CN204685073U - Methanol to olefins reaction equipment - Google Patents
Methanol to olefins reaction equipment Download PDFInfo
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- CN204685073U CN204685073U CN201520285696.7U CN201520285696U CN204685073U CN 204685073 U CN204685073 U CN 204685073U CN 201520285696 U CN201520285696 U CN 201520285696U CN 204685073 U CN204685073 U CN 204685073U
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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
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Abstract
The utility model is a kind of methanol to olefins reaction equipment, comprise a housing, case inside bottom is provided with dense-phase fluidized bed, top is provided with output gas vent, an air chamber is provided with below output gas vent, throughly below air chamber be connected with one or more cyclone separator, tangentially throughly inside each cyclone separator be connected with the first inlet tube, bottom is vertically provided with a conducting in the particle efferent duct of dense-phase fluidized bed, case inside top is provided with a gas-solid separating device, gas-solid separating device and the first inlet tube conducting, dense-phase fluidized bed inner transverse is installed with flase floor.This equipment effectively reduces consersion unit top free space, and Reaction time shorten makes it closer to optimum operation condition, thus improves object product (ethene, propylene) selective and olefin yields, improves the economic benefit of device; Meanwhile, effectively reduce fine particle concentration in cyclone inlet gas, improve the service efficiency of catalyst.
Description
Technical field
The utility model relates to olefin hydrocarbon making by coal, technical field of petrochemical industry, particularly relates to a kind of methanol to olefins reaction equipment of deriving fast with the output gas of quick separating structure.
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.
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.
Utility model content
The purpose of this utility model is to provide a kind of methanol to olefins reaction equipment, effectively reduce consersion unit top free space, Reaction time shorten, make it closer to optimum operation condition, thus improve object product (ethene, propylene) selective and olefin yields, improve the economic benefit of device; Meanwhile, effectively reduce fine particle concentration in cyclone inlet gas, improve the service efficiency of catalyst.
The purpose of this utility model realizes like this, a kind of methanol to olefins reaction equipment, comprise the lower little large housing of a sealing, 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 an air chamber, throughly below described air chamber be connected with one or more cyclone separator, tangentially throughly inside each described cyclone separator be connected with one first inlet tube, a conducting is vertically provided with in the particle efferent duct of described dense-phase fluidized bed bottom each described cyclone separator, described case inside top is provided with a gas-solid separating device, described gas-solid separating device and described first inlet tube conducting, described dense-phase fluidized bed inner transverse is installed with flase floor.
In a better embodiment of the present utility model, described gas-solid separating device bottom opening, described gas-solid separating device bottom outside and described case inside wall are tightly connected, bottom described gas-solid separating device, described case inside space is divided into upper space and lower space, described gas-solid separating device comprises a up/down perforation, the carrier pipe of vertical setting, 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, the first outlet is provided with above described outer cover, described first outlet and described first inlet tube conducting, the first conical section top of a up/down perforation is connected to bottom described carrier pipe, described first conical section diametrically descends flaring, described first conical section lateral wall superjacent air space and described dense-phase fluidized bed from top to down one-way conduction are connected.
In a better embodiment of the present utility model, described shield base is provided with the second conical section of up/down perforation, described second conical section diametrically goes up convergent, form bottom described second conical section bottom described gas-solid separating device, described second conical section bottom outside and described case inside wall are tightly connected, described first conical section is positioned at inside described second conical section, be connected with inside described second conical section by an annular slab bottom described first conical section, on described annular slab, circumference is evenly provided with multiple slotted eye; Described second conical section sidewall is provided with the first through hole, and described particle efferent duct sealing enters described dense-phase fluidized bed by described first through hole; Described first outlet and described first inlet tube coaxial communication.
In a better embodiment of the present utility model, described outer cover comprises the first straight tube be positioned at above described second conical section, described fast separation device is arranged at described first straight tube inner upper, described first straight tube top is connected with the triconic section diametrically going up convergent, described triconic section top is connected with the first end socket, described first end socket sidewall is arranged described first outlet; Described slotted eye circumferential width is greater than the distance between every two slotted eyes, and described slotted eye is arranged with check valve sheet.
