CN106608786A - Method for cooperatively producing ethylbenzene by preparing xylene from alcohol ether - Google Patents
Method for cooperatively producing ethylbenzene by preparing xylene from alcohol ether Download PDFInfo
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- CN106608786A CN106608786A CN201510690223.XA CN201510690223A CN106608786A CN 106608786 A CN106608786 A CN 106608786A CN 201510690223 A CN201510690223 A CN 201510690223A CN 106608786 A CN106608786 A CN 106608786A
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- alcohol ether
- benzene
- dimethylbenzene
- absorption tower
- ethylbenzene
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- C—CHEMISTRY; METALLURGY
- 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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- C—CHEMISTRY; METALLURGY
- 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
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
Abstract
The invention relates to a method for cooperatively producing ethylbenzene by preparing xylene from alcohol ether. The method mainly aims at solving the problem that in the prior art, ethylene and benzene which are of the matched proportion for producing ethylbenzene cannot be obtained while xylene is produced. The method comprises the following steps that an alcohol ether aromatization product is separated into a gas phase I, an oil phase I and an aqueous phase in a separation unit; the gas phase I is sent into an absorption tower, so that part of C2, all C3 and above components are absorbed, absorption liquid is sent into a desorption tower to be separated into light dydrocarbon and residues, the residues are divided into two subsidiary substance flows, the subsidiary substance flow I returns to the absorption tower as an absorbing agent, and the subsidiary substance flow II is sent into an arene conversion and separation unit; the light dydrocarbon is converted into a light dydrocarbon aromatization product through a light dydrocarbon aromatization reactor; the light dydrocarbon aromatization product is separated into a gas phase II and an oil phase II through a gas-liquid separator; and the oil phase I and the oil phase II are sent into the arene conversion and separation unit, and benzene is sent into an ethylbenzene device. By means of the method, the mentioned problem is well solved; and the method can be applied to industrial production for preparing the xylene from the alcohol ether.
Description
Technical field
The present invention relates to a kind of method of alcohol ether dimethylbenzene coproduction ethylbenzene.
Technical background
Aromatic hydrocarbons, particularly light aromatics BTX (benzene,toluene,xylene) are important basic organic chemical industry's materials, its product
Amount and scale are inferior to ethylene and propylene, and its derivant is widely used in chemical products such as chemical fibre, plastics and rubber and fine
In the production of chemicals.In recent years, with petrochemical industry and the continuous development of textile industry, the demand of aromatic hydrocarbons constantly increases.
The main source of current BTX is catalytic reforming and drippolene by-product, and both of which is former as initial production using oil
Material.As the continuous consumption of world's crude oil and rising steadily for international oil price, aromatic hydrocarbons production capacity are suppressed, production cost is significantly
It is soaring.In China, current oil production rate cannot meet the demand of economic development, and external crude oil interdependency is alreadyd exceed
50%, a kind of new technique that can replace petrochemical industry production aromatic hydrocarbons is found for China's chemical enterprise is increased economic efficiency and guarantor
The energy security of barrier country has important strategic importance.
Especially methanol is exactly a very promising aromatics production route by aromatisation production aromatic hydrocarbons to alcohol ether.This aspect
Coal resources in China rich reserves are because, it is highly developed as the technology of raw material production methanol with coal, thus methanol
Yield and price readily satisfy the demand of production aromatic hydrocarbons；On the other hand, methanol problem of excess production capacity is more serious, develops methanol system
Aromatic hydrocarbons technology is then conducive to alleviating this problem, effectively extends Chemical Industry chain, improves the utilization ratio of coal resources.
