; the numbers represent the respective lines.
[ detailed description ] embodiments
Example 1:
adopting the process flow chart shown in figure 1, wherein the feed flow is 2000kg/h, the feed temperature is 35 ℃, and the feed components comprise 50 percent (mass fraction) of tetrahydrofuran and 50 percent (mass fraction) of methanol; the feeding flow of the extracting agent is 3000kg/h, the supplementary feeding flow of the extracting agent is 0.4kg/h, and the feeding temperature of the extracting agent is 55 ℃. The theoretical plate number of the extractive distillation tower is 45, the pressure is 0.3atm (absolute pressure), the 20 th plate is used for feeding, the feeding position of the extracting agent is the 3 rd plate, the sampling position of the measuring line is the 40 th plate, and the reflux ratio is 1.8; the theoretical plate number of the solvent recovery tower is 12, the pressure is 1atm (absolute pressure), the material is fed from the 7 th tower plate, the 4 th tower plate is arranged at the position of the middle reboiler which is extracted by a measuring line, and the reflux ratio is 2.0. After separation, the concentration of the tetrahydrofuran product is 99.95%, the recovery rate is 99.95%, the concentration of the methanol product is 99.93%, and the recovery rate is 99.92%.
Example 2:
adopting the process flow chart shown in figure 1, wherein the feed flow is 3000kg/h, the feed temperature is 35 ℃, and the feed components comprise 50 percent (mass fraction) of tetrahydrofuran and 50 percent (mass fraction) of methanol; the feeding flow of the extracting agent is 4000kg/h, the supplementary feeding flow of the extracting agent is 0.45kg/h, and the feeding temperature of the extracting agent is 55 ℃. The theoretical plate number of the extractive distillation tower is 50, the pressure is 0.3atm (absolute pressure), the 25 th plate is used for feeding, the feeding position of the extracting agent is the 5 th plate, the position of the line extraction is the 42 th plate, and the reflux ratio is 1.9; the theoretical plate number of the solvent recovery tower is 14, the pressure is 1atm (absolute pressure), the 9 th tower plate is used for feeding, the position of the test line extracted and entering the middle reboiler is the 6 th tower plate, and the reflux ratio is 2.4. After separation, the concentration of the tetrahydrofuran product is 99.92 percent, the recovery rate is 99.92 percent, the concentration of the methanol product is 99.94 percent, and the recovery rate is 99.94 percent.
Example 3:
adopting the process flow chart shown in figure 1, wherein the feed flow is 2000kg/h, the feed temperature is 35 ℃, and the feed composition comprises 40 percent (mass fraction) of tetrahydrofuran and 60 percent (mass fraction) of methanol; the feeding flow of the extracting agent is 2800kg/h, the supplementary feeding flow of the extracting agent is 0.28kg/h, and the feeding temperature of the extracting agent is 55 ℃. The theoretical plate number of the extractive distillation tower is 48, the pressure is 0.1atm (absolute pressure), the 22 th plate is used for feeding, the feeding position of the extracting agent is the 4 th plate, the sampling position of the measuring line is the 41 th plate, and the reflux ratio is 2.2; the theoretical plate number of the solvent recovery tower is 15, the pressure is 1atm (absolute pressure), the 10 th tower plate is used for feeding, the position of the test line extracted and entering the middle reboiler is the 7 th tower plate, and the reflux ratio is 2.3. After separation, the concentration of the tetrahydrofuran product is 99.95%, the recovery rate is 99.95%, the concentration of the methanol product is 99.96%, and the recovery rate is 99.96%.
Example 4:
the process flow chart shown in the attached figure 1 is adopted, the feeding flow is 2500kg/h, the feeding temperature is 35 ℃, the feeding composition comprises 60 percent (mass fraction) of tetrahydrofuran and 40 percent (mass fraction) of methanol, the feeding flow of the extractant is 3500kg/h, the supplementary feeding flow of the extractant is 0.65kg/h, and the feeding temperature of the extractant is 55 ℃. The theoretical plate number of the extractive distillation tower is 55, the pressure is 0.2atm (absolute pressure), the 27 th plate is used for feeding, the feeding position of the extracting agent is the 6 th plate, the measuring line extraction position is the 45 th plate, and the reflux ratio is 2.0; the theoretical plate number of the solvent recovery tower is 13, the pressure is 1atm (absolute pressure), the material is fed from the 8 th tower plate, the position of the material which is extracted by a measuring line and enters the middle reboiler is the 5 th tower plate, and the reflux ratio is 2.5. After separation, the concentration of the obtained tetrahydrofuran product is 99.92 percent, the recovery rate is 99.92 percent, the concentration of the methanol product is 99.91 percent, and the recovery rate is 99.91 percent.