In a better embodiment of the present utility model, described outer cover comprises the second straight tube be positioned at above described second conical section, described second straight tube internal diameter is less than described fast separation device contour dimension, the 4th conical section diametrically going up flaring is connected with above described second straight tube, the 3rd straight tube is connected with above described 4th conical section, described fast separation device is arranged at described 3rd straight tube inner upper, described 3rd straight tube top is connected with the 5th conical section diametrically going up convergent, described 5th conical section top is connected with the second end socket, described second end socket sidewall is arranged described first outlet, described slotted eye circumferential width is less than the distance between every two slotted eyes.
In a better embodiment of the present utility model, form bottom described first conical section bottom described gas-solid separating device, described first conical section bottom outside and described case inside wall are tightly connected, described outer cover comprises the 4th straight tube arranged above described first conical section, described fast separation device is arranged at described 4th straight tube inner upper, described 4th straight tube top is connected with the 6th conical section diametrically going up flaring, described 6th conical section top is connected with the 5th straight tube, described 5th straight tube top is connected with the 3rd end socket, described 3rd end socket top arranges described first outlet, described particle efferent duct outlet is positioned at above described first conical section.
In a better embodiment of the present utility model, described hull outside is positioned at described first conical section top position and is provided with 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 second through hole is outside through is connected with catalyst circulation standpipe, described catalyst circulation lower riser end opening is connected with described third through-hole is through obliquely, and described catalyst circulation standpipe is provided with guiding valve.
In a better embodiment of the present utility model, the lower position being positioned at described second through hole above described first conical section lateral wall is provided with loosening distribution device in gas-fluid.
In a better embodiment of the present utility model, described flase floor quantity is one group, two or more sets.
In a better embodiment of the present utility model, 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, and described hull outside is also provided with spent agent efferent duct, and described spent agent efferent duct is connected with described dense-phase fluidized bed bottom is through.
From the above mentioned, methanol to olefins reaction equipment of the present utility model has following beneficial effect:
1, methanol to olefins reaction equipment of the present utility model 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, be provided with carrier pipe and fast separation device in methanol to olefins reaction equipment of the present utility model, 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.
3, in methanol to olefins reaction equipment of the present utility model first conical section lateral wall superjacent air space and dense-phase fluidized bed from top to down one-way conduction be connected, make the catalyst fast return dense-phase fluidized bed separated, improve the service efficiency of catalyst.
Accompanying drawing explanation
The following drawings is only intended to schematically illustrate the utility model and explain, does not limit scope of the present utility model.Wherein:
Fig. 1: be the structural representation of methanol to olefins reaction apparatus embodiments one of the present utility model.
Fig. 2: be the structural representation of methanol to olefins reaction apparatus embodiments two of the present utility model.
Fig. 3: be the structural representation of methanol to olefins reaction apparatus embodiments three of the present utility model.
Fig. 4: be the annular slab schematic diagram of methanol to olefins reaction apparatus embodiments one of the present utility model.
Fig. 5: be the annular slab schematic diagram of methanol to olefins reaction apparatus embodiments two of the present utility model.
Detailed description of the invention
In order to there be understanding clearly to technical characteristic of the present utility model, object and effect, now contrast accompanying drawing and detailed description of the invention of the present utility model is described.
