CN109694295A - The method of arenes selectivity is improved in methanol aromatic hydrocarbons reaction process - Google Patents
The method of arenes selectivity is improved in methanol aromatic hydrocarbons reaction process Download PDFInfo
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- C07—ORGANIC CHEMISTRY
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- 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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- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
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- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
- C07C2529/42—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 containing iron group metals, noble metals or copper
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Abstract
The present invention relates to a kind of methods that arenes selectivity is improved in methanol aromatic hydrocarbons reaction process, mainly solve the problems, such as that arenes selectivity is low in the prior art.The present invention sequentially enters the low temperature conversion area of the close phase section of fluidized-bed reactor, aromatization area by the raw material containing methanol, it is contacted with the catalyst for including ZSM-5 molecular sieve, generate the product stream including lighter hydrocarbons, aromatic hydrocarbons, technical solution into centrifugal station preferably solves the problems, such as this, can be used in the industrial production of aromatic hydrocarbons.
Description
Technical field
The present invention relates to a kind of methods that arenes selectivity is improved in methanol aromatic hydrocarbons reaction process.
Background technique
Aromatic hydrocarbons (especially triphen, benzene Benzene, toluene Toluene, dimethylbenzene Xylene, i.e. BTX) is important substantially
Organic synthesis raw material.By the driving of downstream derivative object demand, the market demand sustainable growth of aromatic hydrocarbons.
It is the main life of aromatic hydrocarbons with the steam cracking process of liquid hydrocarbon (such as naphtha, diesel oil, secondary operation oil) for raw material
Production. art.The technique belongs to petroleum path production technology, in recent years, due to the limited supply of petroleum resources and higher valence
Lattice, cost of material are continuously increased.By factor, alternative materials prepare aromatic hydrocarbons technology and cause to pay close attention to more and more widely.China's coal
Charcoal resource relative abundance.As in recent years efficient, long period catalyst for methanol is succeeded in developing with methanol device enlargement technology, coal
The production cost of base methanol and/or dimethyl ether is greatly lowered, this is methanol and/or dimethyl ether downstream product (alkene, aromatic hydrocarbons
Deng) production provide cheap raw material sources.Accordingly, it is considered to prepare aromatic hydrocarbons using methanol and/or dimethyl ether as raw material.
The technology initially see Chang of Mobil company in 1977 et al. (Journal of Catalysis, 1977,
47,249) methanol and its oxygenate conversion on ZSM-5 molecular sieve catalyst are reported and prepares the hydrocarbons such as aromatic hydrocarbons
Method.1985, Mobil company disclosed methanol, dimethyl ether turns in the United States Patent (USP) US1590321 of its application for the first time
Change the result of study of aromatic hydrocarbons processed, it is catalyst which, which uses the phosphorous ZSM-5 molecular sieve for 2.7 weight %, and reaction temperature is
400~450 DEG C, methanol, dimethyl ether air speed 1.3 (Grams Per Hour)/gram catalyst.
It is generally believed that methanol and/or dimethyl ether are first in acid catalysis during methanol and/or dimethyl ether are for aromatic hydrocarbons
Lower dehydration generates lower carbon number hydrocarbons, and lower carbon number hydrocarbons further occurs aromatization and obtains aromatic hydrocarbons.Therefore Chinese patent
200610012703.1、200910089698.8、201110024191.1、201210254472.0、201010261894.1、
201010116376.0, it 20100108008.1,201010146915.5 proposes to use two reactors, first reactor is anti-
The gas-phase product that should be obtained partly or entirely enters second reactor, and the reaction was continued.However, due to using two reactors, this
There are process flow complexity, cumbersome problems for a little patents.
Chinese patent 201010111821.4,200910090002.3,200810102684.0,200910135643.6,
200910089699.2 use a reactor, only one reaction zone of reactor, using single reaction temperature.Lower carbon number hydrocarbons virtue
The suitable reaction temperature of structureization reaction is higher than oxygenatedchemicals dehydration, is difficult to take into account two classes using single reaction temperature anti-
It answers.Oxygenatedchemicals higher than 500 DEG C at a temperature of, easily generation heat scission reaction generate low value-added methane, one oxidation
Carbon, while increasing coke content.To reduce the reaction of this part, reaction temperature is generally below 500 DEG C, and aromatization of low carbon hydrocarbon reacts
Suitable reaction temperature is higher than 500 DEG C, therefore the problem for causing such prior art arenes selectivity lower.