Alcohol ether aromatic hydrocarbons technology has been known technology, alcohol ethers compound coproduction alkene and aromatic hydrocarbons as disclosed in Tsing-Hua University
Method (CN201410370034), alcohol ether conversion prepare the system and technique (CN201310492824) of benzene and xylol,
A kind of method (CN201410642340) that propylene and BTX are prepared by methanol disclosed in China National Offshore Oil Corporation, China
Disclosed in petrochemical industry limited company, method (CN103664440) of methanol conversion production aromatic hydrocarbons etc., discloses alcohol ether
During aromatic hydrocarbons processed, a series of complex reaction product is generated, including the light hydrocarbons such as hydrogen, methane, ethane, ethylene,
The aromatic hydrocarbons also including BTX etc., and the heavy arene of nine carbon more than ten of carbon.Due to products distribution extensively, BTX target responses are caused
The yield of product is low.In order to improve BTX yields, generally require to arrange light dydrocarbon aromatization reaction device, convert light hydrocarbons
For aromatic hydrocarbons, the system and technique of a kind of methanol or dimethyl ether conversion preparing aromatic hydrocarbon as disclosed in Tsing-Hua University
(CN201010146915) by the aromatic hydrocarbons using C2+ non-aromaticss and in addition to mixing C8 aromatic hydrocarbons and part C9+ hydro carbons then as following
Ring logistics returns respective reaction device and carries out further aromatization, improves the yield and selectivity of aromatic hydrocarbons.But due to circulation
Containing the alkane for being difficult to aromatisation in material, especially ethane, propane etc., cause circulating load huge, and system energy consumption is very high.
A kind of economic method is that ethane and more light component are separated from light-hydrocarbon aromatized raw material, it is to avoid ethane is in lighter hydrocarbons aromatization
Circulative accumulation in change system.A kind of more economical method is that ethane and more light component are separated from light-hydrocarbon aromatized raw material, is kept away
Exempt from ethane circulative accumulation in light-hydrocarbon aromatized system, and therefrom isolate the benzene of ethylene and generation to react, generate high
The ethyl benzene/styrene of added value, develop skill economy.Due in aromatization of methanol reactor, benzene Jing methylation reactions
The speed for generating toluene and dimethylbenzene is very fast, so the aromatic hydrocarbons for obtaining is substantially based on toluene, dimethylbenzene and trimethylbenzene, produces
In product, the content of benzene is very little, matching amount of the ethylene for often generating much larger than the benzene generated required for ethylbenzene.Tsing-Hua University is public
Patent CN201110024191 opened increases by 0.5% cerium using commercial aromatisation Zn/ZSM-5 catalyst or increases by 1.5%
Cerium, the catalyst after change can generate ethylene more with high selectivity than current existing catalyst, but while also cause diformazan
The yield of benzene declines to a great extent.
Prior art cannot obtain the ethylene and benzene of the matching ratio of production ethylbenzene while there is voluminous dimethylbenzene,
The present invention targetedly solves the problems referred to above.
The content of the invention
The technical problem to be solved is to obtain production ethylbenzene in prior art while voluminous dimethylbenzene
A kind of problem of the ethylene and benzene of matching ratio, there is provided method of new alcohol ether dimethylbenzene coproduction ethylbenzene.The method has two
Toluene yield is high, catalyst adaptability is good, the adjustable advantage of the ratio of ethylene and benzene.
To solve the above problems, the technical solution used in the present invention is as follows：A kind of method of alcohol ether dimethylbenzene coproduction ethylbenzene,
Comprise 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 gas phase I, oil phase I and water phase are separated in separative element；3) gas phase I sends into absorption tower absorption two He of part carbon
Whole carbon three and above component, obtain and absorb tail gas and absorbing liquid, absorb tail gas and send into Benzene Device；4) absorbing liquid is sent into
Desorber is separated into lighter hydrocarbons and kettle liquid, and kettle liquid is divided into two share logistics, and sub- stream I returns absorption tower, sub- thing as absorbent
Stream II sends into aromatic hydrocarbons conversion separative element；5) lighter hydrocarbons go light dydrocarbon aromatization reaction device to be converted into light-hydrocarbon aromatized product；6) it is light
Hydrocarbon aromatizing product Jing gas-liquid separator separates are gas phase II and oil phase II, and gas phase II returns to absorption tower；7) oil phase I and oil
Phase II is sent into aromatic hydrocarbons conversion separative element and obtains non-aromatic, benzene, dimethylbenzene and heavy aromatics, and benzene sends into Benzene Device.