Claims (2)
1. An energy-saving process for separating tetrahydrofuran-methanol by heat integration extractive distillation is characterized in that an extractive distillation method and a device used by the process comprise the following parts:
an extractive distillation column T1, a solvent recovery column T2, a condenser C1, a condenser C2, a reflux tank D1, a reflux tank D2, a reboiler R1, a reboiler R2, an intermediate reboiler R3, a preheater E1, a mixer M1 and a separator S1; wherein, a reboiler R1 and a reboiler R2 are respectively connected with the bottoms of the extractive distillation column T1 and the solvent recovery column T2, a condenser C1 and a reflux tank D1 are sequentially connected with the top of the extractive distillation column T1 through pipelines, a condenser C2 and a reflux tank D2 are sequentially connected with the top of the solvent recovery column T2 through pipelines, and an intermediate reboiler R3 is connected with the lower part of the solvent recovery column T2; methanol extracted from the side line of an extractive distillation tower T1 and an extracting agent enter a solvent recovery tower T2, the bottom material of a solvent recovery tower T2 flows through a separator and is divided into two streams, one stream is subjected to heat exchange in a solvent recovery tower T2 intermediate reboiler R3, the other stream is subjected to heat exchange in an extractive distillation tower T1 reboiler R1, the two streams are mixed by a mixer M1 after heat exchange and enter an E1 preheater and are subjected to heat exchange with a feed stream and then enter an extractive distillation tower T1;
an energy-saving process for separating tetrahydrofuran methanol by adopting heat integration extraction rectification comprises the following steps:
(1) the tetrahydrofuran-methanol mixture enters an extractive distillation tower T1 through a pipeline 1 via a preheater E1, a part of materials at the bottom of an extractive distillation tower T1 enters a reboiler R1, the materials are vaporized and then return to the bottom of an extractive distillation tower T1, and the other part of materials at the bottom of the tower enter a mixer M1 through a pipeline 4; a tetrahydrofuran product is extracted from the tower top through a pipeline 2; the material is extracted from the side line of the pipeline 3 and enters a solvent recovery tower T2;
(2) a part of materials at the bottom of the solvent recovery tower T2 enter a reboiler R2, return to the bottom of the solvent recovery tower T2 after vaporization, and extract the other part of materials through a pipeline 8 to enter a separator S1; the methanol product is extracted from the tower top through a pipeline 5;
(3) the solvent recovery tower T2 enters an intermediate reboiler R3 through a side line drawn material of a pipeline 6, and returns to the solvent recovery tower T2 through a pipeline 7 after heat exchange;
(4) the stream in the line 8 is divided into two streams by a separator S1, and one stream enters a reboiler R3 through a line 9 to exchange heat and then enters a mixer M1; the other stream enters reboiler R1 via line 11 and enters mixer M1; make-up lost extractant via line 13;
(5) the material flow is mixed by a mixer M1 and then preheated by a preheater E1 and enters the top of the extractive distillation column T1;
(6) heat integration is respectively realized in an intermediate reboiler R3 and a reboiler R1, a hot material flow from the bottom of a solvent recovery tower T2 is divided into two material flows through a separator S1, one material flow enters the intermediate reboiler R3 through a pipeline 9 to exchange heat with a material extracted from the side line of the solvent recovery tower T2, and the material flows enter a mixer M1 through a pipeline 10 after heat exchange; one material flow enters a reboiler R1 through a pipeline 11 to exchange heat with the material at the bottom of the extractive distillation column T1, and enters a mixer M1 through a pipeline 12 after heat exchange;
wherein the selected extractant is dimethyl sulfoxide; the operation pressure of the extraction rectifying tower T1 is 0.1-0.3 atm; the number of theoretical plates of the extractive distillation tower T1 is 45-55, the feeding position is 20-27, the feeding position of the circulating material flow dimethyl sulfoxide is 3-6, the lateral line extraction position is 40-45, and the reflux ratio of the extractive distillation tower T1 is 1.8-2.2; the operating pressure of the solvent recovery tower T2 is normal pressure 1atm, the number of theoretical plates is 12-15, the position of a feeding plate is 7-10, the position of an intermediate reboiler is 4-7, and the reflux ratio of the solvent recovery tower T2 is 2.0-2.5; the temperature of the top of the extraction rectifying tower T1 is 23.09-33.42 ℃, the temperature of the bottom of the extraction rectifying tower T1 is 160.85-173.08 ℃, the temperature of the top of the solvent recovery tower T2 is 64.26-64.40 ℃, and the temperature of the bottom of the solvent recovery tower is 193.53-193.58 ℃.
2. The energy-saving process for separating tetrahydrofuran-methanol by heat-integrated extractive distillation as claimed in claim 1, wherein the mass fraction of tetrahydrofuran obtained from the top of extractive distillation column T1 is greater than 99.90%, the recovery rate of tetrahydrofuran is greater than 99.90%, the mass fraction of methanol obtained from the top of solvent recovery column T2 is greater than 99.90%, and the recovery rate of methanol is greater than 99.90% under the condition of using dimethyl sulfoxide as extractant.
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| CN109851579B (en) * | 2017-11-30 | 2021-02-09 | 中国石油化工股份有限公司 | Process for producing alkylene oxide |
| CN109232482A (en) * | 2018-10-31 | 2019-01-18 | 重庆大学 | A kind of economic benefits and social benefits are thermally integrated abstraction distillation separation of tetrahydrofuran-methanol-water azeotropic mixture method |
| CN110885283A (en) * | 2019-10-28 | 2020-03-17 | 重庆大学 | Energy-saving process for separating ethyl acetate-ethanol by heat integration extraction rectification with side extraction |
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| EP0022469B1 (en) * | 1979-07-11 | 1983-03-02 | Chemische Werke Hüls Ag | Process for the separation of methanol from mixtures of tetrahydrofuran with methanol and water |
| CN102911139A (en) * | 2012-11-13 | 2013-02-06 | 漆志文 | Recovery and separation method for solvent containing tetrahydrofuran-carbinol system |
| CN106146255A (en) * | 2016-07-21 | 2016-11-23 | 青岛科技大学 | Double column pressure swing extraction coupling rectification separation water, methanol, oxolane system method |
| CN206188692U (en) * | 2016-10-17 | 2017-05-24 | 天津天大凯泰化工科技有限公司 | A device for extracting rectification recovery tetrahydrofuran |
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