CN104672045B - A kind of reaction unit for methanol and/or dimethyl ether low-carbon alkene - Google Patents
A kind of reaction unit for methanol and/or dimethyl ether low-carbon alkene Download PDFInfo
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- CN104672045B CN104672045B CN201310648651.7A CN201310648651A CN104672045B CN 104672045 B CN104672045 B CN 104672045B CN 201310648651 A CN201310648651 A CN 201310648651A CN 104672045 B CN104672045 B CN 104672045B
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The present invention relates to the reaction unit for methanol and/or dimethyl ether low-carbon alkene, relate more specifically to a kind of reaction unit for methanol and/or dimethyl ether low-carbon alkene, it mainly includes dense fluidized bed bioreactor (2), cyclone separator (3), stripper (5), riser (7), dense-phase fluidized bed regenerator (10), cyclone separator (11), stripper (13) and riser (15), wherein dense fluidized bed bioreactor (2) is divided into the individual secondary response district of n (n >=2) by Flow of Goods and Materials controller (17), dense-phase fluidized bed regenerator (10) is divided into the individual secondary regenerator district of m (m >=2) by Flow of Goods and Materials controller (17). the reaction unit utilizing the present invention solves catalyst carbon deposition skewness in prior art, the problem that selectivity of light olefin is relatively low.
Description
Technical field
The present invention relates to a kind of reaction unit for methanol and/or dimethyl ether low-carbon alkene.
Background technology
Low-carbon alkene, i.e. ethylene and propylene, be basic chemical industry raw material two kinds important, and its demand is being continuously increased. Usually, ethylene, propylene are to be produced by petroleum path, but due to the limited supply of petroleum resources and higher price, petroleum resources produce ethylene, the cost of propylene is continuously increased. In recent years, people start to greatly develop the technology of alternative materials conversion ethylene processed, propylene. The technique of preparing olefin by conversion of methanol (MTO) is subject to increasing attention, has realized the production scale of megaton. Along with the development of World Economics, low-carbon alkene, particularly propylene, demand grows with each passing day, and Xi Mai company (CMAI) analyzes and claims, before 2016, ethylene requirements amount by with average annual 4.3% speed increment, propylene demand by with average annual 4.4% speed increment. Due to the rapid growth of China's economy, the annual rate of growth of the demand of China's ethylene and propylene all exceedes world average level.
Early 1980s, UCC company successfully have developed SAPO Series Molecules sieve, wherein SAPO-34 molecular sieve catalyst shows the catalytic performance of excellence for MTO when reacting, there is significantly high selectivity of light olefin, and activity is significantly high, but catalyst loses activity due to carbon distribution in use for some time. In use there is obvious induction period in SAPO-34 molecular sieve catalyst, in induction period, the selectivity of alkene is relatively low, the selectivity of alkane is higher, and along with the increase in response time, selectivity of light olefin is gradually increasing, after induction period, catalyst keeps high selectivity and high activity within a certain period of time, extends as time go on, and the activity of catalyst declines rapidly.
US6166282 discloses a kind of methanol and is converted into technology and the reactor of low-carbon alkene, adopt fast fluidized bed reactor, gas phase is after the gas relatively low Mi Xiangfanyingqu of speed has reacted, after rising to the fast subregion that internal diameter diminishes rapidly, special gas-solid separation equipment initial gross separation is adopted to go out most entrained catalyst.Due to reaction afterproduct gas and catalyst sharp separation, it is effectively prevented the generation of secondary response. Calculating through simulation, compared with traditional bubbling fluidization bed bioreactor, needed for this fast fluidized bed reactor internal diameter and catalyst, reserve all greatly reduces. But in the method, low-carbon alkene carbon base absorption rate is generally individually about 77%, there is the problem that yield of light olefins is relatively low.
CN101402538B discloses a kind of method improving yield of light olefins, the first top, reaction zone that the method employing is converted into low-carbon alkene at methanol arranges a second reaction zone, and this second reaction zone diameter is more than the first reaction zone, to increase product gas time of staying in second reaction zone of the first reaction zone outlet, make unreacted methanol, the dimethyl ether generated and carbon more than four hydrocarbon continue reaction, reach to improve the purpose of yield of light olefins, although the method can improve the yield of low-carbon alkene to a certain extent, but owing to the first reaction zone catalyst out is already provided with more carbon distribution, and carbon more than four hydrocarbon pyrolysis needs higher catalyst activity, therefore in the method, carbon more than the four hydrocarbon transformation efficiency in second reaction zone is still on the low side, thus causing that yield of light olefins is on the low side.