As Fig. 1, Fig. 2, shown in Fig. 3, methanol to olefins reaction equipment 1000 of the present utility model, comprise the lower little large housing 10 of a sealing, 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 an air chamber 102, throughly below air chamber 102 be connected with cyclone separator 30 (prior art), in the present embodiment, the quantity of cyclone separator 30 can be one to two ten, tangentially throughly inside every platform cyclone separator 30 be connected with the first inlet tube 301, in the present embodiment, first inlet tube 301 is rectangular tube, (particle efferent duct 302 is tubular structure in the particle efferent duct 302 of dense-phase fluidized bed 20 to be vertically provided with conducting bottom cyclone separator 30, for clear expression operation principle, simply represent with lines in figure), housing 10 inside upper part is provided with a gas-solid separating device 40, gas-solid separating device 40 top and the first inlet tube 301 conducting, dense-phase fluidized bed 20 inner transverse is installed with flase floor 50.In the present embodiment, flase floor 50 quantity is one group, two or more sets, often organize flase floor 50 to be made up of multiple guide vane 501, flase floor 50 superjacent air space is divided into multiple parallel flow region by guide vane 501, adjacent area makes gas-particle two-phase produce cross flow one due to the setting direction difference of guide vane 501, thus strong shearing and crushing effect are produced to the bubble through flase floor 50, 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 50, be provided with feed distributor 60, bottom housing 10, be provided with unstripped gas entrance 103, be tightly connected with unstripped gas entrance 103 below feed distributor 60; 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, is also provided with spent agent efferent duct 105 outside housing 10, and spent agent efferent duct 105 is connected with dense-phase fluidized bed 20 bottom is through.In the present embodiment, when adopting two groups of flase floors 50, the one group of flase floor 50 being positioned at below is arranged at the position of above feed distributor 60 0.8 to 1.5 meter, and the one group of flase floor 50 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, Figure 2, Figure 3 shows, gas-solid separating device 40 bottom opening, gas-solid separating device 40 bottom outside and housing 10 madial wall are tightly connected, bottom gas-solid separating device 40, housing 10 inner space is divided into upper space and lower space, the carrier pipe 401 that gas-solid separating device 40 comprises a up/down perforation, vertically arranges, carrier pipe 401 top is connected with a fast separation device 402, in the present embodiment, fast separation device 402 is vortex flow quicks parted hair (prior art).Carrier pipe 401 and fast separation device 402 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 403 is provided with from top to down outside carrier pipe 401; the first outlet 4031 is provided with above outer cover 403; first outlet 4031 and the first inlet tube 301 conducting; output gas and partially catalyzed agent solid particle mixture enter cyclone separator 30 by first outlet the 4031, first inlet tube 301, and catalyst solid particle returns dense-phase fluidized bed 20 by the particle efferent duct 302 bottom cyclone separator 30.The first conical section 404 top of a up/down perforation is connected to bottom carrier pipe 401, first conical section 404 diametrically descends flaring, first conical section 404 lateral wall superjacent air space and dense-phase fluidized bed 20 from top to down one-way conduction are connected, exporting from fast separation device 402 the most of catalyst solid particle separated falls above the first conical section 404 lateral wall from top to bottom, first conical section 404 lateral wall superjacent air space and dense-phase fluidized bed 20 from top to down one-way conduction make the catalyst solid particle fast return dense-phase fluidized bed 20 that separates, improve the service efficiency of catalyst.In the present embodiment, the position of above dense-phase fluidized bed 20 Bed level 3 to 6 meters is positioned at bottom the first conical section 404.
Embodiment one
As a kind of preferred embodiment of present embodiment, as shown in Figure 1, the second conical section 4032 of up/down perforation is provided with bottom outer cover 403, second conical section 4032 diametrically goes up convergent, the bottom of gas-solid separating device 40 is formed bottom second conical section 4032, second conical section 4032 bottom outside and housing 10 madial wall are tightly connected, first conical section 404 is positioned at inside the second conical section 4032, be connected with inside the second conical section 4032 by an annular slab 405 bottom first conical section 404, as shown in Figure 4, on annular slab 405, circumference is evenly provided with multiple slotted eye 4051; Second conical section 4032 sidewall is provided with the first through hole 40321, and particle efferent duct 302 seals and enters dense-phase fluidized bed 20 by the first through hole 40321; Outer cover 403 is provided with quantity identical with cyclone separator 30 first export 4031, each first outlet 4031 respectively with the first inlet tube 301 coaxial communication.
As shown in Figure 1, outer cover 403 is included in the first straight tube 4033 above the second conical section 4032, fast separation device 402 is arranged at the first straight tube 4033 inner upper, first straight tube 4033 top is connected with the triconic section 40331 diametrically going up convergent, triconic section 40331 top be connected with the first end socket 40332, the first end socket 40332 sidewall is provided with quantity identical with cyclone separator 30 first export 4031; As shown in Figure 4, slotted eye 4051 circumferential width on annular slab 405 is greater than the distance between every two slotted eyes, is provided with check valve sheet 40511 (prior art) on the downside of slotted eye 4051.Check valve sheet 40511 can ensure the catalyst solid particle unidirectional dense-phase fluidized bed 20 flowing into below from top to bottom above the first conical section 404 sidewall effectively, the unstrpped gas in dense-phase fluidized bed 20 can be stoped upwards to enter above the first conical section 404 sidewall simultaneously, thus avoid unstrpped gas to be mixed in output gas.
