CN106631663A - Energy-saving styrene production device - Google Patents
Energy-saving styrene production device Download PDFInfo
- Publication number
- CN106631663A CN106631663A CN201611069739.3A CN201611069739A CN106631663A CN 106631663 A CN106631663 A CN 106631663A CN 201611069739 A CN201611069739 A CN 201611069739A CN 106631663 A CN106631663 A CN 106631663A
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- China
- Prior art keywords
- tower
- styrene
- ethylbenzene
- crude styrene
- lower pressure
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/32—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by dehydrogenation with formation of free hydrogen
- C07C5/327—Formation of non-aromatic carbon-to-carbon double bonds only
-
- 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
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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
- Y02P20/10—Process efficiency
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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)
Abstract
The invention is mainly applied to the technical field of styrene production, and particularly relates to an energy-saving styrene production device. The energy-saving styrene production device comprises a coarse styrene high pressure tower, wherein material inlets in the upper parts of the coarse styrene high pressure tower and a coarse styrene low pressure tower are respectively connected with a material outlet of an ethylbenzene dehydrogenation system; material outlets in the bottoms of the coarse styrene high pressure tower and the coarse styrene low pressure tower are respectively communicated with a styrene tower; the bottom of the coarse styrene low pressure tower is communicated with a low pressure tower reboiler; the top of the coarse styrene high pressure tower is communicated with a material inlet of an ethylbenzene tower through a tower top gas output pipe; the tower top gas output pipe is communicated with the low pressure tower reboiler; the top of the coarse styrene low pressure tower is communicated with a low pressure tower condenser; the top of the ethylbenzene tower is communicated with an ethylbenzene tower condenser; a tar pipe is arranged at the bottom of a fine styrene tower, and the top of the fine styrene tower is communicated with a styrene tower condenser. Under a condition of not changing the total water-hydrocarbon ratio, the energy-saving production device can increase the steam amount of a steam overheating furnace so as to reduce the outlet temperature of the steam overheating furnace.
Description
Technical field
The present invention relates to a kind of styrene production energy-saving device, is mainly used in cinnamic production technical field.
Background technology
Currently, in the world state-of-the-art ethylbenzene dehydrogenation production technology is Lummus and TOTAL/Badger adabatic dehydrogenation skills
Art, two techniques are quite similar, and respectively have feature.
Lummus later technologies adopt low water hydrocarbon ratio (1.0 or so), phenyl ethylene rectification only to need heating using styrene
Rectification process twice, i.e., first separate ethylbenzene and styrene in crude styrene tower, and the benzene of tower top, toluene and ethylbenzene enter second
Benzene column is separated benzene and toluene with ethylbenzene, and benzene and toluene enter back into benzene toluene tower and further separates.Crude styrene bottoms
Material enters refining benzene ethylene column, and styrene is separated with heavy constituent, and tower top obtains product styrene.Crude styrene tower adopts azeotropic section
Energy technology, i.e. overhead stream ethylbenzene and the condensation of water azeotropic mixture, the ethylbenzene and water after evaporation sends into ethylbenzene dehydrogenation unit and steam
The first dehydrogenation reactor is entered after the mixing of superheater outlet vapor.Due to ethylbenzene and the proportions constant of water azeotropic mixture, in total water hydrocarbon
In the case of constant, the quantity of steam of steam superheating outlet of still also cannot become, to reach certain reaction temperature, Zhi Nengti
The outlet temperature of high steam superheater is realizing.At present, the outlet temperature of the technology steam superheater is more than 900 DEG C,
Very big difficulty is brought to technological operation and engineering design.
TOTAL/Badger later technologies are also adopted by low water hydrocarbon ratio (1.0 or so), and phenyl ethylene rectification is using order essence
Evaporate technique, i.e., first separated benzene, toluene in benzene/methylbenzene tower with ethylbenzene and heavy constituent, ethylbenzene and heavy constituent enter ethylbenzene/
Styrene separating tower is further separated, and tower top obtains ethylbenzene, and tower base stream sends into refining benzene ethylene column, by styrene and heavy constituent point
From tower top obtains product styrene, and the technology styrene need to heat three times.Ethylbenzene/styrene separating tower is become using double tower
Pressure power-saving technology.