CN102276406A discloses the production method of a kind of propylene enhancing. This technology arranges three reaction zones, and the first fast bed reaction zone converts to alkene, riser reaction zone and the second fast bed reaction zone to connect for methanol and is used for converting ethylene, carbon more than four hydrocarbon and unreacted methanol or dimethyl ether. In this patent, the material time of staying in riser reaction zone and the second fast bed reaction zone such as carbon more than four hydrocarbon is shorter, and transformation efficiency is on the low side, thus causing that propene yield is on the low side.
CN102875289A discloses a kind of internal fluidized bed reaction arranging riser reactor, for improving the productivity of low-carbon alkene. First raw material enters fluidized bed reaction zone, contacts with catalyst, generates the product including low-carbon alkene, concurrently forms reclaimable catalyst; Reclaimable catalyst is partly into regenerator regeneration, forms regeneration catalyzing agent, is partly into the port of export and is positioned at the riser within reaction zone, and reclaimable catalyst is promoted in reaction zone by and the second contact raw; Regeneration catalyzing agent returns to fluidized-bed reactor reaction zone. Reaction unit disclosed by this patent is without Stripping section, and reclaimable catalyst will carry portioned product gas and enter regenerator, burns with oxygen, reduces the yield of low-carbon alkene.
The methanol-to-olefins technology that CN102875296A announces is provided with fast bed, down-flow fluidized bed using ECT and three reaction zones of riser. Catalyst circulates between regenerator, fast bed, riser and down-flow fluidized bed using ECT, flows to sufficiently complex, assignment of traffic and control is very difficult, and the activity change of catalyst is bigger.
It is known in the art, the selectivity of low-carbon alkene closely related with the carbon deposition quantity on catalyst, it is ensured that high selectivity of light olefin, SAPO-34 catalyst needs a number of carbon distribution. The main reactor that current MTO technique adopts is fluid bed, and fluid bed is close to complete mixing flow reactor, and catalyst carbon deposit distribution is very wide, is unfavorable for improving the selectivity of low-carbon alkene. The agent alcohol ratio of MTO technique is only small, coking yield is relatively low, realize catalyst circulating load bigger, that be easily controlled, be accomplished by renewing zone by the carbon deposition quantity on catalyst, carbon content uniformity controlling is at certain level, and then reaches the purpose of the carbon deposition quantity on the inner catalyst of control reaction zone, carbon content uniformity.Therefore, the carbon deposition quantity of catalyst in reaction zone and carbon content uniformity are controlled in the key technology that certain level is in MTO technique.
For solving the problems referred to above, several researchers have proposed and upper and lower two reaction zones, the series connection of two fluid beds, fluid bed and the technology such as riser, down-flow fluidized bed using ECT series connection are set in fluid bed, tentatively disclose the method controlling carbon deposition quantity of catalyst and carbon content uniformity, achieve certain beneficial effect, but also increase the complexity of MTO technique simultaneously, control difficulty increase. The present invention proposes the scheme forming multiple secondary response district (renewing zone) by arranging inner member in dense-phase fluidized bed and solves to control the problem of carbon deposition quantity of catalyst and carbon content uniformity, and then improves the selectivity of low-carbon alkene.
Summary of the invention
The technical problem to be solved is the problem that the selectivity of light olefin existed in prior art is not high, it is provided that a kind of new reaction unit improving selectivity of light olefin. This reaction unit in the production of low-carbon alkene, has that catalyst carbon deposition uniformity is good, the advantage of the more high and low carbon olefin production technology better economy of yield of light olefins.
For solving the problems referred to above, the present invention provides a kind of reaction unit for methanol and/or dimethyl ether low-carbon alkene, described reaction unit to include dense fluidized bed bioreactor (2), cyclone separator (3), stripper (5), riser (7), dense-phase fluidized bed regenerator (10), cyclone separator (11), stripper (13) and riser (15); Wherein, reactor feed line (1) is connected with described dense fluidized bed bioreactor (2) bottom; A part for described stripper (5) is among described dense fluidized bed bioreactor (2), and remainder is in described dense fluidized bed bioreactor (2) lower section; Described riser (7) bottom is connected with the bottom of described stripper (5), and the top of described riser (7) is connected with described dense-phase fluidized bed regenerator (10); Regenerator feed pipeline (9) is connected with the bottom of described dense-phase fluidized bed regenerator (10); A part for described stripper (13) is among described dense-phase fluidized bed regenerator (10), and remainder is in described dense-phase fluidized bed regenerator (10) lower section; The bottom of described riser (15) is connected with the bottom of described stripper (13), the top of described riser (15) is connected with described dense fluidized bed bioreactor (2), it is characterized in that, described dense fluidized bed bioreactor (2) and/or dense-phase fluidized bed regenerator (10) has Flow of Goods and Materials controller (17), described dense fluidized bed bioreactor (2) is divided into n secondary response district by described Flow of Goods and Materials controller (17), and the 1st is sequentially connected to the n-th secondary response district; Described dense-phase fluidized bed regenerator (10) is divided into m secondary regenerator district by described Flow of Goods and Materials controller (17), and the 1st is sequentially connected to m-th secondary regenerator district; And wherein n >=2, m >=2.
