CN202336224U - Azeotropic distillation system for mixture of carbinol and tetrahydrofuran - Google Patents
Azeotropic distillation system for mixture of carbinol and tetrahydrofuran Download PDFInfo
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- CN202336224U CN202336224U CN2011203856805U CN201120385680U CN202336224U CN 202336224 U CN202336224 U CN 202336224U CN 2011203856805 U CN2011203856805 U CN 2011203856805U CN 201120385680 U CN201120385680 U CN 201120385680U CN 202336224 U CN202336224 U CN 202336224U
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Abstract
The utility model belongs to the technical field of chemical distillation and particularly discloses an azeotropic distillation system for a mixture of carbinol and tetrahydrofuran. The azeotropic distillation system for the mixture of carbinol and tetrahydrofuran comprises a low-pressure distillation tower and a high-pressure distillation tower which are connected in series, wherein the bottom of the low-pressure distillation tower is provided with a low-pressure tower reboiler; the top of the low-pressure distillation tower is provide with a low-pressure tower condenser; the bottom of the high-pressure distillation tower is provided with a high-pressure tower reboiler; and the top of the high-pressure distillation tower is provided with a high-pressure tower condenser. The azeotropic distillation system disclosed by the utility model can be used for carrying out two-time distillation on the mixture of carbinol and tetrahydrofuran so as to effectively separate the mixture of carbinol and tetrahydrofura, the separated carbinol and tetrahydrofuran are free from entrainer impurities because the entrainer is not used, and therefore purity is higher.
Description
Technical field
The utility model belongs to chemical industry distillation technology field, relates in particular to the azeotropic distillation system of a kind of methyl alcohol and tetrahydrofuran compound.
Background technology
When from methyl alcohol and tetrahydrofuran compound stream, carrying out the rectification and purification oxolane, methyl alcohol and oxolane can form azeotropic mixture, and the conventional distillation method can't be separated oxolane with methyl alcohol, need to use azeotropic distillation.And generally speaking, azeotropic distillation is to change the VLE relation between the separated component through adding suitable separation medium (being entrainer), thereby separation is become different by difficulty.If but in methyl alcohol and tetrahydrofuran compound, added entrainer, then entrainer will get in the oxolane product as impurity, makes it to obtain high-quality oxolane product.
The utility model content
The utility model is intended to overcome the deficiency that above prior art exists, and when a kind of separation of methanol and tetrahydrofuran compound are provided, does not use the separation medium just can realize the azeotropic distillation system that both separate.
The utility model technical solution problem adopts following technical scheme:
The methyl alcohol of the utility model and the azeotropic distillation system of tetrahydrofuran compound comprise the low-pressure distillation tower and the high-pressure rectification tower of series connection; Be provided with the lower pressure column reboiler in the bottom of low-pressure distillation tower, be provided with the lower pressure column condenser at the top of low-pressure distillation tower; Be provided with the high-pressure tower reboiler in the bottom of high-pressure rectification tower, be provided with the high-pressure tower condenser at the top of high-pressure rectification tower.
Further, the condensate outlet of said lower pressure column condenser is connected with first phegma inlet of low-pressure distillation tower, the charging aperture of high-pressure rectification tower through pipeline respectively.Also can connect the lower pressure column return tank successively at the condensate outlet of said lower pressure column condenser, the lower pressure column reflux pump, lower pressure column backflow delivery side of pump is connected with first phegma inlet of low-pressure distillation tower, the charging aperture of high-pressure rectification tower respectively through pipeline.
Further, the condensate outlet of said high-pressure tower condenser is connected with second phegma inlet of low-pressure distillation tower, the phegma inlet of high-pressure rectification tower through pipeline respectively.Also can connect high-pressure tower return tank and high-pressure tower reflux pump at the condensate outlet of said high-pressure tower condenser successively, high-pressure tower backflow delivery side of pump is connected with second phegma inlet of low-pressure distillation tower, the phegma inlet of high-pressure rectification tower respectively through pipeline.
Further, the lower pressure column reflux pump is provided with the 5th flow controller with the pipeline that is connected between the high-pressure rectification tower.
