CN1450037A - Tail gas absorption method for preparing styrene by ethylbenzene dehrogenation - Google Patents
Tail gas absorption method for preparing styrene by ethylbenzene dehrogenation Download PDFInfo
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- CN1450037A CN1450037A CN 02111313 CN02111313A CN1450037A CN 1450037 A CN1450037 A CN 1450037A CN 02111313 CN02111313 CN 02111313 CN 02111313 A CN02111313 A CN 02111313A CN 1450037 A CN1450037 A CN 1450037A
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- ethylbenzene
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Abstract
The present invention relates to a method for absorbing tail gas produced by dehydrogenation of ethylbenzene to prepare styrene, and is aimed at mainly resolving the problems of absorption of dehydrogenation tail gas and low recovery of aromatic hydrocarbon in the dehydrogenation tail gas in the existent industrial production equipment. Said invented technical scheme can adopt the following measures: the dehydrogenation tail gas can be fed from lower portion of tail gas absorption tower, and the absorbent can be fed from upper portion of tail gas absorption tower, in which the dehydrogenation tail gas feeding temp. is 15-48 deg.C, and the absorbent feeding temp. is 5-20 deg.C, and the tower top pressure of the tail gas absorption tower is 125-225 KPa, so that it can better resolve the above-mentioned problems.
Description
Technical field
The present invention relates to a kind of tail gas absorption method of ethyl benzene dehydrogenation preparation of styrene.
Background technology
Vinylbenzene is widely used as production various kinds of resin, plastics and elastomeric raw material, extensively mainly being easy to polymerization (for example generating polystyrene) owing to vinylbenzene or carrying out the adaptability of copolymerization (for example producing rubber with butadiene copolymer) of its range of application.
Cinnamic production with regard to various catalyzer used in dehydrogenating technology and this technology, is all known.Main goal in research is to improve the benefit of this technology at present.Be known that the processing method of ethylbenzene dehydrogenation especially, wherein dehydrogenation is overlapped in the device that comprises two placed in-line dehydrogenation reactors and two reactor intermediary well heaters at least one and is carried out.The operational condition that this technology adopted is that the same 1 mole of ethylbenzene of 3 to 10 moles steam is mixed, and the ingress temperature and pressure of first reactor is respectively 550～680 ℃ and 0.04～0.1MPa (absolute pressure).The temperature and pressure condition at first reactor effluent, second reactor inlet place after side heater is with steam heating is respectively 550～680 ℃ and 0.02～0.08MPa (absolute pressure), and total air speed of ethylbenzene is equal to or greater than 0.15 hour
-1Total air speed of ethylbenzene is meant the ratio of the volumetric flow rate of ethylbenzene with the cumulative volume of catalyzer.By this technology, conversion of ethylbenzene is approximately greater than 65～75%, even higher, and reaches the mole selectivity greater than 94%.But after after a while, this technology can cause the reduction of conversion of ethylbenzene, but this reduction can be remedied through improving temperature of reaction.In fact, it is aging gradually to observe catalyzer after after a while, occurs carbon laydown on catalyzer.This is because the shortcoming that this working system (especially in middle heating unit) exists causes thermal degradation reaction, can produce heavy compounds.It is calculated that the ratio of formed heavy product is about 17000PPm in effusive hydrocarbon polymer per ton, even more.As a result, cause that thus loss of material increases, catalyst efficiency reduces, thereby need clean continually.In order to eliminate the shortcoming of this technology, a kind of process for manufacturing styrene is disclosed among the document CN1006061B.Or rather, it is a kind of processing method through producing phenyl ethylene by ethyl benzene catalytic dehydrogenation.By this method, dehydrogenation comprises in three placed in-line fixed bed dehydrogenation reactors at a cover carries out, and settles one or more heating units between reactor.In well heater, reaction effluent and vapor generation heat exchange and be heated, steam is used for the reacting by heating effluent in the fs, mixes with ethylbenzene in the first dehydrogenation reactor ingress in subordinate phase.According to this invention, this processing method is characterised in that:
Ethylbenzene with steam with steam: ethylbenzene is that the molar ratio between 5: 1 and 13: 1 mixes, in the ingress of above-mentioned each reactor with the temperature of mixture heating up to 580 between to 645 ℃.Mean pressure in first reactor is with absolute manometer, and between 0.06～0.1MPa, in the second and the 3rd reactor, pressure remains between 0.04～0.07MPa with absolute manometer, and the total air speed of ethylbenzene was at 0.20 and 0.35 hour simultaneously
-1Between.