The present invention pointedly proposes technical solution, solves the above problem.
Summary of the invention
The technical problem to be solved by the present invention is to the low technical problems of prior art arenes selectivity, provide a kind of methanol
And/or the method that arenes selectivity is improved in dimethyl ether aromatic hydrocarbons reaction process.This method has the advantages that arenes selectivity is high.
The technical solution adopted by the invention is as follows: improving aromatic hydrocarbons in a kind of methanol and/or dimethyl ether aromatic hydrocarbons reaction process
Selectivity method, the raw material containing methanol and/or dimethyl ether sequentially enter the close phase section of fluidized-bed reactor low temperature conversion area,
Aromatization area, with include ZSM-5 molecular sieve catalyst contact, generate include lighter hydrocarbons, aromatic hydrocarbons product stream, into point
From workshop section；Wherein, low temperature conversion area height is the 20~40% of the close phase section total height of fluidized-bed reactor, aromatization
Area's height is the 60~80% of the close phase section total height of fluidized-bed reactor, and the reaction temperature in aromatization area is than low temperature conversion area
Reaction temperature it is 20~100 DEG C high；Propane/propylene mass ratio in low temperature conversion area outlet gaseous stream is less than 0.8, stream
Fluidized bed reactor exports C5 alkane/C5 alkene mass ratio in gaseous stream less than 1.2, and low temperature conversion area exports methanol conversion
Between 20~85%.
In above-mentioned technical proposal, it is preferable that wide bore distribution plate, low temperature are set between low temperature conversion area and aromatization area
The gaseous stream and catalyst of zone of transformation enter aromatization area by wide bore distribution plate.
In above-mentioned technical proposal, it is preferable that the decaying catalyst in aromatization area is at least divided into two-way, passes through all the way
It recycles inclined tube and returns to low temperature conversion area, enter regenerator all the way and regenerate, the catalyst after regeneration returns to aromatization area.
In above-mentioned technical proposal, it is preferable that the decaying catalyst in the aromatization area is divided into two-way, with weight
Meter, 5~25% return to low temperature conversion area by circulation inclined tube, and 75~95%, which enter regenerator, regenerates.
In above-mentioned technical proposal, it is preferable that the temperature in low temperature conversion area is 450~480 DEG C, highly accounts for the close phase section of reactor
The 25~38% of total height；The reaction temperature in aromatization area is 500~550 DEG C, highly accounts for the close phase section total height of reactor
62~75%.
In above-mentioned technical proposal, it is preferable that the temperature in low temperature conversion area is 450~470 DEG C.In one embodiment of the invention,
The temperature in low temperature conversion area is 460 DEG C.
In above-mentioned technical proposal, it is preferable that the reaction temperature in aromatization area is higher than the reaction temperature in low temperature conversion area
40~70 DEG C.In one embodiment of the invention, the reaction temperature in aromatization area is 40 DEG C higher than the reaction temperature in low temperature conversion area.
In above-mentioned technical proposal, it is preferable that the ratio that close phase section accounts for total reactor height is 40~70%.
In above-mentioned technical proposal, it is preferable that aromatization area internal catalyst bed floor density is 150~450 kilograms/cube
Meter, methanol quality air speed is 0.1~7 hour in fluidized-bed reactor-1；Reaction gauge pressure is 0~0.5 megapascal.
In above-mentioned technical proposal, it is preferable that lighter hydrocarbons logistics returns to the fluidized-bed reaction after centrifugal station is separated
The aromatization area of the close phase section of device.
In above-mentioned technical proposal, it is preferable that the carrier of catalyst is kaolin, aluminium oxide or silica；In catalyst
The mass ratio of active component and carrier is 10~50: 50~90.
