CN106631663B - Energy-saving styrene production device - Google Patents
Energy-saving styrene production device Download PDFInfo
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- CN106631663B CN106631663B CN201611069739.3A CN201611069739A CN106631663B CN 106631663 B CN106631663 B CN 106631663B CN 201611069739 A CN201611069739 A CN 201611069739A CN 106631663 B CN106631663 B CN 106631663B
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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
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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
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- 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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Abstract
The invention is mainly applied to the technical field of styrene production, and particularly relates to an energy-saving styrene production device which comprises a high-pressure crude styrene tower, wherein upper feed inlets of the high-pressure crude styrene tower and the low-pressure crude styrene tower are respectively connected with discharge outlets of an ethylbenzene dehydrogenation system through pipelines, bottom discharge outlets of the high-pressure crude styrene tower and the low-pressure crude styrene tower are respectively communicated with a refined styrene tower, the bottom of the low-pressure crude styrene tower is communicated with a reboiler of the low-pressure crude styrene tower, the top of the high-pressure crude styrene tower is communicated with a feed inlet of an ethylbenzene tower through a top gas output pipe, the top of the top gas output pipe of the top gas is communicated with a reboiler of the low-pressure crude styrene tower, the top of the crude styrene low-pressure tower is communicated with a condenser of the low-pressure ethylbenzene tower, the top of the ethylbenzene tower is communicated with a condenser of the ethylbenzene tower, the bottom of the refined styrene tower is a tar pipe, and the top of the refined styrene tower is communicated with the condenser of the refined styrene tower. The invention can increase the steam quantity of the steam superheating furnace under the condition of unchanged total water-hydrocarbon ratio so as to reduce the outlet temperature of the steam superheating furnace.
Description
Technical Field
The invention relates to an energy-saving styrene production device which is mainly applied to the technical field of styrene production.
Background
Currently, the most advanced international ethylbenzene dehydrogenation production process is the Lummus and TOTAL/Badger adiabatic dehydrogenation technology, and the two processes are quite similar and have characteristics.
The latest technology of Lummes adopts a rectification technology that styrene is rectified by adopting a low water-hydrocarbon ratio (about 1.0) and only needs to be heated twice, namely, ethylbenzene and styrene are separated in a crude styrene tower, benzene, toluene and ethylbenzene at the top of the tower enter an ethylbenzene tower to separate benzene and toluene from ethylbenzene, and benzene and toluene enter a benzene toluene tower to be further separated. And (3) feeding the crude styrene tower bottom material into a refined styrene tower, separating styrene from heavy components, and obtaining the product styrene at the tower top. The crude styrene tower adopts azeotropic energy-saving technology, namely, the top stream is condensed by using an azeotropic mixture of ethylbenzene and water, and the vaporized ethylbenzene and water are sent to an ethylbenzene dehydrogenation unit to be mixed with steam at the outlet of a steam superheating furnace and then enter a first dehydrogenation reactor. Because the ratio of ethylbenzene to water azeotrope is constant, the steam quantity at the outlet of the steam superheating furnace cannot be changed under the condition of constant total water-hydrocarbon ratio, and the aim of achieving a certain reaction temperature can only be achieved by increasing the outlet temperature of the steam superheating furnace. At present, the outlet temperature of the steam superheating furnace of the process technology is above 900 ℃, which brings great difficulty to process operation and engineering design.
The latest technology of TOTAL/Badger adopts low water-hydrocarbon ratio (about 1.0), styrene rectification adopts sequential rectification technology, namely benzene, toluene, ethylbenzene and heavy components are separated in a benzene/toluene tower, the ethylbenzene and the heavy components are further separated in an ethylbenzene/styrene separation tower, ethylbenzene is obtained at the tower top, a tower bottom material flow is sent into a refined styrene tower, styrene and the heavy components are separated at the tower top, and the styrene is obtained at the tower top, and the technology of styrene needs to be heated for three times. The ethylbenzene/styrene separation tower adopts a double-tower pressure-changing energy-saving technology.
Disclosure of Invention
The invention aims to solve the technical problems that: to provide a method for solving the problem that the steam flow of a steam superheating furnace is greatly reduced and the outlet temperature is too high (up to 900 ℃) when azeotropic rectification is adopted again for a crude styrene tower under the condition of low water ratio (about 1.0).
