CN104557363A - Reaction device for preparing ethylene, propylene and arene by methyl alcohol and/or dimethyl ether transformation and reaction method of reaction device - Google Patents

Reaction device for preparing ethylene, propylene and arene by methyl alcohol and/or dimethyl ether transformation and reaction method of reaction device Download PDF

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CN104557363A
CN104557363A CN201310512279.7A CN201310512279A CN104557363A CN 104557363 A CN104557363 A CN 104557363A CN 201310512279 A CN201310512279 A CN 201310512279A CN 104557363 A CN104557363 A CN 104557363A
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reactor
reaction
propylene
methyl alcohol
conversion zone
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CN104557363B (en
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李晓红
王菊
俞志楠
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

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Abstract

The invention relates to a reaction device for preparing ethylene, propylene and arene by methyl alcohol and/or dimethyl ether transformation and a reaction method of the reaction device, and mainly aims at solving the problem of low yield of ethylene, propylene and arene in the prior art. The reaction device comprises a reactor (1), a regenerator (2) and a stripper (3); a raw material (6) enters a first reaction segment (12) of the first reactor (1); a circulating material (7) enters a second reaction segment (14) of the reactor (1) and reacts with a catalyst in a contact manner; the generated reaction product and a carbon deposit catalyst enter the stripper (3); the stripped carbon deposit catalyst enters the regenerator (2) to regenerate through a regeneration inclined pipe (4); and the regenerated catalyst enters the reactor (1) through a regeneration inclined pipe (5), the problem is relatively well solved; and the reaction device and the reaction method can be applied to industrial production of ethylene, propylene and arene.