In a preferred embodiment, described riser (15) top is connected with the 1st secondary response district, and the n-th secondary response district is connected with the material overfall (18) on described stripper (5) top; The top of described dense fluidized bed bioreactor (2) is provided with cyclone separator (3), the top exit of described cyclone separator (3) is connected with product material pipeline (4), and the bottom of described cyclone separator (3) is connected with the n-th secondary response district.
In a preferred embodiment, the top of described riser (7) is connected with the 1st secondary regenerator district, and m-th secondary regenerator district is connected with the material overfall (18) on described stripper (13) top;The top of described dense-phase fluidized bed regenerator (10) is provided with cyclone separator (11), the top exit of described cyclone separator (11) is connected with waste line (12), and the bottom of described cyclone separator (11) is connected with m-th secondary regenerator district.
In a preferred embodiment, 8 >=n >=3.
In a preferred embodiment, 8 >=m >=3.
In a preferred embodiment, described Flow of Goods and Materials controller (17) is made up of dividing plate (19), aperture (20), the descending flow duct of material (21), bottom baffle (22) and heat-obtaining parts (23); Described aperture (20) is positioned at the lower section of described dividing plate (19) and is connected with the descending flow duct of described material (21) bottom, described bottom baffle (22) is positioned at the descending flow duct of described material (21) and the bottom of described aperture (20), and described heat-obtaining parts (23) are fixed on described dividing plate (19).
In a preferred embodiment, described bottom baffle (22) is porous plate or imperforate plate.
Compared with prior art scheme, beneficial effects of the present invention includes but not limited to following several respects:
(1) dense-phase fluidized bed has higher bed density, and catalyst velocity is relatively low, it is low to wear and tear.
(2) speed of the gas in the descending flow duct of material in Flow of Goods and Materials controller is less than or equal to the minimum fluidization velocity of catalyst, catalyst is in close phase stacking states, define the one-way sealing phase transportation flow of catalyst, avoiding the catalyst back-mixing between two neighboring stages reaction zone (or two neighboring stages renewing zone), residence time destribution is narrow.
(3) the heat-obtaining parts in Flow of Goods and Materials controller have the effect controlling reaction zone temperature.
(4) reaction zone is divided into n secondary response district by Flow of Goods and Materials controller, and catalyst passes sequentially through the 1st secondary response district to the n-th secondary response district, and residence time destribution is narrow, and the uniformity of reclaimable catalyst carbon content increases substantially.
(5) renewing zone is divided into m secondary regenerator district by Flow of Goods and Materials controller, and catalyst passes sequentially through the 1st secondary regenerator district to m secondary regenerator district, and residence time destribution is narrow, and the uniformity of regeneration catalyzing agent carbon content increases substantially.
(6) achieve the carbon content being comparatively accurately controlled regeneration catalyzing agent and reclaimable catalyst, and carbon content distribution is comparatively uniform, improves the selectivity of low-carbon alkene, and can regulate and control carbon content according to demand to optimize the ratio of propylene/ethylene.
(7) because the carbon content of catalyst is distributed comparatively uniform, the catalyst inventory needed for reaction zone reduces.
(8) structure in multiple secondary response districts facilitates implementation the maximization of reactor.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention;
Fig. 2 is the structural representation of the dense-phase fluidized bed comprising 4 secondary response districts of the present invention, and wherein the arrow in A-A profile is the catalyst flow direction that secondary response is interval;
Fig. 3 is the structural representation of the dense-phase fluidized bed comprising 4 secondary regenerator districts of the present invention, and wherein the arrow in B-B profile is the catalyst flow direction that secondary regenerator is interval;
Fig. 4 is the structural representation of stripper of the present invention;
Fig. 5 is the structural representation of Flow of Goods and Materials controller of the present invention.