In above-mentioned technical proposal, it is preferable that catalyst load has one or more elements in Zn, Ag, P, Ga, Cu, Mn, Mg
Or oxide, in terms of the weight percent of catalyst, weight content is 0.01~15%.
In above-mentioned technical proposal, it is preferable that be equipped with external heat collector or built-in heat collector in the low temperature conversion area, maintain
Low temperature conversion area temperature, the low temperature catalyst inclined tube of external heat collector and the connector of reactor are located at low temperature conversion area, built-in
Heat collector is located in low temperature conversion area, and built-in heat collector coil pipe height is the 30~100% of low temperature conversion area total height.
In the present invention, by the way that low temperature conversion area, aromatization area is arranged in the close phase section of reactor, methanol is first low
It is highly selective in warm zone of transformation to be converted into the lighter hydrocarbons such as alkene, by the temperature in regulation low temperature conversion area and aromatization area with
And height, control low temperature conversion area export the ratio between the propane/propylene in gaseous stream, reduce the generation of the side reactions such as hydrogen migration,
The alkene production quantity in low temperature conversion area is improved, then the logistics in low temperature conversion area enters aromatization area, in higher temperature
Lower generation aromatic hydrocarbons.Present inventors have surprisingly found that controlling C5 alkane/C5 alkene ratio of reactor outlet, can effectively control
The reaction selectivity of aromatic hydrocarbons is generated in aromatization area processed.Therefore, using method of the invention, by anti-to methanol aromatic hydrocarbons
The accurate control of process is answered, while according to the preferably preferable operating condition of reacting quintessence, substantially increasing arenes selectivity, is obtained
Preferable technical effect.
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]
A kind of method that arenes selectivity is improved in methanol aromatic hydrocarbons reaction process, it is anti-that methanol feedstock sequentially enters fluidized bed
Low temperature conversion area, the aromatization area for answering device, contact with the catalyst of Cu-ZSM-5 molecular sieve, and generating includes lighter hydrocarbons, aromatic hydrocarbons
Product stream, into centrifugal station；Wherein, low temperature conversion area height is the close phase section total height of fluidized-bed reactor
20%, aromatization area height is the 80% of fluidized-bed reactor total height, and the reaction temperature in aromatization area compares low temperature
The reaction temperature of zone of transformation is 20 DEG C high；It is equipped with external heat collector in the low temperature conversion area, maintains low temperature conversion area temperature, it is external
The low temperature catalyst inclined tube of heat collector and the connector of reactor are located at low temperature conversion area, and the low temperature conversion area exports gas gas-phase objects
Propane/propylene mass ratio in stream is 0.75, and C5 alkane/C5 alkene mass ratio in fluidized-bed reactor outlet gaseous stream is
1.14, it is 85% that low temperature conversion area, which exports methanol conversion,；Big pore size distribution is set between low temperature conversion area and aromatization area
Plate, the gaseous stream and catalyst in low temperature conversion area enter aromatization area by wide bore distribution plate, in aromatization area
Decaying catalyst be divided into two-way, by weight, 5% by circulation inclined tube return low temperature conversion area, 95% enter regenerator again
Raw, the catalyst after regeneration returns to aromatization area.The temperature in low temperature conversion area is 480 DEG C.The temperature in aromatization area
It is 500 DEG C, catalyst bed density is 150 kilograms per cubic meter, and methanol quality air speed is 0.1 hour in fluidized-bed reactor-1；
Reaction gauge pressure is 0 megapascal.The weight content of Cu element is 0.01%, Cu-ZSM-5 molecular sieve catalyst in Cu-ZSM-5 molecular sieve
Carrier be kaolin；The mass ratio of active component and carrier is 10: 90 in catalyst.
Reaction result are as follows: it is 98.5% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 69.4 weight carbon-based selectivity of %, BTX one way are 54.7 weight %.
