CN104826559A - Methanol-to-olefin reaction equipment - Google Patents
Methanol-to-olefin reaction equipment Download PDFInfo
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- CN104826559A CN104826559A CN201510222284.3A CN201510222284A CN104826559A CN 104826559 A CN104826559 A CN 104826559A CN 201510222284 A CN201510222284 A CN 201510222284A CN 104826559 A CN104826559 A CN 104826559A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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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 invention provides methanol-to-olefin reaction equipment which comprises a housing. A dense phase fluidized bed is arranged at the lower part of the inner side of the housing. One or more cyclone separators are arranged on the inner side of the housing. A gas-solid separator is disposed at the upper part of the inner side of the housing. The gas-solid separator comprises a first conical section. The bottom of the first conical section is sealingly connected with the inner wall of the housing. The top of the first conical section passes through a delivery pipe and is connected with the bottom of the delivery pipe. Steam stripping gratings are horizontally fixedly arranged in an annular space between the delivery pipe and the inner wall of the housing. A grating plate is horizontally fixedly disposed inside the dense phase fluidized bed. Upper free space of the reaction equipment can be reduced, and reaction time can be shortened to be closest to the optimum operating conditions. Thus, target product selectivity and olefin yield can be raised. Meanwhile, produced gases among catalyst granules and entrained and adsorbed among granule micropores are effectively reduced, target product yield is raised, and load of a regenerator is decreased. In addition, carbon content in the reaction equipment can also be adjusted. Economical benefits of the equipment are increased.
Description
Technical field
The present invention relates to olefin hydrocarbon making by coal, technical field of petrochemical industry, particularly relate to the methanol to olefins reaction equipment that in a kind of reactor with stripping grid, carbon content is adjustable.
Background technology
Low-carbon alkene (ethene and propylene etc.) is petrochemical industry base stock.Current ethene is produced primarily of naphtha steam cracking.The cost producing ethene by naphtha due to petroleum resources shortage is more and more higher.The ethylene production technique that positive active development raw material is abundanter both at home and abroad.Wherein make substantial progress with the research of methanol production ethene and propylene.
Methanol to olefins reaction belongs to gas-solid heterogeneous catalytic reaction, uses gas-solid fluidization technology.The commercial plant of current preparing low carbon olefinic hydrocarbon with methanol adopts conventional dense fluidized bed bioreactor.Dense fluidized bed bioreactor is tubular construction, and lower diameter is little, is highly 6 ~ 8m; Upper diameter expands, and is highly 12 ~ 16m; High 2 ~ the 6m of middle transition section.Be provided with feed distributor at reactor bottom, top is provided with cyclone separator, and dipleg and flutter valve are arranged at the bottom of cyclone separator.The feature that methyl alcohol produces olefin process is: reaction speed is fast, thermal discharge is large, alcohol agent is than low.Reaction requires strictly to control the reaction time, to reach olefine selective and the olefin yields of expection.Existing conventional dense fluidized bed bioreactor controls the reaction time by controlling fluid catalyst controlling level, generally controls at 3 ~ 6m by fluid catalyst controlling level, reaction time 1 ~ 3s.And reactor fluid bed material level has the distance of 15 ~ 20m to top cyclone inlet, gaseous product carries partially catalyzed agent and upwards flows after leaving fluid catalyst charge level, through the free space of 15 ~ 20m, the time of staying reaches 20 ~ 30s, off-target operating condition makes the selective and productive rate of object product (ethene, propylene) decline, and affects the economic interests of device.
Conventional reactor bottom is close phase section, and top is dilute phase section (usual enlarged diameter).Feed process gas at dense-phase fluidized bed bottom gas distributor in production, bubble upwards flows under bed buoyancy, enters dilute phase section through dense-phase bed.Gas entrainment portions fine particle continues upwards to flow, lower at dilute phase section gas flow rate.Owing to being natural subsidence, reactor top dilute phase section requires lower flow velocity, and need to expand device diameters, the fine particle concentration entering top cyclone inlet after natural subsidence is generally 5 ~ 10kg/m
3, to ask fine particle concentration lower than this value, fluidized-bed reactor conventional at present cannot realize.