Description of reference numerals in accompanying drawing is as follows:
1-reactor feed line; The 1st secondary response district charging branch line of 1-1; 1-2 the 2nd secondary response district charging branch line; 1-3 the 3rd secondary response district charging branch line; 1-4 the 4th secondary response district charging branch line; 2-dense fluidized bed bioreactor; 2-1 the 1st secondary response district;2-2 the 2nd secondary response district; 2-3 the 3rd secondary response district; 2-4 the 4th secondary response district; 3-cyclone separator; 4-product material pipeline; 5-stripper; 6-steam pipeline; 7-riser; 8-promotes gas pipeline; 9-regenerator feed pipeline; 9-1 the 1st secondary regenerator district charging branch line; 9-2 the 2nd secondary regenerator district charging branch line; 9-3 the 3rd secondary regenerator district charging branch line; 9-4 the 4th secondary regenerator district charging branch line; 10-dense-phase fluidized bed regenerator; 10-1 the 1st secondary regenerator district; 10-2 the 2nd secondary regenerator district; 10-3 the 3rd secondary regenerator district; 10-4 the 4th secondary regenerator district; 11-cyclone separator; 12-waste line; 13-stripper; 14-steam pipeline; 15-riser; 16-promotes gas pipeline; 17-Flow of Goods and Materials controller; 18-material overfall; 19-dividing plate; 20-aperture; The descending flow duct of 21-material; 22-bottom baffle; 23-heat-obtaining parts.
Detailed description of the invention
In order to improve the selectivity of light olefin in the technique of oxygenatedchemicals preparing low-carbon olefins, the invention provides a kind of methanol and/or the reaction unit of dimethyl ether low-carbon alkene, mainly include dense fluidized bed bioreactor (2), cyclone separator (3), stripper (5), riser (7), dense-phase fluidized bed regenerator (10), cyclone separator (11), stripper (13) and riser (15). reactor feed line (1) is connected with the bottom of dense fluidized bed bioreactor (2), stripper (5) part is in dense fluidized bed bioreactor (2), remainder is positioned at the lower section of dense fluidized bed bioreactor (2), steam pipeline (6) is connected with the bottom of stripper (5), the bottom of riser (7) is connected with the bottom of stripper (5), promote gas pipeline (8) to be connected with the bottom of riser (7), the top of riser 7 is connected with dense-phase fluidized bed regenerator (10), regenerator feed pipeline (9) is connected with the bottom of dense-phase fluidized bed regenerator (10), a part for stripper (13) is in dense-phase fluidized bed regenerator (10), remainder is positioned at dense-phase fluidized bed regenerator (10) lower section, steam pipeline (14) is connected with the bottom of stripper (13), the bottom of riser (15) is connected with the bottom of stripper (13), promote gas pipeline (16) to be connected with the bottom of riser (15), the top of riser (15) is connected with dense fluidized bed bioreactor (2). preferably, described reactor feed line (1) comprises n reaction zone feeds branch line (1-1, ..., 1-n), described dense fluidized bed bioreactor (2) by Flow of Goods and Materials controller (17) be divided into n secondary response district (2-1 ..., 2-n), n >=2, it is preferred to 8 >=n >=3, n reaction zone feeds branch line is connected with n secondary response district respectively, 1st is sequentially connected to the n-th secondary response district, the top of riser (15) is connected with the 1st secondary response district, n-th secondary response district is connected with the material overfall (18) on stripper (5) top, the top of dense fluidized bed bioreactor (2) is provided with cyclone separator (3), the top exit of cyclone separator (3) is connected with product material pipeline (4), and the bottom of cyclone separator (3) is connected with the n-th secondary response district.
Preferably, described regenerator feed pipeline (9) comprises m renewing zone charging branch line (9-1, ..., 9-m), described dense-phase fluidized bed regenerator (10) by Flow of Goods and Materials controller (17) be divided into m secondary regenerator district (10-1 ..., 10-m), m >=2, it is preferred to 8 >=m >=3; M renewing zone charging branch line is connected with m secondary regenerator district respectively;1st is sequentially connected to m-th secondary regenerator district, the top of riser (7) is connected with the 1st secondary regenerator district, m-th secondary regenerator district is connected with the material overfall (18) on stripper (13) top, the top of dense-phase fluidized bed regenerator (10) is provided with cyclone separator (11), the top exit of cyclone separator (11) is connected with waste line (12), and the bottom of cyclone separator (11) is connected with m-th secondary regenerator district.
Preferably, described Flow of Goods and Materials controller (17) is made up of dividing plate (19), aperture (20), the descending flow duct of material (21), bottom baffle (22) and heat-obtaining parts (23). Aperture (20) is positioned at the lower section of dividing plate (19), it is connected with the bottom of the descending flow duct of material (21), bottom baffle (22) can adopt porous plate or imperforate plate, it is positioned at the descending flow duct of material (21) and the bottom of aperture (20), and heat-obtaining parts (23) are fixed on dividing plate (19).
