CN115057756A - Method for separating cyclohexane-isopropanol-water by pervaporation extraction rectification process - Google Patents
Method for separating cyclohexane-isopropanol-water by pervaporation extraction rectification process Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 58
- 238000000605 extraction Methods 0.000 title claims abstract description 38
- 238000005373 pervaporation Methods 0.000 title claims abstract description 27
- QABJMMRWLGSUNH-UHFFFAOYSA-N cyclohexane;propan-2-ol;hydrate Chemical compound O.CC(C)O.C1CCCCC1 QABJMMRWLGSUNH-UHFFFAOYSA-N 0.000 title claims abstract description 20
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims abstract description 68
- 238000000895 extractive distillation Methods 0.000 claims abstract description 49
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 claims abstract description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 29
- 239000012528 membrane Substances 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000000463 material Substances 0.000 claims abstract description 7
- 238000005516 engineering process Methods 0.000 claims abstract description 6
- 239000000203 mixture Substances 0.000 claims description 14
- 239000012465 retentate Substances 0.000 claims description 7
- PHTQWCKDNZKARW-UHFFFAOYSA-N isoamylol Chemical compound CC(C)CCO PHTQWCKDNZKARW-UHFFFAOYSA-N 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 claims description 2
- 239000012466 permeate Substances 0.000 claims description 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 abstract description 9
- 239000003795 chemical substances by application Substances 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000004821 distillation Methods 0.000 abstract description 2
- 238000009792 diffusion process Methods 0.000 abstract 1
- 239000012498 ultrapure water Substances 0.000 abstract 1
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- HGCIXCUEYOPUTN-UHFFFAOYSA-N cyclohexene Chemical compound C1CCC=CC1 HGCIXCUEYOPUTN-UHFFFAOYSA-N 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 2
- 238000005238 degreasing Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002386 leaching Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- XFAHEGIMRQOLMW-UHFFFAOYSA-N C1CCCCC1.C1CCC=CC1.C1=CC=CC=C1 Chemical compound C1CCCCC1.C1CCC=CC1.C1=CC=CC=C1 XFAHEGIMRQOLMW-UHFFFAOYSA-N 0.000 description 1
- FXHOOIRPVKKKFG-UHFFFAOYSA-N N,N-Dimethylacetamide Chemical compound CN(C)C(C)=O FXHOOIRPVKKKFG-UHFFFAOYSA-N 0.000 description 1
- 235000019484 Rapeseed oil Nutrition 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 235000012343 cottonseed oil Nutrition 0.000 description 1
- 239000002385 cottonseed oil Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 239000003085 diluting agent Substances 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 231100000053 low toxicity Toxicity 0.000 description 1
- 239000012046 mixed solvent Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000003825 pressing Methods 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
- 239000005060 rubber Substances 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002966 varnish Substances 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- 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
- C07C2601/00—Systems containing only non-condensed rings
- C07C2601/12—Systems containing only non-condensed rings with a six-membered ring
- C07C2601/14—The ring being saturated
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention relates to a method for separating cyclohexane-isopropanol-water by a pervaporation extraction rectification process and a device suitable for the method. On the basis of the traditional extractive distillation process, by utilizing the pervaporation technology with ethylene glycol as an extracting agent, a cyclohexane-isopropanol-water ternary azeotrope enters an extractive distillation tower from the middle lower part, ethylene glycol as an extracting agent enters the extractive distillation tower from the upper part, high-purity cyclohexane is obtained at the top of the extractive distillation tower after extraction and separation, a material extracted at the bottom of the tower enters a next-stage extractive distillation tower for separation, the extracting agent is fed secondarily at the top of the tower, high-purity isopropanol is obtained at the top of the distillation tower, the material extracted at the bottom of the tower enters a next-stage pervaporation membrane for separation, high-purity water is obtained at a permeation side, and an extracting agent stream extracted at a diffusion side is recycled. The method has the advantages of low energy consumption, simple process, high purity of the separated cyclohexane, isopropanol and water and the like, and the adopted pervaporation assisted extraction and rectification process has obvious advantages compared with the traditional extraction and rectification process.
Description
[ technical field ] A
The invention belongs to the field of chemical separation and purification, particularly relates to a method for separating cyclohexane-isopropanol-water by a pervaporation extraction rectification process, and further relates to a method for separating cyclohexane-isopropanol-water by a process combining pervaporation and extraction rectification by taking ethylene glycol as an extracting agent.
