CN109694294B - Method for preparing aromatic hydrocarbon by efficiently converting methanol - Google Patents

Method for preparing aromatic hydrocarbon by efficiently converting methanol Download PDF

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Publication number
CN109694294B
CN109694294B CN201710982537.6A CN201710982537A CN109694294B CN 109694294 B CN109694294 B CN 109694294B CN 201710982537 A CN201710982537 A CN 201710982537A CN 109694294 B CN109694294 B CN 109694294B
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catalyst
bed
regenerator
regeneration
riser
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CN109694294A (en
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李晓红
齐国祯
金永明
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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    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • CCHEMISTRY; METALLURGY
    • C07ORGANIC CHEMISTRY
    • C07CACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2529/00Catalysts comprising molecular sieves
    • C07C2529/04Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
    • C07C2529/06Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • C07C2529/40Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
    • YGENERAL 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
    • Y02TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02PCLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00Technologies relating to chemical industry
    • Y02P20/50Improvements relating to the production of bulk chemicals
    • Y02P20/584Recycling of catalysts

Abstract

The invention relates to a method for preparing aromatic hydrocarbon by efficiently converting methanol, which mainly solves the problems of low aromatic hydrocarbon yield and serious hydrothermal deactivation of a catalyst in the prior art. The methanol raw material enters a fluidized bed reactor to be in contact reaction with a modified ZSM-5 catalyst under effective reaction conditions; the spent catalyst enters a riser regenerator for regeneration, the obtained semi-regenerated catalyst and the flue gas I enter a riser regeneration cyclone separator connected with the riser regenerator, and the separated semi-regenerated catalyst enters a secondary dense bed zone A for degassing; the regenerated catalyst after degassing is returned to the riser regenerator and regenerated in the fast bed regenerator, and the regenerated catalyst after degassing is degassed in the second dense bed zone B and then fed into the fluidized bed reactor.

Description

Method for preparing aromatic hydrocarbon by efficiently converting methanol
Technical Field
The invention relates to a method for preparing aromatic hydrocarbon by efficiently converting methanol.
Background
Aromatic hydrocarbons (especially triphenyl, benzene, toluene, xylene, i.e., BTX) are important basic organic synthesis feedstocks. Driven by the demand for downstream derivatives, the market demand for aromatics continues to increase.
The catalytic reforming and steam cracking process is the main production process of arene and belongs to the field of petroleum production technology. China has relatively rich coal resources. With the successful development of high-efficiency and long-period methanol catalyst and methanol device upsizing technology in recent years, the production cost of coal-based methanol is greatly reduced, which provides a cheap raw material source for the production of downstream products (olefin, aromatic hydrocarbon and the like) of methanol. Therefore, the production of aromatic hydrocarbons from methanol is considered.
This technology was first reported in 1977 by Chang et al (Journal of Catalysis, 1977, 47, 249) by Mobil corporation to prepare hydrocarbons such as aromatic hydrocarbons by conversion of methanol and its oxygenates over a ZSM-5 molecular sieve catalyst. In 1985, Mobil corporation in its applied US1590321, the first published research results of aromatics production by conversion of methanol and dimethyl ether, which uses 2.7 wt% phosphorus% of ZSM-5 molecular sieve is used as catalyst, the reaction temperature is 400-450 ℃, and the space velocity of methanol and dimethyl ether is 1.3 hours-1
There are many related reports and patents in this field. The patent of the catalyst for preparing aromatic hydrocarbon by methanol: chinese patents CN102372535, CN102371176, CN102371177, CN102372550, CN102372536, CN102371178, CN102416342, CN101550051, U.S. Pat. No. 4,4615995, U.S. Pat. No. 5/0099249A 1, etc. The patent in the aspect of the process for preparing aromatic hydrocarbon by methanol: US patents US4686312, CN 101244969, CN1880288, CN101602646, CN101823929, CN101671226, CN101607858, CN102199069, CN102199446, CN1880288, CN102146010, CN104326859, CN105457568, CN105457569, CN105457570, CN105461497 and the like.
Among them, patents CN105457568, CN105457569, CN105457570 and CN105461497 introduce a double regeneration fluidized bed technology for reducing the problem of hydrothermal deactivation of the catalyst. In the technologies, the catalyst to be regenerated enters a second regenerator after being regenerated by a first regenerator or entering the second regenerator after being settled by a cyclone separator or a settler, and still causes hydrothermal deactivation of the catalyst to a certain extent.