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 60, bubble upwards flows under the buoyancy of dense-phase fluidized bed 20 bed, and bubble is by flase floor 50 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 404 and carrier pipe 401.Due to 10 to 20 times that gas flow rate in carrier pipe 401 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 402 at its top through carrier pipe 401, gas-solid mixture does high speed rotary motion in fast separation device 402, carry out gas solid separation under the influence of centrifugal force, major part catalyst solid particle separation gets off to enter between outer cover 403 and carrier pipe 401, and catalyst solid particle falls into dense-phase fluidized bed 20 by the slotted eye 4051 on annular slab 405 under gravity; The output gas separated from fast separation device 402 carries fraction catalyst solid particle and discharges from the first outlet 4031, 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 dense-phase fluidized bed 20 through particle efferent duct 302, and the output gas separated enters successive container through the self-produced exhaust outlets 101 of air chamber 102.
From the above mentioned, methanol to olefins reaction equipment of the present utility model has following beneficial effect:
1, methanol to olefins reaction equipment of the present utility model 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, be provided with carrier pipe and fast separation device in methanol to olefins reaction equipment of the present utility model, 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.
3, in methanol to olefins reaction equipment of the present utility model first conical section sidewall superjacent air space and dense-phase fluidized bed from top to down one-way conduction be connected, make the catalyst fast return dense-phase fluidized bed separated, improve the service efficiency of catalyst.
Embodiment two
The present embodiment is identical with structure with the general principle of embodiment one, and its difference is the different of outer cover 403 version, the first conical section 404 and dense-phase fluidized bed 20 one-way conduction mode from top to down.
As shown in Figure 2, in the present embodiment two, the second conical section 4032 of up/down perforation is provided with bottom outer cover 403, second conical section 4032 diametrically goes up convergent, the bottom of gas-solid separating device 40 is formed bottom second conical section 4032, second conical section 4032 bottom outside and housing 10 madial wall are tightly connected, first conical section 404 is positioned at inside the second conical section 4032, be connected with inside the second conical section 4032 by an annular slab 405 bottom first conical section 404, as shown in Figure 5, annular slab 405 is evenly provided with multiple slotted eye 4051; Second conical section 4032 sidewall is provided with the first through hole 40321, and particle efferent duct 302 seals and enters dense-phase fluidized bed 20 by the first through hole 40321; Outer cover 403 is provided with quantity identical with cyclone separator 30 first export 4031, each first outlet 4031 respectively with the first inlet tube 301 coaxial communication.
As shown in Figure 2, outer cover 403 is included in the second straight tube 4034 connected above the second conical section 4032, second straight tube 4034 internal diameter is less than the contour dimension of fast separation device 402, the 4th conical section 40341 diametrically going up flaring is connected with above second straight tube 4034, the 3rd straight tube 40342 is connected with above 4th conical section 40341, fast separation device 402 is arranged at the 3rd straight tube 40342 inner upper, 3rd straight tube 40342 top is connected with the 5th conical section 40343 diametrically going up convergent, 5th conical section 40343 top is connected with the second end socket 40344, second end socket 40344 sidewall is provided with quantity identical with cyclone separator 30 first export 4031, as shown in Figure 5, slotted eye 4051 circumferential width on annular slab 405 is less than the distance between every two slotted eyes, less slotted eye makes the narrow space above annular slab 405, between the second conical section 4032 and the first conical section 404 retain the catalyst granules of certain altitude, form material envelope, avoid the unstrpped gas in dense-phase fluidized bed 20 enter above the first conical section 404 and be mixed in output gas.
Operation principle, the course of work of the present embodiment two are identical with embodiment one with beneficial effect, do not repeat them here.
