CN106608786B - The method of alcohol ether dimethylbenzene coproduction ethylbenzene - Google Patents
The method of alcohol ether dimethylbenzene coproduction ethylbenzene Download PDFInfo
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
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Abstract
The present invention relates to a kind of methods of alcohol ether dimethylbenzene coproduction ethylbenzene, and the ethylene and benzene of the matching ratio of production ethylbenzene can not be obtained while mainly solving the problems, such as to exist in the prior art voluminous dimethylbenzene.The present invention is by using the following steps are included: alcohol ether aromatization products are separated into gas phase I, oil phase I and water phase in separative unit；Gas phase I is sent into absorption tower and absorbs part carbon two and whole carbon three and the above component, and absorbing liquid is sent into desorber and is separated into lighter hydrocarbons and kettle liquid, and kettle liquid is divided into two share logistics, and sub- stream I returns to absorption tower as absorbent, and sub- stream I I is sent into aromatic hydrocarbons and converts separative unit；Lighter hydrocarbons go light dydrocarbon aromatization reaction device to be converted into light-hydrocarbon aromatized product；Light-hydrocarbon aromatized product is gas phase II and oily phase II through gas-liquid separator separates；Oily phase I and oil phase II is sent into aromatic hydrocarbons and converts separative unit, and benzene is sent into the technical solution of Benzene Device, preferably solves the above problem, can be used in the industrial production of alcohol ether aromatic hydrocarbons.
Description
Technical field
The present invention relates to a kind of methods of alcohol ether dimethylbenzene coproduction ethylbenzene.
Technical background
Aromatic hydrocarbons, especially light aromatics BTX (benzene,toluene,xylene) are important basic organic chemical industry's material, yield
It is inferior to ethylene and propylene with scale, derivative is widely used in the chemical products such as chemical fibre, plastics and rubber and fining
In the production of product.In recent years, with petrochemical industry and the continuous development of textile industry, the demand of aromatic hydrocarbons constantly increases.When
The main source of preceding BTX is catalytic reforming and drippolene by-product, and both of which is using petroleum as initial raw materials for production.With
The continuous consumption of world's crude oil and rising steadily for international oil price, aromatic hydrocarbons production capacity is suppressed, and production cost is unprecedented soaring.?
China, current oil production rate can no longer meet the demand of economic development, and external crude oil interdependency alreadys exceed 50%, find
It is a kind of to increase economic efficiency instead of the new technology of petrochemical industry production aromatic hydrocarbons for chemical company, China and ensure country
Energy security has important strategic importance.
It is exactly a very promising aromatics production route that alcohol ether especially methanol, which produces aromatic hydrocarbons by aromatisation,.This
Aspect be because of coal resources in China rich reserves, it is highly developed using the technology that coal is raw material production methanol, thus first
The yield and price of alcohol readily satisfy the demand of production aromatic hydrocarbons；On the other hand, methanol problem of excess production capacity is more serious, develops methanol
Aromatic hydrocarbons technology processed is then conducive to alleviate this problem, effectively extends Chemical Industry chain, improves the utilization efficiency of coal resources.