[embodiment 2]
According to condition described in embodiment 1 and step, catalyst is Ga-ZSM-5 molecular sieve, low temperature conversion area height
It is the 40% of the close phase section total height of fluidized-bed reactor, aromatization area height is the 60% of fluidized-bed reactor total height,
The reaction temperature in aromatization area is 100 DEG C higher than the reaction temperature in low temperature conversion area；It is built-in in the low temperature conversion area to take heat
Device, built-in heat collector coil pipe height are the 30% of low temperature conversion area total height；In low temperature conversion area outlet gaseous stream
Propane/propylene mass ratio is 0.5, and it is 0.95 that fluidized-bed reactor, which exports C5 alkane/C5 alkene mass ratio in gaseous stream, low
Warm zone of transformation outlet methanol conversion is 20%；Decaying catalyst in aromatization area is divided into two-way, by weight, 25%
Low temperature conversion area is returned to by circulation inclined tube, 75%, which enters regenerator, regenerates, and the catalyst after regeneration returns to aromatization area.
The temperature in low temperature conversion area is 450 DEG C.The temperature in aromatization area is 550 DEG C, catalyst bed density is 450 kilograms/it is vertical
Square rice, methanol quality air speed is 7 hours in fluidized-bed reactor-1；Reaction gauge pressure is 0.5 megapascal.Ga in Ga-ZSM-5 molecular sieve
The weight content of element is that the carrier of 15%, Ga-ZSM-5 molecular sieve catalyst is aluminium oxide；Active component and load in catalyst
The mass ratio of body is 50: 90.
Reaction result are as follows: it is 99.0% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 70.6 weight carbon-based selectivity of %, BTX one way are 52.9 weight %.
[embodiment 3]
According to condition described in embodiment 1 and step, catalyst is Zn-ZSM-5 molecular sieve, low temperature conversion area height
It is the 30% of the close phase section total height of fluidized-bed reactor, aromatization area height is the 70% of fluidized-bed reactor total height,
The reaction temperature in aromatization area is 40 DEG C higher than the reaction temperature in low temperature conversion area；Built-in take is equipped in the low temperature conversion area
Hot device, built-in heat collector coil pipe height are the 100% of low temperature conversion area total height；In low temperature conversion area outlet gaseous stream
Propane/propylene mass ratio be 0.6, fluidized-bed reactor export gaseous stream in C5 alkane/C5 alkene mass ratio be 1.0,
It is 75% that low temperature conversion area, which exports methanol conversion,；Decaying catalyst in aromatization area is divided into two-way, by weight,
15% returns to low temperature conversion area by circulation inclined tube, and 85%, which enters regenerator, regenerates, and it is anti-that the catalyst after regeneration returns to aromatisation
Answer area.The temperature in low temperature conversion area is 465 DEG C.The temperature in aromatization area is 505 DEG C, and catalyst bed density is 300,000
Gram/cubic metre, methanol quality air speed is 1 hour in fluidized-bed reactor-1；Reaction gauge pressure is 0.2 megapascal.Zn-ZSM-5 molecular sieve
The weight content of middle Zn element is that the carrier of 9%, Zn-ZSM-5 molecular sieve catalyst is silica；Active component in catalyst
Mass ratio with carrier is 50: 50.
Reaction result are as follows: it is 99.9% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 75.1 weight carbon-based selectivity of %, BTX one way are 63.8 weight %.
[embodiment 4]
According to catalyst described in embodiment 3 and step, low temperature conversion area height is the close phase section of fluidized-bed reactor
The 35% of total height, aromatization area height are the 65% of fluidized-bed reactor total height, the reaction temperature in aromatization area
It spends 60 DEG C higher than the reaction temperature in low temperature conversion area；Built-in heat collector, built-in heat collector coil pipe are equipped in the low temperature conversion area
Height is the 80% of low temperature conversion area total height；Propane/propylene mass ratio in low temperature conversion area outlet gaseous stream is
0.5, it is 0.8 that fluidized-bed reactor, which exports C5 alkane/C5 alkene mass ratio in gaseous stream, and low temperature conversion area exports methanol and turns
Rate is 80%；Decaying catalyst in aromatization area is divided into two-way, and by weight, 20% is low by circulation inclined tube return
Warm zone of transformation, 80%, which enters regenerator, regenerates, and the catalyst after regeneration returns to aromatization area.The temperature in low temperature conversion area is
470℃.The temperature in aromatization area is 530 DEG C, and catalyst bed density is 200 kilograms per cubic meter, in fluidized-bed reactor
Methanol quality air speed is 5 hours-1；Reaction gauge pressure is 0.3 megapascal.