In above-mentioned technical proposal, the alcohol ether aromatization products based on carbon-based mass fraction comprising 5～10% ethylene, 0.5～5%
Benzene, 25～35% dimethylbenzene.
In above-mentioned technical proposal, the reaction condition of the alcohol ether aromatization reactor is：450～600 DEG C of reaction temperature, reaction
0.1～0.5MPA of pressure, reaction mass 0.5～4HR of 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, absorbent
Including benzene,toluene,xylene and C9 +At least one in component, in absorbing tail gas, propylene volume fraction is not more than 2%.
In above-mentioned technical proposal, the reaction condition of the light dydrocarbon aromatization reaction device is：500～650 DEG C of reaction temperature, reaction
0.1～1MPA of pressure, reaction mass 0.1～3HR of air speed-1。
In above-mentioned technical proposal, the aromatic hydrocarbons conversion separative element includes toluene disproportionation and alkyl transfering process device, dimethylbenzene
Isomerization process unit.
In above-mentioned technical proposal, the aromatic hydrocarbons conversion separative element includes methylbenzene shape selective disproportionation process unit, heavy aromatics lighting
Process unit, xylene isomerization process device.
In above-mentioned technical proposal, the aromatic hydrocarbons conversion separative element includes that methylbenzene shape selective disproportionation process unit, nine alkyl of benzene carbon turn
Move process unit, xylene isomerization process device.
Using the method for the present invention, the method by absorbing, the ethylene of recovery section from gas phase I so as in lighter hydrocarbons aromatization
That changes part in reactor is converted into benzene, and is separated into benzene in aromatic hydrocarbons conversion separative element.By the technique bar for controlling to absorb
Part, such as absorbs temperature, absorption pressure, absorbent consumption, liquid-gas ratio etc., adjusts absorbance of the ethylene in absorption tower, make
The ethylene of proper proportion is converted into the aromatic hydrocarbons such as benzene and toluene into light-hydrocarbon aromatized unit, then isolates in aromatic hydrocarbons conversion unit
Benzene, so that the yield of benzene increases, and the yield of ethylene is reduced, and finally makes ethylene and the ratio of benzene exactly produce ethylbenzene
Matching ratio.Using the method for the present invention, if aromatic hydrocarbons contained in gas phase I cannot meet the requirement of absorption, can be from virtue
Hydrocarbon conversion separative element draws one arene stream as supplementary absorbent.Using the method for the present invention, existing skill can be adopted
The catalyst of all types of alcohol ether conversion for preparing arene disclosed in art without carrying out any change, therefore this to catalyst
Strong adaptability of the technique in bright to catalyst.Higher dimethylbenzene can then be kept from the high catalyst of dimethylbenzene selective
Yield.Using the method for the present invention, owner can adjust products scheme as needed, and existing aromatic hydrocarbons transformation technology can be with spirit
Configuration living, such as traditional toluene disproportionation and transalkylation technology, the combination technique of methylbenzene shape selective disproportionation and heavy aromatics lighting,
Combination technique of nine transalkylation of methylbenzene shape selective disproportionation and benzene carbon etc..By adjust absorption tower ethylene absorbance, can make be
The ethylene of system and benzene yield keep matching.Using the method for the present invention, the high energy such as dethanizer, ethylene rectifying column need not be set
Consumption, equipment with high investment, are capable of achieving the recycling of tail gas ethylene under not harsh operating condition, and directly obtain
The raw material of high added value ethylbenzene is produced, preferable technique effect is achieved.
Description of the drawings
Schematic flow sheets of the Fig. 1 for the method for the invention.