Alcohol ether aromatic hydrocarbons technology has been well known technology, the alcohol ethers compound coproduction alkene as disclosed in Tsinghua University with
The method (CN201410370034) of aromatic hydrocarbons, alcohol ether conversion prepare the system and technique of benzene and paraxylene
(CN201310492824), a kind of disclosed in China National Offshore Oil Corporation that propylene and the method for BTX are prepared by methanol
(CN201410642340), the method for the conversion of methanol disclosed in Sinopec Group production aromatic hydrocarbons
(CN103664440) etc., during disclosing alcohol ether aromatic hydrocarbons, generate a series of complex reaction product, including hydrogen, first
The light hydrocarbons such as alkane, ethane, ethylene further include the heavy arene of nine ten or more carbon of the aromatic hydrocarbons such as BTX and carbon.Due to product point
Cloth is extensive, causes the yield of BTX goal response product relatively low.In order to improve BTX yield, generally require to be arranged light-hydrocarbon aromatized anti-
Device is answered, light hydrocarbons is made to be converted into aromatic hydrocarbons, the system of a kind of methanol or dimethyl ether conversion preparing aromatic hydrocarbon as disclosed in Tsinghua University
With technique (CN201010146915) by the aromatic hydrocarbons C2+ non-aromatics and in addition to mixing C8 aromatic hydrocarbons and part C9+ hydro carbons then
Respective reaction device is returned as circulation logistics and carries out further aromatization, improves the yield and selectivity of aromatic hydrocarbons.But by
Containing the alkane for being difficult to aromatisation, especially ethane, propane etc. in recycle stock, cause internal circulating load huge, system energy consumption is very
It is high.
A kind of method of economy is that ethane and more light component are separated from light-hydrocarbon aromatized raw material, avoids ethane in lighter hydrocarbons
Circulative accumulation in aromatisation system.A kind of more economical method be ethane and more light component from light-hydrocarbon aromatized raw material point
Out, ethane circulative accumulation in light-hydrocarbon aromatized system is avoided, and the benzene for therefrom isolating ethylene and generation reacts, it is raw
At the ethyl benzene/styrene of high added value, develop skill economy.Since in aromatization of methanol reactor, benzene is anti-through methylating
The rate that toluene and dimethylbenzene should be generated is very fast, so obtained aromatic hydrocarbons substantially based on toluene, dimethylbenzene and trimethylbenzene, produces
The content of benzene is very small in product, and the ethylene often generated is much larger than the matching amount for generating benzene required for ethylbenzene.Tsinghua University is public
The patent CN201110024191 opened increases by 0.5% cerium or increase by 1.5% using commercial aromatisation Zn/ZSM-5 catalyst
Cerium, catalyst after change can generate ethylene than current existing catalyst more with high selectivity, but also lead to two simultaneously
The yield of toluene declines to a great extent.
The prior art can not obtain the ethylene and benzene for producing the matching ratio of ethylbenzene while there is voluminous dimethylbenzene
Problem, the present invention targetedly solve the above problem.
Summary of the invention
The technical problem to be solved by the present invention is to can not obtain production second while voluminous dimethylbenzene in the prior art
The problem of ethylene and benzene of the matching ratio of benzene, provides a kind of method of new alcohol ether dimethylbenzene coproduction ethylbenzene.This method tool
Have the advantages that the ratio of good diformazan benzene yield height, catalyst adaptability, ethylene and benzene is adjustable.
To solve the above problems, The technical solution adopted by the invention is as follows: a kind of side of alcohol ether dimethylbenzene coproduction ethylbenzene
Method, comprising the following steps: 1) reaction raw materials are converted into alcohol ether aromatization products in alcohol ether aromatization reactor；2) alcohol ether aromatization
Change product and is separated into gas phase I, oil phase I and water phase in separative unit；3) gas phase I is sent into absorption tower absorption part carbon two and whole
Carbon three and the above component obtain and absorb tail gas and absorbing liquid, absorb tail gas and are sent into Benzene Device；4) absorbing liquid is sent into desorber point
From for lighter hydrocarbons and kettle liquid, kettle liquid is divided into two share logistics, and sub- stream I returns to absorption tower as absorbent, and sub- stream I I is sent into virtue
Hydrocarbon converts separative unit；5) lighter hydrocarbons go light dydrocarbon aromatization reaction device to be converted into light-hydrocarbon aromatized product；6) light-hydrocarbon aromatized product
It is gas phase II and oily phase II through gas-liquid separator separates, gas phase II returns to absorption tower；7) oil phase I and oil phase II is sent into aromatic hydrocarbons conversion
Separative unit obtains non-aromatic, benzene, dimethylbenzene and heavy aromatics, and benzene is sent into Benzene Device.