Description

The reaction unit of methyl alcohol and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons and reaction method thereof
Technical field
The present invention relates to reaction unit and the reaction method thereof of a kind of methyl alcohol and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons.
Background technology
Ethene, propylene and aromatic hydrocarbons (especially triphen, benzene Benzene, toluene Toluene, dimethylbenzene Xylene, i.e. BTX) are important basic organic synthesis raw materials.By the driving of downstream derivative thing demand, the market requirement sustainable growth of ethene, propylene and aromatic hydrocarbons.
The steam cracking process being raw material with liquid hydrocarbon (as petroleum naphtha, diesel oil, secondary processing oil) is the main production of ethene, propylene and aromatic hydrocarbons.This technique belongs to petroleum path production technology, and in recent years, the supply limited due to petroleum resources and higher price, raw materials cost constantly increases.The factor be subject to, alternative materials is prepared ethene, propylene and aromatic hydrocarbons technology and is caused and pay close attention to more and more widely.Wherein, for coal-based methanol, dme raw material, due to rich coal resources in China, become a kind of important Chemical Manufacture raw material just gradually, become the important supplement of petroleum.Therefore, consider with methyl alcohol and/or dme for raw material prepares ethene, propylene and aromatic hydrocarbons.
In various existing methyl alcohol, dimethyl ether catalysis transformation technology, the product of methanol/dimethyl ether conversion aromatic hydrocarbons comprises ethene, propylene and aromatic hydrocarbons simultaneously.This technology sees the people (Journal of Catalysis, 1977,47,249) such as the Chang of Mobil company in 1977 at first and reports on ZSM-5 molecular sieve catalyzer methyl alcohol and oxygenatedchemicals transforms the method preparing the hydrocarbon polymers such as aromatic hydrocarbons.1985, Mobil company is in its US Patent No. 1590321 of applying for, disclose the result of study of methyl alcohol, dimethyl ether conversion aromatic hydrocarbons first, this research adopt phosphorous be 2.7 % by weight ZSM-5 molecular sieve be catalyzer, temperature of reaction is 400 ~ 450 DEG C, methyl alcohol, dme air speed 1.3 (Grams Per Hour)/gram catalyzer.
Relevant report and the patent in this field are more, but the object product of most of technology is aromatic hydrocarbons, and ethene, propylene belong to by product, and yield is low.Such as, patent in the agent of Methanol arenes catalytic: Chinese patent CN102372535, CN102371176, CN102371177, CN102372550, CN102372536, CN102371178, CN102416342, CN101550051, US Patent No. 4615995, US2002/0099249A1 etc.Such as, patent in Methanol aromatics process: US Patent No. 4686312, Chinese patent ZL101244969, ZL1880288, CN101602646, CN101823929, CN101671226, CN102199069, CN102199446, CN1880288 etc.
In addition, other products such as co-producing light olefins, the gasoline while that technological line being Methanol aromatic hydrocarbons disclosed in some patent, as patent CN102775261, CN102146010, CN102531821, CN102190546, CN102372537 etc.
Wherein, disclosed in patent CN102775261, Multi-function methanol working method and device utilize preparing low carbon olefin hydrocarbon with methanol, gasoline, aromatic hydrocarbons.The method adopts two-step approach production technique, the first step methanol feedstock produces low-carbon alkene under special-purpose catalyst 1 acts on, reaction gas containing low-carbon alkene after heat exchange, chilling, carrying out washing treatment, is synthesized aromatic hydrocarbons and or gasoline by second step under the effect of special-purpose catalyst 2.The reactor of two reaction process can be fixed bed or fluidized-bed.The method adopts two-step approach, and technical process is complicated.
Take methyl alcohol as the technique of raw material production low-carbon alkene and arene parallel cogeneration gasoline disclosed in patent CN102146010.Be raw material with methyl alcohol and adopt molecular sieve catalyst to produce low-carbon alkene and arene parallel cogeneration gasoline through methyl alcohol alkylation reaction and aromatization.The reactor of methyl alcohol alkylation reaction and aromatization is various types of fixed-bed reactor, pressure 0.01 ~ 0.5 MPa, temperature 180 ~ 600 DEG C.Total liquid yield is greater than 70 % by weight, and triphen yield is greater than 90 % by weight.The method also adopts two reactors, and technical process is complicated.
Be the method for the co-fed production low-carbon alkene of methyl alcohol and petroleum naphtha and/or aromatic hydrocarbons disclosed in patent CN102531821, adopt the ZSM-5 catalyzer of load 2.2 ~ 6.0 % by weight La and 1.0 ~ 2.8 % by weight P, fixed-bed reactor or fluidized-bed reactor can be adopted.Temperature of reaction is 550 ~ 670 DEG C, air speed 1.0 ~ 5 (Grams Per Hour)/gram catalyzer.The triolefin yield of the method is higher, but BTX yield is low, only has 5 ~ 17 % by weight.
Patent CN102372537 and CN102190546 discloses the method for preparing propylene by methanol transformation and aromatic hydrocarbons.These two patents develop on the basis of preparing propylene by methanol transformation technology, and propylene is the product of argument, and aromatics yield is lower.
The low problem of ethene, propylene and aromatics yield is all there is in above-mentioned patented technology.Propose technical scheme to the property of the present invention is directed to, solve the problems referred to above.
Summary of the invention
One of technical problem to be solved by this invention is the technical problem that ethene in prior art, propylene and aromatics yield are low, provides the reaction unit of a kind of methyl alcohol and/or dimethyl ether conversion ethene and propylene and aromatic hydrocarbons.This system has ethene, propylene, advantage that aromatics yield is high.
Two of technical problem to be solved by this invention is to provide a kind of reaction method corresponding with one of technical solution problem.
For one of solving the problem, the technical solution used in the present invention is as follows: the reaction unit of a kind of methyl alcohol and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, comprises reactor 1, revivifier 2, stripper 3; Reactor 1 is the first conversion zone 12, First Transition section 13, second conversion zone 14, second transition section 15, the 3rd conversion zone 16 from bottom to up according to this; It is inner that 3rd conversion zone 14 is positioned at stripper 3; The height of reactor first conversion zone 12 accounts for 17 ~ 70% of reactor 1 total height; The diameter ratio of the second conversion zone 14 diameter and the first conversion zone 12 is 0.3 ~ 2:1, and it highly accounts for 20 ~ 75% of reactor 1 total height; The diameter ratio of the 3rd conversion zone 16 diameter and the first conversion zone 12 is 0.3 ~ 1:1, and it highly accounts for 3 ~ 5% of reactor 1 total height; Raw material 6 enters reactor 1 first conversion zone 12, recycle stock 7 enters reactor 1 second conversion zone 14 and catalyst exposure reaction.
In technique scheme, under maximum ethene, propylene operator scheme, the height of reactor first conversion zone 12 accounts for 40 ~ 70% of total reactor height; The diameter ratio of the second conversion zone 14 diameter and the first conversion zone 12 is 0.3 ~ 1:1, and it highly accounts for 20 ~ 50% of total reactor height; The diameter ratio of the 3rd conversion zone 16 diameter and the first conversion zone 12 is 0.3 ~ 1:1, and it highly accounts for 3 ~ 5% of total reactor height.Under maximum aromatic hydrocarbons operator scheme, the height of reactor first conversion zone 12 accounts for 17 ~ 40% of total reactor height; The diameter ratio of the second conversion zone 14 diameter and the first conversion zone 12 is 1 ~ 2:1, and it highly accounts for 50 ~ 75% of total reactor height; The diameter ratio of the 3rd conversion zone 16 diameter and the first conversion zone 12 is 0.3 ~ 1:1, and it highly accounts for 3 ~ 5% of total reactor height.Under coproduction ethene, propylene and aromatic hydrocarbons pattern, the height of reactor first conversion zone 12 accounts for 30 ~ 60% of total reactor height; The diameter ratio of the second conversion zone 14 diameter and the first conversion zone 12 is 0.3 ~ 2:1, and it highly accounts for 30 ~ 65% of total reactor height; The diameter ratio of the 3rd conversion zone 16 diameter and the first conversion zone 12 is 0.3 ~ 1:1, and it highly accounts for 3 ~ 5% of total reactor height.
In technique scheme, the total height of reactor First Transition section 13 and the second transition section 15 accounts for 5% of reactor 1 total height.
In technique scheme, raw material 6 enters the first conversion zone 12 of reactor 1, and recycle stock 7 enters the second conversion zone 14 and the catalyst exposure reaction of reactor 1; The reaction product generated and carbon deposited catalyst enter stripper 3, and the carbon deposited catalyst after stripping enters revivifier 2 through inclined tube 4 to be generated and regenerates, and the catalyzer after regeneration enters reactor first conversion zone 12 through regenerator sloped tube 5.
In technique scheme, reactor 1, for being converted into based on the product of ethene, propylene and aromatic hydrocarbons by the reaction of raw material 6, recycle stock 7 and catalyst exposure; Revivifier 2, removes the coke on carbon deposited catalyst for the mode by burning; Stripper 3, goes out the product that carbon deposited catalyst carries for stripping.
In technique scheme, reactor 1 inside or outer setting heat collector, heat collector height accounts for 30% ~ 95% of height for reactor; Revivifier 2 inside or outer setting heat collector, heat collector height accounts for 30% ~ 80% of revivifier height.
In technique scheme, revivifier 2 and stripper 3 inside are equipped with one group of gas-solid cyclone separator, are 1 ~ 3 grade.
For solve the problem two, the technical solution used in the present invention is as follows: the reaction method of a kind of methyl alcohol and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, adopts above-mentioned reaction unit, and described reaction method comprises following step:
A) raw material 6 enters the first conversion zone 12 of reactor 1, and recycle stock 7 is at the second conversion zone 14 of reactor 1, and catalyst exposure reaction, formation reaction product and carbon deposited catalyst;
