CN204097366U - Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system - Google Patents
Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system Download PDFInfo
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- CN204097366U CN204097366U CN201420567897.1U CN201420567897U CN204097366U CN 204097366 U CN204097366 U CN 204097366U CN 201420567897 U CN201420567897 U CN 201420567897U CN 204097366 U CN204097366 U CN 204097366U
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- dehydrogenation reactor
- dehydrogenation
- ethylbenzene
- waste heat
- heat boiler
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Abstract
The utility model relates to vinylbenzene industrial installation reactive system, be specifically related to a kind of ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system, comprise first dehydrogenation reactor of being connected successively by pipeline, resuperheater, second dehydrogenation reactor, first ethylbenzene superheater, second ethylbenzene superheater, Low Pressure Waste Heat Boiler and low Low Pressure Waste Heat Boiler, first dehydrogenation reactor, resuperheater and the second dehydrogenation reactor, first ethylbenzene superheater is that Π type connects, second dehydrogenation reactor, first ethylbenzene superheater and the second ethylbenzene superheater, Low Pressure Waste Heat Boiler, low Low Pressure Waste Heat Boiler becomes U-shaped connection, this system have modified the layout height of two dehydrogenation reactors and reheater, reduce the pressure drop of reactive system, solve ethylbenzene superheater leakage problem, saved the use of high temperature tubing simultaneously.
Description
Technical field
The utility model relates to vinylbenzene industrial installation reactive system, is specifically related to a kind of ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system.
Background technology
Styrene monomer is important basic organic chemical industry raw material, be widely used in and produce polystyrene, styrofoam, ABS and SAN resin etc., the vinylbenzene overwhelming majority is all obtained by ethylbenzene dehydrogenation production technique, and its Technology mainly contains adiabatic dehydrogenation technique, isothermal dehydrogenating technology and oxidative dehydrogenation process.Wherein the most ripe and most widely used be negative pressure adiabatic dehydrogenation technique.
It is a heat absorption increasing molecule reversible reaction by force that ethylbenzene dehydrogenation generates vinylbenzene, high temperature and low pressure are conducive to this reversible reaction and carry out towards the cinnamic direction of generation, and this adiabatic radial reactor system of two-stage series connection negative pressure just with inter-stage second-heating obtains the reason place of generally applying in ethyl benzene dehydrogenation preparation of styrene industrial production.Intermediate heat is provided with between the reactor of this reactor assembly two series connection, available high-temperature steam carries out second time heating to carrying out adiabatic dehydrogenation reacting rear material in the first dehydrogenation reactor, material is heated up, and enter the second dehydrogenation reactor, proceed adiabatic dehydrogenation reaction, thus charging ethylbenzene can realize higher transformation efficiency.
As mentioned above, this have the advantage of the two-stage series connection reactor negative pressure adiabatic dehydrogenation reactive system of inter-stage second-heating need not query, but face two technical problems: one is how reasonably the high-temperature reactor discharging being in negative pressure to be cooled down thereupon, and by its heat recovery and utilization, to reduce the comprehensive energy consumption of product; Two is how to be used in reclaim high-temperature reactor discharging heat and make it the type selecting of heat-exchange equipment that cools and layout meets high-level efficiency and low pressure drop requirement, the negative pressure operating mode of realization response system better.
For above-mentioned two technical problems, current ethyl benzene dehydrogenation preparation of styrene full scale plant generally adopts unitized exchanger to reclaim the heat of high-temperature reactor discharging, makes it rapid cooling.
What Lummus company adopted is the horizontal combination exchanger of " one " font, as shown in Figure 2, flow sequence is that reaction mass enters the first dehydrogenation reactor from bottom to top, then material enters the second dehydrogenation reactor from top-side discharging, the second dehydrogenation reactor is entered from top to bottom after being arranged on the heating of inner reheater, then enter horizontal three interchanger from bottom sides discharging, then enter downstream and be arranged on high-order air cooler or water cooling.The high temperature section ethylbenzene superheater that the horizontal combination exchanger of " one " font exists easily damages, the second dehydrogenation reactor sidewall discharging shock resistance is large, and make its internal flow produce the defects such as bias current, three heat exchanger exits are positioned at low level, must to upper connecting tube to the air cooler in downstream or water cooler, increase system pipeline length, increase systemic resistance.