In above-mentioned technical proposal, the alcohol ether aromatization products include 5~10% ethylene, 0.5 based on carbon-based mass fraction
~5% benzene, 25~35% dimethylbenzene.
In above-mentioned technical proposal, the reaction condition of the alcohol ether aromatization reactor are as follows: 450~600 DEG C of reaction temperature, instead
Answer 0.1~0.5MPA of pressure, 0.5~4HR of reaction mass air speed-1。
In above-mentioned technical proposal, the absorption tower operating pressure is 0.5~3MPa, and liquid-gas ratio is 150~450L/m3, inhale
Receiving agent includes benzene,toluene,xylene and C9 +At least one of component absorbs propylene volume fraction in tail gas and is not more than 2%.
In above-mentioned technical proposal, the reaction condition of the light dydrocarbon aromatization reaction device are as follows: 500~650 DEG C of reaction temperature, instead
Answer 0.1~1MPA of pressure, 0.1~3HR of reaction mass air speed-1。
In above-mentioned technical proposal, the aromatic hydrocarbons conversion separative unit includes toluene disproportionation and alkyl transfering process device, two
Toluene isomerization process unit.
In above-mentioned technical proposal, aromatic hydrocarbons conversion separative unit includes that methylbenzene shape selective disproportionation process unit, heavy aromatics are light
Matter chemical industry process and equipment, xylene isomerization process device.
In above-mentioned technical proposal, the aromatic hydrocarbons conversion separative unit includes methylbenzene shape selective disproportionation process unit, nine alkane of benzene carbon
Group-transfer process unit, xylene isomerization process device.
Using method of the invention, by the method for absorption, the ethylene of recovery section from gas phase I makes it in lighter hydrocarbons virtue
Part is converted into benzene in structure reactor, and in aromatic hydrocarbons conversion separative unit is separated into benzene.The technique absorbed by control
Condition, such as temperature, absorption pressure, absorbent dosage, liquid-gas ratio are absorbed, absorptivity of the ethylene in absorption tower is adjusted, makes to fit
The aromatic hydrocarbons such as benzene and toluene are converted into when the ethylene of ratio enters light-hydrocarbon aromatized unit, are then isolated in aromatic hydrocarbons conversion unit
Benzene, thus increase the yield of benzene, and the yield of ethylene is reduced, and the ratio of ethylene and benzene is finally made to be exactly for producing ethylbenzene
With ratio.Using method of the invention, if aromatic hydrocarbons contained in gas phase I is unable to satisfy the requirement of absorption, can turn from aromatic hydrocarbons
Change separative unit and draws one arene stream as supplement absorbent.It, can be public using the prior art using method of the invention
The catalyst for all types of alcohol ether conversion for preparing arene opened is without carrying out any change to catalyst, therefore in the present invention
Technique to the adaptable of catalyst.The catalyst for selecting dimethylbenzene selective high can then keep higher dimethylbenzene to receive
Rate.Using method of the invention, owner can be adjusted according to the needs products scheme, and existing aromatic hydrocarbons transformation technology can flexibly match
It sets, such as traditional toluene disproportionation and transalkylation technology, the combination technique of methylbenzene shape selective disproportionation and heavy aromatics lighting, toluene are selected
The combination technique etc. of shape disproportionation and nine transalkylation of benzene carbon.By adjusting the absorptivity of absorption tower ethylene, the second of system can be made
Alkene and benzene yield keep matching.Using method of the invention, the high energy consumptions such as dethanizer, ethylene rectifying column that no setting is required, high throwing
Provide equipment, the recycling of tail gas ethylene can be realized under not harsh operating condition, and directly obtained produce it is high attached
The raw material of value added ethylbenzene achieves preferable technical effect.
Detailed description of the invention
Fig. 1 is the flow diagram of the method for the invention.