B) reaction product and carbon deposited catalyst enter stripper 3, carbon deposited catalyst contacts stripping with stripping fluid 9, carbon deposited catalyst after the stripping after product 8 obtained and stripping, stripped product 8 is separated after carbon deposited catalyst through gas-solid cyclone separator and enters subsequent separation system;
C) carbon deposited catalyst after stripping enters revivifier 2 through inclined tube 4 to be generated and to contact with regenerating medium 10 and burn, and obtains the catalyzer after regenerating and flue gas 11;
D) catalyzer after regeneration enters reactor 1 through regenerator sloped tube 5;
E) part ethane and/or propane and/or C4 and/or C5 and/or C6 is non-aromatic proceeds reaction as recycle stock 7 in the product be separated through separation system, all the other are using the product of ethene, propylene, BTX aromatics as output of products system.
In technique scheme, raw material 6 is methyl alcohol or dme or both mixtures, particular methanol.
In technique scheme, in raw material 6, the mass percentage of water is 0 ~ 30 % by weight, preferably lower than 10 % by weight.
In technique scheme, the temperature of reactor 1 is 400 ~ 550 DEG C, the weight space velocity of raw material 6 is 2 ~ 10 (Grams Per Hours)/gram catalyzer, be 0 ~ 0.5 MPa in gauge pressure reaction pressure, the mass ratio of catalyst recirculation amount and raw material 6 inlet amount is 3 ~ 40: 1, average gas superficial velocity 0.7 ~ 5.0 meter per second.Under maximum ethene, propylene operator scheme, temperature is 480 ~ 550 DEG C, the weight space velocity of raw material 6 is 4 ~ 10 (Grams Per Hours)/gram catalyzer, be 0 ~ 0.3 MPa in gauge pressure reaction pressure, the mass ratio of catalyst recirculation amount and raw material 6 inlet amount is 10 ~ 40: 1, average gas superficial velocity 1.3 ~ 4.0 meter per second; Under maximum aromatic hydrocarbons operator scheme, temperature is 400 ~ 500 DEG C, the weight space velocity of raw material 6 is 2 ~ 4 (Grams Per Hours)/gram catalyzer, be 0.1 ~ 0.5 MPa in gauge pressure reaction pressure, the mass ratio of catalyst recirculation amount and raw material 6 inlet amount is 3 ~ 30: 1, average gas superficial velocity 0.7 ~ 1.3 meter per second; Under coproduction ethene, propylene and aromatic hydrocarbons pattern, temperature is 440 ~ 520 DEG C, the weight space velocity of raw material 6 is 2 ~ 7 (Grams Per Hours)/gram catalyzer, be 0.1 ~ 0.4 MPa in gauge pressure reaction pressure, the mass ratio of catalyst recirculation amount and raw material 6 inlet amount is 5 ~ 35: 1, average gas superficial velocity 0.7 ~ 2.3 meter per second.
In technique scheme, the temperature of revivifier 2 is 580 ~ 720 DEG C, preferably 600 ~ 700 DEG C, preferably 630 ~ 680 DEG C further.
In technique scheme, the charcoal on the catalyzer after regeneration, with the mass percent of catalyzer, content is lower than 0.1 % by weight.
In technique scheme, catalyst activity component is ZSM-5, ZSM-23, ZSM-11, beta-molecular sieve, Y molecular sieve or the mutual composite molecular screen formed, preferred ZSM-5; Carrier is kaolin, aluminum oxide, silicon-dioxide; The mass ratio of active ingredient and carrier is (10 ~ 50): (50 ~ 90), preferably (20 ~ 40): (60 ~ 80).
In technique scheme, catalyst cupport has one or more elements or oxide compound in Zn, Ag, P, Ga, Cu, Mn, Mg, preferred Zn, P; With the mass percent of catalyzer, the element content on a catalyst of load is 0.01 ~ 15 % by weight, preferably 0.02 ~ 8 % by weight.
In technique scheme, the active ingredient of catalyzer is selected from ZSM-5 molecular sieve, with the weight percent meter of catalyzer, and the Zn element of load 0.01 ~ 5 % by weight on catalyzer or oxide compound, the P element of 0.1 ~ 8 % by weight or oxide compound.
In technique scheme, stripping fluid 9 is water vapor or N 2or water vapor and N 2mixture, regenerating medium 10 is air or air and O 2mixture or air and N 2mixture.
The present invention passes through separation and the by product recycle of product in methyl alcohol and/or dimethyl ether catalysis conversion reaction process, realizes the object of the yield of maximum ethene, propylene and aromatic hydrocarbons.And reactor reducing, raw material of different nature and recycle stock can be made to react under reaction conditions suitable separately respectively, improve object product yield further.
Technical scheme provided by the invention, can select different reaction conditionss to realize maximum ethene, propylene, the operator scheme of maximum aromatic hydrocarbons production object different from three kinds, coproduction ethene, propylene and aromatic hydrocarbons.
Adopt technical scheme of the present invention, operate under maximum ethene, propylene pattern, raw material 6 is methyl alcohol, the temperature of reaction of reactor 1 is 500 DEG C, be 0.2 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 5 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 15:1, average gas superficial velocity 1.6 meter per second; Adopt Cu-ZSM-5 catalyzer; Ethene carbon base absorption rate is 25.7 % by weight, propylene carbon base absorption rate is 20.3 % by weight, aromatic hydrocarbons carbon base absorption rate be 40.2 % by weight, BTX carbon base absorption rates is 27.9 % by weight.
Adopt technical scheme of the present invention, operate under maximum aromatic hydrocarbons pattern, raw material 6 is methyl alcohol, the temperature of reaction of reactor 1 is 475 DEG C, be 0.25 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 2 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 7:1, average gas superficial velocity 0.7 meter per second; Adopt Zn-P-ZSM-5 catalyzer; Ethene carbon base absorption rate is 12.1 % by weight, propylene carbon base absorption rate is 7.8 % by weight, aromatic hydrocarbons carbon base absorption rate be 70.5 % by weight, BTX carbon base absorption rates is 55.4 % by weight.
Adopt technical scheme of the present invention, operate under coproduction ethene, propylene and aromatic hydrocarbons pattern, raw material 6 is methyl alcohol, the temperature of reaction of reactor 1 is 460 DEG C, be 0.2 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 3 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 12:1, average gas superficial velocity 1 meter per second; Adopt Zn-Mg-P-ZSM-5 catalyzer; Methanol feeding; Ethene carbon base absorption rate is 17.5 % by weight, propylene carbon base absorption rate is 12.0 % by weight, aromatic hydrocarbons carbon base absorption rate be 58.5 % by weight, BTX carbon base absorption rates is 45.7 % by weight.
Accompanying drawing explanation
Fig. 1 is reaction unit schematic diagram of the present invention,
Fig. 2 is the schematic diagram of reactor.
In Fig. 1 ~ 2,1 is reactor; 2 is revivifier; 3 is stripper; 4 is inclined tube to be generated; 5 is regenerator sloped tube; 6 is raw material; 7 is recycle stock; 8 is product; 9 is stripping fluid; 10 is regenerating medium; 11 is flue gas; 12 is reactor first conversion zone; 13 is reactor First Transition section; 14 is reactor second conversion zone; 15 is reactor second transition section; 16 is reactor the 3rd conversion zone.
Fig. 1 Raw 6 enters the first conversion zone 12 of reactor 1, and recycle stock 7 is at the second conversion zone 14 of reactor 1, and catalyst exposure reaction, formation reaction product and carbon deposited catalyst; Reaction product and carbon deposited catalyst enter stripper 3, and carbon deposited catalyst contacts stripping with stripping fluid 9, the carbon deposited catalyst after the stripping after product 8 obtained and stripping, and stripped product 8 is separated after carbon deposited catalyst through gas-solid cyclone separator and enters subsequent separation system; Carbon deposited catalyst after stripping enters revivifier 2 through inclined tube 4 to be generated and to contact with regenerating medium 10 and burn, and obtains the catalyzer after regenerating and flue gas 11; Catalyzer after regeneration enters reactor 1 through regenerator sloped tube 5; Part ethane and/or propane and/or C4 and/or C5 and/or C6 is non-aromatic proceeds reaction as recycle stock 7 in the product that separation system is separated, all the other are using the product of ethene, propylene, BTX aromatics as output of products system.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
Adopt device as shown in Figure 1.
The diameter of reactor first conversion zone is 4 meters, highly accounts for 50% of total reactor height; The diameter ratio of the second conversion zone diameter and the first conversion zone is 0.5:1, and it highly accounts for 40% of total reactor height; The diameter ratio of the 3rd conversion zone diameter and the second conversion zone is 0.3:1, and it highly accounts for 5% of total reactor height.The height that the height of First Transition section accounts for the 3% of total reactor height, second transition section accounts for 2% of total reactor height.Arrange heat collector outside reactor, heat collector height accounts for 85% of height for reactor.Arrange heat collector outside revivifier, heat collector height accounts for 80% of revivifier height.
The reaction conditions of reactor is: temperature is 500 DEG C, be 0.2 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 5 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 15: 1, average gas superficial velocity 1.3 meter per second.The temperature of revivifier is 650 DEG C.
Stripping fluid is water vapor.Regenerating medium is air.
Take methyl alcohol as raw material, water-content is 5 % by weight.The mass ratio that in recycle stock, Yi Wan ﹕ Bing Wan ﹕ C4 and C5 and C6 is non-aromatic is 2:3:5.Methyl alcohol and recycle stock charge-mass ratio are 15:1.
Adopt Cu-ZSM-5 catalyzer.
The preparation process of Cu-ZSM-5 catalyzer: by ZSM-5 molecular sieve, carrier and binding agent mechanically mixing, add suitable quantity of water, HCl, controls pH value and is not less than 3, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object ZSM-5 catalyst intermediate.The mass ratio of ZSM-5 molecular sieve and matrix is 4:6; The silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 25; Matrix is the mixture of kaolin and aluminium sesquioxide, and both mass ratioes are 7:3.Be the solution of 5% by Cu mass of ion percentage composition, with the weight ratio of solution and catalyzer for 1.74:1 floods, at 120 DEG C dry 5 hours, then put into retort furnace roasting at 550 DEG C and within 6 hours, be prepared into the Cu-ZSM-5 catalyzer that Cu constituent content is 8 % by weight.
Reaction result is in table 1.
 