Therefore, the prior patent technologies have the problems of serious hydrothermal deactivation of the catalyst and low yield of the aromatic hydrocarbon. The invention provides a technical scheme pertinently and solves the problems.
Disclosure of Invention
The invention aims to solve the technical problems of low aromatic hydrocarbon yield and easy hydrothermal inactivation of a catalyst in the prior art, and provides a method for preparing aromatic hydrocarbon by efficiently converting methanol.
In order to solve the problems, the technical scheme adopted by the invention is as follows: the methanol raw material enters a fluidized bed reactor to be in contact reaction with a modified ZSM-5 catalyst under effective reaction conditions to obtain a reaction product containing aromatic hydrocarbon and a spent catalyst, the reaction product is separated by a reactor cyclone separator, and the reaction product enters a subsequent separation system; the spent catalyst enters a riser regenerator to be contacted with a regeneration medium I for regeneration, the obtained semi-regenerated catalyst and the flue gas I enter a riser regeneration cyclone separator connected with the riser regenerator, the separated semi-regenerated catalyst enters a secondary dense bed A area to be contacted with a degassing medium I, and the separated flue gas I enters a subsequent flue gas system; and (2) returning 20-50% of the regenerated catalyst after degassing to the riser regenerator, allowing 50-80% of the regenerated catalyst to enter the fast bed regenerator to be in contact regeneration with a regeneration medium II, allowing the obtained regenerated catalyst and flue gas II to enter a secondary dense bed B area to be in contact with the degassing medium II, allowing the flue gas II to enter a subsequent flue gas system after separation by a cyclone separator, and allowing the regenerated catalyst after degassing to enter a fluidized bed reactor.
In the above technical scheme, preferably, the outlet of the riser reactor is connected with a riser regeneration cyclone separator, and the outlet of the fast bed regenerator is connected with a fast separation device; the outlet of the riser reactor and the riser regeneration cyclone separator are positioned in a zone A of the two dense beds, and the outlet of the fast bed regenerator and the fast separation equipment are positioned in a zone B of the two dense beds; the circulating inclined pipe is connected with a zone A of the secondary dense bed and a fast bed regenerator, the semi-regeneration inclined pipe is connected with the zone A of the secondary dense bed and a riser regenerator, the regeneration inclined pipe is connected with a zone B of the secondary dense bed and a fluidized bed reactor, and the inclined pipe to be regenerated is connected with the riser regenerator and the fluidized bed reactor.
In the technical scheme, preferably, the secondary dense bed is divided into a secondary dense bed area A and a secondary dense bed area B, a partition plate is arranged between the secondary dense bed area A and the secondary dense bed area B, and the height of the partition plate is 60-90% of the total height of the secondary dense bed; the volume ratio of the area A of the secondary dense bed to the area B of the secondary dense bed is (0.3-1): 1.
In the technical scheme, preferably, the temperature of the catalyst in the fast bed regenerator is 620-700 ℃, the density of the catalyst bed layer is 110-250 kg/cubic meter, and the residence time of the catalyst is 5-30 minutes.
In the technical scheme, preferably, the temperature of the catalyst in the riser regenerator is 500-600 ℃, the density of the catalyst is 50-100 kg/cubic meter, and the residence time of the catalyst is 1-5 seconds.
In the technical scheme, preferably, the effective reaction conditions are that the temperature is 440-550 ℃, the reaction gauge pressure is 0-1 MPa, and the weight space velocity of methanol is 0.2-15 hours-1
In the above technical solution, preferably, the effective reaction stripThe temperature of the device is 470-520 ℃, the reaction gauge pressure is 0.02-0.7 MPa, and the weight space velocity of methanol is 0.6-10 hours-1
In the above technical scheme, preferably, the content of carbon on the regenerated catalyst is 0.01-0.39% by mass of the catalyst.
In the above technical solution, preferably, the degassing medium i and the degassing medium ii are nitrogen gas, and the nitrogen gas is heated to a temperature of more than 400 ℃ by a heat-taking coil disposed in the zone a and/or the zone B of the two dense beds.