Embodiment three
As shown in Figure 3, in the present embodiment three, form bottom first conical section 404 bottom gas-solid separating device 40, first conical section 404 bottom outside and housing 10 madial wall are tightly connected, outer cover 403 comprises the 4th straight tube 4035 arranged above the first conical section 404, fast separation device 402 is arranged at the 4th straight tube 4035 inner upper, 4th straight tube 4035 top is connected with the 6th conical section 40351 diametrically going up flaring, 6th conical section 40351 top is connected with the 5th straight tube 40352, 5th straight tube 40352 top is connected with the 3rd end socket 40353, 3rd end socket 40353 top is provided with the first outlet 4031, first outlet 4031 and the first inlet tube 301 conducting.Particle efferent duct 302 outlet is positioned at above the first conical section 404, and the catalyst solid particle of discharging in particle efferent duct 302 falls into above the first conical section 404 lateral wall.
As shown in Figure 3, be positioned at the first conical section 404 top position outside housing 10 and be provided with the second through hole 106, be positioned at dense-phase fluidized bed 20 upper position outside housing 10 and be provided with third through-hole 107, second through hole 106 is outside through is connected with catalyst circulation standpipe 108, catalyst circulation standpipe 108 lower ending opening is connected with third through-hole 107 is through obliquely, catalyst circulation standpipe 108 is provided with guiding valve 1081 (prior art), guiding valve 1081 ensures the catalyst solid particle unidirectional dense-phase fluidized bed 20 flowing into below from top to bottom above the first conical section 404 sidewall, the unstrpped gas in dense-phase fluidized bed 20 is avoided to enter above the first conical section 404 and be mixed in output gas.In order to ensure that the catalyst solid particle separated in fast separation device 402 enters catalyst circulation standpipe 108 smoothly, avoid being formed above the first conical section 404 sidewall overstocking, the lower position being positioned at the second through hole 106 above the first conical section 404 sidewall is provided with loosening distribution device in gas-fluid 109 (prior art).
When the methanol to olefins reaction equipment 1000 of the present embodiment three works, methanol feedstock gas enters bottom dense-phase fluidized bed 20 from feed distributor 60, bubble upwards flows under the buoyancy of dense-phase fluidized bed 20 bed, and bubble is by flase floor 50 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 404 and carrier pipe 401.Due to 10 to 20 times that gas flow rate in carrier pipe 401 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 402 at its top through carrier pipe 401, gas-solid mixture does high speed rotary motion in fast separation device 402, carry out gas solid separation under the influence of centrifugal force, major part catalyst solid particle separation gets off to enter between outer cover 403 and carrier pipe 401, and catalyst solid particle returns dense-phase fluidized bed 20 by catalyst circulation standpipe 108 under gravity; The output gas separated from fast separation device 402 carries fraction catalyst solid particle and discharges from the first outlet 4031, 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 dense-phase fluidized bed 20 through particle efferent duct 302, and the output gas separated enters successive container through the self-produced exhaust outlets 101 of air chamber 102.
The beneficial effect of the present embodiment three is identical with embodiment one, does not repeat them here.
The foregoing is only the schematic detailed description of the invention of the utility model, and be not used to limit scope of the present utility model.Any those skilled in the art, equivalent variations done under the prerequisite not departing from design of the present utility model and principle and amendment, all should belong to the scope of the utility model protection.
Claims (10)
1. a methanol to olefins reaction equipment, comprise the lower little large housing of a sealing, 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 an air chamber, throughly below described air chamber be connected with one or more cyclone separator, tangentially throughly inside each described cyclone separator be connected with one first inlet tube, a conducting is vertically provided with in the particle efferent duct of described dense-phase fluidized bed bottom each described cyclone separator, it is characterized in that: described case inside top is provided with a gas-solid separating device, described gas-solid separating device and described first inlet tube conducting, described dense-phase fluidized bed inner transverse is installed with flase floor.
2. methanol to olefins reaction equipment as claimed in claim 1, it is characterized in that: described gas-solid separating device bottom opening, described gas-solid separating device bottom outside and described case inside wall are tightly connected, bottom described gas-solid separating device, described case inside space is divided into upper space and lower space, described gas-solid separating device comprises a up/down perforation, the carrier pipe of vertical setting, 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, the first outlet is provided with above described outer cover, described first outlet and described first inlet tube conducting, the first conical section top of a up/down perforation is connected to bottom described carrier pipe, described first conical section diametrically descends flaring, described first conical section lateral wall superjacent air space and described dense-phase fluidized bed from top to down one-way conduction are connected.