In Fig. 1,1 is reaction raw materials；2 is alcohol ether aromatization products；3 is gas phase I；4 is gas phase II；5 is gaseous mixture
Phase；6 is oil phase I；7 is water phase；8 are absorption tail gas；9 is absorbing liquid；10a is absorbent, and 10b is to supplement absorbent；
11 is lighter hydrocarbons；12 is light-hydrocarbon aromatized product；13 is desorbing tower bottoms；14 is oil phase II；15 is sub- stream I I；16
To mix oil phase；17 is non-aromatic；18 is benzene；19 is dimethylbenzene；20 is heavy aromatics；21 is ethylbenzene；22 fill for ethylbenzene
Put tail gas.A is alcohol ether aromatization reactor, and B is separative element, and C is absorption tower, and D is desorber, and E is lighter hydrocarbons virtue
Structure reactor, F are gas-liquid separator, and G Benzene Devices, H are that aromatic hydrocarbons converts separative element.
Brief description of the process is as follows：The reaction raw materials Jing alcohol ether aromatization reactors such as methanol and/or dimethyl ether are converted into alcohol ether aromatization
Change product；Alcohol ether aromatization products are separated into gas phase I, oil phase I and water phase in separative element；Gas phase I is sent into absorption tower and is inhaled
Receiving portions carbon two and whole carbon three and above component, obtain and absorb tail gas and absorbing liquid, absorb tail gas and send into Benzene Device；Inhale
Receive liquid feeding desorber and be separated into lighter hydrocarbons and kettle liquid, kettle liquid is divided into two share logistics, and sub- stream I is returned as absorbent and absorbed
Tower, sub- stream I I send into aromatic hydrocarbons conversion separative element；Lighter hydrocarbons go light dydrocarbon aromatization reaction device to be converted into light-hydrocarbon aromatized product；
Light-hydrocarbon aromatized product Jing gas-liquid separator separates are gas phase II and oil phase II, and gas phase II returns to absorption tower；Oil phase I and oil phase
II sends into aromatic hydrocarbons conversion separative element and obtains non-aromatic, benzene, dimethylbenzene and heavy aromatics, and benzene is sent into Benzene Device and ethylbenzene is obtained.
Below by embodiment, the invention will be further elaborated, but is not limited only to the present embodiment.
Specific embodiment
【Embodiment 1】
Technological process as shown in Figure 1, flow feed for the methanol of 140kmol/hr and react in alcohol ether aromatization reactor,
Using containing Zn 7% ZSM-5 alcohol ether aromatized catalysts, 450 DEG C of alcohol ether aromatization temperature, pressure 0.1MPa,
Catalyst quality air speed 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
Operating pressure is 1.0MPa, and liquid-gas ratio is 325L/m3, absorbent includes benzene,toluene,xylene, and absorption tower ethylene is inhaled
Yield is 58.6%, without propylene in absorption tail gas.Aromatic hydrocarbons conversion separative element adopts traditional toluene disproportionation and transalkylation technology,
And xylene isomerization reaction device is set the o-Dimethylbenzene and meta-xylene in mixed xylenes is converted into xylol.From
The part toluene of aromatic hydrocarbons conversion separative element as supplementing absorbent 10a, absorption tower, desorber, benzene column and toluene tower it
Between circulate.The benzene and ethylene yield of the embodiment is close to equimolar, and product is that ethylbenzene yield is 3.82kmol/hr, and dimethylbenzene is produced
Measure as 8.38kmol/hr.
【Embodiment 2】
Technological process as shown in Figure 1, flow feed for the methanol of 140kmol/hr and react in alcohol ether aromatization reactor,
Using containing Zn 1.2% ZSM-5 alcohol ether aromatized catalysts, 550 DEG C of alcohol ether aromatization temperature, pressure 0.2MPa,
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
Operating pressure is 3MPa, and liquid-gas ratio is 152L/m3, absorbent includes benzene,toluene,xylene, absorption tower ethylene absorption
Rate is 61.3%, without propylene in absorption tail gas.Aromatic hydrocarbons conversion separative element adopts traditional toluene disproportionation and transalkylation technology, and
Xylene isomerization reaction device is set the o-Dimethylbenzene and meta-xylene in mixed xylenes is converted into xylol.The enforcement
The benzene and ethylene yield of example is close to equimolar, and it is 3.50kmol/hr that product is ethylbenzene yield, and diformazan benzene yield is 9.87kmol/hr.