The decoration form that China Petrochemical Industry's technology adopts as shown in Figure 3, flow sequence is that reaction mass enters the first dehydrogenation reactor from bottom to top, then material enters the second dehydrogenation reactor from top discharge from top to bottom by one section of pipeline, then discharging from the side enters ethylbenzene superheater, then enter bigeminy heat exchanger package, then enter downstream and be arranged on high-order air cooler or water cooler.Flow arrangement adopts " L " type combination exchanger, although solve horizontal superheater to hold flimsy problem, it is large equally to there is the second dehydrogenation reactor sidewall discharging shock resistance in this arrangement form, and make its internal flow produce the defects such as bias current, and in order to connect the first dehydrogenation reactor and the second dehydrogenation reactor, first dehydrogenation reactor outlet must increase the pipeline being about 8 meters, same bigeminy heat exchanger exit is positioned at low level, must to upper connecting tube to the air cooler in downstream or water cooler, increase system pipeline length, increase systemic resistance.
Badger company adopt be decoration form as shown in Figure 4, flow sequence is that reaction mass enters the first dehydrogenation reactor from top to bottom, then three equipment are entered from top to bottom by pipeline from bottom to top again by resuperheater and the second dehydrogenation reactor, from three device bottom dischargings, then enter downstream and be arranged on high-order air cooler or water cooler.Must increase the pipeline of about about 12 meters to connect the second dehydrogenation reactor and three equipment, same three heat exchanger exits are positioned at low level, to upper connecting tube to the air cooler in downstream or water cooler, must increase system pipeline length, increase systemic resistance.
Utility model content
According to above deficiency of the prior art, the technical problems to be solved in the utility model is: provide a kind of ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system, reduces reactive system pressure drop, solves ethylbenzene superheater leakage problem, saves the use of high temperature tubing simultaneously.
Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system described in the utility model, comprise first dehydrogenation reactor of being connected successively by pipeline, resuperheater, second dehydrogenation reactor, first ethylbenzene superheater, second ethylbenzene superheater, Low Pressure Waste Heat Boiler and low Low Pressure Waste Heat Boiler, first dehydrogenation reactor, resuperheater and the second dehydrogenation reactor, first ethylbenzene superheater is that Π type connects, first dehydrogenation reactor, resuperheater is positioned at Π type and connects side, second dehydrogenation reactor, first ethylbenzene superheater is positioned at Π type and connects opposite side, second dehydrogenation reactor, first ethylbenzene superheater and the second ethylbenzene superheater, Low Pressure Waste Heat Boiler, low Low Pressure Waste Heat Boiler becomes U-shaped connection, second dehydrogenation reactor, first ethylbenzene superheater is positioned at U-shaped connection side, second ethylbenzene superheater, Low Pressure Waste Heat Boiler, low Low Pressure Waste Heat Boiler is positioned at U-shaped connection opposite side, the first described dehydrogenation reactor is provided with air inlet mixer, and low Low Pressure Waste Heat Boiler is provided with discharge pipe.
This system architecture is compact, has saved the use of high temperature tubing, have modified two dehydrogenation reactors and the highly unmatched problem of reheater layout, and reduces reactive system pressure drop, solve the problem that two ethylbenzene superheaters leak.
Resuperheater during described Π type connects is connected by expansion joint with the second dehydrogenation reactor.
The first ethylbenzene superheater in described U-shaped connection is connected by expansion joint with the second ethylbenzene superheater.
Principle of work and process:
By main steam and the mixed gas that merges through overheated vaporization ethylbenzene raw material, the first dehydrogenation reactor is entered from bottom to top by air inlet mixer, there is the chemical reactions such as ethylbenzene dehydrogenation and lower the temperature, enter resuperheater, again heat up with the superheated vapour indirect heat exchange in resuperheater, enter the second dehydrogenation reactor, again lower the temperature after there is the chemical reactions such as ethylbenzene dehydrogenation, reaction mass enters the first ethylbenzene superheater from top to bottom, then the second ethylbenzene superheater is entered from bottom to top by band expansion joint pipeline, reaction mass temperature is reduced, again successively through Low Pressure Waste Heat Boiler, low Low Pressure Waste Heat Boiler, reaction mass is lowered the temperature by the low-pressure steam of output and low low-pressure steam respectively, then delivery of steam is to downstream steam pipe network system, reclaim the heat of pyroreaction discharging, reaction mass is exported by discharge pipe.