3. methanol to olefins reaction equipment as claimed in claim 2, it is characterized in that: described shield base is provided with the second conical section of up/down perforation, described second conical section diametrically goes up convergent, form bottom described second conical section bottom described gas-solid separating device, described second conical section bottom outside and described case inside wall are tightly connected, described first conical section is positioned at inside described second conical section, be connected with inside described second conical section by an annular slab bottom described first conical section, on described annular slab, circumference is evenly provided with multiple slotted eye; Described second conical section sidewall is provided with the first through hole, and described particle efferent duct sealing enters described dense-phase fluidized bed by described first through hole; 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: described outer cover comprises the first straight tube be positioned at above described second conical section, described fast separation device is arranged at described first straight tube inner upper, described first straight tube top is connected with the triconic section diametrically going up convergent, described triconic section top is connected with the first end socket, described first end socket sidewall is arranged described first outlet; Described slotted eye circumferential width is greater than the distance between every two slotted eyes, and described slotted eye is arranged with check valve sheet.
5. methanol to olefins reaction equipment as claimed in claim 3, it is characterized in that: described outer cover comprises the second straight tube be positioned at above described second conical section, described second straight tube internal diameter is less than described fast separation device contour dimension, the 4th conical section diametrically going up flaring is connected with above described second straight tube, the 3rd straight tube is connected with above described 4th conical section, described fast separation device is arranged at described 3rd straight tube inner upper, described 3rd straight tube top is connected with the 5th conical section diametrically going up convergent, described 5th conical section top is connected with the second end socket, described second end socket sidewall is arranged described first outlet, described slotted eye circumferential width is less than the distance between every two slotted eyes.
6. methanol to olefins reaction equipment as claimed in claim 2, it is characterized in that: form bottom described first conical section bottom described gas-solid separating device, described first conical section bottom outside and described case inside wall are tightly connected, described outer cover comprises the 4th straight tube arranged above described first conical section, described fast separation device is arranged at described 4th straight tube inner upper, described 4th straight tube top is connected with the 6th conical section diametrically going up flaring, described 6th conical section top is connected with the 5th straight tube, described 5th straight tube top is connected with the 3rd end socket, described 3rd end socket top arranges described first outlet, described particle efferent duct outlet is positioned at above described first conical section.
7. methanol to olefins reaction equipment as claimed in claim 6, it is characterized in that: described hull outside is positioned at described first conical section top position and is provided with 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 second through hole is outside through is connected with catalyst circulation standpipe, described catalyst circulation lower riser end opening is connected with described third through-hole is through obliquely, and described catalyst circulation standpipe is provided with guiding valve.
8. methanol to olefins reaction equipment as claimed in claim 7, is characterized in that: the lower position being positioned at described second through hole above described first conical section lateral wall is provided with loosening distribution device in gas-fluid.
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, and described hull outside is also provided with spent agent efferent duct, and described spent agent efferent duct is connected with described dense-phase fluidized bed bottom is through.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520285696.7U CN204685073U (en) | 2015-05-05 | 2015-05-05 | Methanol to olefins reaction equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520285696.7U CN204685073U (en) | 2015-05-05 | 2015-05-05 | Methanol to olefins reaction equipment |
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| Publication Number | Publication Date |
|---|---|
| CN204685073U true CN204685073U (en) | 2015-10-07 |
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| CN201520285696.7U Withdrawn - After Issue CN204685073U (en) | 2015-05-05 | 2015-05-05 | Methanol to olefins reaction equipment |
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| CN (1) | CN204685073U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104801243A (en) * | 2015-05-05 | 2015-07-29 | 中国石油大学(北京) | Methanol-to-olefin reaction device |
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2015
- 2015-05-05 CN CN201520285696.7U patent/CN204685073U/en not_active Withdrawn - After Issue
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104801243A (en) * | 2015-05-05 | 2015-07-29 | 中国石油大学(北京) | Methanol-to-olefin reaction device |
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| C14 | Grant of patent or utility model | ||
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| AV01 | Patent right actively abandoned |
Granted publication date: 20151007 Effective date of abandoning: 20170301 |
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| AV01 | Patent right actively abandoned |