CN107213666B - Separation device for benzene in toluene methanol alkylation reaction product - Google Patents
Separation device for benzene in toluene methanol alkylation reaction product Download PDFInfo
- Publication number
- CN107213666B CN107213666B CN201610166038.5A CN201610166038A CN107213666B CN 107213666 B CN107213666 B CN 107213666B CN 201610166038 A CN201610166038 A CN 201610166038A CN 107213666 B CN107213666 B CN 107213666B
- Authority
- CN
- China
- Prior art keywords
- toluene
- benzene
- tower
- communicated
- rectifying tower
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Links
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 153
- 239000007795 chemical reaction product Substances 0.000 title abstract description 9
- 238000005804 alkylation reaction Methods 0.000 title abstract description 8
- 238000000926 separation method Methods 0.000 title abstract description 7
- BKBMACKZOSMMGT-UHFFFAOYSA-N methanol;toluene Chemical compound OC.CC1=CC=CC=C1 BKBMACKZOSMMGT-UHFFFAOYSA-N 0.000 title abstract description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims abstract description 168
- 238000010992 reflux Methods 0.000 claims abstract description 49
- 238000011084 recovery Methods 0.000 claims abstract description 26
- 239000007791 liquid phase Substances 0.000 claims abstract description 24
- 239000012071 phase Substances 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 description 16
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- 230000029936 alkylation Effects 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
Classifications
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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
- B01D3/16—Fractionating columns in which vapour bubbles through liquid
-
- 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
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4216—Head stream
-
- 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
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
Abstract
The invention discloses a separation device of benzene in toluene methanol alkylation reaction products, wherein a reboiler is communicated with a toluene rectifying tower, 3-10 tower plates are arranged in the toluene rectifying tower above a side outlet, and a gas phase outlet arranged at the upper part of the toluene rectifying tower is communicated with a reflux tank through a condenser; the side outlet is communicated with the cooler, and toluene coming out of the cooler is sent out; the reboiler is communicated with the benzene recovery tower, the reflux tank is communicated with a gas phase outlet arranged at the upper part of the benzene recovery tower through a condenser, gas phase coming out of the reflux tank is sent out, one part of liquid phase benzene coming out of the reflux tank is sent out, the other part of liquid phase benzene flows back into the benzene recovery tower through a reflux port, and toluene coming out of a liquid phase outlet arranged at the lower part of the benzene recovery tower is sent out; the liquid phase benzene from the reflux tank communicated with the toluene rectifying tower enters the toluene rectifying tower through the reflux port of the toluene rectifying tower, and the gas phase from the reflux tank communicated with the toluene rectifying tower enters the benzene recovery tower through the feed port of the benzene recovery tower.
Description
Technical Field
The invention relates to a device for separating benzene from toluene methanol alkylation reaction products, which is mainly used for separating benzene from the reaction products in the production process of preparing paraxylene by toluene methanol alkylation.
Background
In the production process of preparing paraxylene by alkylation of toluene and methanol, benzene and other noncondensable gases in the reaction product account for about 1%, xylene accounts for 26%, toluene is 73%, toluene can enter the reactor to be used as raw material for further reaction, and thus separation of toluene in the reaction product becomes an indispensable link. In the production process, toluene separation is carried out in a toluene rectifying tower, an alkylation reaction product enters the toluene rectifying tower, and a gas phase at the top of the tower is condensed by a condenser and enters a reflux tank. In the reflux drum, the uncondensed light fraction gas enters a fuel gas system as fuel gas; one part of liquid benzene in the reflux tank is refluxed into the toluene rectifying tower, and the other part is sent to the tank area; the recombination coming out from the bottom of the toluene rectifying tower is sent to the xylene rectifying tower, and the side line is cooled to get toluene. The benzene content in the toluene rectifying tower feed is very low and is below 1%, so that the benzene concentration extracted from the tower top is 99%, the number of tower plates is more than 26, the reflux amount of benzene is large, the energy consumption is high due to the large reflux amount of benzene, and the production cost of enterprises is increased.
Disclosure of Invention
The invention solves the technical problem of providing the toluene separation device with simple equipment, small reflux quantity and low energy consumption.