[ background ] A method for producing a semiconductor device
Cyclohexane is a colorless, pungent liquid, insoluble in water, soluble in most organic solvents, commonly used as a solvent for rubbers, paints, varnishes, and diluents for adhesives. Because of its low toxicity, it is commonly used for degreasing, depainting and extracting essential oils. Isopropanol is a colorless liquid, is used as photographic chemicals, essence and analytical reagents, is used for organic synthesis and pharmacy, and has wide application as an organic raw material and a solvent. Isopropanol is freely miscible with water and has a greater solubility for lipophilic substances than ethanol. In the petroleum industry, it is commonly used as an extractant for cottonseed oil, and also for degreasing animal derived tissue membranes. The mixed solvent of isopropanol and cyclohexane has the advantages of simultaneously leaching alcohol and alkane solvents, and has been widely used as a leaching solvent in rapeseed oil peeling and low-temperature pressing processes.
Cyclohexane, isopropanol and water easily form ternary azeotrope and pairwise azeotrope, the azeotropic temperature of the ternary azeotrope is 337.45K under normal pressure, and the composition of the molar azeotrope is 74 percent of cyclohexane, 18.5 percent of IPA and 7.5 percent of water. Because of the existence of azeotrope in the mixture, the effective separation can not be realized by adopting the common rectification method.
Chinese patent (CN104774130B) discloses a method for separating a mixture of cyclohexane and isopropanol by extractive distillation, which takes a mixture of dimethyl sulfoxide and N, N-dimethylacetamide as an extracting agent, has the advantages of low energy consumption, high recovery rate, simple process, safety, environmental protection and no pollution, and can realize clean production.
Chinese patent (CN102617262B) discloses an energy-saving process for separating cyclohexane-cyclohexene-benzene, which changes the traditional four-tower and two-time extractive distillation process into one-time extractive distillation, completes the separation process of cyclohexene and cyclohexane and the separation process of cyclohexene and benzene while completing the extractive distillation separation of cyclohexane/benzene, and greatly reduces the energy consumption required by the separation process. The invention overcomes the defects of the prior art, and has remarkable practicability and extremely remarkable energy-saving effect.
The prior technology for separating and treating the azeotrope has the problems of high energy consumption, serious environmental pollution and the like, and the process for separating and treating the cyclohexane-isopropanol-water ternary azeotrope has the technical limitation.
The invention adopts a method of separating cyclohexane-isopropanol-water by heat integration extraction and rectification of a mixed extractant, and realizes that the purity of the separated cyclohexane, isoamylol and water is up to more than 99.9 percent by utilizing the difference of solubility and boiling point; the energy-saving process is utilized, the separation cost is reduced, and the method has low energy consumption and simple process.
[ summary of the invention ]
[ problem to be solved ]
The invention aims to provide a process for separating cyclohexane-isopropanol-water by a pervaporation extraction rectification process.
It is another object of the present invention to provide a method for separating cyclohexane-isopropanol-water using the process pervaporation extractive distillation process.
It is another object of the present invention to provide the use of a pervaporation extractive distillation process to separate alkanol water azeotropes.
[ solution ]
The invention is realized by the following technical scheme.
A method for separating cyclohexane-isopropanol-water by pervaporation extraction rectification technology is characterized in that a device for realizing the method mainly comprises the following parts: an extractive distillation tower (T1), an extractive distillation tower (T2), membrane equipment (V), a condenser (C1), a condenser (C2), a condenser (C3), a condenser (C4), a condenser (C5), a reboiler (H1), a reboiler (H2), a pump (P1) and a pump (P2); the bottom of the extractive distillation column (T1) is connected with a reboiler (H1) and a pump (P1) and is connected into the extractive distillation column (T2); the bottom of the extractive distillation column (T2) is connected with a reboiler (H2), a pump (P2) and a condenser (C3) and enters membrane equipment (V); the permeation side of the membrane device (V) is connected with a condenser (C4), and the retentate side is connected with the condenser (C5) and enters a circulating pipeline;
the method for separating cyclohexane-isopropanol-water by adopting the device to carry out the pervaporation extraction rectification process comprises the following steps:
(1) the mixture of cyclohexane, isopropanol and water enters from the middle lower part of an extractive distillation tower (T1), after extraction, distillation and separation, the top of the tower is condensed by a condenser (C1) to obtain high-purity cyclohexane, and the mixture of isopropanol and water enters an extractive distillation tower (T2) from the bottom of the extractive distillation tower (T1) through a reboiler (H1) and a pump (P1);
(2) after the extraction and rectification of the extractive distillation tower (T2), the high-purity isopropanol is obtained after the tower top is condensed by a condenser (C2), and the bottom material flow enters a membrane device (V) after passing through a reboiler (H2), a pump (P2) and a condenser (C3);
(3) after pervaporation of the membrane equipment (V), the permeation side is connected with a condenser (C4), and the retentate side is connected with a condenser (C5) and enters a circulating pipeline;
the membrane device employs pervaporation technology.