In the above technical scheme, preferably, the regeneration medium i and the regeneration medium ii, and the degassing medium i and the degassing medium ii are dehydrated and then enter the riser regenerator, the fast bed regenerator, the two dense bed a area and the two dense bed B area, and the water partial pressure of the regeneration medium i and the regeneration medium ii, and the water partial pressure of the degassing medium i and the degassing medium ii are not higher than 2 kpa at 20 ℃.
In the above technical solution, preferably, the modifying element of the modified ZSM-5 molecular sieve catalyst is at least one of Zn, La, P, Ga, Mn, Ag, and Cu, and the content of the modifying element is 0.01 to 15% by weight of the catalyst.
In the technical scheme, preferably, the modifying elements are P and Zn, and the ratio of P to Zn is 10: 1-1: 1.
In the technical scheme, more preferably, the ratio of P to Zn is 7: 1-3: 1.
The regeneration medium is an oxygen-containing gas, typically a mixture of air, air and nitrogen.
The invention provides a technical scheme of double regenerators, wherein a riser regenerator mainly completes a hydrogen burning process, and a fast bed regenerator completes a carbon burning process. And the semi-regenerated catalyst obtained by hydrogen burning enters a double dense bed to remove the entrained moisture of the catalyst, and the water partial pressure of the regeneration medium and the degassing medium entering the regenerator is strictly controlled, so that the water partial pressure in the fast bed regenerator is lower than the water partial pressure obviously causing the hydrothermal deactivation of the catalyst. By the measure, the hydrothermal deactivation phenomenon of the metal modified ZSM series catalyst can be effectively weakened, the activity of the catalyst is maintained, and the higher yield of the aromatic hydrocarbon is obtained.
By adopting the technical scheme of the invention, the aromatic hydrocarbon carbon-based yield can be maintained above 63 weight percent all the time after 1000 hours of operation, and a better technical effect is achieved.
Drawings
FIG. 1 is a schematic flow chart of the present invention. In FIG. 1, 1 is a fluidized bed reactor; 2 is a riser regenerator; 3 is a dense bed; 4 is a fast bed regenerator; 5 is a reactor cyclone separator; 6 is a riser tube regeneration cyclone separator; 7 is a cyclone separator; 8, fast separation equipment; 9 is a methanol raw material; 10 is a reaction product; 11 is a regeneration medium I; 12 is regeneration medium II; 13 is a degassing medium II; 14 is flue gas I; 15 is flue gas II; 16 is a regenerated catalyst; 17 is spent catalyst; 18 is a semi-regenerated catalyst; 19 is the degassed regenerated catalyst returning to the riser regenerator; 20 is a clapboard; 21 is a zone A of a dense bed; 22 is a zone B of a dense bed; 23 is degassing medium I; 24 is a semi-regenerative inclined tube; 25 is a circulating inclined tube; 26 is a regeneration inclined tube; 27 is a to-be-grown inclined tube.
Detailed Description
[ example 1 ]
The methanol raw material with the methanol mass percentage content of 100 percent enters a fluidized bed reactor and a modified ZSM-5 catalyst at the temperature of 440 ℃, the reaction gauge pressure is 0 MPa, and the weight space velocity of the methanol is 0.2 hour-1The reaction product containing the aromatic hydrocarbon and the catalyst to be generated are obtained and are separated by a cyclone separator of the reactor, and the reaction product enters a subsequent separation system; the spent catalyst enters a riser regenerator to be contacted with a regeneration medium I for regeneration, the obtained semi-regenerated catalyst and the flue gas I enter a riser regeneration cyclone separator connected with the riser regenerator, the separated semi-regenerated catalyst enters a secondary dense bed A area to be contacted with a degassing medium I, and the separated flue gas I enters a subsequent flue gas system; and (2) returning 20% of the regenerated catalyst after degassing to the riser regenerator, allowing 80% of the regenerated catalyst after degassing to enter the fast bed regenerator to be in contact regeneration with a regeneration medium II, allowing the obtained regenerated catalyst and flue gas II to enter a secondary dense bed B area to be in contact with the degassing medium II, allowing the flue gas II to enter a subsequent flue gas system after separation by a cyclone separator, and allowing the regenerated catalyst after degassing to enter a fluidized bed reactor.
The second dense bed is divided into a second dense bed area A and a second dense bed area B, a partition board is arranged between the second dense bed area A and the second dense bed area B, and the height of the partition board is 60% of the total height of the second dense bed; the volume ratio of the region A of the dense bed to the region B of the dense bed is 0.3: 1.