Further, on the pipeline between high-pressure tower reflux pump and low-pressure distillation tower second phegma inlet, be provided with the first flow controller, be provided with first temperature controller on low-pressure distillation tower top, the first flow controller is connected with first temperature controller.
Further; The lower pressure column return tank is provided with first fluid level controller; The pipeline that is connected between first phegma inlet of lower pressure column reflux pump and low-pressure distillation tower is provided with the 3rd flow controller, and first fluid level controller is connected with the 3rd flow controller; The high-pressure tower return tank is provided with second fluid level controller, and the pipeline that is connected between the phegma inlet of high-pressure tower reflux pump and high-pressure rectification tower is provided with the 4th flow controller, and second fluid level controller is connected with the 4th flow controller.
Further, the pipeline between low-pressure distillation tower and the lower pressure column condenser is provided with the low-pressure distillation tower pressure controller; Pipeline between high-pressure rectification tower and the high-pressure tower condenser is provided with high-pressure rectification pressure tower controller.
Further, on the low-pressure steam inlet pipeline of lower pressure column reboiler, second flow controller is set, second temperature controller is set on low-pressure distillation tower, second flow controller is connected with second temperature controller.
Further, the lower pressure column reflux pump is provided with the 5th flow controller with the pipeline that is connected between the high-pressure rectification tower.
The beneficial effect of the utility model is embodied in the following aspects:
1, the azeotropic distillation system of methyl alcohol of the utility model and tetrahydrofuran compound adopts the low-pressure distillation tower and the high-pressure rectification tower of series connection to carry out twice rectifying; Can effectively separate with tetrahydrofuran compound methyl alcohol; And because need not to use entrainer; So methyl alcohol and oxolane after separating do not have entrainer impurity, purity is higher.
2, the azeotropic distillation system of methyl alcohol of the utility model and tetrahydrofuran compound is rational in infrastructure, can comprehensively control distillation process.
Description of drawings
Fig. 1 is the structural representation of the azeotropic distillation system of the utility model methyl alcohol and tetrahydrofuran compound.
Mark is illustrated as among the figure: 1: low-pressure distillation tower; 2: the high-pressure rectification tower; 3: the lower pressure column reboiler; 4: the lower pressure column condenser; 5: the high-pressure tower reboiler; 6: the high-pressure tower condenser; 7: the lower pressure column return tank; 8: the lower pressure column reflux pump; 9: the high-pressure tower return tank; 10: the high-pressure tower reflux pump; 11: the low-pressure distillation tower pressure controller; 12: high-pressure rectification pressure tower controller; 13: the first flow controller; 14: the first temperature controllers; 15: the second flow controllers; 16: the second temperature controllers; 17: the first fluid level controllers; 18: the three flow controllers; 19: the second fluid level controllers; 20: the four flow controllers; 21: the five flow controllers; 22: discharging pump; 23: the six flow controllers; 24: the three fluid level controllers; 25: the seven flow controllers; 26: the four fluid level controllers; 27: the eight flow controllers; 28: the nine flow controllers; 29: the first phegma inlets; 30: the second phegma inlets; 31: the charging aperture of low-pressure distillation tower; 32: the charging aperture of high-pressure rectification tower; 33: the phegma inlet.
The specific embodiment
Describe in further detail below in conjunction with the specific embodiment of accompanying drawing to the utility model, following embodiment is used to explain the utility model, but is not used for limiting the protection domain of the utility model.
As shown in Figure 1, the azeotropic distillation system of the utility model methyl alcohol and tetrahydrofuran compound comprises the low-pressure distillation tower 1 and high-pressure rectification tower 2 of series connection; Be provided with lower pressure column reboiler 3 in the bottom of low-pressure distillation tower 1, be provided with lower pressure column condenser 4 at the top of low-pressure distillation tower 1; Be provided with high-pressure tower reboiler 5 in the bottom of high-pressure rectification tower 2, be provided with high-pressure tower condenser 6 at the top of high-pressure rectification tower 2.