The beneficial effect that the utility model is compared with prior art had is: ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system, have modified the layout height of two dehydrogenation reactors and reheater, reduce the pressure drop of reactive system, solve ethylbenzene superheater leakage problem, save the use of high temperature tubing simultaneously.
Accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
Fig. 2 is Lummus typical case ethyl benzene dehydrogenation preparation of styrene device schematic diagram;
Tu3Shi China Petrochemical Industry typical case ethyl benzene dehydrogenation preparation of styrene device schematic diagram;
Fig. 4 is Badger typical case ethyl benzene dehydrogenation preparation of styrene device schematic diagram.
In figure: 1, the first dehydrogenation reactor; 2, resuperheater; 3, the second dehydrogenation reactor; 4, discharge pipe; 5, low Low Pressure Waste Heat Boiler; 6, the first ethylbenzene superheater; 7, Low Pressure Waste Heat Boiler; 8, the second ethylbenzene superheater; 9, air inlet mixer.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described further:
As shown in Figure 1, ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system, comprise first dehydrogenation reactor 1 of being connected successively by pipeline, resuperheater 2, second dehydrogenation reactor 3, first ethylbenzene superheater 6, second ethylbenzene superheater 8, Low Pressure Waste Heat Boiler 7 and low Low Pressure Waste Heat Boiler 5, first dehydrogenation reactor 1, resuperheater 2 and the second dehydrogenation reactor 3, first ethylbenzene superheater 6 connects in Π type, first dehydrogenation reactor 1, resuperheater 2 is positioned at Π type and connects side, second dehydrogenation reactor 3, first ethylbenzene superheater 6 is positioned at Π type and connects opposite side, second dehydrogenation reactor 3, first ethylbenzene superheater 6 and the second ethylbenzene superheater 8, Low Pressure Waste Heat Boiler 7, the U-shaped connection of low Low Pressure Waste Heat Boiler 5 one-tenth, second dehydrogenation reactor 3, first ethylbenzene superheater 6 is positioned at U-shaped connection side, second ethylbenzene superheater 8, Low Pressure Waste Heat Boiler 7, low Low Pressure Waste Heat Boiler 5 is positioned at U-shaped connection opposite side, first dehydrogenation reactor 1 is provided with air inlet mixer 9, and low Low Pressure Waste Heat Boiler 5 is provided with discharge pipe 4.
Resuperheater 2 during Π type connects is connected by expansion joint with the second dehydrogenation reactor 3.
The first ethylbenzene superheater 6 in U-shaped connection is connected by expansion joint with the second ethylbenzene superheater 8.
By main steam and the mixed gas that merges through overheated vaporization ethylbenzene raw material, temperature is 580 DEG C ~ 650 DEG C, pressure is 60 ~ 120kPaA, the first dehydrogenation reactor 1 is entered from bottom to top by air inlet mixer 9, radial direction is diverted through beds circlewise, there is the chemical reactions such as ethylbenzene dehydrogenation and be cooled to 500 DEG C ~ 560 DEG C, enter resuperheater 2, again 580 DEG C ~ 650 DEG C are warming up to the superheated vapour indirect heat exchange in resuperheater 2, enter the second dehydrogenation reactor 3, outer shroud runner radial direction along the second dehydrogenation reactor 3 is diverted through beds circlewise, 500 DEG C ~ 560 DEG C are again cooled to after there is the chemical reactions such as ethylbenzene dehydrogenation, reaction mass enters the first ethylbenzene superheater 6 from top to bottom, then the second ethylbenzene superheater 8 is entered from bottom to top by band expansion joint pipeline, by vaporization ethylbenzene and water be superheated to 450 DEG C ~ 550 DEG C, reaction mass temperature is reduced to 330 DEG C ~ 400 DEG C, again successively through Low Pressure Waste Heat Boiler 7, low Low Pressure Waste Heat Boiler 5, reaction mass is reduced to 110 DEG C ~ 140 DEG C by the low-pressure steam of output and low low-pressure steam respectively, then delivering vapor is to downstream steam pipe network system, reclaim the heat of pyroreaction material, reaction mass is exported by discharge pipe 4.