The invention relates to an energy-saving styrene production device, which comprises a crude styrene high-pressure tower and a crude styrene low-pressure tower, wherein upper feed inlets of the crude styrene high-pressure tower and the crude styrene low-pressure tower are respectively connected with discharge ports of an ethylbenzene dehydrogenation system through pipelines, bottom discharge ports of the crude styrene high-pressure tower and the crude styrene low-pressure tower are respectively communicated with a refined styrene tower, the bottom of the crude styrene high-pressure tower is communicated with a high-pressure tower reboiler, the bottom of the crude styrene low-pressure tower is communicated with a low-pressure tower reboiler, the top of the crude styrene high-pressure tower is communicated with an ethylbenzene tower feed port through a tower top gas output pipe, the tower top gas output pipe is communicated with a low-pressure tower reboiler, the top of the crude styrene low-pressure tower is communicated with a low-pressure tower condenser, outlets of the low-pressure tower condenser are respectively communicated with the top of the crude styrene low-pressure tower and the ethylbenzene tower feed ports, the top of the ethylbenzene tower is communicated with a refined styrene tower, the top of the ethylbenzene tower is a tar pipe, and the top of the refined styrene tower is communicated with the refined styrene tower condenser.
And a feed inlet of the ethylbenzene dehydrogenation system is communicated with an outlet of the steam superheating furnace, and an ethylbenzene feed pipe is communicated with the ethylbenzene dehydrogenation system.
The ethylbenzene dehydrogenation process adopts a rectification process that styrene is heated twice only by adopting low water-hydrocarbon ratio (about 1.0), namely ethylbenzene and styrene are separated in a crude styrene tower, benzene, toluene and ethylbenzene at the top of the tower enter an ethylbenzene tower to separate benzene, toluene and ethylbenzene, and benzene and toluene enter a benzene toluene tower to be further separated. And (3) feeding the crude styrene tower bottom material into a styrene rectifying tower, separating the styrene from heavy components, and obtaining the product styrene at the tower top. The crude styrene tower adopts a double-tower coupling energy-saving technology, namely one crude styrene tower is divided into two high-pressure and low-pressure towers, and the top gas of the high-pressure tower is used as a reboiler heat source of the low-pressure tower, so that the consumption of circulating water of a condenser at the top of the high-pressure tower is saved, and the consumption of steam of a reboiler of the low-pressure tower is also saved. The energy-saving effect is remarkable, and the water content in ethylbenzene evaporation can be reduced because the azeotropic evaporation technology of ethylbenzene and water is not adopted, so that the water vapor amount in the steam superheating furnace is increased. In the case of ethylbenzene dehydrogenation technology using a low water to hydrocarbon ratio (about 1.0), the outlet temperature of the steam superheating furnace may be below 840 ℃. It will also become possible to use lower water ratios in the future.
The beneficial effects of the invention are as follows:
the rectification of styrene adopts a rectification process that styrene only needs to be heated twice, a double-tower coupling energy-saving technology is adopted in a crude styrene tower, ethylbenzene and a small amount of water are heated and vaporized by a waste heat exchanger, and compared with the azeotropic process, the water quantity is greatly reduced. Therefore, the steam amount of the steam superheating furnace can be increased under the condition that the total water-hydrocarbon ratio is unchanged, so that the outlet temperature of the steam superheating furnace can be reduced.
Drawings
Fig. 1 is a schematic structural view of the present invention.
In the figure: 1. a steam superheating furnace; 2. an ethylbenzene dehydrogenation system; 3. a crude styrene higher pressure column; 4. a top gas outlet pipe; 5. a low pressure column reboiler; 6. a crude styrene low pressure column; 7. a low pressure column condenser; 8. an ethylbenzene column; 9. an ethylbenzene column condenser; 10. a refined styrene column; 11. a refined styrene column condenser; 12. a high pressure column reboiler; 13. and a discharging pipe of the ethylbenzene tower.