[embodiment 2]
Adopt device as shown in Figure 1.
The diameter of reactor first conversion zone is 1.5 meters, highly accounts for 17% of total reactor height; The diameter ratio of the second conversion zone diameter and the first conversion zone is 2:1, and it highly accounts for 75% of total reactor height; The diameter ratio of the 3rd conversion zone diameter and the second conversion zone is 1:1, and it highly accounts for 3% of total reactor height.The height that the height of First Transition section accounts for the 2% of total reactor height, second transition section accounts for 3% of total reactor height.Arrange heat collector outside reactor, heat collector height accounts for 95% of height for reactor.Arrange heat collector outside revivifier, heat collector height accounts for 30% of revivifier height.
The reaction conditions of reactor is: temperature is 400 DEG C, be 0.5 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 4 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 3: 1, average gas superficial velocity 1.3 meter per second.The temperature of revivifier is 680 DEG C.
Stripping fluid is N 2.Regenerating medium is air.
Take methyl alcohol as raw material, water-content is 30 % by weight.The mass ratio that in recycle stock, Yi Wan ﹕ Bing Wan ﹕ C4 and C5 and C6 is non-aromatic is 1:1:8.Methyl alcohol and recycle stock charge-mass ratio are 12:1.
Adopt Ag-Y-ZSM-23 catalyzer.
The preparation process of Ag-Y-ZSM-23 catalyzer: by Y molecular sieve, ZSM-23 molecular screen, carrier and binding agent mechanically mixing, add suitable quantity of water, HCl, control pH value and be not less than 3, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object Y-ZSM-23 catalyst intermediate.The mass ratio of molecular sieve and matrix is 1:9; Y molecular sieve and ZSM-23 molecular screen mass ratio are 3:7; The silicoaluminophosphate molecular ratio of Y molecular sieve is 10; The silicoaluminophosphate molecular ratio of ZSM-23 molecular screen is 60; Matrix is the mixture of kaolin and aluminium sesquioxide, and both mass ratioes are 8:2.Be the solution of 1% by Ag mass of ion percentage composition, flood than for 0.1:1 with solution and catalyst weight, at 120 DEG C dry 5 hours, then put into retort furnace roasting at 550 DEG C and within 6 hours, be prepared into the Ag-Y-ZSM-23 catalyzer that Ag constituent content is 0.1 % by weight.
Reaction result is in table 1.
 