In Fig. 1,1 is reaction raw materials；2 be alcohol ether aromatization products；3 be gas phase I；4 be gas phase II；5 be mixing gas phase；6
For oily phase I；7 be water phase；8 be absorption tail gas；9 be absorbing liquid；10a is absorbent, and 10b is supplement absorbent；11 be lighter hydrocarbons；12
For light-hydrocarbon aromatized product；13 be desorption tower bottoms；14 be oily phase II；15 be sub- stream I I；16 be miscella phase；17 be non-
Virtue；18 be benzene；19 be dimethylbenzene；20 be heavy aromatics；21 be ethylbenzene；22 be Benzene Device tail gas.A is alcohol ether aromatization
Device, B are separative unit, and C is absorption tower, and D is desorber, and E is light dydrocarbon aromatization reaction device, and F is gas-liquid separator, G ethylbenzene dress
It sets, H is that aromatic hydrocarbons converts separative unit.
Brief description of the process is as follows: the reaction raw materials such as methanol and/or dimethyl ether are converted into alcohol ether through alcohol ether aromatization reactor
Aromatization products；Alcohol ether aromatization products are separated into gas phase I, oil phase I and water phase in separative unit；Gas phase I is sent into absorption tower
Part carbon two and whole carbon three and the above component are absorbed, obtains and absorbs tail gas and absorbing liquid, tail gas is absorbed and is sent into Benzene Device；It inhales
It receives liquid feeding desorber and is separated into lighter hydrocarbons and kettle liquid, kettle liquid is divided into two share logistics, and sub- stream I is returned as absorbent to be absorbed
Tower, sub- stream I I are sent into aromatic hydrocarbons and convert separative unit；Lighter hydrocarbons go light dydrocarbon aromatization reaction device to be converted into light-hydrocarbon aromatized product；Gently
Hydrocarbon aromatizing product is gas phase II and oily phase II through gas-liquid separator separates, and gas phase II returns to absorption tower；Oily phase I and oil phase II are sent
Enter aromatic hydrocarbons conversion separative unit and obtain non-aromatic, benzene, dimethylbenzene and heavy aromatics, benzene is sent into Benzene Device and ethylbenzene is made.
The present invention will be further described below by way of examples, but is not limited only to the present embodiment.
Specific embodiment
[embodiment 1]
Process flow as shown in Figure 1, the methanol that flow is 140kmol/hr feed anti-in alcohol ether aromatization reactor
It answers, using the ZSM-5 alcohol ether aromatized catalyst containing Zn 7%, 450 DEG C of alcohol ether aromatization temperature, pressure 0.1MPa is urged
Agent mass space velocity 0.5hr-1.Alcohol ether aromatization products composition in based on carbon-based mass fraction comprising 5% ethylene, 0.7% benzene,
28% dimethylbenzene.Light dydrocarbon aromatization reaction temperature is 500 DEG C, pressure 0.3MPa, catalyst quality air speed 2hr-1.Absorption tower operation
Pressure is 1.0MPa, liquid-gas ratio 325L/m3, absorbent includes benzene,toluene,xylene, and absorption tower ethylene absorption rate is
58.6%, it absorbs in tail gas without propylene.Aromatic hydrocarbons converts separative unit using traditional toluene disproportionation and transalkylation technology, and is arranged
Xylene isomerization reaction device in mixed xylenes ortho-xylene and meta-xylene be converted into paraxylene.Turn from aromatic hydrocarbons
Change the part toluene of separative unit as supplement absorbent 10a, is recycled between absorption tower, desorber, benzene column and toluene tower.It should
The benzene and ethylene yield of embodiment are close to equimolar, and product is that ethylbenzene yield is 3.82kmol/hr, and diformazan benzene yield is
8.38kmol/hr。