There is a kind of methanol to olefins reaction device at present, by traditional settling section, change carrier pipe into, greatly reduce the time of staying of reactor product at free space.Meanwhile, pre-separation facility is adopted to be separated fast with catalyst by product gas.But owing to still there is gas-solid skewness in dense-phase fluidized bed, the problem that gas-particle two-phase back-mixing is serious, this can cause the generation of byproduct equally, and object product yield and conversion ratio reduce.
The catalyst that methanol-to-olefins uses has elliposoidal cage and the three-dimensional open-framework of oxygen eight ring formation, can the production ethene of efficient selective and propylene, and some high intermediate carbon, high-carbon hydrocarbon or the branched chain hydrocarbon produced in molecular sieve cannot diffuse out, be gathered in cage and produce carbon distribution.Carbon distribution can not only make catalysqt deactivation, and affects the distribution of product.In order to ensure the productive rate of product gas ethene, propylene in commercial plant, the carbon content of necessary results of regular determination catalyst.
Coke on regenerated catalyst is comparatively large by the impact of operating condition, and generally speaking, coke content is high, and catalyst activity reduces, thus the conversion ratio of directly impact reaction, ethene, productivity of propylene are declined.Coke content also can not be too low, because carbon plays the effect of guard catalyst to a certain extent, can suppress overreaction, the service life of extending catalyst.Under normal condition, the optimum range of regenerated catalyst coke content is 1.5 ~ 2.0%, and the optimum range of the coke content of reclaimable catalyst is 7.0 ~ 7.5%.Commercial plant data show, if the coke content of catalyst is lower than optimum range, the productive rate of ethene, propylene is very low; Higher than optimum range, catalyst activity reduces, and ethene, productivity of propylene reduce, and now primary product is dimethyl ether.Therefore coke on regenerated catalyst is controlled in optimum range, significantly can improve conversion ratio and the yield of object product.
In methanol to olefins reaction, catalyst from reactor out after, between particles, can carry and adsorb a certain amount of product gas secretly in granule pores, this part gas accounts for 2 ~ 4% of product population, if after this part product gas stripping, then allow this part catalyst enter into regenerator, the loss of useful product gas can be effectively reduced, and bringing into due to this part product gas, regenerator load can be increased.
Thus, the present inventor relies on experience and the practice of being engaged in relevant industries for many years, proposes a kind of methanol to olefins reaction equipment, to overcome the defect of prior art.
Summary of the invention
The object of the present invention is to provide a kind of methanol to olefins reaction equipment, effectively reduce consersion unit top free space, Reaction time shorten, makes it closer to optimum operation condition, thus improves object product (ethene, propylene) selective and olefin yields; Meanwhile, the output gas effectively reduce between catalyst granules, carrying secretly and adsorb between granule pores, improves object product yield, reduces the load of regenerator, can also regulate carbon content in consersion unit, improve the economic benefit of device.
The object of the present invention is achieved like this, a kind of methanol to olefins reaction equipment, comprise a seal casinghousing, described case inside bottom is provided with dense-phase fluidized bed, described case top is provided with output gas vent, described case inside is positioned at below described output gas vent and is provided with one or more cyclone separator, tangentially throughly inside each described cyclone separator be connected with one first inlet tube, a particle efferent duct is vertically provided with bottom each described cyclone separator, described case inside top is provided with a gas-solid separating device, with described first inlet tube conducting above described gas-solid separating device, described gas-solid separating device comprises one and diametrically goes up convergent, first conical section of up/down perforation, be tightly connected with described inner walls bottom described first conical section, described first conical section top is through is connected to a up/down perforation, bottom the carrier pipe of vertical setting, laterally stripping grid is fixedly installed in annular space between described carrier pipe and described inner walls, be positioned at above described first conical section lateral wall, the first shell space is formed below described stripping grid and between described inner walls, described first shell space side and described dense-phase fluidized bed conducting, described first shell space opposite side and turned on outside, described dense-phase fluidized bed inner transverse is fixedly installed flase floor.
In a better embodiment of the present invention, described carrier pipe top is connected with a fast separation device, be provided with an outer cover from top to down outside described carrier pipe and described fast separation device, above described outer cover, be provided with the first outlet, described first outlet and described first inlet tube conducting; Described shield base opening is positioned at above described stripping grid.