According to another preferred embodiment of the invention, it is characterized in that: the operating pressure of the extraction and rectification tower (T1) is 1atm, the number of tower plates is 30-45, the temperature of the extraction and rectification tower (T1) is 80-115 ℃, the operating pressure of the extraction and rectification tower (T2) is 1atm, the number of tower plates is 25-35, and the temperature of the extraction and rectification tower (T2) is 80-190 ℃.
According to another preferred embodiment of the invention, it is characterized in that: the bottom of the extractive distillation column (T2) enters the membrane device (V) after passing through a reboiler (H2), a pump (P2) and a condenser (C3).
According to another preferred embodiment of the invention, it is characterized in that: after pervaporation, the permeate side of the membrane device (V) is connected to a condenser (C4), and the retentate side is connected to a condenser (C5) and enters the circulation line.
According to another preferred embodiment of the invention, it is characterized in that: in the ternary mixed solution of cyclohexane, isopropanol and water, the mass fraction of cyclohexane is 70-75%, the mass fraction of isopropanol is 10-20%, and the mass fraction of isoamyl alcohol is 5-20%.
According to another preferred embodiment of the invention, it is characterized in that: the purity of the cyclohexane recovered from the top of the extractive distillation column (T1) is higher than 99.97%, the purity of the isopropanol recovered from the top of the extractive distillation column (T2) is higher than 99.92%, and the purity of the water recovered from the permeation side of the membrane device (V) is higher than 99.91%.
[ advantageous effects ]
Compared with the prior art, the invention has the following beneficial effects:
(1) the method is adopted to separate the ternary mixture of cyclohexane, isopropanol and water to obtain high-purity cyclohexane, isopropanol and water, so that the high-purity component can be obtained from the ternary azeotropic mixture, and the problem that the cyclohexane, the isopropanol and the water are difficult to separate is solved.
(2) The method has the advantages of simple process, less investment equipment, high purity of the separated cyclohexane, the isopropyl alcohol and the water and the like.
(3) The method adopts a method that the bottom material of an extractive distillation column (T2) flows through a reboiler (H2), a pump (P2) and a condenser (C3) and then enters membrane equipment (V), the permeation side is connected with the condenser (C4), and the retentate side is connected with the condenser (C5) and enters a circulating pipeline, so that the energy consumption loss is greatly reduced, and the cost is saved.
[ description of the drawings ]
FIG. 1 is a flow chart of the process for separating cyclohexane-isopropanol-water by pervaporation extractive distillation.
In the figure, T1 and T2-extractive distillation columns; c1, C2, C3, C4, C5-condenser; h1, H2-reboiler; v-membrane equipment; p1, P2-pump; the numbers represent the respective lines.
[ detailed description ] embodiments
Example 1:
the feed flow is 100kmol/h, the feed contains 74 percent of cyclohexane, 18.5 percent of isopropanol and 7.5 percent of water (mole fraction), the number of theoretical plates of the extraction and rectification tower (T1) is 19, the number of theoretical plates of the extraction and rectification tower (T2) is 28, and the membrane area of the membrane device (V) is 246.5m 2 The mixture of cyclohexane, isopropanol and water enters from the middle-lower part of an extractive distillation column (T1), the circulating stream enters from the top of the extractive distillation column (T1), the operating pressure of the extractive distillation column (T1) is 1atm, and the operation of the extractive distillation column (T2)The pressure was 1atm, and the purity of cyclohexane after separation was 99.97%, the purity of isopropyl alcohol was 99.92%, and the purity of water was 99.91%.
Example 2:
the feed flow is 140kmol/h, the feed contains 74 percent of cyclohexane, 18.5 percent of isopropanol and 7.5 percent of water (mole fraction), the number of theoretical plates of the extraction and rectification tower (T1) is 22, the number of theoretical plates of the extraction and rectification tower (T2) is 30, and the membrane area of the membrane device (V) is 250.2m 2 The mixture of cyclohexane, isopropanol and water enters from the middle lower part of an extraction and rectification tower (T1), the circulating material flow enters from the top of the extraction and rectification tower (T1), the operating pressure of the extraction and rectification tower (T1) is 1atm, the operating pressure of the extraction and rectification tower (T2) is 1atm, the purity of the separated cyclohexane is 99.93%, the purity of the isopropanol is 99.91%, and the purity of the water is 99.9%.
Example 3:
the feed flow is 140kmol/h, the feed contains 80 percent of cyclohexane, 15 percent of isopropanol and 5 percent of water (mole fraction), the theoretical plate number of the extractive distillation column (T1) is 23, the theoretical plate number of the extractive distillation column (T2) is 32, and the membrane area of the membrane device (V) is 253.6m 2 The mixture of cyclohexane, isopropanol and water enters from the middle lower part of an extraction and rectification tower (T1), the circulating material flow enters from the top of the extraction and rectification tower (T1), the operating pressure of the extraction and rectification tower (T1) is 1atm, the operating pressure of the extraction and rectification tower (T2) is 1atm, the purity of the separated cyclohexane is 99.94%, the purity of the isopropanol is 99.93%, and the purity of the water is 99.91%.