[embodiment 2]
Process flow as shown in Figure 1, the methanol that flow is 140kmol/hr feed anti-in alcohol ether aromatization reactor
It answers, using the ZSM-5 alcohol ether aromatized catalyst containing Zn 1.2%, 550 DEG C, pressure 0.2MPa of alcohol ether aromatization temperature,
Catalyst quality air speed 2hr-1.Alcohol ether aromatization products composition in based on carbon-based mass fraction comprising 8% ethylene, 0.5% benzene,
33% dimethylbenzene.Light dydrocarbon aromatization reaction temperature is 550 DEG C, pressure 0.1MPa, catalyst quality air speed 3hr-1.Absorption tower operation
Pressure is 3MPa, liquid-gas ratio 152L/m3, absorbent includes benzene,toluene,xylene, and absorption tower ethylene absorption rate is 61.3%,
It absorbs in tail gas without propylene.Aromatic hydrocarbons converts separative unit using traditional toluene disproportionation and transalkylation technology, and dimethylbenzene is arranged
Isomerization reactor in mixed xylenes ortho-xylene and meta-xylene be converted into paraxylene.The benzene and second of the embodiment
Alkene yield is close to equimolar, and product is that ethylbenzene yield is 3.50kmol/hr, and diformazan benzene yield is 9.87kmol/hr.
[embodiment 3]
Process flow as shown in Figure 1, the dimethyl ether that flow is 70kmol/hr feed anti-in alcohol ether aromatization reactor
It answers, using the ZSM-5 alcohol ether aromatized catalyst containing Zn 7% and Cu 2%, 600 DEG C of alcohol ether aromatization temperature, pressure
0.4MPa, catalyst quality air speed 3hr-1.It include 9% ethylene, 3% based on carbon-based mass fraction in alcohol ether aromatization products composition
Benzene, 31% dimethylbenzene.Light dydrocarbon aromatization reaction temperature is 600 DEG C, pressure 0.1MPa, catalyst quality air speed 2.5hr-1.It absorbs
Tower operating pressure is 1.5MPa, liquid-gas ratio 233L/m3, absorbent includes benzene,toluene,xylene, absorption tower ethylene absorption rate
It is 65.7%, absorbs in tail gas without propylene.Aromatic hydrocarbons converts separative unit using traditional toluene disproportionation and transalkylation technology, and sets
Set xylene isomerization reaction device in mixed xylenes ortho-xylene and meta-xylene be converted into paraxylene.The embodiment
Benzene and ethylene yield close to equimolar, it is 4.46kmol/hr that product, which is ethylbenzene yield, and diformazan benzene yield is 9.43kmol/hr.
[embodiment 4]
Process flow as shown in Figure 1, the dimethyl ether that flow is 70kmol/hr feed anti-in alcohol ether aromatization reactor
It answers, wherein methanol volume fraction is 44%, is reacted in alcohol ether aromatization reactor, using the ZSM-5 alcohol ether containing Ga 3.6%
Aromatized catalyst, 480 DEG C, pressure 0.3MPa of alcohol ether aromatization temperature, catalyst quality air speed 2hr-1.Alcohol ether aromatisation
It include 7% ethylene, 1% benzene, 32% dimethylbenzene based on carbon-based mass fraction in product composition.Light dydrocarbon aromatization reaction temperature is
650 DEG C, pressure 1MPa, catalyst quality air speed 0.5hr-1.Absorption tower operating pressure is 2MPa, liquid-gas ratio 182L/m3, absorb
Agent includes benzene,toluene,xylene, and absorption tower ethylene absorption rate is 57.6%, is absorbed in tail gas without propylene.Aromatic hydrocarbons conversion separation is single
Xylene isomerization reaction device is arranged the neighbour two in mixed xylenes using traditional toluene disproportionation and transalkylation technology in member
Toluene and meta-xylene are converted into paraxylene.For the benzene and ethylene yield of the embodiment close to equimolar, product is ethylbenzene yield
For 4.21kmol/hr, diformazan benzene yield is 9.589kmol/hr.