The temperature of the catalyst in the fast bed regenerator was 620 ℃, the density of the catalyst bed was 250 kg/m, and the catalyst residence time was 30 minutes.
The catalyst temperature in the riser regenerator was 500 ℃, the catalyst density was 100 kg/m, and the catalyst residence time was 5 seconds.
The carbon content on the regenerated catalyst was 0.39% by mass of the catalyst.
The degassing medium I and the degassing medium II are nitrogen, and the nitrogen is heated to more than 400 ℃ through a heat taking coil arranged in the area A of the two dense beds and/or the area B of the two dense beds.
And the regeneration medium I and the regeneration medium II as well as the degassing medium I and the degassing medium II are dehydrated and then enter the riser regenerator and the fast bed regenerator as well as the zone A and the zone B of the double dense bed, and the water partial pressure of the regeneration medium I and the regeneration medium II as well as the water partial pressure of the degassing medium I and the degassing medium II is 1.99 kilopascal at the temperature of 20 ℃.
A Zn-La-P-ZSM-5 catalyst is adopted, and the mass percentage of the catalyst is that the Zn element content is 7%, the La element content is 5%, and the P element content is 3%.
The results show that the aromatic hydrocarbon single-pass carbon-based yield can be maintained above 51 wt% after running for 1000 hours.
[ example 2 ]
According to the conditions and steps described in example 1, a methanol feedstock containing 10% by mass of methanol was fed into a fluidized bed reactor and the catalyst was operated at 550 ℃, a reaction gauge pressure of 1 MPa, and a methanol weight space velocity of 15 hours-1Under the condition of (1); 50% of the regenerated catalyst after degassing returns to the riser regenerator, and 50% of the regenerated catalyst after degassing enters the fast bed regenerator to be in contact regeneration with a regeneration medium II.
The height of the partition board is 90% of the total height of the secondary dense bed; the volume ratio of the region A of the dense bed to the region B of the dense bed is 1: 1.
The temperature of the catalyst in the fast bed regenerator is 700 ℃, the density of the catalyst bed layer is 110 kg/cubic meter, and the residence time of the catalyst is 5 minutes.
The catalyst temperature in the riser regenerator was 600 ℃, the catalyst density was 50 kg/m, and the catalyst residence time was 1 second.
The carbon content on the regenerated catalyst was 0.01% by mass of the catalyst.
The water partial pressures of the regeneration medium I and the regeneration medium II and the degassing medium I and the degassing medium II are all 1 kPa at 20 ℃.
Adopts Zn-ZSM-5 catalyst, and the Zn element content is 0.01 percent by mass percent of the catalyst.
The results show that the single-pass carbon-based yield of the aromatic hydrocarbon can be maintained above 53 wt% after running for 1000 hours.
[ example 3 ]
According to the conditions and steps described in example 1, a methanol feedstock containing 98% by mass of methanol was fed into a fluidized bed reactor and the catalyst was operated at 490 ℃, a reaction gauge pressure of 0.3 MPa and a methanol weight space velocity of 4 hours-1Under the condition of (1); 30% of the regenerated catalyst after degassing returns to the riser regenerator, and 70% of the regenerated catalyst after degassing enters the fast bed regenerator to be in contact regeneration with a regeneration medium II.
The height of the partition is 70% of the total height of the dense bed; the volume ratio of the region A of the dense bed to the region B of the dense bed is 0.8: 1.
The temperature of the catalyst in the fast bed regenerator is 650 ℃, the density of the catalyst bed layer is 180 kg/cubic meter, and the residence time of the catalyst is 25 minutes.
The catalyst temperature in the riser regenerator was 570 ℃, the catalyst density was 82 kg/m, and the catalyst residence time was 4 seconds.
The carbon content on the regenerated catalyst was 0.1% by mass of the catalyst.
The water partial pressures of the regeneration medium I and the regeneration medium II and the degassing medium I and the degassing medium II are all 0.01 kilopascal at 20 ℃.
A Zn-P-ZSM-5 catalyst is adopted, and the content of Zn element is 1.5 percent and the content of P element is 2.1 percent in percentage by mass of the catalyst.
The results show that the yield of the aromatic hydrocarbon carbon base can be maintained above 63 wt% after running for 1000 hours.