In a better embodiment of the present invention, described outer cover comprises the first straight tube be positioned at above described stripping grid, described fast separation device is arranged at described first straight tube inner upper, described first straight tube top is connected with the second conical section diametrically going up convergent, described second conical section top is connected with the first end socket, described first end socket sidewall is arranged described first outlet; Described first outlet and described first inlet tube coaxial communication.
In a better embodiment of the present invention, be provided with a particle above described stripping grid and pass through device, described particle comprises by device the conical hopper that diametrically descends convergent, up/down perforation, be tightly connected with described housing sidewall above described conical hopper, described conical hopper sidewall is provided with multiple sieve aperture, through connection one straight length bottom described conical hopper.
In a better embodiment of the present invention, below described particle efferent duct, be provided with loosening distribution device in gas-fluid.
In a better embodiment of the present invention, described outer cover comprises the second straight tube arranged above described stripping grid, described second straight tube internal diameter is less than described fast separation device contour dimension, described second straight tube top is connected with the triconic section diametrically going up flaring, described triconic section top is connected with the 3rd straight tube, described fast separation device is arranged at described 3rd straight tube inner upper, described 3rd straight tube top is connected with the second end socket, and described second end socket top arranges described first outlet; Be provided with air chamber below described product exhaust outlets, be communicated with described cyclone separator top bottom described air chamber.
In a better embodiment of the present invention, below described stripping grid, be provided with stripped vapor entrance; The housing sidewall that described first shell space is corresponding is provided with the first through hole and the second through hole, described hull outside is positioned at described dense-phase fluidized bed upper position and is provided with third through-hole, described first through hole is outside through is connected with catalyst circulation pipe, described catalyst circulation pipe lower ending opening is connected with described third through-hole is through obliquely, and described second through hole is outside through is connected with spent agent efferent duct.
In a better embodiment of the present invention, described catalyst circulation pipe is provided with guiding valve.
In a better embodiment of the present invention, described flase floor quantity is one group, two or more sets.
In a better embodiment of the present invention, be provided with feed distributor below described flase floor, described housing bottom is provided with unstripped gas entrance, is connected below described feed distributor with described unstripped gas inlet seal; Described hull outside is provided with regenerative agent ascending pipe, and described regenerative agent ascending pipe is connected with described dense-phase fluidized bed top is through.
From the above mentioned, methanol to olefins reaction equipment provided by the invention has following beneficial effect:
1, methanol to olefins reaction equipment of the present invention is provided with flase floor in dense-phase fluidized bed inside, flase floor produces strong shearing and crushing effect to the bubble through baffle layer, significantly can reduce the size of bubble in dense-phase fluidized bed, improve the contact effect of gas-solid; Meanwhile, improve the operational stability with dense-phase fluidized bed that is uniformly distributed of gas phase, reduce solid particle back-mixing vertically, and then improve the homogeneity of device interior radial temperature, improve conversion ratio and the yield of target product.
2, in methanol to olefins reaction equipment of the present invention, above first conical section lateral wall, stripping grid is set, make the catalyst solid particle separated through stripping, reduce the intragranular carbon distribution of catalyst solid, by the catalyst circulation pipe of stripping section and dense-phase fluidized bed conducting, can catalyst solid particulate carbonaceous amount in flexible modulation dense-phase fluidized bed, conversion ratio and the yield of target product can be improved; Catalyst solid particle enters regenerator again after stripping, can improve object product yield, reduce the load of regenerator.
3, be provided with carrier pipe and fast separation device in methanol to olefins reaction equipment of the present invention, make output gas equipment leading out fast, reduce the time of staying in a device, thus decrease the generation of byproduct, improve the yield of output gas; Simultaneously under the effect of fast separation device, in gas-solid mixture, most of catalyst solid particle separation out falls into underlying space, effectively reduces fine particle concentration in cyclone inlet gas.
Accompanying drawing explanation
The following drawings is only intended to schematically illustrate the present invention and explain, not delimit the scope of the invention.Wherein:
Fig. 1: be the structural representation of methanol to olefins reaction apparatus embodiments one of the present invention.
Fig. 2: be the structural representation of methanol to olefins reaction apparatus embodiments two of the present invention.
Detailed description of the invention
In order to there be understanding clearly to technical characteristic of the present invention, object and effect, now contrast accompanying drawing and the specific embodiment of the present invention is described.