The high-temperature gas resultant that above-mentioned reactor is discharged reclaims heat through cooling condensation step by step, and the technology lime set (dehydrogenation liquid and water) that enters the downstream handles and two systems of vent gas treatment further process.
The technology lime set is handled and the effect of two systems of vent gas treatment is to make the resultant of dehydrogenation reaction realize separating with water and tail gas, and makes dehydrogenation reactor system be in the negative pressure operating mode.The major equipment of wherein dehydrogenation lime set and stripping system is stripping tower and water-and-oil separator (gravity separator of dehydrogenation liquid and water), and their function is to realize separating of water and hydro carbons, obtains dehydrogenation liquid.Exhaust treatment system comprises the tail gas compression and absorbs that major equipment has tail-gas compressor, tail gas absorber and desorption tower etc.Their function is to reclaim hydrogen and hydro carbons in the reaction product, and makes dehydrogenation reactor system form the negative-pressure operation condition.
The compressor suction tank that the logistics that the non-condensable gases of being collected by technology lime set treatment system (tail gas) merges into enters system is aspirated by tail-gas compressor, compressed boosting, and the vapour-liquid two-phase logistics of discharge enters the compressor drain tank, realizes gas-liquid separation.Enter the exhaust gas cooler shell side from the logistics of compressor drain tank tank deck expellant gas, the condensation that is cooled with the water coolant heat exchange of tube side, the expellant gas stream portions enters tail gas absorber.The logistics that enters tail gas absorber is main hydrogen, methane, carbonic acid gas, benzene, toluene, ethylbenzene, vinylbenzene, non-aromatic and vapour mixture that water is formed.The operating procedure on present industrial absorption tower is as follows: the absorption tower of adopting filling-material structure, the about 43KPa of cat head working pressure, about 38 ℃ of operation feeding temperature, about 38 ℃ of absorption agent temperature, the about 53KPa of working pressure at the bottom of the tower, service temperature is about 46 ℃ at the bottom of the tower, in 70,000 tons of/year vinylbenzene full scale plants, after tail gas absorber absorbed, aromaticity content was about 30 kilograms/hour in the tail gas, and aromatic recovery rate is about 85.5% in the dehydrogenated tail gas.
Introduce a kind of phenyl ethylene rectification technology in the document U.S. Pat 4615769, be mainly the power-saving technology in ethylbenzene, the vinylbenzene separation, do not related to the problems such as absorption of dehydrogenated tail gas.A kind of ethylbenzene and cinnamic separating technology have been introduced in the document U.S. Pat 5386075.In this technology, be mainly ethylbenzene and separate and the utilization of energy, do not relate to the problem that dehydrogenated tail gas absorbs equally with cinnamic.
Summary of the invention
Technical problem to be solved by this invention is the absorption problem that does not relate to dehydrogenated tail gas in the existing document, and in the existing industrial installation in the dehydrogenated tail gas aromatic recovery rate lower, the problem that aromatic hydrocarbons loss is bigger provides a kind of tail gas absorption method of new ethyl benzene dehydrogenation preparation of styrene.This method has aromatic recovery rate height in the dehydrogenated tail gas, the few characteristics of aromatic hydrocarbons loss amount in the dehydrogenated tail gas.