[ example 4 ]
According to the catalyst, conditions and steps described in example 3, a methanol raw material with a methanol mass percentage of 95% enters a fluidized bed reactor, the catalyst is at 470 ℃, the reaction gauge pressure is 0.5 MPa, and the methanol weight space velocity is 4 hours-1Under the condition of (1); 40% of the regenerated catalyst after degassing returns to the riser regenerator, and 60% of the regenerated catalyst after degassing enters the fast bed regenerator to be in contact regeneration with a regeneration medium II.
The height of the partition board is 60 percent of the total height of the dense bed; the volume ratio of the region A of the dense bed to the region B of the dense bed is 0.9: 1.
The temperature of the catalyst in the fast bed regenerator is 660 ℃, the density of the catalyst bed layer is 200 kg/cubic meter, and the residence time of the catalyst is 25 minutes.
The catalyst temperature in the riser regenerator was 540 ℃, the catalyst density was 95 kg/m, and the catalyst residence time was 4 seconds.
The carbon content on the regenerated catalyst was 0.15% by mass of the catalyst.
The water partial pressures of the regeneration medium I and the regeneration medium II and the degassing medium I and the degassing medium II are all 0.1 kilopascal at 20 ℃.
The result shows that the aromatic hydrocarbon single-pass carbon-based yield can be maintained above 60 wt% after running for 1000 hours.
[ example 5 ]
According to the catalyst, conditions and steps described in example 3, a methanol feedstock with a methanol mass percent of 100% enters a fluidized bed reactor and the catalyst is operated at a temperature of 520 ℃, a reaction gauge pressure of 0.02 MPa and a methanol weight space velocity of 0.6 h-1Under the condition of (1).
The temperature of the catalyst in the fast bed regenerator is 680 ℃, the density of the catalyst bed layer is 150 kg/cubic meter, and the residence time of the catalyst is 10 minutes.
The catalyst temperature in the riser regenerator was 590 ℃, the catalyst density was 70 kg/m, and the catalyst residence time was 2 seconds.
The carbon content of the regenerated catalyst is lower than 0.2 percent in terms of mass percent of the catalyst.
The water partial pressures of the regeneration medium I and the regeneration medium II and the degassing medium I and the degassing medium II are respectively lower than 1 kilopascal at the temperature of 20 ℃.
The result shows that the single-pass carbon-based yield of the aromatic hydrocarbon can be maintained above 55 weight percent after 1000 hours of operation.
[ example 6 ]
The catalyst, conditions and procedure described in example 5 were followed with the methanol feed to the fluidized bed reactor and the catalyst at 470 deg.C, a reaction gauge pressure of 0.7 MPa, and a methanol weight space velocity of 10 hours-1Under the condition of (1).
The temperature of the catalyst in the fast bed regenerator was 630 ℃, the density of the catalyst bed was 250 kg/m, and the catalyst residence time was 30 minutes.
The catalyst temperature in the riser regenerator was 540 ℃, the catalyst density was 100 kg/m, and the catalyst residence time was 5 seconds.
The result shows that the single-pass carbon-based yield of the aromatic hydrocarbon can be maintained above 55 weight percent after 1000 hours of operation.
Comparative example 1
The feed and catalyst of example 1 were used except that no semi-regeneration inclined tube was provided between the riser regenerator and the dense bed A. The results show that the aromatics single-pass carbon-based yield is 45 wt%.
Comparative example 2
The feed and catalyst of example 1 were used except that the dense bed was not partitioned. The results show that the aromatics single-pass carbon-based yield is 46 wt%.
Comparative example 3
The feed and catalyst of example 1 were used except that the height of the partition was 50% of the total height of the two-bed dense bed; the volume ratio of the region A of the dense bed to the region B of the dense bed is 1.2: 1. . The results show that the single-pass carbon-based yield of the aromatic hydrocarbon is 48 wt%.