【Embodiment 3】
Technological process as shown in Figure 1, flow feed for the dimethyl ether of 70kmol/hr and react in alcohol ether aromatization reactor,
Using the ZSM-5 alcohol ether aromatized catalysts containing Zn 7% and Cu 2%, 600 DEG C of alcohol ether aromatization temperature, pressure
0.4MPa, catalyst quality air speed 3hr-1.Alcohol ether aromatization products composition in based on carbon-based mass fraction comprising 9% ethylene,
3% benzene, 31% dimethylbenzene.Light dydrocarbon aromatization reaction temperature is 600 DEG C, pressure 0.1MPa, catalyst quality air speed 2.5hr-1。
Absorption tower operating pressure is 1.5MPa, and liquid-gas ratio is 233L/m3, absorbent includes benzene,toluene,xylene, absorption tower
Ethylene absorption rate is 65.7%, without propylene in absorption tail gas.Aromatic hydrocarbons conversion separative element is using traditional toluene disproportionation and transalkylation
Technology, and xylene isomerization reaction device is set the o-Dimethylbenzene and meta-xylene in mixed xylenes is converted into xylol.
The benzene and ethylene yield of the embodiment is close to equimolar, and product is that ethylbenzene yield is 4.46kmol/hr, and diformazan benzene yield is
9.43kmol/hr。
【Embodiment 4】
Technological process as shown in Figure 1, flow feed for the dimethyl ether of 70kmol/hr and react in alcohol ether aromatization reactor,
Wherein methanol volume fraction is 44%, is reacted in alcohol ether aromatization reactor, using the virtue of the ZSM-5 alcohol ethers containing Ga 3.6%
Structure catalyst, 480 DEG C of alcohol ether aromatization temperature, pressure 0.3MPa, catalyst quality air speed 2hr-1.Alcohol ether aromatization
Comprising 7% ethylene, 1% benzene, 32% dimethylbenzene based on carbon-based mass fraction in change product composition.Light dydrocarbon aromatization reaction temperature
For 650 DEG C, pressure 1MPa, catalyst quality air speed 0.5hr-1.Absorption tower operating pressure is 2MPa, and liquid-gas ratio is 182L/m3,
Absorbent includes benzene,toluene,xylene, and absorption tower ethylene absorption rate is 57.6%, without propylene in absorption tail gas.Aromatic hydrocarbons is converted
Separative element is using traditional toluene disproportionation and transalkylation technology, and arranges xylene isomerization reaction device in mixed xylenes
O-Dimethylbenzene and meta-xylene be converted into xylol.The benzene and ethylene yield of the embodiment is close to equimolar, and product is second
Benzene yield is 4.21kmol/hr, and diformazan benzene yield is 9.589kmol/hr.
【Embodiment 5】
Technological process as shown in Figure 1, flow feed for the methanol of 140kmol/hr and react in alcohol ether aromatization reactor,
Using containing Zn 7% ZSM-5 alcohol ether aromatized catalysts, 500 DEG C of alcohol ether aromatization temperature, pressure 0.5MPa,
Catalyst quality air speed 4hr-1.Alcohol ether aromatization products composition in based on carbon-based mass fraction comprising 10% ethylene, 5% benzene,
26% dimethylbenzene.Light dydrocarbon aromatization reaction temperature is 550 DEG C, pressure 0.7MPa, catalyst quality air speed 0.1hr-1.Absorb
Tower operating pressure is 0.5MPa, and liquid-gas ratio is 450L/m3, absorbent includes benzene,toluene,xylene, absorption tower ethylene
Absorbance is 67.2%, and in absorbing tail gas, propylene volume fraction is 0.01%.Aromatic hydrocarbons conversion separative element is using traditional toluene disproportionation
With transalkylation technology, and xylene isomerization reaction device is set the o-Dimethylbenzene in mixed xylenes and meta-xylene are converted
For xylol.The part toluene of separative element is converted as supplementing absorbent 10a from aromatic hydrocarbons, absorption tower, desorber,
Circulate between benzene column and toluene tower.The benzene and ethylene yield of the embodiment is close to equimolar, and product ethylbenzene yield is
2.86kmol/hr, diformazan benzene yield are 8.77kmol/hr.