The condensate outlet of said lower pressure column condenser 4 is connected with first phegma inlet 29 of low-pressure distillation tower 1, the charging aperture 32 of high-pressure rectification tower through pipeline respectively.Also can connect lower pressure column return tank 7 successively at the condensate outlet of said lower pressure column condenser 4, lower pressure column reflux pump 8, the outlet of lower pressure column reflux pump 8 through pipeline respectively with the charging aperture 32 of first phegma of low-pressure distillation tower 1 inlet 29, high-pressure rectification tower.
The condensate outlet of said high-pressure tower condenser 6 phegma on second phegma inlet 30 through pipeline and low-pressure distillation tower 1, high-pressure rectification tower 2 tops is respectively gone into 33 mouthfuls and is connected.Also can connect high-pressure tower return tank 9 successively at the condensate outlet of said high-pressure tower condenser 6; High-pressure tower reflux pump 10, the outlet of high-pressure tower reflux pump 10 is connected with second phegma inlet 30 of low-pressure distillation tower 1, the phegma inlet 33 of high-pressure rectification tower 2 respectively through pipeline.
On the pipeline between second phegma inlet 30 of high-pressure tower reflux pump 10 and low-pressure distillation tower 1, be provided with first flow controller 13, be provided with first temperature controller 14 on low-pressure distillation tower 1 top, first flow controller 13 is connected with first temperature controller 14.
Pipeline between low-pressure distillation tower 1 and the lower pressure column condenser 4 is provided with low-pressure distillation tower pressure controller 11; Be provided with high-pressure rectification pressure tower controller 12 in the pipeline between high-pressure rectification tower 2 and high-pressure tower condenser 6.
Lower pressure column return tank 7 is provided with first fluid level controller 17; The pipeline that is connected between first phegma inlet 29 of lower pressure column reflux pump 8 and low-pressure distillation tower 1 is provided with the 3rd flow controller 18, the first fluid level controllers 17 and is connected with the 3rd flow controller 18; High-pressure tower return tank 9 is provided with second fluid level controller 19; The pipeline that is connected between the phegma inlet 33 of high-pressure tower reflux pump 10 and high-pressure rectification tower 2 is provided with the 4th flow controller 20, the second fluid level controllers 19 and is connected with the 4th flow controller 20.
Lower pressure column reflux pump 8 is provided with the 5th flow controller 21 with the pipeline that is connected between the high-pressure rectification tower 2.
The tower bottoms outlet conduit of low-pressure distillation tower 1 is provided with discharging pump 22 and the 7th flow controller 25, is provided with the 3rd fluid level controller 24, the seven flow controllers 25 in the bottom of low-pressure distillation tower 1 and is connected with the 3rd fluid level controller 24.Charging aperture at low-pressure distillation tower 1 is provided with the 9th flow controller 28.
The steam inlet of high-pressure tower reboiler 5 is provided with the 6th flow controller 23.
The tower bottoms outlet conduit of high-pressure rectification tower 2 is provided with the 8th flow controller 27, is provided with the 4th fluid level controller 26, the eight flow controllers 27 at high-pressure rectification tower 2 and is connected with the 4th fluid level controller 26.
The operation principle of the utility model: as shown in Figure 1, low-pressure distillation tower 1 is operated under normal pressure, and used lower pressure column reboiler 3 uses low-pressure steam (LPS), and the operating pressure of high-pressure rectification tower 2 is higher, and used high-pressure tower reboiler 5 uses middle pressure steam (MPS).Low-pressure distillation tower 1 is controlled at pressurized operation through low-pressure distillation tower pressure controller 11, and high-pressure rectification tower 2 is controlled at high-voltage operation through high-pressure rectification pressure tower controller 12.The principle of utilizing the content of tetrahydrofuran in methyl alcohol-oxolane azeotropic mixture composition to raise and reduce with pressure; In low-pressure distillation tower 1, oxolane is separated from methyl alcohol-oxolane azeotropic mixture; The composition that slightly distillates from cat head is mainly to pump into the high-pressure rectification tower 2 behind the rectifying thing of oxolane again and separates once more, obtains highly purified oxolane and methyl alcohol.