In a preferred embodiment, the schematic flow sheet of preparing light olefins from methanol of the present invention is as shown in Figure 1. the raw material being mainly methanol and/or dimethyl ether enters dense fluidized bed bioreactor (2), contact with catalyst, generate gaseous products logistics and reclaimable catalyst, gaseous products logistics and the reclaimable catalyst carried secretly enter cyclone separator (3), gaseous products logistics enters later separation workshop section through the outlet of cyclone separator, the reclaimable catalyst carried secretly enters the n-th secondary response district through the dipleg of cyclone separator, regeneration catalyzing agent is through stripper (13), riser (15) enters dense fluidized bed bioreactor 2, and sequentially through the 1st to the n-th secondary response district, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst is then through stripper (5), riser (7) enters dense-phase fluidized bed regenerator (10), and sequentially through the 1st to m-th secondary regenerator district, regeneration catalyzing agent is formed after making charcoal. described catalyst preferably includes the catalyst of SAPO molecular sieve, more preferably includes the catalyst of SAPO-34 molecular sieve.
In a specific embodiment, the structural representation of the dense-phase fluidized bed comprising 4 secondary response districts of the present invention is as in figure 2 it is shown, arrow in the A-A profile catalyst flow direction that to be secondary response interval. 3 Flow of Goods and Materials controllers (17) and a baffle plate are vertically arranged, and dense-phase fluidized bed reaction zone is divided into 4 secondary response districts, and catalyst is sequentially by the 1st to the 4th secondary response district, subsequently into stripper.
In a specific embodiment, the structural representation of the dense-phase fluidized bed comprising 4 secondary regenerator districts of the present invention is as it is shown on figure 3, arrow in the B-B profile catalyst flow direction that to be secondary regenerator interval. 3 Flow of Goods and Materials controllers (17) and a baffle plate are vertically arranged, and dense-phase fluidized bed renewing zone is divided into 4 secondary regenerator districts, and catalyst is sequentially by the 1st to the 4th secondary regenerator district, subsequently into stripper.
Preferably, the structural representation of stripper of the present invention (5 and 13) is as shown in Figure 4. Opening on the tube wall of stripper (5) top is as the material overfall (18) between the n-th secondary response district and stripper (5); Opening on the tube wall of stripper (13) top is as the material overfall (18) between m-th secondary regenerator district and stripper (13).
Preferably, the structural representation of Flow of Goods and Materials controller of the present invention is as shown in Figure 5. Flow of Goods and Materials controller (17) is made up of dividing plate (19), aperture (20), the descending flow duct of material (21), bottom baffle (22) and heat-obtaining parts (23).Catalyst is by entering the descending flow duct of material above descending flow duct, wherein gas superficial linear velocity is less than or equal to minimum fluidization velocity, catalyst in the descending flow duct of material is in close phase stacking states, form Flow of Goods and Materials motive force, promote catalyst to flow into secondary response district (or renewing zone) thereafter through aperture. Heat-obtaining parts can adopt coil arrangement, is fixed on dividing plate.
Preferably, in described dense-phase fluidized bed reaction zone, gas superficial linear velocity is 0.1-1.5m/s; In described dense-phase fluidized bed renewing zone, gas superficial linear velocity is 0.1-1.5m/s; In described Flow of Goods and Materials controller, gas superficial linear velocity is less than or equal to the minimum fluidization velocity of catalyst; Described catalyst preferably includes the catalyst of SAPO molecular sieve, more preferably includes the catalyst of SAPO-34 molecular sieve; Being provided with charging aperture bottom described reaction zone, charging includes methanol and/or dimethyl ether etc.; The stripping fluid of described stripper (13) comprises steam; Bottom, described renewing zone (10) is provided with regenerating medium entrance, and regenerating medium includes air, oxygen denuded air, steam etc.; The reaction temperature of described reaction zone (2) is 400-550 DEG C, and bed density is 200-1200kg/m3, the average coke content of catalyst is incremented by the n-th secondary response district successively by the 1st secondary response district, and the average coke content in the 1st secondary response district is 0.5-3wt%, and the average coke content in the n-th secondary response district is 7-10wt%; The reaction temperature of described renewing zone (10) is 500-700 DEG C, and bed density is 200-1200kg/m3, the average coke content of catalyst is successively decreased to m-th secondary regenerator district successively by the 1st secondary regenerator district, and the average coke content in the 1st secondary regenerator district is 3-10wt%, and the average coke content in m-th secondary regenerator district is 0-3wt%. The method adopting the present invention, it is possible to reach to control carbon deposition quantity of catalyst, improve carbon content uniformity and improve the purpose of selectivity of light olefin, there is bigger technical advantage, can be used in the commercial production of low-carbon alkene.