Claims (6)
1. A method for separating cyclohexane-isopropanol-water by pervaporation extraction rectification technology is characterized in that a device for realizing the method mainly comprises the following parts: an extractive distillation tower (T1), an extractive distillation tower (T2), membrane equipment (V), a condenser (C1), a condenser (C2), a condenser (C3), a condenser (C4), a condenser (C5), a reboiler (H1), a reboiler (H2), a pump (P1) and a pump (P2); the bottom of the extractive distillation column (T1) is connected with a reboiler (H1) and a pump (P1) and is connected into the extractive distillation column (T2); the bottom of the extractive distillation column (T2) is connected with a reboiler (H2), a pump (P2) and a condenser (C3) and enters membrane equipment (V); the permeation side of the membrane device (V) is connected with a condenser (C4), and the retentate side is connected with the condenser (C5) and enters a circulating pipeline;
the method for separating cyclohexane-isopropanol-water by adopting the device to carry out the pervaporation extraction rectification process comprises the following steps:
(1) the mixture of cyclohexane, isopropanol and water enters from the middle lower part of an extractive distillation tower (T1), after extractive distillation separation, the mixture of isopropanol and water enters an extractive distillation tower (T2) from the bottom of the extractive distillation tower (T1) through a reboiler (H1) and a pump (P1) after the mixture of isopropanol and water is condensed by a condenser (C1) at the top of the tower to obtain high-purity cyclohexane;
(2) after the extraction and rectification of the extractive distillation tower (T2), the high-purity isopropanol is obtained after the tower top is condensed by a condenser (C2), and the bottom material flow enters a membrane device (V) after passing through a reboiler (H2), a pump (P2) and a condenser (C3);
(3) after pervaporation of the membrane equipment (V), the permeation side is connected with a condenser (C4), and the retentate side is connected with a condenser (C5) and enters a circulating pipeline;
the membrane device employs pervaporation technology.
2. The method for separating cyclohexane-isopropanol-water by pervaporation extractive distillation process as claimed in claim 1, wherein: the operating pressure of the extraction and rectification tower (T1) is 1atm, the number of tower plates is 30-45, the temperature of the extraction and rectification tower (T1) is 80-115 ℃, the operating pressure of the extraction and rectification tower (T2) is 1atm, the number of tower plates is 25-35, and the temperature of the extraction and rectification tower (T2) is 80-190 ℃.
3. The method for separating cyclohexane-isopropanol-water by pervaporation extractive distillation process as claimed in claim 1, wherein: the bottom of the extractive distillation column (T2) enters the membrane device (V) after passing through a reboiler (H2), a pump (P2) and a condenser (C3).
4. The method for separating cyclohexane-isopropanol-water by pervaporation extraction and rectification process according to claim 1, wherein the method comprises the following steps: after pervaporation, the permeate side of the membrane device (V) is connected to a condenser (C4), and the retentate side is connected to a condenser (C5) and enters the circulation line.
5. The method for separating cyclohexane-isopropanol-water by pervaporation extractive distillation process as claimed in claim 1, wherein: in the ternary mixed solution of cyclohexane, isopropanol and water, the mass fraction of cyclohexane is 70-75%, the mass fraction of isopropanol is 10-20%, and the mass fraction of isoamylol is 5-20%.
6. The method for separating cyclohexane-isopropanol-water by pervaporation extractive distillation process as claimed in claim 1, wherein: the purity of the cyclohexane recovered from the top of the extractive distillation column (T1) is higher than 99.97%, the purity of the isopropanol recovered from the top of the extractive distillation column (T2) is higher than 99.92%, and the purity of the water recovered from the permeation side of the membrane device (V) is higher than 99.91%.
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Cited By (2)
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| CN115745744A (en) * | 2022-11-25 | 2023-03-07 | 青岛科技大学 | Method for separating ethylene glycol monomethyl ether-ethanol-water azeotrope by coupling extractive distillation and pervaporation |
| CN115819184A (en) * | 2022-11-23 | 2023-03-21 | 青岛科技大学 | Energy-saving process for separating n-propanol-n-propyl ether-water by imidazole ionic liquid extractive distillation-pervaporation coupling |
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|---|---|---|---|---|
| CN115819184A (en) * | 2022-11-23 | 2023-03-21 | 青岛科技大学 | Energy-saving process for separating n-propanol-n-propyl ether-water by imidazole ionic liquid extractive distillation-pervaporation coupling |
| CN115745744A (en) * | 2022-11-25 | 2023-03-07 | 青岛科技大学 | Method for separating ethylene glycol monomethyl ether-ethanol-water azeotrope by coupling extractive distillation and pervaporation |
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