As Fig. 1, shown in Fig. 2, methanol to olefins reaction equipment 1000 of the present invention, comprise a seal casinghousing 10, housing 10 lower inside is provided with dense-phase fluidized bed 20, housing 10 top is provided with output gas vent 101, be positioned at inside housing 10 below output gas vent 101 and be provided with one or more cyclone separator 30 (prior art), in the present embodiment, the quantity of cyclone separator 30 can be one to two ten, tangentially throughly inside each described cyclone separator 30 be connected with one first inlet tube 301, in the present embodiment, first inlet tube 301 is rectangular tube, (particle efferent duct 302 is tubular structure to be vertically provided with a particle efferent duct 302 bottom each cyclone separator 30, for clear expression operation principle, simply represent with lines in figure), in order to ensure catalyst solid particle one-way flow from top to bottom, flutter valve 3021 is provided with bottom particle efferent duct 302, housing 10 inside upper part is provided with a gas-solid separating device 40, with the first inlet tube 301 conducting above gas-solid separating device 40, gas-solid separating device 40 comprises the first conical section 401 that diametrically goes up convergent, up/down perforation, in the present embodiment, is positioned at the position of above dense-phase fluidized bed 20 Bed level 3 to 6 meters bottom the first conical section 401, be connected with housing 10 inner wall sealing bottom first conical section 401, first conical section 401 top is through is connected to a up/down perforation, bottom the carrier pipe 402 of vertical setting, laterally stripping grid 50 is fixedly installed in annular space between carrier pipe 402 and housing 10 inwall, be positioned at above the first conical section 401 lateral wall, the first shell space 102 is formed below stripping grid 50 and between housing 10 inwall, first shell space 102 side and dense-phase fluidized bed 20 conducting, in order to regulate the catalyst solid particulate carbonaceous amount in dense-phase fluidized bed 20, conversion ratio and the yield of target product can be improved, first shell space 102 opposite side and turned on outside, under the effect at stripped vapor of the catalyst solid particle of stripping grid 50, output gas between removing catalyst granules, between granule pores, through stripping, the intragranular carbon distribution of catalyst solid reduces, catalyst solid particle enters outside regenerator (prior art, not shown) again after stripping, can improve object product yield, reduce the load of regenerator.
As shown in Figure 1 and Figure 2, dense-phase fluidized bed 20 inner transverse is fixedly installed flase floor 60.In the present embodiment, flase floor 60 quantity is one group, two or more sets, often organize flase floor 60 to be made up of multiple guide vane 601, flase floor 60 superjacent air space is divided into multiple parallel flow region by guide vane 601, adjacent area makes gas-particle two-phase produce cross flow one due to the setting direction difference of guide vane 601, thus strong shearing and crushing effect are produced to the bubble through flase floor 60, significantly reduce the size of bubble in dense-phase fluidized bed 20, improve the contact effect of gas-solid; Meanwhile, improve the operational stability with dense-phase fluidized bed that is uniformly distributed of gas phase, reduce catalyst solid particle back-mixing vertically, and then improve the homogeneity of device interior radial temperature, improve conversion ratio and the yield of target product.In the present embodiment, below flase floor 60, be provided with feed distributor 70, bottom housing 10, be provided with unstripped gas entrance 103, be tightly connected with unstripped gas entrance 103 below feed distributor 70; Housing 10 arranged outside has regenerative agent ascending pipe 104, and regenerative agent ascending pipe 104 is connected with dense-phase fluidized bed 20 top is through.In the present embodiment, when adopting two groups of flase floors 60, the one group of flase floor 60 being positioned at below is arranged at the position of above feed distributor 70 0.8 to 1.5 meter, and the one group of flase floor 60 being positioned at top is arranged at the position of below dense-phase fluidized bed 20 Bed level 0.3 to 0.8 meter.