For the present invention is better described, it is simple to understand technical scheme, the typical but non-limiting embodiment of the present invention is as follows:
Embodiment 1
4 secondary response districts are set in dense fluidized bed bioreactor, 4 secondary regenerator districts are set in dense-phase fluidized bed regenerator, the raw material being mainly methanol and/or dimethyl ether enters dense fluidized bed bioreactor, contact with the catalyst including SAPO-34 molecular sieve, the gaseous products logistics generated and reclaimable catalyst, gaseous phase materials and the reclaimable catalyst carried secretly enter cyclone separator, gaseous products logistics enters later separation workshop section through the outlet of cyclone separator, and the reclaimable catalyst carried secretly enters the 4th secondary response district through the dipleg of cyclone separator. Regeneration catalyzing agent enters dense fluidized bed bioreactor through stripper, riser, and sequentially through the 1st to 4 secondary response districts, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst enters dense-phase fluidized bed regenerator then through stripper, riser, and sequentially through the 1st to 4 secondary regenerator districts, after making charcoal, form regeneration catalyzing agent. Dense-phase fluidized bed reactor reaction condition is: reaction temperature is 400 DEG C, and gaseous line speed is 0.3m/s, and bed density is 1000kg/m3, the average coke content in the 1st secondary response district is 2wt%, and the average coke content in the 2nd secondary response district is 6wt%, and the average coke content in the 3rd secondary response district is 8wt%, and the average coke content in the 4th secondary response district is 10wt%;Dense-phase fluidized bed regenerator reaction condition is: reaction temperature is 500 DEG C, and gaseous line speed is 0.3m/s, and bed density is 1000kg/m3, the average coke content in the 1st secondary regenerator district is 7wt%, and the average coke content in the 2nd secondary regenerator district is 4wt%, and the average coke content in the 3rd secondary regenerator district is 2wt%, and the average coke content in the 4th secondary regenerator district is 1wt%. Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 91.1wt%.
Embodiment 2
3 secondary response districts are set in dense fluidized bed bioreactor, 2 secondary regenerator districts are set in dense-phase fluidized bed regenerator, the raw material being mainly methanol and/or dimethyl ether enters dense fluidized bed bioreactor, contact with the catalyst including SAPO-34 molecular sieve, the gaseous products logistics generated and reclaimable catalyst, gaseous phase materials and the reclaimable catalyst carried secretly enter cyclone separator, gaseous products logistics enters later separation workshop section through the outlet of cyclone separator, and the reclaimable catalyst carried secretly enters the 3rd secondary response district through the dipleg of cyclone separator. Regeneration catalyzing agent enters dense fluidized bed bioreactor through stripper, riser, and sequentially through the 1st to 3 secondary response districts, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst enters dense-phase fluidized bed regenerator then through stripper, riser, and sequentially through the 1st to 2 secondary regenerator districts, after making charcoal, form regeneration catalyzing agent. Dense-phase fluidized bed reactor reaction condition is: reaction temperature is 450 DEG C, and gaseous line speed is 0.5m/s, and bed density is 900kg/m3, the average coke content in the 1st secondary response district is 3wt%, and the average coke content in the 2nd secondary response district is 7wt%, and the average coke content in the 3rd secondary response district is 9wt%; Dense-phase fluidized bed regenerator reaction condition is: reaction temperature is 600 DEG C, and gaseous line speed is 0.7m/s, and bed density is 700kg/m3, the average coke content in the 1st secondary regenerator district is 4wt%, and the average coke content in the 2nd secondary regenerator district is 2wt%. Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 90.5wt%.
Embodiment 3
6 secondary response districts are set in dense fluidized bed bioreactor, 5 secondary regenerator districts are set in dense-phase fluidized bed regenerator, the raw material being mainly methanol and/or dimethyl ether enters dense fluidized bed bioreactor, contact with the catalyst including SAPO-34 molecular sieve, the gaseous products logistics generated and reclaimable catalyst, gaseous phase materials and the reclaimable catalyst carried secretly enter cyclone separator, gaseous products logistics enters later separation workshop section through the outlet of cyclone separator, and the reclaimable catalyst carried secretly enters the 6th secondary response district through the dipleg of cyclone separator. Regeneration catalyzing agent enters dense fluidized bed bioreactor through stripper, riser, and sequentially through the 1st to 6 secondary response district, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst enters dense-phase fluidized bed regenerator then through stripper, riser, and sequentially through the 1st to 5 secondary regenerator district, after making charcoal, form regeneration catalyzing agent. Dense-phase fluidized bed reactor reaction condition is: reaction temperature is 480 DEG C, and gaseous line speed is 0.7m/s, and bed density is 700kg/m3The average coke content in the 1st secondary response district is 1wt%, the average coke content in the 2nd secondary response district is 3wt%, the average coke content in the 3rd secondary response district is 4wt%, the average coke content in the 4th secondary response district is 5wt%, the average coke content in the 5th secondary response district is 6wt%, and the average coke content in the 6th secondary response district is 7wt%;Dense-phase fluidized bed regenerator reaction condition is: reaction temperature is 650 DEG C, and gaseous line speed is 1.0m/s, and bed density is 500kg/m3The average coke content in the 1st secondary regenerator district is 5wt%, the average coke content in the 2nd secondary regenerator district is 3wt%, the average coke content in the 3rd secondary regenerator district is 2wt%, the average coke content in the 4th secondary regenerator district is 1wt%, and the average coke content in the 5th secondary regenerator district is 0.01wt%. Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 91.4wt%.
Below to the present invention have been described in detail, but the invention is not limited in detailed description of the invention described herein. It will be appreciated by those skilled in the art that in the case without departing from the scope of the present invention, it is possible to make other changes and deformation. The scope of the invention limits.
Claims (7)
1. the reaction unit for methanol and/or dimethyl ether low-carbon alkene, it is characterized in that, described reaction unit includes dense fluidized bed bioreactor (2), the first cyclone separator (3), the first stripper (5), the first riser (7), dense-phase fluidized bed regenerator (10), the second cyclone separator (11), the second stripper (13) and the second riser (15); Wherein, reactor feed line (1) is connected with described dense fluidized bed bioreactor (2) bottom; A part for described first stripper (5) is among described dense fluidized bed bioreactor (2), and remainder is in described dense fluidized bed bioreactor (2) lower section; Described first riser (7) bottom is connected with the bottom of described first stripper (5), and the top of described first riser (7) is connected with described dense-phase fluidized bed regenerator (10); Regenerator feed pipeline (9) is connected with the bottom of described dense-phase fluidized bed regenerator (10); A part for described second stripper (13) is among described dense-phase fluidized bed regenerator (10), and remainder is in described dense-phase fluidized bed regenerator (10) lower section; The bottom of described second riser (15) is connected with the bottom of described second stripper (13), the top of described second riser (15) is connected with described dense fluidized bed bioreactor (2), wherein said dense fluidized bed bioreactor (2) and/or dense-phase fluidized bed regenerator (10) has Flow of Goods and Materials controller (17), described dense fluidized bed bioreactor (2) is divided into n secondary response district by described Flow of Goods and Materials controller (17), and the 1st is sequentially connected to the n-th secondary response district; Described dense-phase fluidized bed regenerator (10) is divided into m secondary regenerator district by described Flow of Goods and Materials controller (17), and the 1st is sequentially connected to m-th secondary regenerator district; And wherein n >=2, m >=2.
2. reaction unit according to claim 1, it is characterized in that, described second riser (15) top is connected with the 1st secondary response district, and the n-th secondary response district is connected with the material overfall (18) on described first stripper (5) top; The top of described dense fluidized bed bioreactor (2) is provided with the first cyclone separator (3), the top exit of described first cyclone separator (3) is connected with product material pipeline (4), and the bottom of described first cyclone separator (3) is connected with the n-th secondary response district.
3. reaction unit according to claim 1, it is characterized in that, the top of described first riser (7) is connected with the 1st secondary regenerator district, and m-th secondary regenerator district is connected with the material overfall (18) on described second stripper (13) top;The top of described dense-phase fluidized bed regenerator (10) is provided with the second cyclone separator (11), the top exit of described second cyclone separator (11) is connected with waste line (12), and the bottom of described second cyclone separator (11) is connected with m-th secondary regenerator district.
4. reaction unit according to claim 1, it is characterised in that 8 >=n >=3.
5. reaction unit according to claim 1, it is characterised in that 8 >=m >=3.
6. the reaction unit according to any one of claim 1-5, it is characterized in that, described Flow of Goods and Materials controller (17) is made up of dividing plate (19), aperture (20), the descending flow duct of material (21), bottom baffle (22) and heat-obtaining parts (23); Described aperture (20) is positioned at the lower section of described dividing plate (19) and is connected with the descending flow duct of described material (21) bottom, described bottom baffle (22) is positioned at the descending flow duct of described material (21) and the bottom of described aperture (20), and described heat-obtaining parts (23) are fixed on described dividing plate (19).
7. reaction unit according to claim 6, it is characterised in that described bottom baffle (22) is porous plate or imperforate plate.
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Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DK3078414T3 (en) * | 2013-12-03 | 2018-10-22 | Dalian Inst Chem & Physics Cas | REACTION DEVICE FOR THE PREPARATION OF LIGHT OLEFINES FROM METHANOL AND / OR DIMETHYLETHER |
| WO2018072142A1 (en) * | 2016-10-19 | 2018-04-26 | 中国科学院大连化学物理研究所 | Method and device for manufacturing propene and c4 hydrocarbon |
| CN107963957B (en) * | 2016-10-19 | 2022-01-25 | 中国科学院大连化学物理研究所 | Method and device for preparing propylene and C4 hydrocarbon |
| US10710940B2 (en) | 2016-10-19 | 2020-07-14 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Turbulent fluidized-bed reactor, device, and method using oxygen-containing compound for manufacturing propene and C4 hydrocarbon |
| SG11201903490UA (en) * | 2016-10-19 | 2019-05-30 | Dalian Inst Chemical Physics Cas | Method and device for manufacturing propene and c4 hydrocarbon |
| CN107961743B (en) * | 2016-10-19 | 2021-12-31 | 中国科学院大连化学物理研究所 | Fast fluidized bed reactor, device and method for preparing propylene and C4 hydrocarbons from oxygen-containing compounds |
| CN107961745B (en) * | 2016-10-19 | 2021-12-14 | 中国科学院大连化学物理研究所 | Turbulent fluidized bed reactor, device and method for preparing propylene and C4 hydrocarbons from oxygen-containing compounds |
| CN108794291B (en) * | 2017-04-27 | 2020-11-27 | 中国科学院大连化学物理研究所 | Fluidized bed device and method for preparing p-xylene and co-producing low-carbon olefin by methanol and/or dimethyl ether and toluene |
| CN108786672B (en) * | 2017-04-27 | 2021-01-26 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing low-carbon olefin by using methanol and/or dimethyl ether and benzene |
| CN108786671B (en) * | 2017-04-27 | 2021-04-23 | 中国科学院大连化学物理研究所 | Fluidized bed device and method for preparing p-xylene and co-producing low-carbon olefin by methanol and/or dimethyl ether and benzene |
| CN108786670B (en) | 2017-04-27 | 2021-01-26 | 中国科学院大连化学物理研究所 | Method for preparing p-xylene and co-producing low-carbon olefin by methanol and/or dimethyl ether and toluene |
| US20230139652A1 (en) * | 2020-03-19 | 2023-05-04 | China Petroleum & Chemical Corporation | Method for regulating the gas velocity of the empty bed in a fluidized bed |
| CN114377621B (en) * | 2020-10-16 | 2024-03-19 | 中国科学院大连化学物理研究所 | Fluidized bed reactor, device and application |
| KR20230013253A (en) * | 2020-10-16 | 2023-01-26 | 달리안 인스티튜트 오브 케미컬 피직스, 차이니즈 아카데미 오브 사이언시즈 | Recycling device, device for producing low carbon olefin and its application |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
| CN101239871A (en) * | 2007-02-07 | 2008-08-13 | 中国石油化工股份有限公司 | Method for increasing selectivity of low-carbon olefins in methanol or dimethyl ether converting process |
| CN101698629A (en) * | 2009-11-04 | 2010-04-28 | 兆威兴业有限公司 | Device for preparing low-carbon olefin by adopting methanol or dimethyl ether |
| CN103193574A (en) * | 2012-01-10 | 2013-07-10 | 中国石油化工股份有限公司 | On-stream method of methanol to light olefin reaction-regeneration device |
-
2013
- 2013-12-03 CN CN201310648651.7A patent/CN104672045B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
| CN101239871A (en) * | 2007-02-07 | 2008-08-13 | 中国石油化工股份有限公司 | Method for increasing selectivity of low-carbon olefins in methanol or dimethyl ether converting process |
| CN101698629A (en) * | 2009-11-04 | 2010-04-28 | 兆威兴业有限公司 | Device for preparing low-carbon olefin by adopting methanol or dimethyl ether |
| CN103193574A (en) * | 2012-01-10 | 2013-07-10 | 中国石油化工股份有限公司 | On-stream method of methanol to light olefin reaction-regeneration device |
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