Concrete separation process is following: methyl alcohol (MeOH) and oxolane (THF) mixture the 9th flow controller 28 of flowing through afterwards enters into low-pressure distillation tower 1 from the charging apertures 31 of low-pressure distillation tower; In low-pressure distillation tower 1, vaporized by the low-pressure steam of lower pressure column reboiler 3 heating back; The not methyl alcohol of vaporization extraction at the bottom of the tower; The methyl alcohol of the high content of tetrahydrofuran after the vaporization-oxolane azeotropic mixture steam gets into the lower pressure column condenser 4 from cat head and is condensed; Condensate liquid is collected in the lower pressure column return tank 7; Lime set in the lower pressure column return tank 7 is under the effect of lower pressure column reflux pump 8, and a part is sent into high-pressure rectification tower 2 through the 5th flow controller 21, and part entering the 3rd flow controller 18 after first fluid level controller 17 is set is sent into low-pressure distillation tower 1 again and refluxed as tower.After the methyl alcohol of high content of tetrahydrofuran-oxolane azeotrope stream gets into high-pressure rectification tower 2; In high-pressure rectification tower 2, vaporized by the heating of the middle pressure steam of high-pressure tower reboiler 5; The methyl alcohol of the low content of tetrahydrofuran after the vaporization-oxolane azeotropic mixture steam gets into high-pressure tower condenser 6 from cat head and is condensed; Condensate liquid is collected in the high-pressure tower return tank 9; Lime set in the high-pressure tower return tank 9 is through high-pressure tower reflux pump 10, and a part is sent into low-pressure distillation tower 1 through first flow controller 13, and part entering four flow controllers 20 after second fluid level controller 19 is set are sent into high-pressure rectification tower 2 again and refluxed as tower.Wherein the methyl alcohol in the high-pressure rectification tower 2 all is admitted to low-pressure distillation tower 1 through first flow controller 13, isolated oxolane product after the 4th fluid level controller 26 at the bottom of high-pressure rectification tower 2 towers is set oxolane extraction flows through the extraction at the bottom of high-pressure rectification tower 2 towers of the 8th flow controller 27.
During control, set first flow controller 13, carry out tandem control, to keep the oxolane storage in the low-pressure distillation tower 1 through low-pressure distillation tower 1 top first temperature controller 14.Control second flow controller 15 through low-pressure distillation tower 1 bottom second temperature controller, 16 tandems, guarantee that oxolane does not fall into low-pressure distillation tower 1 tower still, and influence methanol product purity.
The above embodiment; The just preferred embodiment of the utility model; Be not to limit the utility model practical range; So all according to the described conspicuous change of the utility model claim, and other does not break away from the change of the utility model essence, all should be included within the protection domain of the utility model.
Claims (10)
1. the azeotropic distillation system of methyl alcohol and tetrahydrofuran compound is characterized in that: the low-pressure distillation tower (1) and the high-pressure rectification tower (2) that comprise series connection; Be provided with lower pressure column reboiler (3) in the bottom of low-pressure distillation tower (1), be provided with lower pressure column condenser (4) at the top of low-pressure distillation tower (1); Be provided with high-pressure tower reboiler (5) in the bottom of high-pressure rectification tower (2), be provided with high-pressure tower condenser (6) at the top of high-pressure rectification tower (2).
2. the azeotropic distillation system of methyl alcohol according to claim 1 and tetrahydrofuran compound is characterized in that: the condensate outlet of said lower pressure column condenser (4) is connected with the charging aperture (32) that the smart tower of first phegma inlet (29), high pressure of low-pressure distillation tower (1) heats up in a steamer through pipeline respectively.
3. the azeotropic distillation system of methyl alcohol according to claim 1 and tetrahydrofuran compound is characterized in that: the condensate outlet of said high-pressure tower condenser (6) is connected with second phegma inlet (30) of low-pressure distillation tower (1), the phegma inlet (33) of high-pressure rectification tower (2) through pipeline respectively.
4. the azeotropic distillation system of methyl alcohol according to claim 1 and tetrahydrofuran compound; It is characterized in that: the condensate outlet of said lower pressure column condenser (4) is connected with lower pressure column return tank (7) and lower pressure column reflux pump (8) in turn, and the outlet of lower pressure column reflux pump (8) is connected with first phegma inlet (29) of low-pressure distillation tower (1), the charging aperture (32) of high-pressure rectification tower respectively through pipeline.