For solving the problems of the technologies described above, the technical solution used in the present invention is as follows: a kind of tail gas absorption method of ethyl benzene dehydrogenation preparation of styrene, contain benzene, toluene, ethylbenzene and cinnamic vapour mixture enter the bottom of tail gas absorber, absorption agent enters from tail gas absorber top, wherein the feeding temperature of vapour mixture is 15～48 ℃, absorption agent is a Residual oil, the absorption agent feeding temperature is 5～20 ℃, the liquid vapour weight ratio of absorption agent and vapour mixture is 3.0～5.5, the stage number of tail gas absorber is 5～20 blocks of theoretical trays, the tail gas absorber tower top pressure is 125～225KPa, vapour mixture is after absorption agent absorbs, tower bottoms removes desorption tower, the oil-containing lime set water separator that deoils, and the cat head non-condensable gas goes out-of-bounds.
In the technique scheme, absorption agent Residual oil preferred version is many ethylbenzene Residual oil, and more preferably scheme is the mixture that contains triethyl-benzene and tetrem benzene, and absorption agent feeding temperature preferable range is 7～12 ℃.The stage number preferable range of tail gas absorber is 6～12 blocks of theoretical trays, and the tail gas absorber preferred version is the material filling type structure, and tail gas absorber tower top pressure preferable range is 140～210KPa.
Owing to adopt lower Residual oil absorption agent feeding temperature and increase the absorption tower tower top pressure, the absorption agent Residual oil is improved greatly to the aromatic hydrocarbons assimilation effect in the dehydrogenated tail gas among the present invention.Confirm through test, by technical scheme of the present invention, aromatic recovery rate can reach 99.8% in the dehydrogenated tail gas, in 200,000 tons of/year vinylbenzene full scale plants, adopt technical scheme of the present invention, after tail gas absorber absorbed, aromaticity content only was 1.1 kilograms/hour in the dehydrogenated tail gas, promptly per hour can reduce nearly 28.9 kilograms aromatic hydrocarbons loss, obtain better technical effect.
The present invention is further elaborated below by embodiment.
Embodiment [embodiment 1]
Dehydrogenated tail gas is 521.5 kilograms/hour of hydrogen by mass rate, 44.5 kilograms/hour in methane, 290.4 kilograms/hour of carbonic acid gas, 139.2 kilograms/hour of benzene, 58.3 kilograms/hour of toluene, 1.8 kilograms/hour of non-aromaticss, 172.5 kilograms/hour in ethylbenzene, 160.2 kilograms of/hour vapour mixtures of forming of 103.1 kilograms/hour of vinylbenzene and water enter the tail gas absorber bottom, the many ethylbenzene Residual oil that contains the mixture of triethyl-benzene and tetrem benzene enters from tail gas absorber top as absorption agent, wherein the vapour mixture feeding temperature is 38 ℃, the absorption agent feeding temperature is 10 ℃, tail gas absorber is a packing tower, theoretical plate number is 10, liquid vapour weight ratio is 4.0, the tail gas absorber tower top pressure is 190KPa, after absorption agent absorbs, tail gas absorber cat head non-condensable gas is formed and flow is: 521.5 kilograms/hour of hydrogen, 44.5 kilograms/hour in methane, 1.1 kilograms/hour of 290.4 kilograms/hour of carbonic acid gas and vinylbenzene, aromatic recovery rate is 99.8% in the dehydrogenated tail gas.[embodiment 2]
Press condition and the step of embodiment 1, just changing the absorption agent feeding temperature is 15 ℃, and the tail gas absorber theoretical plate number is 10, and the tail gas absorber tower top pressure is 190KPa, and its result is 96.7% for aromatic recovery rate in the dehydrogenated tail gas.[embodiment 3]
Press condition and the step of embodiment 1, just changing the absorption agent feeding temperature is 10 ℃, and the tail gas absorber tower top pressure is 160KPa, and its result is 98.1% for aromatic recovery rate in the dehydrogenated tail gas.[comparative example 1]
Press condition and the step of embodiment 1, just changing the absorption agent feeding temperature is 38 ℃, and the tail gas absorber tower top pressure is 43KPa, and its result is 85.8% for aromatic recovery rate in the dehydrogenated tail gas.