【Embodiment 6】
Technological process as shown in Figure 1, flow feed for the methanol of 140kmol/hr and react in alcohol ether aromatization reactor,
Using with 4 identical catalyst of embodiment and reaction condition, aromatic hydrocarbons conversion separative element adopts methylbenzene shape selective disproportionation and heavy aromatics
Lighting combination technique, and xylene isomerization reaction device is set the o-Dimethylbenzene in mixed xylenes and meta-xylene conversion
For xylol.Absorption tower operating pressure is 1.5MPa, and liquid-gas ratio is 247L/m3, absorbent include benzene, toluene, two
Toluene, absorption tower ethylene absorption rate is 51.7%, without propylene in absorption tail gas.The benzene and ethylene yield of the embodiment are close to etc. and to rub
You, product ethylbenzene yield is 4.76kmol/hr, and diformazan benzene yield is 9.26kmol/hr.
【Embodiment 7】
Technological process as shown in Figure 1, flow feed for the methanol of 140kmol/hr and react in alcohol ether aromatization reactor,
Using with 5 identical catalyst of embodiment and reaction condition, aromatic hydrocarbons conversion separative element adopts methylbenzene shape selective disproportionation and benzene carbon nine
Transalkylation combination technique, and xylene isomerization reaction device is set the o-Dimethylbenzene and meta-xylene in mixed xylenes turn
Turn to xylol.Absorption tower operating pressure is 2.5MPa, and liquid-gas ratio is 156L/m3, absorbent include benzene, toluene,
Dimethylbenzene, absorption tower ethylene absorption rate is 69.8%, without propylene in absorption tail gas.The benzene and ethylene yield of the embodiment are close to etc.
Mole, product ethylbenzene yield is 2.77kmol/hr, and diformazan benzene yield is 8.83kmol/hr.
【Embodiment 8】
Technological process as shown in Figure 1, flow feed for the methanol of 140kmol/hr and react in alcohol ether aromatization reactor,
Using with 5 identical catalyst of embodiment and reaction condition, aromatic hydrocarbons conversion separative element adopts methylbenzene shape selective disproportionation and benzene carbon nine
Transalkylation combination technique, and xylene isomerization reaction device is set the o-Dimethylbenzene and meta-xylene in mixed xylenes turn
Turn to xylol.Absorption tower operating pressure is 0.3MPa, and liquid-gas ratio is 500L/m3, absorbent include benzene, toluene,
Dimethylbenzene, absorption tower ethylene absorption rate is 32.2%, and in absorbing tail gas, propylene content is 2.1vol%.The embodiment cannot be obtained
Matching magnitude benzene and ethylene, product ethylbenzene yield be 1.96kmol/hr, diformazan benzene yield be 8.83kmol/hr, by-product second
Alkene 0.77kmol/hr.
【Comparative example】
Patent CN201110024191 disclosed embodiment shows toluene, dimethylbenzene and C in methanol aromatic product10Aromatic hydrocarbons
Total content be 20～25%.Xylene content obtained in this method is 25～35%, toluene, dimethylbenzene and C10Aromatic hydrocarbons it is total
Content is higher than then 40%.In patent CN201110024191 disclosed embodiment, the mol 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 (10)
1. a kind of method of alcohol ether dimethylbenzene coproduction ethylbenzene, comprises the following steps：1) reaction raw materials are anti-in alcohol ether aromatisation
Alcohol ether aromatization products are converted in answering device；2) alcohol ether aromatization products be separated in separative element gas phase I, oil phase I and
Water phase；3) gas phase I sends into absorption tower absorption part carbon two and whole carbon three and above component, obtains and absorbs tail gas and absorption
Liquid, absorbs tail gas and sends into 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 shares
Logistics, sub- stream I return to absorption tower as absorbent, and sub- stream I I sends into aromatic hydrocarbons conversion separative element；5) lighter hydrocarbons go gently
Hydrocarbon aromatizing reactor is converted into light-hydrocarbon aromatized product；6) light-hydrocarbon aromatized product Jing gas-liquid separator separates are gas phase II
With oil phase II, gas phase II return absorption tower；7) oil phase I and oil phase II send into aromatic hydrocarbons conversion separative element obtain non-aromatic, benzene,
Dimethylbenzene and heavy aromatics, benzene send into Benzene Device.
2. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that the alcohol ether aromatisation
Product is based on carbon-based mass fraction comprising 5～10% ethylene, 0.5～5% benzene, 25～35% dimethylbenzene.
3. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that the alcohol ether aromatisation
The reaction condition of reactor is：450～600 DEG C of reaction temperature, 0.1～0.5MPA of reaction pressure, reaction mass air speed
0.5～4HR-1。
4. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that the absorption tower operation
Pressure is 0.5～3MPa, and liquid-gas ratio is 150～450L/m3。
5. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that inhale in the absorption tower
Receive agent and contain benzene,toluene,xylene and C9 +At least one in component.
6. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that absorb propylene in tail gas
Volume fraction is not more than 2%.
7. the method for alcohol ether dimethylbenzene coproduction ethylbenzene according to claim 1, it is characterised in that described light-hydrocarbon aromatized
The reaction condition of reactor is：500～650 DEG C of reaction temperature, 0.1～1MPA of reaction pressure, reaction mass 0.1～3HR of air speed-1。
8. according to any one of claim 1～7 alcohol ether dimethylbenzene coproduction ethylbenzene method, it is characterised in that the virtue
Hydrocarbon conversion separative element includes toluene disproportionation and alkyl transfering process device, xylene isomerization process device.
9. according to any one of claim 1～7 alcohol ether dimethylbenzene coproduction ethylbenzene method, it is characterised in that the virtue
Hydrocarbon conversion separative element includes methylbenzene shape selective disproportionation process unit, heavy aromatics lighting process unit, xylene isomerization process
Device.
10. according to any one of claim 1～7 alcohol ether dimethylbenzene coproduction ethylbenzene method, it is characterised in that the virtue
Hydrocarbon conversion separative element includes methylbenzene shape selective disproportionation process unit, nine alkyl transfering process device of benzene carbon, xylene isomerization chemical industry
Process and equipment.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109694305A (en) * | 2017-10-20 | 2019-04-30 | 中国石油化工股份有限公司 | The method that methanol converts dimethylbenzene coproduction ethylbenzene and isopropylbenzene processed |
| CN111377785A (en) * | 2018-12-28 | 2020-07-07 | 中国石油天然气股份有限公司 | Method for producing aromatic hydrocarbon from methanol |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3911041A (en) * | 1974-09-23 | 1975-10-07 | Mobil Oil Corp | Conversion of methanol and dimethyl ether |
| CN1075707A (en) * | 1992-02-19 | 1993-09-01 | 先进提取技术有限公司 | Reclaim the absorption process of ethene and hydrogen |
| CN101333143A (en) * | 2008-07-25 | 2008-12-31 | 北京惠尔三吉绿色化学科技有限公司 | Method for producing arene from petroleum cracking dry gas |
| CN101486624A (en) * | 2009-02-19 | 2009-07-22 | 山东科技大学 | Complexing recycling process for dilute ethylene suspension bed |
| CN101602643A (en) * | 2009-07-24 | 2009-12-16 | 中国海洋石油总公司 | A kind of methyl alcohol/dimethyl ether conversion is produced the method for ethylene and propylene and co-producing p-Xylol |
| CN101602648A (en) * | 2009-07-24 | 2009-12-16 | 中国海洋石油总公司 | A kind of methyl alcohol/dimethyl ether conversion prepares the method for p-Xylol |