[embodiment 5]
Process flow as shown in Figure 1, the methanol that flow is 140kmol/hr feed anti-in alcohol ether aromatization reactor
It answers, using the ZSM-5 alcohol ether aromatized catalyst containing Zn 7%, 500 DEG C of alcohol ether aromatization temperature, pressure 0.5MPa is urged
Agent mass space velocity 4hr-1.It include 10% ethylene, 5% benzene, 26% based on carbon-based mass fraction in alcohol ether aromatization products composition
Dimethylbenzene.Light dydrocarbon aromatization reaction temperature is 550 DEG C, pressure 0.7MPa, catalyst quality air speed 0.1hr-1.Absorption tower operation pressure
Power is 0.5MPa, liquid-gas ratio 450L/m3, absorbent includes benzene,toluene,xylene, and absorption tower ethylene absorption rate is 67.2%,
Absorbing propylene volume fraction in tail gas is 0.01%.Aromatic hydrocarbons converts separative unit using traditional toluene disproportionation and transalkylation skill
Art, and be arranged xylene isomerization reaction device in mixed xylenes ortho-xylene and meta-xylene be converted into paraxylene.
Part toluene from aromatic hydrocarbons conversion separative unit is as supplement absorbent 10a, in absorption tower, desorber, benzene column and toluene tower
Between recycle.For the benzene and ethylene yield of the embodiment close to equimolar, product ethylbenzene yield is 2.86kmol/hr, and dimethylbenzene produces
Amount is 8.77kmol/hr.
[embodiment 6]
Process flow as shown in Figure 1, the methanol that flow is 140kmol/hr feed anti-in alcohol ether aromatization reactor
Answer, using with the identical catalyst of embodiment 4 and reaction condition, aromatic hydrocarbons convert separative unit using methylbenzene shape selective disproportionation and weight virtue
Hydrocarbon lighting combination technique, and xylene isomerization reaction device is set the ortho-xylene and meta-xylene turn in mixed xylenes
Turn to paraxylene.Absorption tower operating pressure is 1.5MPa, liquid-gas ratio 247L/m3, absorbent includes benzene,toluene,xylene,
Absorption tower ethylene absorption rate is 51.7%, is absorbed in tail gas without propylene.The benzene and ethylene yield of the embodiment are produced close to equimolar
Product ethylbenzene yield is 4.76kmol/hr, and diformazan benzene yield is 9.26kmol/hr.
[embodiment 7]
Process flow as shown in Figure 1, the methanol that flow is 140kmol/hr feed anti-in alcohol ether aromatization reactor
Answer, using with the identical catalyst of embodiment 5 and reaction condition, aromatic hydrocarbons convert separative unit use methylbenzene shape selective disproportionation and benzene carbon
Nine transalkylation combination techniques, and xylene isomerization reaction device is set the ortho-xylene and meta-xylene in mixed xylenes
It is converted into paraxylene.Absorption tower operating pressure is 2.5MPa, liquid-gas ratio 156L/m3, absorbent includes benzene, toluene, diformazan
Benzene, absorption tower ethylene absorption rate are 69.8%, are absorbed in tail gas without propylene.The benzene and ethylene yield of the embodiment close to etc. rub
You, product ethylbenzene yield is 2.77kmol/hr, and diformazan benzene yield is 8.83kmol/hr.