Further, as shown in Figure 1 and Figure 2, carrier pipe 402 top is connected with a fast separation device 403, and in the present embodiment, fast separation device 403 is vortex flow quicks parted hair (prior art).Carrier pipe 402 and fast separation device 403 make output gas derive methanol to olefins reaction equipment 1000 fast, reduce the time of staying in a device, thus decrease the generation of byproduct, improve the yield of output gas.An outer cover 404 is provided with from top to down outside carrier pipe 402 and fast separation device 403; the first outlet 4041 is provided with above outer cover 404; first outlet 4041 and the first inlet tube 301 conducting; outer cover 404 bottom opening is positioned at above stripping grid 50; output gas and partially catalyzed agent solid particle mixture enter cyclone separator 30 by first outlet the 4041, first inlet tube 301, and catalyst solid particle is returned above stripping grid 50 by the particle efferent duct 302 bottom cyclone separator 30.
Further, stripped vapor entrance 501 is provided with below stripping grid 50, housing 10 sidewall of the first shell space 102 correspondence is provided with the first through hole 1021 and the second through hole 1022, be positioned at dense-phase fluidized bed 20 upper position outside housing 10 and be provided with third through-hole 105, first through hole 1021 is outside through is connected with catalyst circulation pipe 106, catalyst circulation pipe 106 lower ending opening is connected with third through-hole 105 is through obliquely, catalyst circulation pipe 106 is provided with guiding valve 1061, guiding valve 1061 ensures the catalyst solid particle unidirectional dense-phase fluidized bed 20 flowing into below from top to bottom in the first shell space 102, the unstrpped gas in dense-phase fluidized bed 20 is avoided to enter above the first shell space 102 and be mixed in output gas, and regulate catalyst solid particle back amount by aperture adjustment, second through hole 1022 is outside through is connected with spent agent efferent duct 107, and spent agent efferent duct 107 other end is connected to regenerator (prior art, not shown).
Embodiment one
As shown in Figure 1, outer cover 404 comprises the first straight tube 4042 be positioned at above stripping grid 50, fast separation device 403 is arranged at the first straight tube 4042 inner upper, first straight tube 4042 top is connected with the second conical section 4043 diametrically going up convergent, second conical section 4043 top is connected with the first end socket 4044, first end socket 4044 sidewall is arranged the first outlet 4041, first outlet 4041 and the first inlet tube 301 coaxial communication.As shown in Figure 1, a particle is provided with by device 51 above stripping grid 50, particle comprises by device 51 conical hopper 511 that diametrically descends convergent, up/down perforation, be tightly connected with housing 10 sidewall above conical hopper 511, conical hopper 511 sidewall is provided with multiple sieve aperture 5111, in the present embodiment, the percent opening of sieve aperture 5111 is 3% ~ 5%, through connection one straight length 512 bottom conical hopper 511.The space high speed of the catalyst solid particle separated in fast separation device 403 between carrier pipe 402 and the first straight tube 4042 rotates, particle decreases catalyst solid particle with gas axially upwardly back-mixing by device 51, and catalyst solid particle falls into stripping grid 50 through particle by device 51 and carries out stripping; In order to avoid catalyst solid particle is piled up below particle efferent duct 302, below particle efferent duct 302, be provided with loosening distribution device in gas-fluid 3022.
When the methanol to olefins reaction equipment 1000 of the present embodiment one works, methanol feedstock gas enters bottom dense-phase fluidized bed 20 from feed distributor 70, bubble upwards flows under the buoyancy of dense-phase fluidized bed 20 bed, and bubble is by flase floor 60 shearing-crushing, and size reduces; Catalyst solid particle contacts in bubble and dense-phase fluidized bed 20 is also converted into the alkene such as ethene, propylene output gas with catalyst reaction, output gas is entrained with partially catalyzed agent solid particle to be continued upwards to flow, along with gas rises, part large granular catalyst settles down gradually, after the free space of 3 to 6 meters, enter the first conical section 401 and carrier pipe 402.Due to 10 to 20 times that gas flow rate in carrier pipe 402 is dilute phase space flow velocity above the inner dense-phase fluidized bed 20 of housing 10, significantly shortened (generally can shorten to 1 to 2 second) output gas time of staying in methanol to olefins reaction equipment 1000.
The output gas carrying partially catalyzed agent solid particle enters the fast separation device 403 at its top through carrier pipe 402, gas-solid mixture does high speed rotary motion in fast separation device 403, carry out gas solid separation under the influence of centrifugal force, major part catalyst solid particle separation gets off to enter between outer cover 404 and carrier pipe 402, catalyst solid particle enters stripping grid 50 through particle by device 51 under gravity, steam is entered by stripped vapor entrance 501 and carries out stripping to particle, catalyst solid particle after stripping is divided into two parts, a part returns dense-phase fluidized bed 20 through catalyst circulation pipe 106, another part enters regenerator regeneration through spent agent efferent duct 107.
The output gas separated from fast separation device 403 carries fraction catalyst solid particle and discharges from the first outlet 4041, and in output gas, catalyst fines granule density is from 20 ~ 30Kg/m common response equipment
3be down to 0.2 ~ 0.3Kg/m
3, output gas enters in cyclone separator 30 through the first inlet tube 301, and the catalyst solid particle separated returns above stripping grid 50 through particle efferent duct 302, and the self-produced exhaust outlets 101 of the output gas separated enters successive container.
From the above mentioned, methanol to olefins reaction equipment provided by the invention has following beneficial effect:
1, methanol to olefins reaction equipment of the present invention is provided with flase floor in dense-phase fluidized bed inside, flase floor produces strong shearing and crushing effect to the bubble through baffle layer, significantly can reduce the size of bubble in dense-phase fluidized bed, improve the contact effect of gas-solid; Meanwhile, improve the operational stability with dense-phase fluidized bed that is uniformly distributed of gas phase, reduce solid particle back-mixing vertically, and then improve the homogeneity of device interior radial temperature, improve conversion ratio and the yield of target product.
2, in methanol to olefins reaction equipment of the present invention, above first conical section lateral wall, stripping grid is set, make the catalyst solid particle separated through stripping, reduce the intragranular carbon distribution of catalyst solid, by the catalyst circulation pipe of stripping section and dense-phase fluidized bed conducting, can catalyst solid particulate carbonaceous amount in flexible modulation dense-phase fluidized bed, conversion ratio and the yield of target product can be improved; Catalyst solid particle enters regenerator again after stripping, can improve object product yield, reduce the load of regenerator.
3, be provided with carrier pipe and fast separation device in methanol to olefins reaction equipment of the present invention, make output gas draw equipment fast, reduce the time of staying in a device, thus decrease the generation of byproduct, improve the yield of output gas; Simultaneously under the effect of fast separation device, in gas-solid mixture, most of catalyst solid particle separation out falls into underlying space, effectively reduces fine particle concentration in cyclone inlet gas.
Embodiment two
The present embodiment is identical with structure with the general principle of embodiment one, its difference is, as shown in Figure 2, outer cover 404 comprises the second straight tube 4045 arranged above stripping grid 50, second straight tube 4045 internal diameter is less than fast separation device 403 contour dimension, second straight tube 4045 top is connected with the triconic section 4046 diametrically going up flaring, triconic section 4046 top is connected with the 3rd straight tube 4047, fast separation device 403 is arranged at the 3rd straight tube 4047 inner upper, 3rd straight tube 4047 top is connected with the second end socket 4048, second end socket 4048 top is provided with the first outlet 4041, first outlet 4041 and the first inlet tube 301 conducting.In the present embodiment, below the product exhaust outlets 101 at housing 10 top, be provided with air chamber 1011, be communicated with cyclone separator 30 top bottom air chamber 1011.
When the methanol to olefins reaction equipment 1000 of the present embodiment two works, methanol feedstock gas enters bottom dense-phase fluidized bed 20 from feed distributor 70, bubble upwards flows under the buoyancy of dense-phase fluidized bed 20 bed, and bubble is by flase floor 60 shearing-crushing, and size reduces; Catalyst solid particle contacts in bubble and dense-phase fluidized bed 20 is also converted into the alkene such as ethene, propylene output gas with catalyst reaction, output gas is entrained with partially catalyzed agent solid particle to be continued upwards to flow, along with gas rises, part large granular catalyst settles down gradually, after the free space of 3 to 6 meters, enter the first conical section 401 and carrier pipe 402.Due to 10 to 20 times that gas flow rate in carrier pipe 402 is dilute phase space flow velocity above the inner dense-phase fluidized bed 20 of housing 10, significantly shortened (generally can shorten to 1 to 2 second) output gas time of staying in methanol to olefins reaction equipment 1000.
The output gas carrying partially catalyzed agent solid particle enters the fast separation device 403 at its top through carrier pipe 402, gas-solid mixture does high speed rotary motion in fast separation device 403, carry out gas solid separation under the influence of centrifugal force, major part catalyst solid particle separation gets off to enter between outer cover 404 and carrier pipe 402, catalyst solid particle enters stripping grid 50 under gravity, steam is entered by stripped vapor entrance 501 and carries out stripping to particle, catalyst solid particle after stripping is divided into two parts, a part returns dense-phase fluidized bed 20 through catalyst circulation pipe 106, another part enters regenerator regeneration through spent agent efferent duct 107.
The output gas separated from fast separation device 403 carries fraction catalyst solid particle and discharges from the first outlet 4041, and in output gas, catalyst fines granule density is from 20 ~ 30Kg/m common response equipment
3be down to 0.2 ~ 0.3Kg/m
3output gas enters in cyclone separator 30 through the first inlet tube 301, the catalyst solid particle separated returns above stripping grid 50 through particle efferent duct 302, and the self-produced exhaust outlets 101 of the air chamber 1011 of the output gas separated through cyclone separator 30 top enters successive container.
The present embodiment beneficial effect is identical with embodiment one, does not repeat them here.
The foregoing is only the schematic detailed description of the invention of the present invention, and be not used to limit scope of the present invention.Any those skilled in the art, equivalent variations done under the prerequisite not departing from design of the present invention and principle and amendment, all should belong to the scope of protection of the invention.
Claims (10)
1. a methanol to olefins reaction equipment, comprise a seal casinghousing, described case inside bottom is provided with dense-phase fluidized bed, described case top is provided with output gas vent, described case inside is positioned at below described output gas vent and is provided with one or more cyclone separator, tangentially throughly inside each described cyclone separator be connected with one first inlet tube, a particle efferent duct is vertically provided with bottom each described cyclone separator, it is characterized in that: described case inside top is provided with a gas-solid separating device, with described first inlet tube conducting above described gas-solid separating device, described gas-solid separating device comprises one and diametrically goes up convergent, first conical section of up/down perforation, be tightly connected with described inner walls bottom described first conical section, described first conical section top is through is connected to a up/down perforation, bottom the carrier pipe of vertical setting, laterally stripping grid is fixedly installed in annular space between described carrier pipe and described inner walls, be positioned at above described first conical section lateral wall, the first shell space is formed below described stripping grid and between described inner walls, described first shell space side and described dense-phase fluidized bed conducting, described first shell space opposite side and turned on outside, described dense-phase fluidized bed inner transverse is fixedly installed flase floor.
2. methanol to olefins reaction equipment as claimed in claim 1, it is characterized in that: described carrier pipe top is connected with a fast separation device, an outer cover is provided with from top to down outside described carrier pipe and described fast separation device, the first outlet is provided with, described first outlet and described first inlet tube conducting above described outer cover; Described shield base opening is positioned at above described stripping grid.
3. methanol to olefins reaction equipment as claimed in claim 2, it is characterized in that: described outer cover comprises the first straight tube be positioned at above described stripping grid, described fast separation device is arranged at described first straight tube inner upper, described first straight tube top is connected with the second conical section diametrically going up convergent, described second conical section top is connected with the first end socket, described first end socket sidewall is arranged described first outlet; Described first outlet and described first inlet tube coaxial communication.
4. methanol to olefins reaction equipment as claimed in claim 3, it is characterized in that: be provided with a particle above described stripping grid and pass through device, described particle comprises by device the conical hopper that diametrically descends convergent, up/down perforation, be tightly connected with described housing sidewall above described conical hopper, described conical hopper sidewall is provided with multiple sieve aperture, through connection one straight length bottom described conical hopper.
5. methanol to olefins reaction equipment as claimed in claim 4, is characterized in that: be provided with loosening distribution device in gas-fluid below described particle efferent duct.
6. methanol to olefins reaction equipment as claimed in claim 2, it is characterized in that: described outer cover comprises the second straight tube arranged above described stripping grid, described second straight tube internal diameter is less than described fast separation device contour dimension, described second straight tube top is connected with the triconic section diametrically going up flaring, described triconic section top is connected with the 3rd straight tube, described fast separation device is arranged at described 3rd straight tube inner upper, described 3rd straight tube top is connected with the second end socket, and described second end socket top arranges described first outlet; Be provided with air chamber below described product exhaust outlets, be communicated with described cyclone separator top bottom described air chamber.
7. methanol to olefins reaction equipment as claimed in claim 1, is characterized in that: be provided with stripped vapor entrance below described stripping grid; The housing sidewall that described first shell space is corresponding is provided with the first through hole and the second through hole, described hull outside is positioned at described dense-phase fluidized bed upper position and is provided with third through-hole, described first through hole is outside through is connected with catalyst circulation pipe, described catalyst circulation pipe lower ending opening is connected with described third through-hole is through obliquely, and described second through hole is outside through is connected with spent agent efferent duct.
8. methanol to olefins reaction equipment as claimed in claim 7, is characterized in that: described catalyst circulation pipe is provided with guiding valve.
9. methanol to olefins reaction equipment as claimed in claim 1, is characterized in that: described flase floor quantity is one group, two or more sets.
10. methanol to olefins reaction equipment as claimed in claim 1, it is characterized in that: be provided with feed distributor below described flase floor, described housing bottom is provided with unstripped gas entrance, is connected below described feed distributor with described unstripped gas inlet seal; Described hull outside is provided with regenerative agent ascending pipe, and described regenerative agent ascending pipe is connected with described dense-phase fluidized bed top is through.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106045808A (en) * | 2016-06-01 | 2016-10-26 | 石宝珍 | Reaction method and device for preparing hydrocarbon products from methyl alcohol |
| CN111715153A (en) * | 2019-03-18 | 2020-09-29 | 江苏博颂化工科技有限公司 | Alkane dehydrogenation circulating fluidized bed reaction device |
| CN115501822A (en) * | 2021-06-23 | 2022-12-23 | 中国石油化工股份有限公司 | Convection type fluidized bed reactor and application thereof |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060147355A1 (en) * | 2004-12-30 | 2006-07-06 | Beech James H Jr | Fluidizing a population of catalyst particles having a low catalyst fines content |
| CN202962434U (en) * | 2012-04-27 | 2013-06-05 | 李小燕 | Reactor, with isolation awl and predissociation function, for alkene preparation by methanol |
| CN203411513U (en) * | 2013-07-09 | 2014-01-29 | 刘英聚 | Fluidized bed grid equipment |
| CN104474978A (en) * | 2014-12-12 | 2015-04-01 | 神华集团有限责任公司 | Device and method for preparing alkene from methanol and/or dimethyl ether |
| CN204685072U (en) * | 2015-05-05 | 2015-10-07 | 中国石油大学(北京) | Methanol to olefins reaction equipment |
-
2015
- 2015-05-05 CN CN201510222284.3A patent/CN104826559B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20060147355A1 (en) * | 2004-12-30 | 2006-07-06 | Beech James H Jr | Fluidizing a population of catalyst particles having a low catalyst fines content |
| CN202962434U (en) * | 2012-04-27 | 2013-06-05 | 李小燕 | Reactor, with isolation awl and predissociation function, for alkene preparation by methanol |
| CN203411513U (en) * | 2013-07-09 | 2014-01-29 | 刘英聚 | Fluidized bed grid equipment |
| CN104474978A (en) * | 2014-12-12 | 2015-04-01 | 神华集团有限责任公司 | Device and method for preparing alkene from methanol and/or dimethyl ether |
| CN204685072U (en) * | 2015-05-05 | 2015-10-07 | 中国石油大学(北京) | Methanol to olefins reaction equipment |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106045808A (en) * | 2016-06-01 | 2016-10-26 | 石宝珍 | Reaction method and device for preparing hydrocarbon products from methyl alcohol |
| CN106045808B (en) * | 2016-06-01 | 2019-07-26 | 石宝珍 | Methanol hydrocarbon products reaction method and device |
| CN111715153A (en) * | 2019-03-18 | 2020-09-29 | 江苏博颂化工科技有限公司 | Alkane dehydrogenation circulating fluidized bed reaction device |
| CN111715153B (en) * | 2019-03-18 | 2022-08-05 | 江苏博颂化工科技有限公司 | Alkane dehydrogenation circulating fluidized bed reaction device |
| CN115501822A (en) * | 2021-06-23 | 2022-12-23 | 中国石油化工股份有限公司 | Convection type fluidized bed reactor and application thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104826559B (en) | 2016-11-16 |
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