This system architecture is compact, has saved the use of high temperature tubing, have modified two dehydrogenation reactors and the highly unmatched problem of reheater layout, and reduces reactive system pressure drop, solve the problem that two ethylbenzene superheaters leak.
Claims (3)
1. ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system, is characterized in that: comprise first dehydrogenation reactor (1) of being connected successively by pipeline, resuperheater (2), second dehydrogenation reactor (3), first ethylbenzene superheater (6), second ethylbenzene superheater (8), Low Pressure Waste Heat Boiler (7) and low Low Pressure Waste Heat Boiler (5), the first dehydrogenation reactor (1), resuperheater (2) and the second dehydrogenation reactor (3), first ethylbenzene superheater (6) connects in Π type, the first dehydrogenation reactor (1), resuperheater (2) is positioned at Π type and connects side, the second dehydrogenation reactor (3), first ethylbenzene superheater (6) is positioned at Π type and connects opposite side, the second dehydrogenation reactor (3), first ethylbenzene superheater (6) and the second ethylbenzene superheater (8), Low Pressure Waste Heat Boiler (7), low Low Pressure Waste Heat Boiler (5) becomes U-shaped connection, the second dehydrogenation reactor (3), first ethylbenzene superheater (6) is positioned at U-shaped connection side, the second ethylbenzene superheater (8), Low Pressure Waste Heat Boiler (7), low Low Pressure Waste Heat Boiler (5) is positioned at U-shaped connection opposite side, described the first dehydrogenation reactor (1) is provided with air inlet mixer (9), and low Low Pressure Waste Heat Boiler (5) is provided with discharge pipe (4).
2. ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system according to claim 1, is characterized in that: the resuperheater (2) during described Π type connects is connected by expansion joint with the second dehydrogenation reactor (3).
3. ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system according to claim 1 and 2, is characterized in that: the first ethylbenzene superheater (6) in described U-shaped connection is connected by expansion joint with the second ethylbenzene superheater (8).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420567897.1U CN204097366U (en) | 2014-09-29 | 2014-09-29 | Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420567897.1U CN204097366U (en) | 2014-09-29 | 2014-09-29 | Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system |
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| CN204097366U true CN204097366U (en) | 2015-01-14 |
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| CN201420567897.1U Withdrawn - After Issue CN204097366U (en) | 2014-09-29 | 2014-09-29 | Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104230616A (en) * | 2014-09-29 | 2014-12-24 | 山东齐鲁石化工程有限公司 | Dehydrogenation reaction system for conducting ethylbenzene dehydrogenation to prepare styrene |
| CN109180412A (en) * | 2018-09-29 | 2019-01-11 | 狄风君 | A kind of chemicals production technology optimization method |
| CN115452306A (en) * | 2022-09-23 | 2022-12-09 | 中国空气动力研究与发展中心超高速空气动力研究所 | Two-stage series heat accumulating type heater and use method thereof |
-
2014
- 2014-09-29 CN CN201420567897.1U patent/CN204097366U/en not_active Withdrawn - After Issue
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104230616A (en) * | 2014-09-29 | 2014-12-24 | 山东齐鲁石化工程有限公司 | Dehydrogenation reaction system for conducting ethylbenzene dehydrogenation to prepare styrene |
| CN104230616B (en) * | 2014-09-29 | 2016-06-08 | 山东齐鲁石化工程有限公司 | Ethyl benzene dehydrogenation preparation of styrene dehydrogenation reactor system |
| CN109180412A (en) * | 2018-09-29 | 2019-01-11 | 狄风君 | A kind of chemicals production technology optimization method |
| CN109180412B (en) * | 2018-09-29 | 2021-09-03 | 安徽昊源化工集团有限公司 | Chemical product production process optimization method |
| CN115452306A (en) * | 2022-09-23 | 2022-12-09 | 中国空气动力研究与发展中心超高速空气动力研究所 | Two-stage series heat accumulating type heater and use method thereof |
| CN115452306B (en) * | 2022-09-23 | 2024-03-29 | 中国空气动力研究与发展中心超高速空气动力研究所 | Two-stage series heat accumulating type heater and application method thereof |
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| Date | Code | Title | Description |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20150114 Effective date of abandoning: 20160608 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |