CN104672045A - Reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether - Google Patents
Reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether Download PDFInfo
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- CN104672045A CN104672045A CN201310648651.7A CN201310648651A CN104672045A CN 104672045 A CN104672045 A CN 104672045A CN 201310648651 A CN201310648651 A CN 201310648651A CN 104672045 A CN104672045 A CN 104672045A
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- 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 invention relates to a reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether, in particular to a reaction device for preparing low-carbon olefin by employing methyl alcohol and/or dimethyl ether. The reaction device mainly comprises a dense-phase fluidized bed reactor (2), a cyclone separator (3), a stripper (5), a lift pipe (7), a dense-phase fluidized bed regenerator (10), a cyclone separator (11), a stripper (13) and a lift pipe (15), wherein the dense-phase fluidized bed reactor (2) is partitioned into n (n is greater than or equal to 2) secondary reaction zones by material flow controllers (17); and the dense-phase fluidized bed regenerator (10) is partitioned into m (m is greater than or equal to 2) secondary regeneration zones by the material flow controllers (17). By virtue of the reaction device, the problems in the prior art that carbon deposit distribution of a catalyst is uneven and low-carbon olefin selectivity is relatively low are solved.
Description
Technical field
The present invention relates to a kind of reaction unit for methyl alcohol and/or dimethyl ether low-carbon alkene.
Background technology
Low-carbon alkene, i.e. ethene and propylene, be two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are produced by petroleum path, but due to the limited supply of petroleum resources and higher price, produce ethene by petroleum resources, the cost of propylene constantly increases.In recent years, people start to greatly develop the technology that alternative materials transforms ethene processed, propylene.The technique of preparing olefin by conversion of methanol (MTO) is subject to increasing attention, has realized the industrial scale of megaton.Along with the development of world economy, 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 growth of the demand of China's ethene 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 excellent catalytic performance when reacting for MTO, there is very high selectivity of light olefin, and activity is very high, but catalyzer loses activity due to carbon distribution in use for some time.In use there is obvious inductive phase in SAPO-34 molecular sieve catalyst, within inductive phase, the selectivity of alkene is lower, the selectivity of alkane is higher, and along with the increase in reaction times, selectivity of light olefin rises gradually, after inductive phase, catalyzer keeps high selectivity and high activity within a certain period of time, and along with the continuation of time extends, the activity of catalyzer declines rapidly.
Technology and reactor that a kind of methanol conversion is low-carbon alkene is disclosed in US6166282, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas 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 after product gas and catalyzer sharp separation, effectively prevent the generation of secondary reaction.Through analog calculation, compared with traditional bubbling fluidization bed bioreactor, needed for this fast fluidized bed reactor internal diameter and catalyzer, reserve all greatly reduces.But in the method, low-carbon alkene carbon base absorption rate is generally all about 77%, there is the problem that yield of light olefins is lower.
CN101402538B discloses a kind of method improving yield of light olefins, the method adopts and arranges a second reaction zone on the first top, reaction zone that methanol conversion is low-carbon alkene, and this second reaction zone diameter is greater than the first reaction zone, to increase the residence time of product gas in second reaction zone of the first reaction zone outlet, make unreacted methyl alcohol, the dme generated and carbon more than four hydrocarbon continue reaction, reach the object improving yield of light olefins, although the method can improve the yield of low-carbon alkene to a certain extent, but because the first reaction zone catalyzer is out with more carbon distribution, and carbon more than four hydrocarbon pyrolysis needs higher catalyst activity, therefore carbon more than the four hydrocarbon transformation efficiency in the method in second reaction zone is still on the low side, thus cause yield of light olefins on the low side.
CN102276406A discloses a kind of production method of propylene enhancing.This technology arranges three reaction zones, and the first fast bed reaction zone is used for methanol conversion to alkene, and riser reaction zone and the series connection of the second fast bed reaction zone are for transforming ethene, carbon more than four hydrocarbon and unreacted methyl alcohol or dme.In this patent, the residence time of material 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 causes propene yield on the low side.
CN102875289A discloses a kind of fluidized bed reaction of internal layout riser reactor, for improving the productive rate of low-carbon alkene.First raw material enters fluidized bed reaction zone, with catalyst exposure, generates the product comprising low-carbon alkene, forms reclaimable catalyst simultaneously; A reclaimable catalyst part enters revivifier regeneration, and form regenerated catalyst, a part enters the riser tube that exit end is positioned at inside, reaction zone, with the second contact raw, is promoted to by reclaimable catalyst in reaction zone; Regenerated catalyst 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 revivifier, burns with oxygen, reduces the output of low-carbon alkene.
The methanol-to-olefins technology that CN102875296A announces is provided with fast bed, down-flow fluidized bed using ECT and riser tube three reaction zones.Catalyzer at revivifier, fast bed, circulate between riser tube and down-flow fluidized bed using ECT, flow to very complicated, assignment of traffic and control very difficult, the activity change of catalyzer is larger.
Known in the field, the selectivity of low-carbon alkene is closely related with the carbon deposition quantity on catalyzer, ensure high selectivity of light olefin, SAPO-34 catalyzer needs the carbon distribution of some amount.The main reactor that current MTO technique adopts is fluidized-bed, and fluidized-bed is close to complete mixing flow reactor, and catalyst carbon deposit distribution is very wide, is unfavorable for the selectivity improving low-carbon alkene.The agent alcohol of MTO technique is less than very, coking yield is lower, realize larger, hold manageable catalyst recirculation amount, just to need in breeding blanket by the carbon deposition quantity on catalyzer, carbon content uniformity controlling at certain level, and then reach the object of the carbon deposition quantity controlled on the inner catalyst of reaction zone, carbon content homogeneity.Therefore, control carbon deposition quantity of catalyst in reaction zone and carbon content homogeneity in certain level be the gordian technique in MTO technique.
For solving the problem, several researchers have proposed and upper and lower two reaction zones, two fluidized-bed series connection, fluidized-bed and the technology such as riser tube, down-flow fluidized bed using ECT series connection are set in fluidized-bed, tentatively disclose the method controlling carbon deposition quantity of catalyst and carbon content homogeneity, achieve certain beneficial effect, but also increase complicacy, the increase of control difficulty of MTO technique simultaneously.The present invention proposes the scheme forming multiple second order reaction district (breeding blanket) by arranging inner member in dense phase fluidized bed and solve the problem controlling carbon deposition quantity of catalyst and carbon content homogeneity, and then improve the selectivity of low-carbon alkene.
Summary of the invention
Technical problem to be solved by this invention is the problem that the selectivity of light olefin that exists in prior art is not high, provides a kind of reaction unit of raising selectivity of light olefin newly.This reaction unit is used for, in the production of low-carbon alkene, having the advantage of catalyst carbon deposition good uniformity, yield of light olefins more high and low carbon olefin production technique better economy.
For solving the problem, the invention provides a kind of reaction unit for methyl alcohol and/or dimethyl ether low-carbon alkene, described reaction unit comprises dense fluidized bed bioreactor (2), cyclonic separator (3), stripper (5), riser tube (7), dense phase fluidized bed revivifier (10), cyclonic separator (11), stripper (13) and riser tube (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 rest part is in described dense fluidized bed bioreactor (2) below; Described riser tube (7) bottom is connected with the bottom of described stripper (5), and the top of described riser tube (7) is connected with described dense phase fluidized bed revivifier (10); Regenerator feed pipeline (9) is connected with the bottom of described dense phase fluidized bed revivifier (10); A part for described stripper (13) is among described dense phase fluidized bed revivifier (10), and rest part is in described dense phase fluidized bed revivifier (10) below; The bottom of described riser tube (15) is connected with the bottom of described stripper (13), the top of described riser tube (15) is connected with described dense fluidized bed bioreactor (2), it is characterized in that, in described dense fluidized bed bioreactor (2) and/or dense phase fluidized bed revivifier (10), there is Flow of Goods and Materials controller (17), described dense fluidized bed bioreactor (2) is divided into n second order reaction district by described Flow of Goods and Materials controller (17), and the 1st is sequentially connected to the n-th second order reaction district; Described dense phase fluidized bed revivifier (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 secondary regenerator district; And wherein n >=2, m >=2.
In a preferred embodiment, described riser tube (15) top is connected with the 1st second order reaction district, and the n-th second order reaction district is connected with the material overflow port (18) on described stripper (5) top; The top of described dense fluidized bed bioreactor (2) is provided with cyclonic separator (3), the top exit of described cyclonic separator (3) is connected with product material pipeline (4), and the bottom of described cyclonic separator (3) is connected with the n-th second order reaction district.
In a preferred embodiment, the top of described riser tube (7) is connected with the 1st secondary regenerator district, and m secondary regenerator district is connected with the material overflow port (18) on described stripper (13) top; The top of described dense phase fluidized bed revivifier (10) is provided with cyclonic separator (11), the top exit of described cyclonic separator (11) is connected with waste line (12), and the bottom of described cyclonic separator (11) is connected with m 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 below 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 bottom of the descending flow duct of described material (21) and 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 effect 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 lower, it is low to wear and tear.
(2) the gas speed 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 catalyzer, catalyzer is in close phase stacking states, define the one-way sealing phase transportation flow of catalyzer, avoid the catalyzer back-mixing between adjacent second order reaction district (or adjacent secondary regenerator district), 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 second order reaction district by Flow of Goods and Materials controller, and catalyzer is successively by the 1st second order reaction district of second order reaction district to the n-th, and residence time destribution is narrow, and the homogeneity of reclaimable catalyst carbon content increases substantially.
(5) breeding blanket is divided into m secondary regenerator district by Flow of Goods and Materials controller, and catalyzer passes through the 1st secondary regenerator district successively to m secondary regenerator district, and residence time destribution is narrow, and the homogeneity of regenerated catalyst carbon content increases substantially.
(6) achieve the carbon content controlling regenerated catalyst and reclaimable catalyst comparatively accurately, and carbon content distribution is comparatively even, 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) the carbon content distribution because of catalyzer is comparatively even, and the catalyst inventory needed for reaction zone reduces.
(8) structure in multiple second order reaction district is convenient to the maximization of realization response device.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention;
Fig. 2 is the structural representation comprising the dense phase fluidized bed in 4 second order reaction districts of the present invention, and the arrow wherein in A-A sectional view is the catalyzer flow direction in second order reaction interval;
Fig. 3 is the structural representation comprising the dense phase fluidized bed in 4 secondary regenerator districts of the present invention, and the arrow wherein in B-B sectional view is the catalyzer flow direction in secondary regenerator 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; 1-1 the 1st second order reaction district charging branch line; 1-2 the 2nd second order reaction district charging branch line; 1-3 the 3rd second order reaction district charging branch line; 1-4 the 4th second order reaction district charging branch line; 2-dense fluidized bed bioreactor; 2-1 the 1st second order reaction district; 2-2 the 2nd second order reaction district; 2-3 the 3rd second order reaction district; 2-4 the 4th second order reaction district; 3-cyclonic separator; 4-product material pipeline; 5-stripper; 6-water vapour pipeline; 7-riser tube; 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 revivifier; 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-cyclonic separator; 12-waste line; 13-stripper; 14-water vapour pipeline; 15-riser tube; 16-promotes gas pipeline; 17-Flow of Goods and Materials controller; 18-material overflow port; 19-dividing plate; 20-aperture; The descending flow duct of 21-material; 22-bottom baffle; 23-heat-obtaining parts.
Embodiment
In order to improve the selectivity of light olefin in the technique of oxygenatedchemicals preparing low-carbon olefins, the invention provides the reaction unit of a kind of methyl alcohol and/or dimethyl ether low-carbon alkene, mainly comprise dense fluidized bed bioreactor (2), cyclonic separator (3), stripper (5), riser tube (7), dense phase fluidized bed revivifier (10), cyclonic separator (11), stripper (13) and riser tube (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), rest part is positioned at the below of dense fluidized bed bioreactor (2), water vapour pipeline (6) is connected with the bottom of stripper (5), the bottom of riser tube (7) is connected with the bottom of stripper (5), promote gas pipeline (8) to be connected with the bottom of riser tube (7), the top of riser tube 7 is connected with dense phase fluidized bed revivifier (10), regenerator feed pipeline (9) is connected with the bottom of dense phase fluidized bed revivifier (10), a part for stripper (13) is in dense phase fluidized bed revivifier (10), rest part is positioned at dense phase fluidized bed revivifier (10) below, water vapour pipeline (14) is connected with the bottom of stripper (13), the bottom of riser tube (15) is connected with the bottom of stripper (13), promote gas pipeline (16) to be connected with the bottom of riser tube (15), the top of riser tube (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 second order reaction district (2-1 ..., 2-n), n >=2, are preferably 8 >=n >=3; N reaction zone feeds branch line is connected with n second order reaction district respectively; 1st is sequentially connected to the n-th second order reaction district, the top of riser tube (15) is connected with the 1st second order reaction district, n-th second order reaction district is connected with the material overflow port (18) on stripper (5) top, the top of dense fluidized bed bioreactor (2) is provided with cyclonic separator (3), the top exit of cyclonic separator (3) is connected with product material pipeline (4), and the bottom of cyclonic separator (3) is connected with the n-th second order reaction district.
Preferably, described regenerator feed pipeline (9) comprises m breeding blanket charging branch line (9-1,9-m), described dense phase fluidized bed revivifier (10) by Flow of Goods and Materials controller (17) be divided into m secondary regenerator district (10-1 ..., 10-m), m >=2, are preferably 8 >=m >=3; M breeding blanket charging branch line is connected with m secondary regenerator district respectively; 1st is sequentially connected to m secondary regenerator district, the top of riser tube (7) is connected with the 1st secondary regenerator district, m secondary regenerator district is connected with the material overflow port (18) on stripper (13) top, the top of dense phase fluidized bed revivifier (10) is provided with cyclonic separator (11), the top exit of cyclonic separator (11) is connected with waste line (12), and the bottom of cyclonic separator (11) is connected with m 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 below of dividing plate (19), be 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 bottom of the descending flow duct of material (21) and 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 as shown in Figure 1.The raw material being mainly methyl alcohol and/or dme enters dense fluidized bed bioreactor (2), with catalyst exposure, generate gaseous products logistics and reclaimable catalyst, gaseous products logistics and the reclaimable catalyst carried secretly enter cyclonic separator (3), gaseous products logistics enters later separation workshop section through the outlet of cyclonic separator, the reclaimable catalyst carried secretly enters the n-th second order reaction district through the dipleg of cyclonic separator, regenerated catalyst is through stripper (13), riser tube (15) enters dense fluidized bed bioreactor 2, and sequentially through the 1st to the n-th second order reaction district, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst is again through stripper (5), riser tube (7) enters dense phase fluidized bed revivifier (10), and sequentially through the 1st to m secondary regenerator district, regenerated catalyst is formed after making charcoal.Described catalyzer preferably includes the catalyzer of SAPO molecular sieve, more preferably comprises the catalyzer of SAPO-34 molecular sieve.
In a specific embodiment, as shown in Figure 2, the arrow in A-A sectional view is the catalyzer flow direction in second order reaction interval to the structural representation comprising the dense phase fluidized bed in 4 second order reaction districts of the present invention.3 Flow of Goods and Materials controllers (17) and a baffle plate are vertically arranged, and dense phase fluidized bed reaction zone are divided into 4 second order reaction districts, and catalyzer sequentially by the 1st to the 4th second order reaction district, then enters stripper.
In a specific embodiment, as shown in Figure 3, the arrow in B-B sectional view is the catalyzer flow direction in secondary regenerator interval to the structural representation comprising the dense phase fluidized bed in 4 secondary regenerator districts of the present invention.3 Flow of Goods and Materials controllers (17) and a baffle plate are vertically arranged, and dense phase fluidized bed breeding blanket are divided into 4 secondary regenerator districts, and catalyzer sequentially by the 1st to the 4th secondary regenerator district, then enters stripper.
Preferably, the structural representation of stripper of the present invention (5 and 13) as shown in Figure 4.Opening on the tube wall of stripper (5) top is as the material overflow port (18) between the n-th second order reaction district and stripper (5); Opening on the tube wall of stripper (13) top is as the material overflow port (18) between m secondary regenerator district and stripper (13).
Preferably, the structural representation of Flow of Goods and Materials controller of the present invention 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).Catalyzer 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, catalyzer in the descending flow duct of material is in close phase stacking states, form Flow of Goods and Materials impellent, promote catalyzer through inflow second order reaction district (or breeding blanket) thereafter, aperture.Heat-obtaining parts can adopt coil arrangement, are 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 breeding blanket, 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 catalyzer; Described catalyzer preferably includes the catalyzer of SAPO molecular sieve, more preferably comprises the catalyzer of SAPO-34 molecular sieve; Be provided with opening for feed bottom described reaction zone, charging comprises methyl alcohol and/or dme etc.; The stripping fluid of described stripper (13) comprises water vapour; Bottom, described breeding blanket (10) is provided with regenerating medium entrance, and regenerating medium comprises air, oxygen-denuded air, water vapour etc.; The temperature of reaction of described reaction zone (2) is 400-550 DEG C, and bed density is 200-1200kg/m
3, the average coke content of catalyzer is increased progressively successively by second order reaction district of the 1st second order reaction district to the n-th, and the average coke content in the 1st second order reaction district is 0.5-3wt%, and the average coke content in the n-th second order reaction district is 7-10wt%; The temperature of reaction of described breeding blanket (10) is 500-700 DEG C, and bed density is 200-1200kg/m
3, the average coke content of catalyzer is successively decreased to m 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 secondary regenerator district is 0-3wt%.Adopt method of the present invention, can reach and control carbon deposition quantity of catalyst, improve carbon content homogeneity and improve the object of selectivity of light olefin, there is larger technical superiority, can be used in the industrial production of low-carbon alkene.
For better the present invention being described, be convenient to understand technical scheme of the present invention, typical but non-limiting embodiment of the present invention is as follows:
Embodiment 1
4 second order reaction districts are set in dense fluidized bed bioreactor, 4 secondary regenerator districts are set in dense phase fluidized bed revivifier, the raw material being mainly methyl alcohol and/or dme enters dense fluidized bed bioreactor, with the catalyst exposure comprising SAPO-34 molecular sieve, the gaseous products logistics generated and reclaimable catalyst, gaseous phase materials and the reclaimable catalyst carried secretly enter cyclonic separator, gaseous products logistics enters later separation workshop section through the outlet of cyclonic separator, and the reclaimable catalyst carried secretly enters the 4th second order reaction district through the dipleg of cyclonic separator.Regenerated catalyst enters dense fluidized bed bioreactor through stripper, riser tube, and sequentially through the 1st to 4 second order reaction districts, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst enters dense phase fluidized bed revivifier through stripper, riser tube again, and sequentially through the 1st to 4 secondary regenerator districts, after making charcoal, form regenerated catalyst.Dense phase fluidized bed reactor reaction condition is: temperature of reaction is 400 DEG C, and gaseous line speed is 0.3m/s, and bed density is 1000kg/m
3, the average coke content in the 1st second order reaction district is 2wt%, and the average coke content in the 2nd second order reaction district is 6wt%, and the average coke content in the 3rd second order reaction district is 8wt%, and the average coke content in the 4th second order reaction district is 10wt%; Dense phase fluidized bed revivifier reaction conditions is: temperature of reaction is 500 DEG C, and gaseous line speed is 0.3m/s, and bed density is 1000kg/m
3, 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 second order reaction districts are set in dense fluidized bed bioreactor, 2 secondary regenerator districts are set in dense phase fluidized bed revivifier, the raw material being mainly methyl alcohol and/or dme enters dense fluidized bed bioreactor, with the catalyst exposure comprising SAPO-34 molecular sieve, the gaseous products logistics generated and reclaimable catalyst, gaseous phase materials and the reclaimable catalyst carried secretly enter cyclonic separator, gaseous products logistics enters later separation workshop section through the outlet of cyclonic separator, and the reclaimable catalyst carried secretly enters the 3rd second order reaction district through the dipleg of cyclonic separator.Regenerated catalyst enters dense fluidized bed bioreactor through stripper, riser tube, and sequentially through the 1st to 3 second order reaction districts, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst enters dense phase fluidized bed revivifier through stripper, riser tube again, and sequentially through the 1st to 2 secondary regenerator districts, after making charcoal, form regenerated catalyst.Dense phase fluidized bed reactor reaction condition is: temperature of reaction is 450 DEG C, and gaseous line speed is 0.5m/s, and bed density is 900kg/m
3, the average coke content in the 1st second order reaction district is 3wt%, and the average coke content in the 2nd second order reaction district is 7wt%, and the average coke content in the 3rd second order reaction district is 9wt%; Dense phase fluidized bed revivifier reaction conditions is: temperature of reaction is 600 DEG C, and gaseous line speed is 0.7m/s, and bed density is 700kg/m
3, 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 second order reaction districts are set in dense fluidized bed bioreactor, 5 secondary regenerator districts are set in dense phase fluidized bed revivifier, the raw material being mainly methyl alcohol and/or dme enters dense fluidized bed bioreactor, with the catalyst exposure comprising SAPO-34 molecular sieve, the gaseous products logistics generated and reclaimable catalyst, gaseous phase materials and the reclaimable catalyst carried secretly enter cyclonic separator, gaseous products logistics enters later separation workshop section through the outlet of cyclonic separator, and the reclaimable catalyst carried secretly enters the 6th second order reaction district through the dipleg of cyclonic separator.Regenerated catalyst enters dense fluidized bed bioreactor through stripper, riser tube, and sequentially through the 1 to 6 second order reaction district, reclaimable catalyst is formed after carbon distribution, reclaimable catalyst enters dense phase fluidized bed revivifier through stripper, riser tube again, and sequentially through the 1 to 5 secondary regenerator district, after making charcoal, form regenerated catalyst.Dense phase fluidized bed reactor reaction condition is: temperature of reaction is 480 DEG C, and gaseous line speed is 0.7m/s, and bed density is 700kg/m
3the average coke content in the 1st second order reaction district is 1wt%, the average coke content in the 2nd second order reaction district is 3wt%, the average coke content in the 3rd second order reaction district is 4wt%, the average coke content in the 4th second order reaction district is 5wt%, the average coke content in the 5th second order reaction district is 6wt%, and the average coke content in the 6th second order reaction district is 7wt%; Dense phase fluidized bed revivifier reaction conditions is: temperature of reaction is 650 DEG C, and gaseous line speed is 1.0m/s, and bed density is 500kg/m
3the 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 invention has been detailed description, but the present invention is not limited to embodiment 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, other changes and distortion can be made.Scope of the present invention is defined by the following claims.