The technical scheme of the invention is that the separation device of benzene in toluene methanol alkylation reaction products comprises a toluene rectifying tower, a reboiler, a condenser, a cooler and a reflux tank, wherein the toluene rectifying tower is provided with a feed inlet, a gas phase outlet, a liquid phase outlet, a reflux port and a side line outlet; the side outlet is communicated with the cooler, and toluene coming out of the cooler is sent out; the benzene recovery tower is provided with a feed inlet, a gas phase outlet, a liquid phase outlet and a reflux tank, the reboiler is communicated with the benzene recovery tower, the reflux tank is communicated with the gas phase outlet arranged at the upper part of the benzene recovery tower through a condenser, gas phase coming out of the reflux tank is sent outwards, part of liquid phase benzene coming out of the reflux tank is sent outwards, the other part of liquid phase returns to the benzene recovery tower through the reflux port, and toluene coming out of the liquid phase outlet arranged at the lower part of the benzene recovery tower is sent outwards; the tower plate of the toluene rectifying tower is provided with 3-10 blocks, liquid-phase benzene coming out of a reflux tank communicated with the toluene rectifying tower enters the toluene rectifying tower through a reflux port of the toluene rectifying tower, and gas phase coming out of the reflux tank communicated with the toluene rectifying tower enters a benzene recovery tower through a feed port of the benzene recovery tower.
The invention reduces the tower plate arranged above the side outlet from 26 original blocks to 3-10 blocks because the liquid phase benzene coming out of the reflux tank communicated with the toluene rectifying tower is totally refluxed into the toluene rectifying tower, thereby reducing the height of the toluene rectifying tower, improving the internal temperature of the toluene rectifying tower, ensuring the gas phase benzene content coming out of the reflux tank communicated with the toluene rectifying tower to be 10-20%, and the extraction amount to be 5-10% of the feeding amount; the gas phase benzene is separated by a benzene recovery tower. Compared with the prior art, the reflux quantity of the liquid-phase benzene from the reflux tank communicated with the toluene rectifying tower is reduced to 20-30%, and the energy consumption can be reduced by 30-50%.
Drawings
Fig. 1 is a schematic diagram of the structure of the invention.
Detailed Description
The invention is further described in detail by referring to the accompanying drawings, and comprises a toluene rectifying tower 2, a reboiler 18, a condenser 4, a cooler 15 and a reflux tank 5, wherein a feed inlet 17, a gas phase outlet 3, a liquid phase outlet 1, a reflux inlet 14 and a side line outlet 16 are arranged on the toluene rectifying tower 2, the reboiler 18 is communicated with the toluene rectifying tower 2, tower plates 3-10 are arranged in the toluene rectifying tower 2 above the side line outlet 16, the number of the tower plates can be set according to actual needs, and a gas outlet 3 arranged at the upper part of the toluene rectifying tower 2 is communicated with the reflux tank 5 through the condenser 4; a side outlet 16 is communicated with the cooler 15, and toluene coming out of the cooler 15 is sent out; the benzene recovery tower 6 is provided with a feed inlet 11, a gas phase outlet 7, a liquid phase outlet 13 and a reflux inlet 10, the reboiler 12 is communicated with the benzene recovery tower 6, the reflux tank 9 is communicated with the gas phase outlet 7 through the condenser 8, gas phase coming out of the reflux tank 9 is sent out, one part of liquid phase benzene coming out of the reflux tank 9 is sent out, the other part of liquid phase returns to the benzene recovery tower 6 through the reflux inlet 10, and toluene coming out of the liquid phase outlet 13 is sent out; liquid-phase benzene from the reflux drum 5 communicated with the toluene rectifying tower 2 enters the toluene rectifying tower 2 through a reflux port 14 of the toluene rectifying tower 2, and gas phase from the reflux drum 5 communicated with the toluene rectifying tower 2 enters the benzene recovery tower 6 through a feed port 11 of the benzene recovery tower 6.
The above-mentioned embodiments are only preferred embodiments of the present invention, and the protection scope of the present invention is not limited to the above-mentioned embodiments, and all technical solutions belonging to the concept of the present invention belong to the protection scope of the present invention. It should be noted that modifications and adaptations to the invention without departing from the principles thereof are intended to be within the scope of the invention as set forth in the following claims.