Reaction result are as follows: it is 99.9% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 73.8 weight carbon-based selectivity of %, BTX one way are 61.2 weight %.
[embodiment 5]
According to catalyst described in embodiment 3 and step, low temperature conversion area height is the close phase section of fluidized-bed reactor
The 23% of total height, aromatization area height are the 77% of fluidized-bed reactor total height, the reaction temperature in aromatization area
It spends 90 DEG C higher than the reaction temperature in low temperature conversion area；It is equipped with external heat collector in the low temperature conversion area, maintains low temperature conversion area
Temperature, the low temperature catalyst inclined tube of external heat collector and the connector of reactor are located at low temperature conversion area；The low temperature conversion area
Exporting the propane/propylene mass ratio in gaseous stream is 0.1, and fluidized-bed reactor exports C5 alkane/C5 alkene in gaseous stream
Hydrocarbon mass ratio is 0.3, and it is 40% that low temperature conversion area, which exports methanol conversion,；Decaying catalyst in aromatization area is divided into two
Road, by weight, 10% returns to low temperature conversion area by circulation inclined tube, and 90%, which enters regenerator, regenerates, the catalyst after regeneration
Return to aromatization area.The temperature in low temperature conversion area is 455 DEG C.The temperature in aromatization area is 545 DEG C, catalyst bed
Density is 170 kilograms per cubic meter, and methanol quality air speed is 6.5 hours in fluidized-bed reactor-1；Reaction gauge pressure is 0.15 megapascal.
Reaction result are as follows: it is 99.9% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 70.7 weight carbon-based selectivity of %, BTX one way are 57.9 weight %.
[embodiment 6]
According to condition described in embodiment 3 and step, only catalyst is Zn-P-ZSM-5 molecular sieve, the low temperature conversion
Built-in heat collector is equipped in area, built-in heat collector coil pipe height is the 70% of low temperature conversion area total height；Lighter hydrocarbons logistics is separating
Workshop section returns to the aromatization area of the fluidized-bed reactor after separating.The weight of Zn element in Zn-P-ZSM-5 molecular sieve
Measuring content is 5%, and the weight content of P element is that the carrier of 1.5%, Zn-P-ZSM-5 molecular sieve catalyst is aluminium oxide；Catalysis
The mass ratio of active component and carrier is 40: 70 in agent.
Reaction result are as follows: it is 99.6% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 74.6 weight carbon-based selectivity of %, BTX one way are 61.2 weight %.
[embodiment 7]
According to condition as described in example 4 and step, catalyst is the contact of Zn-Ga-ZSM-5 molecular sieve catalyst.Zn-
It is 1.5 weight % that Zn constituent content, which is 2.5 weight %, Ga constituent contents, in Ga-ZSM-5 molecular sieve catalyst, is lived in catalyst
Property component and carrier mass ratio be 50: 50.
Reaction result are as follows: it is 99.3% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 73.1 weight carbon-based selectivity of %, BTX one way are 57.2 weight %.
[comparative example 1]
According to the catalyst of embodiment 3, only subregion, reaction temperature are not 500 DEG C to fluidized-bed reactor, catalyst bed
Density is 300 kilograms per cubic meter, and methanol quality air speed is 1 hour-1；Reaction gauge pressure is 0.2 megapascal.
Reaction result are as follows: it is 98.5% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 65.1 weight carbon-based selectivity of %, BTX one way are 48.7 weight %.
[comparative example 2]
According to the catalyst of embodiment 3, condition and step, only low temperature conversion area height is the close phase section of fluidized-bed reactor
The 50% of total height, aromatization area height are the 50% of the close phase section total height of fluidized-bed reactor.
Reaction result are as follows: it is 99.8% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 68.5 weight carbon-based selectivity of %, BTX one way are 51.9 weight %.
[comparative example 3]
According to the catalyst, reactor and step of embodiment 3, only the reaction temperature in aromatization area compares low temperature conversion
The reaction temperature in area is 10 DEG C high.