5. the azeotropic distillation system of methyl alcohol according to claim 4 and tetrahydrofuran compound is characterized in that: lower pressure column reflux pump (8) is provided with the 5th flow controller (21) with the pipeline that is connected between the high-pressure rectification tower (2).
6. the azeotropic distillation system of methyl alcohol according to claim 1 and tetrahydrofuran compound; It is characterized in that: the condensate outlet of said high-pressure tower condenser (6) is connected with high-pressure tower return tank (9) in turn; High-pressure tower reflux pump (10), the outlet of high-pressure tower reflux pump (10) is connected with second phegma inlet (30) of low-pressure distillation tower (1), the phegma inlet (33) of high-pressure rectification tower (2) respectively through pipeline.
7. the azeotropic distillation system of methyl alcohol according to claim 6 and tetrahydrofuran compound; It is characterized in that: on the pipeline between high-pressure tower reflux pump (10) and low-pressure distillation tower (1) the second phegma inlet, be provided with first flow controller (13); Be provided with first temperature controller (14) on the top of low-pressure distillation tower (1), first flow controller (13) is connected with first temperature controller (14).
8. according to the azeotropic distillation system of claim 6 or 7 described methyl alcohol and tetrahydrofuran compound; It is characterized in that: lower pressure column return tank (7) is provided with first fluid level controller (17); The pipeline that is connected between first phegma inlet of lower pressure column reflux pump (8) and low-pressure distillation tower (1) is provided with the 3rd flow controller (18), and first fluid level controller (17) is connected with the 3rd flow controller (18); High-pressure tower return tank (9) is provided with second fluid level controller (19); The pipeline that is connected between the phegma inlet of high-pressure tower reflux pump (10) and high-pressure rectification tower (2) is provided with the 4th flow controller (20), and second fluid level controller (19) is connected with the 4th flow controller (20).
9. the azeotropic distillation system of methyl alcohol according to claim 1 and tetrahydrofuran compound is characterized in that: the pipeline between low-pressure distillation tower (1) and the lower pressure column condenser (4) is provided with low-pressure distillation tower pressure controller (11); Pipeline between high-pressure rectification tower (2) and the high-pressure tower condenser (6) is provided with high-pressure rectification pressure tower controller (12).
10. the azeotropic distillation system of methyl alcohol according to claim 1 and tetrahydrofuran compound; It is characterized in that: second flow controller (15) is set on the low-pressure steam inlet pipeline of lower pressure column reboiler (3); Second temperature controller (16) is set on low-pressure distillation tower (1), and second flow controller (15) is connected with second temperature controller (16).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203856805U CN202336224U (en) | 2011-10-11 | 2011-10-11 | Azeotropic distillation system for mixture of carbinol and tetrahydrofuran |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011203856805U CN202336224U (en) | 2011-10-11 | 2011-10-11 | Azeotropic distillation system for mixture of carbinol and tetrahydrofuran |
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| CN202336224U true CN202336224U (en) | 2012-07-18 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN2011203856805U Expired - Fee Related CN202336224U (en) | 2011-10-11 | 2011-10-11 | Azeotropic distillation system for mixture of carbinol and tetrahydrofuran |
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| CN (1) | CN202336224U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN113461644A (en) * | 2021-07-21 | 2021-10-01 | 江苏盈天化学有限公司 | Method for recovering tetrahydrofuran from waste solvent |
-
2011
- 2011-10-11 CN CN2011203856805U patent/CN202336224U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN106146255B (en) * | 2016-07-21 | 2019-03-01 | 青岛科技大学 | Double column pressure swing extracts coupling rectification and separates water, methanol, tetrahydrofuran object system, method |
| CN113461644A (en) * | 2021-07-21 | 2021-10-01 | 江苏盈天化学有限公司 | Method for recovering tetrahydrofuran from waste solvent |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20120718 Termination date: 20151011 |
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| EXPY | Termination of patent right or utility model |