| CN102134178A (en) * | 2011-01-21 | 2011-07-27 | 清华大学 | Device and method for preparing ethylbenzene by catalytic conversion of alcohol ether |
| CN103752346A (en) * | 2013-12-09 | 2014-04-30 | 中国科学院山西煤炭化学研究所 | Catalyst for aromatization of low-carbon mixed hydrocarbons in Fischer-Tropsch synthesis tail gas and its preparation method and use |
| CN103772125A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Method for preparing ethylbenzene by using refinery dry gas as raw material |
| CN103864565A (en) * | 2014-03-20 | 2014-06-18 | 华电煤业集团有限公司 | System and method of preparing paraxylene by alcohol/ether conversion |
| CN106608805A (en) * | 2015-10-23 | 2017-05-03 | 中国石油化工股份有限公司 | C3 fraction liquid phase selective hydrogenation method |
| CN106608804A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Method for removing oxygen from oxygen-containing light hydrocarbons |
-
2015
- 2015-10-22 CN CN201510690223.XA patent/CN106608786B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3911041A (en) * | 1974-09-23 | 1975-10-07 | Mobil Oil Corp | Conversion of methanol and dimethyl ether |
| CN1075707A (en) * | 1992-02-19 | 1993-09-01 | 先进提取技术有限公司 | Reclaim the absorption process of ethene and hydrogen |
| CN101333143A (en) * | 2008-07-25 | 2008-12-31 | 北京惠尔三吉绿色化学科技有限公司 | Method for producing arene from petroleum cracking dry gas |
| CN101486624A (en) * | 2009-02-19 | 2009-07-22 | 山东科技大学 | Complexing recycling process for dilute ethylene suspension bed |
| CN101602643A (en) * | 2009-07-24 | 2009-12-16 | 中国海洋石油总公司 | A kind of methyl alcohol/dimethyl ether conversion is produced the method for ethylene and propylene and co-producing p-Xylol |
| CN101602648A (en) * | 2009-07-24 | 2009-12-16 | 中国海洋石油总公司 | A kind of methyl alcohol/dimethyl ether conversion prepares the method for p-Xylol |
| CN102134178A (en) * | 2011-01-21 | 2011-07-27 | 清华大学 | Device and method for preparing ethylbenzene by catalytic conversion of alcohol ether |
| CN103772125A (en) * | 2012-10-25 | 2014-05-07 | 中国石油化工股份有限公司 | Method for preparing ethylbenzene by using refinery dry gas as raw material |
| CN103752346A (en) * | 2013-12-09 | 2014-04-30 | 中国科学院山西煤炭化学研究所 | Catalyst for aromatization of low-carbon mixed hydrocarbons in Fischer-Tropsch synthesis tail gas and its preparation method and use |
| CN103864565A (en) * | 2014-03-20 | 2014-06-18 | 华电煤业集团有限公司 | System and method of preparing paraxylene by alcohol/ether conversion |
| CN106608804A (en) * | 2015-10-22 | 2017-05-03 | 中国石油化工股份有限公司 | Method for removing oxygen from oxygen-containing light hydrocarbons |
| CN106608805A (en) * | 2015-10-23 | 2017-05-03 | 中国石油化工股份有限公司 | C3 fraction liquid phase selective hydrogenation method |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109694305A (en) * | 2017-10-20 | 2019-04-30 | 中国石油化工股份有限公司 | The method that methanol converts dimethylbenzene coproduction ethylbenzene and isopropylbenzene processed |
| CN109694305B (en) * | 2017-10-20 | 2021-12-28 | 中国石油化工股份有限公司 | Method for preparing dimethylbenzene and co-producing ethylbenzene and isopropylbenzene by methanol conversion |
| CN111377785A (en) * | 2018-12-28 | 2020-07-07 | 中国石油天然气股份有限公司 | Method for producing aromatic hydrocarbon from methanol |
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