Detailed Description
The invention is further described below with reference to the accompanying drawings:
as shown in figure 1, the energy-saving styrene production device comprises a high-pressure crude styrene tower 3 and a low-pressure crude styrene tower 6, wherein upper feed inlets of the high-pressure crude styrene tower 3 and the low-pressure crude styrene tower 6 are respectively connected with discharge ports of an ethylbenzene dehydrogenation system 2 through pipelines, bottom discharge ports of the high-pressure crude styrene tower 3 and the low-pressure crude styrene tower 6 are respectively communicated with a refined styrene tower 10, the bottom of the high-pressure crude styrene tower 3 is communicated with a high-pressure tower reboiler 12, the bottom of the low-pressure crude styrene tower 6 is communicated with a low-pressure tower reboiler 5, the top of the high-pressure crude styrene tower 3 is communicated with a feed port of an ethylbenzene tower 8 through a top gas output pipe 4, the top gas output pipe 4 is communicated with a low-pressure tower reboiler 5, the top of the low-pressure crude styrene tower 6 is communicated with a feed port of the ethylbenzene tower 8, the outlet of the low-pressure tower condenser 7 is respectively communicated with the top of the ethylbenzene tower 8, the bottom of the ethylbenzene tower 8 is communicated with a discharge pipe 13, and the top of the refined styrene tower 10 is communicated with the top of the refined styrene tower 11. The feed inlet of the ethylbenzene dehydrogenation system 2 is communicated with the outlet of the steam superheating furnace 1, and the ethylbenzene feed pipe is communicated with the ethylbenzene dehydrogenation system 2.
The crude styrene tower adopts a double-tower coupling energy-saving technology, namely one crude styrene tower is divided into two high-pressure and low-pressure towers, and the top gas of the high-pressure tower is used as a reboiler heat source of the low-pressure tower, so that the consumption of circulating water of a condenser at the top of the high-pressure tower is saved, and the consumption of steam of a reboiler 5 of the low-pressure tower is also saved. The energy-saving effect is remarkable, and the water content in ethylbenzene evaporation can be reduced because the azeotropic evaporation technology of ethylbenzene and water is not adopted, so that the water vapor amount in the steam superheating furnace 1 is increased. In the case of ethylbenzene dehydrogenation process technology using a low water to hydrocarbon ratio (about 1.0), the outlet temperature of the steam superheating furnace 1 may be 840 ℃ or lower. It will also become possible to use lower water ratios in the future.
Claims (1)
1. An energy-conserving apparatus for producing of styrene, its characterized in that: the high-pressure crude styrene tower (3) and the low-pressure crude styrene tower (6) are included, upper feed inlets of the high-pressure crude styrene tower (3) and the low-pressure crude styrene tower (6) are respectively connected with discharge outlets of an ethylbenzene dehydrogenation system (2) through pipelines, bottom discharge outlets of the high-pressure crude styrene tower (3) and the low-pressure crude styrene tower (6) are respectively communicated with a refined styrene tower (10), the bottom of the high-pressure crude styrene tower (3) is communicated with a high-pressure tower reboiler (12), the bottom of the low-pressure crude styrene tower (6) is communicated with a low-pressure tower reboiler (5), the top of the high-pressure crude styrene tower (3) is communicated with a feed inlet of an ethylbenzene tower (8) through a top gas output pipe (4), the top gas output pipe (4) is communicated with the low-pressure tower reboiler (5), the bottom of the low-pressure crude styrene tower (6) is communicated with a ethylbenzene condenser (7), outlets of the low-pressure styrene tower (7) are respectively communicated with the top of the high-pressure crude styrene tower, the top of the ethylbenzene tower (8) is communicated with a top of the ethylbenzene condenser (9), the top of the ethylbenzene tower (9) is communicated with the top of the refined styrene tower (Jiao Youguan), and the top of the ethylbenzene (52) is communicated with the top of the refined styrene tower (11);
the feed inlet of the ethylbenzene dehydrogenation system (2) is communicated with the outlet of the steam superheating furnace (1), and the ethylbenzene feed pipe is communicated with the ethylbenzene dehydrogenation 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 |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201611069739.3A CN106631663B (en) | 2016-11-28 | 2016-11-28 | Energy-saving styrene production device |
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| CN106631663A CN106631663A (en) | 2017-05-10 |
| CN106631663B true CN106631663B (en) | 2023-06-27 |
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| CN201611069739.3A Active CN106631663B (en) | 2016-11-28 | 2016-11-28 | Energy-saving styrene production device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN113877227B (en) * | 2021-09-28 | 2022-09-30 | 常州瑞华化工工程技术股份有限公司 | Styrene refining method for providing heat source required by separation tower through combination of falling film reboiler and heat pump technology |
| 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 |
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 |
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| CN106631663A (en) | 2017-05-10 |
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