Claims (7)
1. the reaction unit for methyl alcohol and/or dimethyl ether low-carbon alkene, it is characterized in that, described reaction unit comprises dense fluidized bed bioreactor (2), cyclonic separator (3), stripper (5), riser tube (7), dense phase fluidized bed revivifier (10), cyclonic separator (11), stripper (13) and riser tube (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 rest part is in described dense fluidized bed bioreactor (2) below; Described riser tube (7) bottom is connected with the bottom of described stripper (5), and the top of described riser tube (7) is connected with described dense phase fluidized bed revivifier (10); Regenerator feed pipeline (9) is connected with the bottom of described dense phase fluidized bed revivifier (10); A part for described stripper (13) is among described dense phase fluidized bed revivifier (10), and rest part is in described dense phase fluidized bed revivifier (10) below; The bottom of described riser tube (15) is connected with the bottom of described stripper (13), the top of described riser tube (15) is connected with described dense fluidized bed bioreactor (2), in wherein said dense fluidized bed bioreactor (2) and/or dense phase fluidized bed revivifier (10), there is Flow of Goods and Materials controller (17), described dense fluidized bed bioreactor (2) is divided into n second order reaction district by described Flow of Goods and Materials controller (17), and the 1st is sequentially connected to the n-th second order reaction district; Described dense phase fluidized bed revivifier (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 secondary regenerator district; And wherein n >=2, m >=2.
2. reaction unit according to claim 1, it is characterized in that, described riser tube (15) top is connected with the 1st second order reaction district, and the n-th second order reaction district is connected with the material overflow port (18) on described stripper (5) top; The top of described dense fluidized bed bioreactor (2) is provided with cyclonic separator (3), the top exit of described cyclonic separator (3) is connected with product material pipeline (4), and the bottom of described cyclonic separator (3) is connected with the n-th second order reaction district.
3. reaction unit according to claim 1, it is characterized in that, the top of described riser tube (7) is connected with the 1st secondary regenerator district, and m secondary regenerator district is connected with the material overflow port (18) on described stripper (13) top; The top of described dense phase fluidized bed revivifier (10) is provided with cyclonic separator (11), the top exit of described cyclonic separator (11) is connected with waste line (12), and the bottom of described cyclonic separator (11) is connected with m secondary regenerator district.
4. reaction unit according to claim 1, is characterized in that, 8 >=n >=3.
5. reaction unit according to claim 1, is characterized 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 below 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 bottom of the descending flow duct of described material (21) and described aperture (20), and described heat-obtaining parts (23) are fixed on described dividing plate (19).
7. reaction unit according to claim 6, is characterized in that, described bottom baffle (22) is porous plate or imperforate plate.
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Effective date of registration: 20230404 Address after: 116318 Xingang village, Changxing Island Economic Zone, Dalian, Liaoning Patentee after: Zhongke New Catalytic Technology (Dalian) Co.,Ltd. Address before: 116023 No. 457, Zhongshan Road, Liaoning, Dalian Patentee before: DALIAN INSTITUTE OF CHEMICAL PHYSICS, CHINESE ACADEMY OF SCIENCES |