[embodiment 8]
Process flow as shown in Figure 1, the methanol that flow is 140kmol/hr feed anti-in alcohol ether aromatization reactor
Answer, using with the identical catalyst of embodiment 5 and reaction condition, aromatic hydrocarbons convert separative unit use methylbenzene shape selective disproportionation and benzene carbon
Nine transalkylation combination techniques, and xylene isomerization reaction device is set the ortho-xylene and meta-xylene in mixed xylenes
It is converted into paraxylene.Absorption tower operating pressure is 0.3MPa, liquid-gas ratio 500L/m3, absorbent includes benzene, toluene, diformazan
Benzene, absorption tower ethylene absorption rate are 32.2%, and absorbing propylene content in tail gas is 2.1vol%.The embodiment can not be matched
The benzene and ethylene of magnitude, product ethylbenzene yield are 1.96kmol/hr, and diformazan benzene yield is 8.83kmol/hr, by-product ethylene
0.77kmol/hr。
[comparative example]
Patent CN201110024191 disclosed embodiment shows toluene, dimethylbenzene and C in methanol aromatic product10Virtue
The total content of hydrocarbon is 20~25%.Xylene content made from this method is 25~35%, toluene, dimethylbenzene and C10Aromatic hydrocarbons
Total content is then higher than 40%.In patent CN201110024191 disclosed embodiment, the molar ratio of benzene and ethylene is 1.2~1.5,
And the benzene and ethylene consumed in styrene device is close to equimolar ratio, i.e. 1:1.
Claims (8)
1. a kind of method of alcohol ether dimethylbenzene coproduction ethylbenzene, comprising the following steps: 1) reaction raw materials are in alcohol ether aromatization
Alcohol ether aromatization products are converted into device；2) alcohol ether aromatization products are separated into gas phase I, oil phase I and water phase in separative unit；
3) gas phase I is sent into absorption tower absorption part carbon two and whole carbon three and the above component, obtains and absorbs tail gas and absorbing liquid, absorbs tail
Pneumatic transmission enters Benzene Device；4) absorbing liquid is sent into desorber and is separated into lighter hydrocarbons and kettle liquid, and kettle liquid is divided into two share logistics, sub- stream I
Absorption tower is returned to as absorbent, sub- stream I I is sent into aromatic hydrocarbons and converts separative unit；5) lighter hydrocarbons go light dydrocarbon aromatization reaction device to turn
Turn to light-hydrocarbon aromatized product；6) light-hydrocarbon aromatized product is gas phase II and oily phase II through gas-liquid separator separates, and gas phase II is returned
Go back to absorption tower；7) oil phase I and oil phase II is sent into aromatic hydrocarbons conversion separative unit and obtains non-aromatic, benzene, dimethylbenzene and heavy aromatics, and benzene is sent into
Benzene Device；
Wherein, the alcohol ether aromatization products based on carbon-based mass fraction comprising 5~10% ethylene, 0.5~5% benzene, 25~
35% dimethylbenzene；The absorption tower operating pressure is 0.5~3MPa, and liquid-gas ratio is 150~450L/m3。
2. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that the alcohol ether aromatisation is anti-
Answer the reaction condition of device are as follows: 450~600 DEG C of reaction temperature, 0.1~0.5MPA of reaction pressure, 0.5~4HR of reaction mass air speed-1。
3. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that absorbed in the absorption tower
Agent contains benzene,toluene,xylene and C9 +At least one of component.
4. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that absorb propylene body in tail gas
Fraction is not more than 2%.
5. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that described light-hydrocarbon aromatized anti-
Answer the reaction condition of device are as follows: 500~650 DEG C of reaction temperature, 0.1~1MPA of reaction pressure, 0.1~3HR of reaction mass air speed-1。
6. the method for any one alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1~5, it is characterised in that the aromatic hydrocarbons
Converting separative unit includes toluene disproportionation and alkyl transfering process device, xylene isomerization process device.
7. the method for any one alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1~5, it is characterised in that the aromatic hydrocarbons
Conversion separative unit includes methylbenzene shape selective disproportionation process unit, heavy aromatics lighting process unit, xylene isomerization process dress
It sets.
8. the method for any one alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1~5, it is characterised in that the aromatic hydrocarbons
Converting separative unit includes methylbenzene shape selective disproportionation process unit, nine alkyl transfering process device of benzene carbon, xylene isomerization process
Device.
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