[embodiment 3]
Adopt device as shown in Figure 1.
The diameter of reactor first conversion zone is 6 meters, highly accounts for 70% of total reactor height; The diameter ratio of the second conversion zone diameter and the first conversion zone is 0.3:1, and it highly accounts for 20% of total reactor height; The diameter ratio of the 3rd conversion zone diameter and the second conversion zone is 0.3:1, and it highly accounts for 5% of total reactor height.The height that the height of First Transition section accounts for the 2.5% of total reactor height, second transition section accounts for 2.5% of total reactor height.Arrange heat collector in reactor, heat collector height accounts for 30% of height for reactor.Arrange heat collector in revivifier, heat collector height accounts for 30% of revivifier height.
The reaction conditions of reactor is: temperature is 550 DEG C, be 0 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 10 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 40: 1, average gas superficial velocity 4 meter per second.The temperature of revivifier is 580 DEG C.
Stripping fluid is water vapor.Regenerating medium is air and O 2mixture, volume ratio is 8: 2.
Take methyl alcohol as raw material, water-content is 10 % by weight.The mass ratio that in recycle stock, Bing Wan ﹕ C4 and C5 and C6 is non-aromatic is 2:8.Methyl alcohol and recycle stock charge-mass ratio are 10:1.
Adopt Ga-beta catalyst.
The preparation process of Ga-beta catalyst: by beta-molecular sieve, carrier and binding agent mechanically mixing, add suitable quantity of water, HCl, controls pH value and is not less than 4, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object beta catalyst intermediates.The mass ratio of beta-molecular sieve and matrix is 5:5; The silicoaluminophosphate molecular ratio of beta-molecular sieve is 20; Matrix is the mixture of kaolin, silicon-dioxide and aluminium sesquioxide, and the mass ratio of three is 7:1:2.Be the solution of 2% by Ga mass of ion percentage composition, flood than for 0.4:1 with solution and catalyst weight, at 120 DEG C dry 5 hours, then put into retort furnace roasting at 550 DEG C and within 6 hours, be prepared into the Ga-beta catalyst that Ga constituent content is 0.8 % by weight.
Reaction result is in table 1.
 