Reaction result are as follows: it is 99.8% that fluidized-bed reactor, which exports methanol conversion, and the carbon-based selectivity of aromatic hydrocarbons one way is
The 66.2 weight carbon-based selectivity of %, BTX one way are 50.2 weight %.
Claims (10)
1. a kind of method for improving arenes selectivity in methanol and/or dimethyl ether aromatic hydrocarbons reaction process, contains methanol and/or two
The raw material of methyl ether sequentially enters the low temperature conversion area of the close phase section of fluidized-bed reactor, aromatization area, with include ZSM-5 molecule
The catalyst of sieve contacts, and the product stream including lighter hydrocarbons, aromatic hydrocarbons is generated, into centrifugal station；Wherein, the low temperature conversion area is high
Degree is the 20~40% of the close phase section total height of fluidized-bed reactor, and aromatization area height is that the close phase section of fluidized-bed reactor is total
The 60~80% of height, the reaction temperature in aromatization area are 20~100 DEG C higher than the reaction temperature in low temperature conversion area；It is described low
For propane/propylene mass ratio in warm zone of transformation outlet gaseous stream less than 0.8, fluidized-bed reactor exports the C5 in gaseous stream
For alkane/C5 alkene mass ratio less than 1.2, low temperature conversion area exports methanol conversion between 20~85%.
2. the method that arenes selectivity is improved in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that wide bore distribution plate is arranged between low temperature conversion area and aromatization area, the gaseous stream in low temperature conversion area and urge
Agent enters aromatization area by wide bore distribution plate.
3. the method that arenes selectivity is improved in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that the decaying catalyst in aromatization area is at least divided into two-way, low temperature conversion is returned to by circulation inclined tube all the way
Area enters regenerator all the way and regenerates, and the catalyst after regeneration returns to aromatization area.
4. the method that arenes selectivity is improved in methanol according to claim 3 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that the decaying catalyst in the aromatization area is divided into two-way, by weight, 5~25% pass through circulation inclined tube
Low temperature conversion area is returned to, 75~95%, which enter regenerator, regenerates.
5. the method that arenes selectivity is improved in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that the temperature in low temperature conversion area is 450~480 DEG C, the 25~38% of the close phase section total height of reactor are highly accounted for；Virtue
The reaction temperature of structure reaction zone is 500~550 DEG C, highly accounts for the 62~75% of the close phase section total height of reactor.
6. the method that arenes selectivity is improved in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that aromatization area internal catalyst bed floor density is 150~450 kilograms per cubic meter, first in fluidized-bed reactor
Alcohol mass space velocity is 0.1~7 hour-1；Reaction gauge pressure is 0~0.5 megapascal.
7. the method that arenes selectivity is improved in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that lighter hydrocarbons logistics returns to the aromatization of the close phase section of the fluidized-bed reactor after centrifugal station is separated
Area.
8. the method that arenes selectivity is improved in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that the carrier of catalyst is kaolin, aluminium oxide or silica；The quality of active component and carrier in catalyst
Than being 10~50: 50~90.
9. the method that arenes selectivity is improved in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process,
It is characterized in that catalyst load has one or more elements or oxide in Zn, Ag, P, Ga, Cu, Mn, Mg, with catalyst
Weight percent meter, weight content are 0.01~15%.
10. improving the side of arenes selectivity in methanol according to claim 1 and/or dimethyl ether aromatic hydrocarbons reaction process
Method, it is characterised in that be equipped with external heat collector or built-in heat collector in the low temperature conversion area, maintain low temperature conversion area temperature, outside
The connector of the low temperature catalyst inclined tube and reactor of setting heat collector is located at low temperature conversion area, and built-in heat collector is located at low temperature conversion
In area, built-in heat collector coil pipe height is the 30~100% of low temperature conversion area total height.
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| CN104549074A (en) * | 2013-10-28 | 2015-04-29 | 中国石油化工股份有限公司 | Coaxial type sectional fluidized bed reaction device for preparing ethylene, propylene and aromatic hydrocarbon by converting methyl alcohol and/or dimethyl ether, and reaction method of reaction device |
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