Claims (7)
1, a kind of tail gas absorption method of ethyl benzene dehydrogenation preparation of styrene, contain benzene, toluene, ethylbenzene and cinnamic vapour mixture enter the bottom of tail gas absorber, absorption agent enters from tail gas absorber top, wherein the feeding temperature of vapour mixture is 15～48 ℃, absorption agent is a Residual oil, the absorption agent feeding temperature is 5～20 ℃, the liquid vapour weight ratio of absorption agent and vapour mixture is 3.0～5.5, the stage number of tail gas absorber is 5～20 blocks of theoretical trays, the tail gas absorber tower top pressure is 125～225KPa, and vapour mixture is after absorption agent absorbs, and tower bottoms removes desorption tower, the oil-containing lime set water separator that deoils, the cat head non-condensable gas goes out-of-bounds.
2,, it is characterized in that the absorption agent Residual oil is many ethylbenzene Residual oil according to the tail gas absorption method of the described ethyl benzene dehydrogenation preparation of styrene of claim 1.
3,, it is characterized in that many ethylbenzene Residual oil is the mixture that contains triethyl-benzene and tetrem benzene according to the tail gas absorption method of the described ethyl benzene dehydrogenation preparation of styrene of claim 2.
4,, it is characterized in that the absorption agent feeding temperature is 7～12 ℃ according to the tail gas absorption method of the described ethyl benzene dehydrogenation preparation of styrene of claim 1.
5, according to the tail gas absorption method of the described ethyl benzene dehydrogenation preparation of styrene of claim 1, the stage number that it is characterized in that tail gas absorber is 6～12 blocks of theoretical trays.
6,, it is characterized in that tail gas absorber is the material filling type structure according to the tail gas absorption method of the described ethyl benzene dehydrogenation preparation of styrene of claim 5.
7,, it is characterized in that the tail gas absorber tower top pressure is 140～210KPa according to the tail gas absorption method of the described ethyl benzene dehydrogenation preparation of styrene of claim 1.
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| Application Number | Priority Date | Filing Date | Title |
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| CNB021113130A CN1182091C (en) | 2002-04-10 | 2002-04-10 | Tail gas absorption method for preparing styrene by ethylbenzene dehrogenation |
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| CNB021113130A CN1182091C (en) | 2002-04-10 | 2002-04-10 | Tail gas absorption method for preparing styrene by ethylbenzene dehrogenation |
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| CN1182091C CN1182091C (en) | 2004-12-29 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101766917B (en) * | 2009-01-07 | 2012-03-14 | 中国石油化工股份有限公司 | Method for recovering low-temperature heat at top of ethylbenzene/styrene separating tower |
| CN103908868A (en) * | 2014-04-15 | 2014-07-09 | 大连理工大学 | Separation method for removing styrene from ethylbenzene-dehydrogenation tail gas and recovering hydrogen |
| CN114515497A (en) * | 2020-11-19 | 2022-05-20 | 中国石油化工股份有限公司 | Treatment system and treatment method for divinylbenzene production tail gas |
-
2002
- 2002-04-10 CN CNB021113130A patent/CN1182091C/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101766917B (en) * | 2009-01-07 | 2012-03-14 | 中国石油化工股份有限公司 | Method for recovering low-temperature heat at top of ethylbenzene/styrene separating tower |
| CN103908868A (en) * | 2014-04-15 | 2014-07-09 | 大连理工大学 | Separation method for removing styrene from ethylbenzene-dehydrogenation tail gas and recovering hydrogen |
| CN103908868B (en) * | 2014-04-15 | 2016-03-02 | 大连理工大学 | Remove the method for styrene and recover hydrogen in ethylbenzene dehydrogenation tail gas |
| CN114515497A (en) * | 2020-11-19 | 2022-05-20 | 中国石油化工股份有限公司 | Treatment system and treatment method for divinylbenzene production tail gas |
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| CN1182091C (en) | 2004-12-29 |
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