[embodiment 4]
Adopt device as shown in Figure 1.
The diameter of reactor first conversion zone is 3 meters, highly accounts for 31% of total reactor height; The diameter ratio of the second conversion zone diameter and the first conversion zone is 1.5:1, and it highly accounts for 60% of total reactor height; The diameter ratio of the 3rd conversion zone diameter and the second conversion zone is 0.5:1, and it highly accounts for 4% of total reactor height.The height that the height of First Transition section accounts for the 3% of total reactor height, second transition section accounts for 2% of total reactor height.Arrange heat collector outside reactor, heat collector height accounts for 60% of height for reactor.Arrange heat collector outside revivifier, heat collector height accounts for 70% of revivifier height.
The reaction conditions of reactor is: temperature is 500 DEG C, be 0.5 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 4 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 30: 1, average gas superficial velocity 1.3 meter per second.The temperature of revivifier is 700 DEG C.
Stripping fluid is water vapor and N 2mixture, volume ratio is 5: 5.Regenerating medium is air and N 2mixture, volume ratio is 9: 1.
Take dme as raw material.The mass ratio that in recycle stock, Yi Wan ﹕ C4 and C5 and C6 is non-aromatic is 3:7.Methyl alcohol and recycle stock charge-mass ratio are 14:1.
Adopt Mn-ZSM-11 catalyzer.
The preparation process of Mn-ZSM-11 catalyzer: by ZSM-11 molecular sieve, carrier and binding agent mechanically mixing, add suitable quantity of water, HCl, control pH value and be not less than 3, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object ZSM-11 catalyst intermediate.The mass ratio of ZSM-11 molecular sieve and matrix is 3:7; The silicoaluminophosphate molecular ratio of ZSM-11 molecular sieve is 50; Matrix is the mixture of kaolin and aluminium sesquioxide, and both mass ratioes are 7:3.Be the solution of 10% by Mn mass of ion percentage composition, with the weight ratio of solution and catalyzer for 1:1 floods, at 120 DEG C dry 5 hours, then put into retort furnace roasting at 550 DEG C and within 6 hours, be prepared into the Mn-ZSM-11 catalyzer that Mn constituent content is 9.09 % by weight.
Reaction result is in table 1.
 
[embodiment 5]
Adopt the device of embodiment 4.
The reaction conditions of reactor is: temperature is 475 DEG C, be 0.25 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 2 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 20: 1, average gas superficial velocity 0.7 meter per second.The temperature of revivifier is 630 DEG C.
Stripping fluid is water vapor.Regenerating medium is air and O 2mixture, volume ratio is 9: 1.
Take methyl alcohol as raw material, water-content is 15 % by weight.In recycle stock, the mass ratio of Yi Wan ﹕ propane is 5:5.Methyl alcohol and recycle stock charge-mass ratio are 16:1.
Adopt Zn-P-ZSM-5 catalyzer.
The preparation process of Zn-P-ZSM-5 catalyzer: by ZSM-5 molecular sieve, carrier and binding agent mechanically mixing, add suitable quantity of water, H 3pO 4, control pH value and be not less than 3, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object P-ZSM-5 catalyst intermediate.H 3pO 4the concentration of solution is 1 % by weight, and the weight ratio of solution and molecular sieve is 1.53:1.The mass ratio of ZSM-5 molecular sieve and matrix is 3.5:6.5; The silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 25; Matrix is the mixture of kaolin and aluminium sesquioxide, and both mass ratioes are 7:3.Be the solution of 5% by Zn mass of ion percentage composition, flood than for 0.6:1 with solution and P-ZSM-5 catalyst weight, drying 5 hours at 120 DEG C, put into retort furnace roasting 6 hours at 550 DEG C again, being prepared into Zn constituent content is 2.87 % by weight, and P element content is the Zn-P-ZSM-5 catalyzer of 1.48 % by weight.
Reaction result is in table 1.
 
[embodiment 6]
Adopt device as shown in Figure 1.
The diameter of reactor first conversion zone is 4 meters, highly accounts for 40% of total reactor height; The diameter ratio of the second conversion zone diameter and the first conversion zone is 0.8:1, and it highly accounts for 52% of total reactor height; The diameter ratio of the 3rd conversion zone diameter and the second conversion zone is 0.5:1, and it highly accounts for 3% of total reactor height.The height that the height of First Transition section accounts for the 2% of total reactor height, second transition section accounts for 3% of total reactor height.Arrange heat collector in reactor, heat collector height accounts for 90% of height for reactor.Arrange heat collector outside revivifier, heat collector height accounts for 50% of revivifier height.
The reaction conditions of reactor is: temperature is 520 DEG C, be 0.4 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 7 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 35: 1, average gas superficial velocity 2.3 meter per second.The temperature of revivifier is 600 DEG C.
Stripping fluid is water vapor and N 2mixture, volume ratio is 2: 8.Regenerating medium is air and O 2mixture, volume ratio is 5: 5.
Take methyl alcohol as raw material, water-content is 3 % by weight.The mass ratio that in recycle stock, Yi Wan ﹕ Bing Wan ﹕ C4 and C5 and C6 is non-aromatic is 3:3:4.Methyl alcohol and recycle stock charge-mass ratio are 12.5:1.
Adopt ZSM-5-beta catalyst.
The preparation process of ZSM-5-beta catalyst: by ZSM-5 molecular sieve, beta-molecular sieve, carrier and binding agent mechanically mixing, add suitable quantity of water, HCl, control pH value and be not less than 3, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object ZSM-5-beta catalysts.The mass ratio of ZSM-5 and beta-molecular sieve and matrix is 3.5: 6.5.The silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 38; The silicoaluminophosphate molecular ratio of beta-molecular sieve is 20; The mass ratio of ZSM-5 and beta-molecular sieve is 9:1.Matrix is the mixture of kaolin, silicon-dioxide and aluminium sesquioxide, and the mass ratio of three is 5:2:3.
Reaction result is in table 1.
 