The content of the invention
The technical problem to be solved in the present invention is：A kind of solution under low water ratio (1.0 or so), if crude styrene tower is provided
Azeotropic distillation is adopted again, is greatly decreased will steam superheater steam flow, the problem of its outlet temperature too high (up to 900 DEG C).
Styrene production energy-saving device of the present invention, including crude styrene high-pressure tower and crude styrene lower pressure column, slightly
The upper feed inlet of styrene high-pressure tower and crude styrene lower pressure column connects respectively the discharging opening of Ethylbenzene hydrogen removal system by pipeline,
The bottom discharge mouth of crude styrene high-pressure tower and crude styrene lower pressure column is respectively communicated with refining benzene ethylene column, crude styrene high-pressure tower
Bottom connects high-pressure tower reboiler, the bottom connection lower pressure column reboiler of crude styrene lower pressure column, crude styrene high pressure column overhead
Ethylbenzene tower charging aperture, tower overhead gas efferent duct connection lower pressure column reboiler, crude styrene lower pressure column are connected by tower overhead gas efferent duct
Tower top connects lower pressure column condenser, and lower pressure column condensator outlet connects respectively with crude styrene low pressure column overhead, ethylbenzene tower charging aperture
It is logical, ethylbenzene column overhead connection ethylbenzene tower condenser, ethylbenzene tower condenser discharging opening respectively with ethylbenzene column overhead, ethylbenzene tower discharge nozzle
Connection, refining benzene ethylene column bottom of towe is tar pipe, and top connects refining benzene Ethylene Fractionator condenser.
The feeding mouth of described Ethylbenzene hydrogen removal system connects the outlet of steam superheater, the connection ethylbenzene dehydrogenation of ethylbenzene feeding pipe
System.
Ethylbenzene dehydrogenation technology of the present invention adopts low water hydrocarbon ratio (1.0 or so), phenyl ethylene rectification only to need using styrene
Heating rectification process twice, i.e., first separate ethylbenzene and styrene in crude styrene tower, and the benzene of tower top, toluene and ethylbenzene enter
Enter ethylbenzene tower to be separated benzene and toluene with ethylbenzene, benzene and toluene enter back into benzene toluene tower and further separates.Crude styrene tower
Substrate material enters phenyl ethylene rectification tower, and styrene is separated with heavy constituent, and tower top obtains product styrene.Crude styrene tower is adopted
Double tower coupling energy-saving technology, will a crude styrene tower be divided into two high-low pressure towers, the tower overhead gas of high-pressure tower is used as lower pressure column
Reboiler thermal source, both saved high-pressure tower overhead condenser circulation water consumption, lower pressure column reboiler steam consumption is saved again.
Energy-saving effect is notable, simultaneously because using ethylbenzene and water azeotropic vaporization technology, it is possible to reduce the content of water in ethylbenzene evaporation,
It is possibly realized the steam vapour amount in increasing steam superheater.Low water hydrocarbon ratio (1.0 or so) is adopted in ethylbenzene dehydrogenation technology
In the case of, the outlet temperature of steam superheater can be below 840 DEG C.Also make to be possibly realized using lower water ratio from now on.
The invention has the beneficial effects as follows：
Phenyl ethylene rectification need to only heat rectification process twice using styrene, and crude styrene tower adopts double tower coupling energy-saving
Technology, ethylbenzene and a small amount of water Jing waste heat exchangers are heated and vaporized, and compared with azeotropic, the water yield is greatly decreased.Therefore, in Zong Shui
Hydrocarbon is than in the case of constant, increasing steam superheater quantity of steam, to reduce steam superheating heater outlet temperature.
Description of the drawings
Fig. 1 is the structural representation of the present invention.
In figure：1st, steam superheater；2nd, Ethylbenzene hydrogen removal system；3rd, crude styrene high-pressure tower；4th, tower overhead gas efferent duct；5th, it is low
Pressure tower reboiler；6th, crude styrene lower pressure column；7th, lower pressure column condenser；8th, ethylbenzene tower；9th, ethylbenzene tower condenser；10th, refining benzene second
Alkene tower；11st, refining benzene Ethylene Fractionator condenser；12nd, high-pressure tower reboiler；13rd, ethylbenzene tower discharge nozzle.
Specific embodiment
The present invention is described further below in conjunction with the accompanying drawings：
As shown in figure 1, styrene production energy-saving device of the present invention, including crude styrene high-pressure tower 3 and crude benzol second
The upper feed inlet of alkene lower pressure column 6, crude styrene high-pressure tower 3 and crude styrene lower pressure column 6 connects ethylbenzene and takes off by pipeline respectively
The bottom discharge mouth of the discharging opening of hydrogen system 2, crude styrene high-pressure tower 3 and crude styrene lower pressure column 6 is respectively communicated with refining benzene ethene
Tower 10, the bottom of crude styrene high-pressure tower 3 connects high-pressure tower reboiler 12, the bottom connection lower pressure column of crude styrene lower pressure column 6
Reboiler 5, the tower top of crude styrene high-pressure tower 3 connects the charging aperture of ethylbenzene tower 8 by tower overhead gas efferent duct 4, and tower overhead gas efferent duct 4 connects
Logical lower pressure column reboiler 5, the tower top of crude styrene lower pressure column 6 connection lower pressure column condenser 7, lower pressure column condenser 7 export respectively with
Crude styrene low pressure column overhead, the connection of the charging aperture of ethylbenzene tower 8, the tower top of ethylbenzene tower 8 connection ethylbenzene tower condenser 9, ethylbenzene tower condensation
The discharging opening of device 9 is connected respectively with the tower top of ethylbenzene tower 8, ethylbenzene tower discharge nozzle 13, and the bottom of towe of refining benzene ethylene column 10 is tar pipe, and top connects
Logical refining benzene Ethylene Fractionator condenser 11.The feeding mouth of Ethylbenzene hydrogen removal system 2 connects the outlet of steam superheater 1, and ethylbenzene feeding pipe connects
Logical Ethylbenzene hydrogen removal system 2.
Crude styrene tower adopts double tower coupling energy-saving technology, will a crude styrene tower be divided into two high-low pressure towers, it is high
The tower overhead gas of pressure tower had both saved high-pressure tower overhead condenser circulation water consumption as the reboiler thermal source of lower pressure column, saved again
Lower pressure column reboiler 5 steam consumption.Energy-saving effect is notable, simultaneously because using ethylbenzene and water azeotropic vaporization technology, can
The content of water, is possibly realized the steam vapour amount in increasing steam superheater 1 in reduce ethylbenzene evaporation.In ethylbenzene dehydrogenation technique
, using in the case of low water hydrocarbon ratio (1.0 or so), the outlet temperature of steam superheater 1 can be below 840 DEG C for technology.Also the present is made
It is possibly realized using lower water ratio afterwards.
Claims (2)
1. a kind of styrene production energy-saving device, it is characterised in that：Including crude styrene high-pressure tower (3) and crude styrene lower pressure column
(6), the upper feed inlet of crude styrene high-pressure tower (3) and crude styrene lower pressure column (6) connects ethylbenzene dehydrogenation by pipeline respectively
The bottom discharge mouth of the discharging opening of system (2), crude styrene high-pressure tower (3) and crude styrene lower pressure column (6) is respectively communicated with refining benzene
Ethylene column (10), bottom connection high-pressure tower reboiler (12) of crude styrene high-pressure tower (3), the bottom of crude styrene lower pressure column (6)
Portion's connection lower pressure column reboiler (5), crude styrene high-pressure tower (3) tower top connects ethylbenzene tower (8) and enters by tower overhead gas efferent duct (4)
Material mouth, tower overhead gas efferent duct (4) connection lower pressure column reboiler (5), crude styrene lower pressure column (6) tower top connection lower pressure column condenser
(7), lower pressure column condenser (7) outlet is connected respectively with crude styrene low pressure column overhead, ethylbenzene tower charging aperture, ethylbenzene tower (8) tower
Top connection ethylbenzene tower condenser (9), ethylbenzene tower condenser (9) discharging opening respectively with ethylbenzene column overhead, ethylbenzene tower discharge nozzle (13)
Connection, refining benzene ethylene column (10) bottom of towe is tar pipe, and top connects refining benzene Ethylene Fractionator condenser (11).