Claims (9)

1. A method for preparing aromatic hydrocarbon by methanol high-efficiency conversion comprises the steps that a methanol raw material enters a fluidized bed reactor to be in contact reaction with a modified ZSM-5 catalyst, a reaction product containing aromatic hydrocarbon and a spent catalyst are obtained and are separated by a reactor cyclone separator, and the reaction product enters a subsequent separation system; the second dense bed is divided into a second dense bed area A and a second dense bed area B, a catalyst to be regenerated enters a riser regenerator to be in contact regeneration with a regeneration medium I, the obtained semi-regenerated catalyst and the flue gas I enter a riser regeneration cyclone separator connected with the riser regenerator, the separated semi-regenerated catalyst enters the second dense bed area A to be in contact with a degassing medium I, and the separated flue gas I enters a subsequent flue gas system; 20-50% of the regenerated catalyst after degassing returns to the riser regenerator, 50-80% of the regenerated catalyst enters the fast bed regenerator to be in contact regeneration with a regeneration medium II, the obtained regenerated catalyst and flue gas II enter a secondary dense bed B area to be in contact with the degassing medium II, the flue gas II is separated by a cyclone separator and enters a subsequent flue gas system, and the regenerated catalyst after degassing enters a fluidized bed reactor; wherein, the semi-regeneration inclined pipe is connected with a zone A of the two dense beds and a riser regenerator; a partition plate is arranged between the area A of the secondary dense bed and the area B of the secondary dense bed, and the height of the partition plate is 60-90% of the total height of the secondary dense bed; the volume ratio of the area A of the secondary dense bed to the area B of the secondary dense bed is (0.3-1): 1.
2. The method for preparing aromatic hydrocarbons through efficient methanol conversion according to claim 1, wherein the outlet of the riser regenerator is connected with a riser regeneration cyclone separator, and the outlet of the fast bed regenerator is connected with a fast separation device; the outlet of the riser regenerator and the riser regeneration cyclone separator are positioned in a zone A of the secondary dense bed, and the outlet of the fast bed regenerator and the fast separation equipment are positioned in a zone B of the secondary dense bed; the circulating inclined pipe is connected with a zone A of the secondary dense bed and a fast bed regenerator, the regenerating inclined pipe is connected with a zone B of the secondary dense bed and a fluidized bed reactor, and the inclined pipe to be regenerated is connected with a riser regenerator and the fluidized bed reactor.
3. The method for preparing the aromatic hydrocarbon through the efficient conversion of the methanol according to claim 1, wherein the temperature of the catalyst in the fast bed regenerator is 620-700 ℃, the density of a catalyst bed layer is 110-250 kg/m, and the residence time of the catalyst is 5-30 minutes.
4. The method for preparing aromatic hydrocarbons through efficient methanol conversion according to claim 1, wherein the temperature of the catalyst in the riser regenerator is 500-600 ℃, the density of the catalyst is 50-100 kg/m, and the residence time of the catalyst is 1-5 seconds.
5. The method for preparing the aromatic hydrocarbon through efficient methanol conversion according to claim 1, wherein the reaction conditions of the contact reaction are that the temperature is 440-550 ℃, the reaction gauge pressure is 0-1 MPa, and the weight space velocity of the methanol is 0.2-15 hours-1
6. The method for preparing aromatic hydrocarbons through efficient methanol conversion according to claim 1, wherein the content of carbon on the regenerated catalyst is 0.01-0.39% by mass of the catalyst.
7. The method for preparing aromatic hydrocarbons through efficient methanol conversion according to claim 1, wherein the degassing medium I and the degassing medium II are nitrogen, and the nitrogen is heated to above 400 ℃ through a heat-taking coil arranged in the zone A and/or the zone B of the two dense beds.
8. The method for preparing aromatic hydrocarbons through efficient methanol conversion according to claim 1, wherein the regeneration medium I and the regeneration medium II and the degassing medium I and the degassing medium II are dehydrated and then enter the riser regenerator, the fast bed regenerator, the zone A of the double dense bed and the zone B of the double dense bed, and the water partial pressure of the regeneration medium I and the regeneration medium II and the water partial pressure of the degassing medium I and the degassing medium II are not higher than 2 kPa at 20 ℃.
9. The method for preparing aromatic hydrocarbons through efficient methanol conversion according to claim 1, wherein the modifying element of the modified ZSM-5 molecular sieve catalyst is at least one of Zn, La, P, Ga, Mn, Ag and Cu, and the content of the modifying element is 0.01-15% by weight of the catalyst.
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CN105457570B (en) * 2014-09-09 2018-04-06 中国石油化工股份有限公司 The coaxial-type two-stage regeneration reaction unit and its reaction method of methanol or dimethyl ether conversion producing light olefins and aromatic hydrocarbons
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