[embodiment 7]
Adopt the device of embodiment 6.
The reaction conditions of reactor is: temperature is 440 DEG C, be 0.1 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 2 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 5: 1, average gas superficial velocity 0.9 meter per second.The temperature of revivifier is 720 DEG C.
Stripping fluid is water vapor.Regenerating medium is air and N 2mixture, volume ratio is 7: 3.
Take methyl alcohol as raw material, water-content is 7 % by weight.The mass ratio that in recycle stock, Yi Wan ﹕ Bing Wan ﹕ C4 and C5 and C6 is non-aromatic is 0.5:0.5:9.Methyl alcohol and recycle stock charge-mass ratio are 20:1.
Adopt Zn-Ag-P-ZSM-5 catalyzer.
The preparation process of Zn-Ag-P-ZSM-5 catalyzer: by ZSM-5 molecular sieve, carrier and binding agent mechanically mixing, add suitable quantity of water, H 3pO 4, control pH value and be not less than 3, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object P-ZSM-5 catalyst intermediate.H 3pO 4the concentration of solution is 2.5 % by weight, and the weight ratio of solution and molecular sieve is 2:1.The mass ratio of ZSM-5 molecular sieve and matrix is 3.5:6.5; The silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 28; Matrix is the mixture of kaolin and aluminium sesquioxide, and both mass ratioes are 8:2.Be 1% by Ag mass of ion percentage composition, Zn mass of ion percentage composition is the solution of 3%, flood than for 0.8:1 with solution and P-ZSM-5 catalyst weight, drying 5 hours at 120 DEG C, put into retort furnace roasting 6 hours at 550 DEG C again, being prepared into Zn constituent content is 2.32 % by weight, Ag constituent content is 0.78 % by weight, and P element content is the Zn-Ag-P-ZSM-5 catalyzer of 1.51 % by weight.
Reaction result is in table 1.
 
[embodiment 8]
Adopt device as shown in Figure 1.
The diameter of reactor first conversion zone is 4 meters, highly accounts for 50% of total reactor height; The diameter ratio of the second conversion zone diameter and the first conversion zone is 0.7:1, and it highly accounts for 42% of total reactor height; The diameter ratio of the 3rd conversion zone diameter and the second conversion zone is 0.4:1, and it highly accounts for 3% of total reactor height.The height that the height of First Transition section accounts for the 2.5% of total reactor height, second transition section accounts for 2.5% of total reactor height.Arrange heat collector outside reactor, heat collector height accounts for 90% of height for reactor.Arrange heat collector in revivifier, heat collector height accounts for 80% of revivifier height.
The reaction conditions of reactor is: temperature is 490 DEG C, be 0.2 MPa in gauge pressure reaction pressure, the weight space velocity of methyl alcohol is 2 (Grams Per Hours)/gram catalyzer, and the mass ratio of catalyst recirculation amount and methanol feeding amount is 35: 1, average gas superficial velocity 0.8 meter per second.The temperature of revivifier is 630 DEG C.
Stripping fluid is water vapor and N 2mixture, volume ratio is 8: 2.Regenerating medium is air and O 2mixture, volume ratio is 7: 3.
Take methyl alcohol as raw material.The mass ratio that in recycle stock, Yi Wan ﹕ Bing Wan ﹕ C4 and C5 and C6 is non-aromatic is 1:1:8.Methyl alcohol and recycle stock charge-mass ratio are 30:1.
Adopt Zn-Mg-P-ZSM-5 catalyzer.
The preparation process of Zn-Mg-P-ZSM-5 catalyzer: by ZSM-5 molecular sieve, carrier and binding agent mechanically mixing, add suitable quantity of water, H 3pO 4, control pH value and be not less than 3, slurry agitation evenly after at 500 DEG C spray shaping, make 60 ~ 300 object P-ZSM-5 catalyst intermediate.H 3pO 4the concentration of solution is 4 % by weight, and the weight ratio of solution and molecular sieve is 2:1.The mass ratio of ZSM-5 molecular sieve and matrix is 3:7; The silicoaluminophosphate molecular ratio of ZSM-5 molecular sieve is 32; Matrix is the mixture of kaolin and aluminium sesquioxide, and both mass ratioes are 7:3.Be 2% by Mg mass of ion percentage composition, Zn mass of ion percentage composition is the solution of 3%, flood than for 1:1 with solution and P-ZSM-5 catalyst weight, drying 5 hours at 120 DEG C, put into retort furnace roasting 6 hours at 550 DEG C again, being prepared into Zn constituent content is 2.86 % by weight, Mg constituent content is 1.9 % by weight, and P element content is the Zn-Mg-P-ZSM-5 catalyzer of 2.35 % by weight.
Reaction result is in table 1.
 
Table 1
Yield of ethene, % by weight Propene yield, % by weight Aromatics yield, % by weight
Embodiment 1 26.7 19.1 42.8
Embodiment 2 12.3 9.8 61.9
Embodiment 3 29.2 18.5 39.7
Embodiment 4 13.8 9.2 63.7
Embodiment 5 11.7 8.4 69.1
Embodiment 6 17.9 15.2 51.7
Embodiment 7 15.8 14.7 55
Embodiment 8 18.1 13.4 57.3

Claims (10)

1. a reaction unit for methyl alcohol and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, comprises reactor (1), revivifier (2), stripper (3); Reactor (1) is the first conversion zone (12), First Transition section (13), the second conversion zone (14), the second transition section (15), the 3rd conversion zone (16) from bottom to up according to this; It is inner that 3rd conversion zone (14) is positioned at stripper (3); The height of reactor first conversion zone (12) accounts for 17 ~ 70% of reactor (1) total height; The diameter ratio of the second conversion zone (14) diameter and the first conversion zone (12) is 0.3 ~ 2:1, and it highly accounts for 20 ~ 75% of reactor (1) total height; The diameter ratio of the 3rd conversion zone (16) diameter and the first conversion zone (12) is 0.3 ~ 1:1, and it highly accounts for 3 ~ 5% of reactor (1) total height; Raw material (6) reacts at reactor (1) second conversion zone (14) and catalyst exposure at reactor (1) first conversion zone (12), recycle stock (7).
2. the reaction unit of methyl alcohol according to claim 1 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, is characterized in that the total height of reactor First Transition section (13) and the second transition section (15) accounts for 5% of reactor (1) total height.
3. the reaction unit of methyl alcohol according to claim 1 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, it is characterized in that the reaction product that reactor (1) generates and carbon deposited catalyst enter stripper (3), carbon deposited catalyst after stripping enters revivifier (2) regeneration through inclined tube to be generated (4), and the catalyzer after regeneration enters reactor first conversion zone (12) through regenerator sloped tube (5).
4. the reaction unit of methyl alcohol according to claim 1 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, it is characterized in that reactor (1) inside or outer setting heat collector, heat collector height accounts for 30% ~ 95% of height for reactor; Revivifier (2) inside or outer setting heat collector, heat collector height accounts for 30% ~ 80% of revivifier height.
5. the reaction unit of methyl alcohol according to claim 1 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, is characterized in that revivifier (2) and stripper (3) inside are equipped with 1 ~ 3 grade of gas-solid cyclone separator.
6. a reaction method for methyl alcohol and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, adopt the reaction unit described in any one in claim 1 ~ 5, reaction method comprises following step:
A) raw material (6) enters first conversion zone (12) of reactor (1), and recycle stock (7) is at second conversion zone (14) of reactor (1), and catalyst exposure reaction, formation reaction product and carbon deposited catalyst;
B) reaction product and carbon deposited catalyst enter stripper (3), carbon deposited catalyst contacts stripping with stripping fluid (9), carbon deposited catalyst after the stripped product (8) obtained and stripping, stripped product (8) is separated after carbon deposited catalyst through gas-solid cyclone separator and enters subsequent separation system;
C) carbon deposited catalyst after stripping enters revivifier (2) through inclined tube to be generated (4) and to contact with regenerating medium (10) and burn, and obtains the catalyzer after regenerating and flue gas (11);
D) catalyzer after regeneration enters reactor (1) through regenerator sloped tube (5);
E) part ethane and/or propane and/or C4 and/or C5 and/or C6 is non-aromatic proceeds reaction as recycle stock (7) in the product be separated through separation system, all the other are using the product of ethene, propylene, BTX aromatics as output of products system.
7. the reaction method of methyl alcohol according to claim 6 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, it is characterized in that the temperature of reactor (1) is 400 ~ 550 DEG C, the weight space velocity of raw material (6) is 2 ~ 10 (Grams Per Hours)/gram catalyzer, be 0 ~ 0.5 MPa in gauge pressure reaction pressure, the mass ratio of catalyst recirculation amount and raw material (6) inlet amount is 3 ~ 40: 1, average gas superficial velocity 0.7 ~ 5.0 meter per second; The temperature of revivifier (2) is 580 ~ 720 DEG C, the charcoal on the catalyzer after regeneration, and with the mass percent of catalyzer, content is lower than 0.1 % by weight.
8. the reaction method of methyl alcohol according to claim 6 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, is characterized in that the active ingredient of catalyzer is ZSM-5, ZSM-23, ZSM-11, beta-molecular sieve, Y molecular sieve or the mutual composite molecular screen formed; Carrier is kaolin, aluminum oxide, silicon-dioxide; The mass ratio of active ingredient and carrier is (10 ~ 50): (50 ~ 90); Catalyst cupport has one or more elements or oxide compound in Zn, Ag, P, Ga, Cu, Mn, Mg, and with the mass percent of catalyzer, its content is 0.01 ~ 15 % by weight.
9. the reaction method of methyl alcohol according to claim 6 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, it is characterized in that raw material (6) is for methyl alcohol or dme or both mixtures, the mass percentage of water is 0.01 ~ 30 % by weight.
10. the reaction method of methyl alcohol according to claim 6 and/or dimethyl ether conversion ethene, propylene and aromatic hydrocarbons, is characterized in that stripping fluid (9) is for water vapor or N 2or water vapor and N 2mixture, regenerating medium (10) is air or air and O 2mixture or air and N 2mixture.
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109694297A (en) * 2017-10-20 2019-04-30 中国石油化工股份有限公司 The method for maintaining high arenes selectivity during methanol aromatic hydrocarbons
CN110818521A (en) * 2018-08-07 2020-02-21 中石化广州工程有限公司 Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102276398A (en) * 2010-06-11 2011-12-14 中国石油化工股份有限公司 Method for producing low-carbon olefin by using methanol as raw material
CN102463081A (en) * 2010-11-17 2012-05-23 中国石油化工股份有限公司 Reaction device for preparing low-carbon olefin

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102276398A (en) * 2010-06-11 2011-12-14 中国石油化工股份有限公司 Method for producing low-carbon olefin by using methanol as raw material
CN102463081A (en) * 2010-11-17 2012-05-23 中国石油化工股份有限公司 Reaction device for preparing low-carbon olefin

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109694297A (en) * 2017-10-20 2019-04-30 中国石油化工股份有限公司 The method for maintaining high arenes selectivity during methanol aromatic hydrocarbons
CN109694297B (en) * 2017-10-20 2022-02-01 中国石油化工股份有限公司 Method for maintaining high aromatic selectivity in process of preparing aromatic hydrocarbon from methanol
CN110818521A (en) * 2018-08-07 2020-02-21 中石化广州工程有限公司 Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound
CN110818521B (en) * 2018-08-07 2022-06-07 中石化广州工程有限公司 Device and method for preparing aromatic hydrocarbon and low-carbon olefin by using oxygen-containing compound

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