2. styrene production energy-saving device according to claim 1, it is characterised in that：The pan feeding of Ethylbenzene hydrogen removal system (2)
The outlet of mouth connection steam superheater (1), ethylbenzene feeding pipe connection Ethylbenzene hydrogen removal system (2).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611069739.3A CN106631663B (en) | 2016-11-28 | 2016-11-28 | Energy-saving styrene production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611069739.3A CN106631663B (en) | 2016-11-28 | 2016-11-28 | Energy-saving styrene production device |
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| Publication Number | Publication Date |
|---|---|
| CN106631663A true CN106631663A (en) | 2017-05-10 |
| CN106631663B CN106631663B (en) | 2023-06-27 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201611069739.3A Active CN106631663B (en) | 2016-11-28 | 2016-11-28 | Energy-saving styrene production device |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115304446A (en) * | 2022-08-31 | 2022-11-08 | 连云港石化有限公司 | Process setting and operating technology of water combined transportation and cooking tower of styrene device |
| WO2023050988A1 (en) * | 2021-09-28 | 2023-04-06 | 常州瑞华化工工程技术股份有限公司 | Styrene refining method having combination of falling-film reboiler and heat pump technology to supply heat source required by separation column |
| RU2802428C1 (en) * | 2021-09-28 | 2023-08-28 | Чангжоу Руихуа Хемикал Энжинииринг Техноложи Ко., Лтд. | Method for styrene purification using combined action of falling film reboilers and heat pump technology to obtain a heat source for separating column |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1736961A (en) * | 2005-04-26 | 2006-02-22 | 蓝仁水 | Styrene separation process |
| CN102086409A (en) * | 2010-08-16 | 2011-06-08 | 中国海洋石油总公司 | Cracked gasoline high and low pressure thermal coupling separation technology |
| CN202951270U (en) * | 2012-12-14 | 2013-05-29 | 天津大学 | Variable-pressure heat integrated rectifying device for separating ethanol and methylbenzene |
| CN206375840U (en) * | 2016-11-28 | 2017-08-04 | 山东齐鲁石化工程有限公司 | Styrene production energy-saving device |
-
2016
- 2016-11-28 CN CN201611069739.3A patent/CN106631663B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1736961A (en) * | 2005-04-26 | 2006-02-22 | 蓝仁水 | Styrene separation process |
| CN102086409A (en) * | 2010-08-16 | 2011-06-08 | 中国海洋石油总公司 | Cracked gasoline high and low pressure thermal coupling separation technology |
| CN202951270U (en) * | 2012-12-14 | 2013-05-29 | 天津大学 | Variable-pressure heat integrated rectifying device for separating ethanol and methylbenzene |
| CN206375840U (en) * | 2016-11-28 | 2017-08-04 | 山东齐鲁石化工程有限公司 | Styrene production energy-saving device |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2023050988A1 (en) * | 2021-09-28 | 2023-04-06 | 常州瑞华化工工程技术股份有限公司 | Styrene refining method having combination of falling-film reboiler and heat pump technology to supply heat source required by separation column |
| RU2802428C1 (en) * | 2021-09-28 | 2023-08-28 | Чангжоу Руихуа Хемикал Энжинииринг Техноложи Ко., Лтд. | Method for styrene purification using combined action of falling film reboilers and heat pump technology to obtain a heat source for separating column |
| CN115304446A (en) * | 2022-08-31 | 2022-11-08 | 连云港石化有限公司 | Process setting and operating technology of water combined transportation and cooking tower of styrene device |
| CN115304446B (en) * | 2022-08-31 | 2023-11-03 | 连云港石化有限公司 | Flow setting of styrene device water intermodal transportation and digestion tower |
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| Publication number | Publication date |
|---|---|
| CN106631663B (en) | 2023-06-27 |
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