Claims (1)
1. The device comprises a toluene rectifying tower, a reboiler, a condenser, a cooler and a reflux tank, wherein the toluene rectifying tower is provided with a feed inlet, a gas phase outlet, a liquid phase outlet, a reflux port and a side line outlet; the side outlet is communicated with the cooler, and toluene coming out of the cooler is sent out, and the side outlet is characterized in that: the benzene recovery tower is provided with a feed inlet, a gas phase outlet, a liquid phase outlet and a reflux tank, the reboiler is communicated with the benzene recovery tower, the reflux tank is communicated with the gas phase outlet arranged at the upper part of the benzene recovery tower through a condenser, gas phase coming out of the reflux tank is sent outwards, part of liquid phase benzene coming out of the reflux tank is sent outwards, the other part of liquid phase returns to the benzene recovery tower through the reflux port, and toluene coming out of the liquid phase outlet arranged at the lower part of the benzene recovery tower is sent outwards; the tower plate of the toluene rectifying tower is provided with 3-10 blocks, liquid-phase benzene coming out of a reflux tank communicated with the toluene rectifying tower enters the toluene rectifying tower through a reflux port of the toluene rectifying tower, and gas phase coming out of the reflux tank communicated with the toluene rectifying tower enters a benzene recovery tower through a feed port of the benzene recovery tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610166038.5A CN107213666B (en) | 2016-03-22 | 2016-03-22 | Separation device for benzene in toluene methanol alkylation reaction product |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610166038.5A CN107213666B (en) | 2016-03-22 | 2016-03-22 | Separation device for benzene in toluene methanol alkylation reaction product |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107213666A CN107213666A (en) | 2017-09-29 |
| CN107213666B true CN107213666B (en) | 2023-10-31 |
Family
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610166038.5A Active CN107213666B (en) | 2016-03-22 | 2016-03-22 | Separation device for benzene in toluene methanol alkylation reaction product |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107213666B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115888800A (en) * | 2022-09-22 | 2023-04-04 | 河南永大化工科技有限公司 | Shape-selective catalyst for p-diethylbenzene and preparation method and application thereof |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4041091A (en) * | 1976-02-19 | 1977-08-09 | Uop Inc. | Fractionation of aromatic streams |
| CN1544582A (en) * | 2003-11-20 | 2004-11-10 | 北京欣博通石油化工设备有限公司 | Process for olefin removal from refinery gas |
| CN101367704A (en) * | 2008-09-17 | 2009-02-18 | 天津大学 | System and operation method for recycling benezene and pure methylbenzene from crude benzole hydrogenation liquid |
| CN103755515A (en) * | 2014-01-02 | 2014-04-30 | 中山大学 | Method and equipment for producing benzene and dimethyl benzene through methylbenzene dismutation |
| CN104027995A (en) * | 2013-05-30 | 2014-09-10 | 中石化上海工程有限公司 | Method for separating benzene, ethylbenzene, poly-ethylbenzene and heavy component mixture series |
| CN104109065A (en) * | 2014-06-07 | 2014-10-22 | 宁夏宝塔石化科技实业发展有限公司 | Method of preparing xylene by alkylation of benzene and methanol |
-
2016
- 2016-03-22 CN CN201610166038.5A patent/CN107213666B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4041091A (en) * | 1976-02-19 | 1977-08-09 | Uop Inc. | Fractionation of aromatic streams |
| CN1544582A (en) * | 2003-11-20 | 2004-11-10 | 北京欣博通石油化工设备有限公司 | Process for olefin removal from refinery gas |
| CN101367704A (en) * | 2008-09-17 | 2009-02-18 | 天津大学 | System and operation method for recycling benezene and pure methylbenzene from crude benzole hydrogenation liquid |
| CN104027995A (en) * | 2013-05-30 | 2014-09-10 | 中石化上海工程有限公司 | Method for separating benzene, ethylbenzene, poly-ethylbenzene and heavy component mixture series |
| CN103755515A (en) * | 2014-01-02 | 2014-04-30 | 中山大学 | Method and equipment for producing benzene and dimethyl benzene through methylbenzene dismutation |
| CN104109065A (en) * | 2014-06-07 | 2014-10-22 | 宁夏宝塔石化科技实业发展有限公司 | Method of preparing xylene by alkylation of benzene and methanol |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107213666A (en) | 2017-09-29 |
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| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20180213 Address after: Huixian City, Xinxiang City, Henan province 453600 the Great Wall Avenue South Middle Henan Yongda Chemical Technology Co., Ltd. Applicant after: Henan Yongda Chemical Technology Co.,Ltd. Address before: Huixian City, Xinxiang City, Henan province 453600 the Great Wall Avenue South Middle Henan Yongda Chemical Co. Ltd. Applicant before: HENAN YONGDA CHEMICAL Co.,Ltd. |
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| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |