CN104474978A - Device and method for preparing alkene from methanol and/or dimethyl ether - Google Patents
Device and method for preparing alkene from methanol and/or dimethyl ether Download PDFInfo
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- CN104474978A CN104474978A CN201410773621.3A CN201410773621A CN104474978A CN 104474978 A CN104474978 A CN 104474978A CN 201410773621 A CN201410773621 A CN 201410773621A CN 104474978 A CN104474978 A CN 104474978A
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- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/04—Ethylene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/06—Propene
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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- Y02P20/50—Improvements relating to the production of bulk chemicals
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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
- Y02P20/00—Technologies relating to chemical industry
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- Y02P20/584—Recycling of catalysts
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Abstract
The invention provides a device and method for preparing alkene from methanol and/or dimethyl ether. The device for preparing alkene from methanol and/or dimethyl ether comprises a reactor, a flow guiding hood, a regenerator, a reactor third-stage cyclone separator and a regenerator third-stage cyclone separator, wherein the reactor comprises a reaction area and an isolated area from bottom to top and further comprises a product gas outlet; the flow guiding hood is arranged in the isolated area; the regenerator comprises a regenerated flue gas outlet; the reactor third-stage cyclone separator comprises a product gas inlet and a catalyst-to-be-regenerated fine powder outlet; the regenerator third-stage cyclone separator comprises a regenerated flue gas inlet and a regenerated catalyst fine powder outlet, the regenerator further comprises a catalyst-to-be-regenerated fine powder inlet, and the catalyst-to-be-regenerated fine powder inlet is connected with the catalyst-to-be-regenerated fine powder outlet through a catalyst-to-be-regenerated fine powder conveying pipeline. The device for preparing alkene from methanol and/or dimethyl ether further comprises an air bubble breaking part, wherein the air bubble breaking part is arranged in the reaction area, and a plurality of breaking holes are formed in the air bubble breaking part. The device and the method have the advantage that the problems that the selectivity of low-carbon alkenes is low and a catalyst runs away and is high in consumption are solved.
Description
Technical field
The present invention relates to olefin producing technologies field, in particular to the device and method of a kind of methyl alcohol and/or dimethyl ether alkene.
Background technology
At present, the low-carbon alkene such as ethene, propylene is the most basic industrial chemicals, and especially the production capacity of ethene is one of mark of a measurement countries and regions chemical industry level.The main mode of production of ethene, propylene take oil as the cracking mode of raw material, and as naphtha steam cracking, heavy oil catalytic pyrolysis and ethane dehydrogenation etc., wherein, catalytic cracking unit is by-product propylene also.The ethene of China, the main source of propylene are by naphtha steam cracking, and the long-range actual production of market demand of the low-carbon alkenes such as the ethene of China, propylene, a large amount of import ethene of annual needs, acryloyl derivative make up market has openings.
China's oil resource critical shortage, within 2012, dependence on foreign countries for oil reaches more than 55%, has a strong impact on China's energy strategy safety.Be that ethene, the production of propylene route in source will consume valuable petroleum resources with petroleum base, due to rich coal resources in China, carry out coal-based alkene production line significant.Like this, can petroleum resource consumption be reduced on the one hand, improve coal utilization efficiency and economic worth on the other hand.The production line of coal-based alkene is: polyethylene and polypropylene are produced in coal gasification, purified synthesis gas, synthesising gas systeming carbinol, methanol-to-olefins, separation of olefins and olefinic polymerization.The output relative surplus of current China methyl alcohol, methanol market is low, utilizes producing low-carbon olefin through methanol transformation can not only alleviate the market shortage of ethene, propylene, also improves methanol production Business Economic Benefit simultaneously.
Preparing light olefins from methanol adopts silicoaluminophosphamolecular molecular sieves (being called for short SAPO-34 molecular sieve), higher carbon compounds can be produced in course of reaction, higher carbon compounds is not by the aperture of silicoaluminophosphamolecular molecular sieves, and higher carbon compounds remains in silicoaluminophosphamolecular molecular sieves.In silicoaluminophosphamolecular molecular sieves, form carbon distribution like this, easily blocking silicoaluminophosphamolecular molecular sieves duct, causes the catalytic activity of the catalyst of silicoaluminophosphamolecular molecular sieves to reduce.Because catalyst can periodically regenerate, the carbon deposit burning catalyst surface just can recover catalyst activity.
Patent reports the method and apparatus of multiple methanol-to-olefins both at home and abroad, usual methanol-to-olefins device comprises reactor and regenerator, and reactor and regenerator all adopt fluid bed.But also there is the not high problem of ethene, Propylene Selectivity and the large problem of catalyst consumption in methanol-to-olefins device of the prior art.Wherein, ethene, Propylene Selectivity are not high is mainly manifested in two aspects: on the one hand, be strong exothermal reaction because regenerator burns, regenerator arranges heat collector and takes superfluous heat away, maintains the temperature stabilization of regenerator.High-temperature regenerated catalyst enters reactor after stripper, and the temperature entering the regenerated catalyst in reactor can reach 600 DEG C ~ 630 DEG C, and the temperature of regenerated catalyst is far above the reaction temperature in reactor 400 DEG C ~ 500 DEG C.The regenerated catalyst of excessive temperature and gas-phase methanol haptoreaction, cause methyl alcohol that the low value products of side reaction generation CO and methane easily occurs, which decrease the yield of the high value products such as ethene, propylene; On the other hand, the top in the fluidized-bed reactor in methanol-to-olefins device is provided with dilute phase settling section, is conducive to reacting gas product and catalyst separation.But, the secondary response such as hydrogen migration, polymerization may be there is and generates the accessory substance such as ethane, propane, coke in the target product overstands in the reactor such as ethene, propylene, butylene, reduce ethene, propylene selective.
The patent of Sinopec Group " methyl alcohol or dimethyl ether produce the method for ethene, propylene " (application number 200610117351.6) discloses the structure of reactor of a kind of time of staying that shortens product in reaction compartment.Reactor comprises emulsion zone and dilute phase decanting zone, and emulsion zone and dilute phase decanting zone are all positioned in the reactor, arranges gas-solid quick separating district, outside reactor, arrange cyclone separator on the top of emulsion zone.Significantly can reduce the volume of dilute phase decanting zone like this, shorten the product time of staying in the reactor, inject terminator, cessation reaction in the bottom in gas-solid quick separating district simultaneously.But cyclone separator is arranged on the outside of reactor, and cyclone separator belongs to pressure vessel, like this can aggrandizement apparatus investment.And on engineering construction, how cyclone separator is fixed also is a difficult problem.In addition, although said apparatus reduces the volume of dilute phase decanting zone to a certain extent, still can there is alkene secondary conversion reaction to a certain degree in the bottom of dilute phase decanting zone, be unfavorable for the selective of raising ethene, propylene.
Patent " a kind of preparing low carbon olefinic hydrocarbon with methanol reactor " (application number 201220166104.6) discloses a kind of methanol to olefins reaction device.The product of this reactor, without the dilute phase decanting zone of reactor, directly enters the cyclone separator of reactor, has fully phased out dilute phase decanting zone through parallel works.This reactor eliminates dilute phase decanting zone, shortens the product time of staying in the reactor.But, cancel the catalyst granules amount that dilute phase decanting zone significantly increases the entrance of cyclone separator, affect the efficiency of cyclone separator, may catalyst also can be caused to discharge together with gas product, cause catalyst to run agent, significantly increase the consumption of catalyst.
Methanol-to-olefins device generally adopts SAPO-34 molecular sieve catalyst, and catalyst is expensive, and methanol-to-olefins device catalyst consumption causes greatly catalyst cost in methanol-to-olefins device operation process high, affects the economic benefit of methanol-to-olefins device.Catalyst consumption mainly circulates between reactor and regenerator due to catalyst, collide between catalyst granules, collide between catalyst granules and wall and catalyst carry between reactor and regenerator wearing and tearing etc. produce catalyst fines.Two stage cyclone separator separation and recovery catalyst fines is all provided with in reactor and regenerator, outside reactor and regenerator, the further recovery of catalyst fines of three-stage cyclone separator is set, the catalyst fines that reactor three-stage cyclone separator reclaims is too little due to particle diameter, is difficult to retrieval system and utilizes further.In addition, the catalyst fines that particle diameter is less enters chilling water wash system with gas product from reactor three-stage cyclone separator.Shenhua Group Co., Ltd applies for a patent " product of the method that molecular sieve catalyst micro mist recycles and acquisition thereof and application " (application number 201110253729), the catalyst fines reclaimed by reactor three-stage cyclone separator is after roasting, again be prepared into raw catelyst to re-use, reduce the cost of catalyst.But in the catalyst recovery tank of reactor three-stage cyclone separator, because gas product is with steam and C
5above hydro carbons, in the catalyst recovery tank of reactor three-stage cyclone separator, temperature is lower, steam and C
5above Hydrocarbon Organic generation condensation, oil, water and catalyst fines easily and mud, cause the catalyst recovery tank of reactor three-stage cyclone separator to unload agent difficulty like this, and, catalyst fines and water Long Term Contact also can reduce the activity of catalyst, thus cause catalyst to be difficult to recycle.
Summary of the invention
The present invention aims to provide the device and method of a kind of methyl alcohol and/or dimethyl ether alkene, the problem that selectivity of light olefin in prior art is low to solve, catalyst runs agent and catalyst consumption is high.
To achieve these goals, according to an aspect of the present invention, provide the device of a kind of methyl alcohol and/or dimethyl ether alkene, comprising: reactor, comprise by lower from upper reaction zone and isolated area, reactor also comprises product gas outlet; Kuppe, is arranged in isolated area, and reactor is separated into reaction zone and isolated area by kuppe; Regenerator, comprises regenerated flue gas outlet; Reactor three-stage cyclone separator, comprise gas product entrance and the outlet of reclaimable catalyst fine powder, gas product entrance is connected with product gas outlet; Regenerator three-stage cyclone separator, comprise regenerated flue gas entrance and regenerated catalyst fines outlet, regenerated flue gas entrance exports with regenerated flue gas and is connected, regenerator also comprises reclaimable catalyst fine powder entrance, reclaimable catalyst fine powder entrance and reclaimable catalyst fine powder are exported and are connected by reclaimable catalyst fine powder conveyance conduit, and reclaimable catalyst fine powder conveyance conduit is provided with the reclaimable catalyst fine powder conveying pot for carrying reclaimable catalyst fine powder; The device of methyl alcohol and/or dimethyl ether alkene also comprises bubble breaking portion, and bubble breaking portion is arranged in reaction zone, and the circumferential edge in bubble breaking portion is connected on the inwall of reactor, and bubble breaking portion is provided with multiple broken hole.
Further, reactor also comprises methanol feeding mouth, and the position in the vertical direction in bubble breaking portion is higher than the position of methanol feeding mouth.
Further, bubble breaking portion is grid.
Further, grid comprises one or more layers.
Further, reactor also comprises cyclone separator, cyclone separator is arranged in isolated area, kuppe comprises taper section and dilute phase pipe, the opening at the top of the aperture efficiency taper section of the bottom of taper section is large, and the bottom of taper section is connected on the inwall of reactor, and the top of taper section is connected to the bottom of dilute phase pipe, the top of dilute phase pipe is connected with the entrance of cyclone separator, and taper section is provided with the through hole of the dipleg for dodging cyclone separator.
Further, reactor also comprises regenerated catalyst inlet and reclaimable catalyst outlet; Regenerator comprises reclaimable catalyst entrance and regenerated catalyst outlet, and reclaimable catalyst outlet is connected by reclaimable catalyst conveyance conduit with reclaimable catalyst entrance, and regenerated catalyst outlet is connected by regenerated catalyst road with regenerated catalyst inlet; The device of methyl alcohol and/or dimethyl ether alkene also comprises cooler and first stripper of separate setting, cooler is arranged on regenerated catalyst road, and the first stripper is arranged on regenerated catalyst road or the first stripper is arranged on the inwall of regenerator.
Further, the first stripper is arranged between cooler and regenerated catalyst outlet.
Further, the first stripper is arranged between cooler and regenerated catalyst inlet.
Further, the position in the vertical direction of regenerator is higher than the position of reactor.
Further, reactor and regenerator are coaxially arranged.
According to a further aspect in the invention, provide a kind of method of methyl alcohol and/or dimethyl ether alkene, comprise the following steps: make the methyl alcohol in reactor and/or dimethyl ether and regenerated catalyst produce gas product in reaction zone haptoreaction, the method of methyl alcohol and/or dimethyl ether alkene is further comprising the steps of: pass through bubble breaking portion bubble crushing in the reaction region to strengthen gas-solid contact, and gas product enters cyclone separator by kuppe and generates accessory substance with ethene suppressing, propylene generation secondary response; The gas product separated in the reactor enters in reactor three-stage cyclone separator and proceeds to be separated, the reclaimable catalyst fine powder separated in reactor three-stage cyclone separator enters in regenerator and regenerates, and the reclaimable catalyst fine powder after regeneration reclaims from regeneration three-stage cyclone separator.
Further, gas product is further comprising the steps of after cyclone separator is separated: the reclaimable catalyst separated in the reactor enters in regenerator and regenerates, and enters in reactor after the regenerated catalyst cooling after regeneration.
Apply technical scheme of the present invention, reactor comprises by lower from upper reaction zone and isolated area, and kuppe is arranged in isolated area, and reactor is separated into reaction zone and isolated area by kuppe.Said structure eliminates the dilute phase decanting zone in reactor, shortens the gas product time of staying in the reactor, efficiently avoid the situation that ethene, converting propylene are the accessory substance such as ethane, propane, coke of low value by gas product generation secondary response.Owing to eliminating dilute phase decanting zone, the catalyst entrainment amount being entered the entrance of cyclone separator by kuppe can obviously increase.In reaction zone, arrange bubble breaking portion, the circumferential edge in bubble breaking portion is connected on the inwall of reactor, and bubble breaking portion is provided with multiple broken hole.Bubble breaking portion can broken air pocket, improves gas-solid contact effect, gives full play to the catalytic activity of catalyst, make reaction area liquefaction bed more stable.Such bubble breaking portion can reduce the catalyst that the interface between emulsion zone in reaction zone and dilute-phase zone causes due to air pocket fragmentation and splash, considerably reduce the concentration of the catalyst granules entering cyclone separator, reduce the load of cyclone separator, efficiently avoid the problem that cyclone separator runs agent, improve the efficiency of cyclone separator, thus effectively improve the selective of the low-carbon alkene such as ethene, propylene of the device of methyl alcohol and/or dimethyl ether alkene, improve economic benefit.The gas product that reactor produces enters into reactor three-stage cyclone separator by product gas outlet and gas product entrance, and the reclaimable catalyst fine powder that reactor three-stage cyclone separator is separated is entered into regenerator regenerated by the outlet of reclaimable catalyst fine powder, reclaimable catalyst fine powder conveying pot, reclaimable catalyst fine powder conveyance conduit and reclaimable catalyst fine powder entrance.The regenerated catalyst fines of the drying after regeneration enters into regenerator three-stage cyclone separator by regenerated flue gas outlet, and the regenerated catalyst fines of the isolated drying of regenerator three-stage cyclone separator reclaims from regenerated catalyst fines outlet.Dry regenerated catalyst fines is convenient to handling and conveying, thus recycles catalyst fines, effectively reduces the catalyst operating cost of the device of methyl alcohol and/or dimethyl ether alkene.Said structure efficiently solves the problem that low carbon selectivity is low, catalyst runs agent and catalyst consumption is high.
Accompanying drawing explanation
The Figure of description forming a application's part is used to provide a further understanding of the present invention, and schematic description and description of the present invention, for explaining the present invention, does not form inappropriate limitation of the present invention.In the accompanying drawings:
Fig. 1 shows the structural representation of the embodiment one according to the device of methanol-to-olefins of the present invention;
Fig. 2 shows the structural representation of the embodiment two according to the device of methanol-to-olefins of the present invention; And
Fig. 3 shows the structural representation of the embodiment three according to the device of methanol-to-olefins of the present invention.
Above-mentioned accompanying drawing comprises the following drawings mark:
10, reactor; 11a, reaction zone; 11b, isolated area; 12, kuppe; 121, taper section; 122, dilute phase pipe; 13, bubble breaking portion; 14, cyclone separator; 15, methanol feeding mouth; 16, regenerated catalyst inlet; 17, reclaimable catalyst outlet; 18, product gas outlet; 19, the first heat collector; 20, regenerator; 21, reclaimable catalyst entrance; 22, regenerated catalyst outlet; 23, regenerated flue gas outlet; 24, the second heat collector; 25, reclaimable catalyst fine powder entrance; 30, reclaimable catalyst conveyance conduit; 31, the second stripper; 32, the first guiding valve; 40, regenerated catalyst road; 41, the second guiding valve; 50, cooler; 51, fluidized gas entrance; 52, heat-obtaining outlet; 53, water inlet; 54, first gas outlet is returned; 55, entrance is cooled; 56, coolant outlet; 60, the first stripper; 61, stripping gas entrance; 62, second gas outlet is returned; 63, stripping inlet; 64, stripping outlet; 71a, methyl alcohol supply department; 71b, gas supply department; 71c, fluidized gas supply department; 71d, the second stripping gas supply department; 71e, air supply portion; 81, first letter shoot road is returned; 82, second letter shoot road is returned; 83, reclaimable catalyst fine powder conveyance conduit; 91, reactor three-stage cyclone separator; 911, gas product entrance; 912, reclaimable catalyst fine powder outlet; 92, regenerator three-stage cyclone separator; 921, regenerated flue gas entrance; 922, regenerated catalyst fines outlet; 93, reclaimable catalyst fine powder conveying pot; 94, chilling water wash system; 95, residual neat recovering system.
Detailed description of the invention
It should be noted that, when not conflicting, the embodiment in the application and the feature in embodiment can combine mutually.Below with reference to the accompanying drawings and describe the present invention in detail in conjunction with the embodiments.
Embodiment one to the embodiment three of the application describes the device (i.e. the device of methanol-to-olefins) adopting material benzenemethanol producing olefinic hydrocarbons, will introduce the device of methyl alcohol producing olefinic hydrocarbons in detail below.Certainly, the raw material of producing olefinic hydrocarbons also can adopt the mixture of dimethyl ether or methyl alcohol and dimethyl ether, the device of the device of dimethyl ether alkene and methyl alcohol and dimethyl ether alkene and the device of methanol-to-olefins similar, in this not go into detail.
As shown in Figure 1, the device of the methanol-to-olefins of embodiment one comprises reactor 10, kuppe 12, regenerator 20, reactor three-stage cyclone separator 91 and regenerator three-stage cyclone separator 92, reactor 10 comprises by lower from upper reaction zone 11a and isolated area 11b, reactor 10 also comprises product gas outlet 18, kuppe 12 is arranged in isolated area 11b, reactor 10 is separated into reaction zone 11a and isolated area 11b by kuppe 12, regenerator 20 comprises regenerated flue gas outlet 23, reactor three-stage cyclone separator 91 comprises gas product entrance 911 and reclaimable catalyst fine powder outlet 912, gas product entrance 911 is connected with product gas outlet 18, regenerator three-stage cyclone separator 92 comprises regenerated flue gas entrance 921 and regenerated catalyst fines outlet 922, regenerated flue gas entrance 921 and regenerated flue gas export 23 and are connected, regenerator 20 also comprises reclaimable catalyst fine powder entrance 25, reclaimable catalyst fine powder entrance 25 and reclaimable catalyst fine powder are exported 912 and are connected by reclaimable catalyst fine powder conveyance conduit 83, reclaimable catalyst fine powder conveyance conduit 83 is provided with the reclaimable catalyst fine powder conveying pot 93 for carrying reclaimable catalyst fine powder, the device of methanol-to-olefins also comprises bubble breaking portion 13, bubble breaking portion 13 is arranged in reaction zone 11a, the circumferential edge in bubble breaking portion 13 is connected on the inwall of reactor 10, bubble breaking portion 13 is provided with multiple broken hole.
The device of the methanol-to-olefins of Application Example one, reactor 10 comprises by lower that kuppe 12 is arranged in isolated area 11b from upper reaction zone 11a and isolated area 11b, and reactor 10 is separated into reaction zone 11a and isolated area 11b by kuppe 12.Said structure eliminates the dilute phase decanting zone in reactor 10, shorten the gas product time of staying in reactor 10, efficiently avoid the situation that ethene, converting propylene are the accessory substance such as ethane, propane, coke of low value by gas product generation secondary response.Owing to eliminating dilute phase decanting zone, the catalyst entrainment amount being entered the entrance of cyclone separator by kuppe 12 can obviously increase.In reaction zone 11a, arrange bubble breaking portion 13, the circumferential edge in bubble breaking portion 13 is connected on the inwall of reactor 10, and bubble breaking portion 13 is provided with multiple broken hole.Bubble breaking portion 13 can broken air pocket, improves gas-solid contact effect, gives full play to the catalytic activity of catalyst, make reaction zone 11a fluidized-bed layer more stable.Such bubble breaking portion 13 can reduce the catalyst that the interface between emulsion zone in reaction zone 11a and dilute-phase zone causes due to air pocket fragmentation and splash, significantly reduce the concentration of the catalyst granules entering cyclone separator, reduce the load of cyclone separator, efficiently avoid the problem that cyclone separator runs agent, improve the efficiency of cyclone separator, thus effectively improve the selective of the low-carbon alkene such as ethene, propylene of the device of methanol-to-olefins, improve economic benefit.The gas product that reactor 10 produces enters into reactor three-stage cyclone separator 91 by product gas outlet 18 and gas product entrance 911, and the reclaimable catalyst fine powder that reactor three-stage cyclone separator 91 is separated enters into regenerator 20 by reclaimable catalyst fine powder outlet 912, reclaimable catalyst fine powder conveying pot 93, reclaimable catalyst fine powder conveyance conduit 83 and reclaimable catalyst fine powder entrance 25 and regenerates.The regenerated catalyst fines of the drying after regeneration enters into regenerator three-stage cyclone separator 92 by regenerated flue gas outlet 23, and the regenerated catalyst fines of the isolated drying of regenerator three-stage cyclone separator 92 reclaims from regenerated catalyst fines outlet 922.Dry regenerated catalyst fines is convenient to handling and conveying, thus recycles catalyst fines, effectively reduces the catalyst operating cost of the device of methanol-to-olefins.Said structure efficiently solves the problem that low carbon selectivity is low, catalyst runs agent and catalyst consumption is high.
In order to make bubble breaking portion 13 broken air pocket effectively, in embodiment one, reactor 10 also comprises methanol feeding mouth 15, and the position in the vertical direction in bubble breaking portion 13 is higher than the position of methanol feeding mouth 15.Methanol feeding mouth 15 place of reactor 10 is provided with gas distribution grid, and gas distribution grid has carried out distributing and fragmentation to charging methyl alcohol, does not need to arrange bubble breaking portion 13 at methanol feeding reaction zone.Bubble is when emulsion zone moves from bottom to top, and bubble can be grown up rapidly, needs the bubble in broken emulsion zone.
In order to make bubble breaking portion 13 more effectively broken air pocket, in embodiment one, reaction zone comprises methanol feeding reaction zone, emulsion zone, regenerated catalyst inlet reaction zone and dilute phase reaction zone from bottom to top, and bubble breaking portion 13 is arranged in regenerated catalyst inlet reaction zone.Bubble breaking portion 13 is arranged in the emulsion zone of reactor 10, prevents bubble from the motion process that dense-phase bed is bottom-up, growing up to air pocket.Can carry and splash a large amount of catalyst secretly due to bubble fragmentation on emulsion zone and dilute-phase zone interface and enter dilute phase, thus bubble breaking portion 13 is arranged on the effect that dilute phase does not have bubble crushing and prevents catalyst from splashing.Therefore, bubble breaking portion 13 is preferably disposed on emulsion zone or emulsion zone near the position at dilute-phase zone interface, prevents broken bubble from emulsion zone, continuing rising or again grow up.Thus can consider to arrange one or more layers.After arranging bubble breaking portion 13, the particle entrainment amount entering dilute phase in cold model experiment device decreases 20 ~ 40%.
In order to maintain the concentration of the solid-phase catalyst particle of the entrance of cyclone separator 14 and ensure the separating effect of cyclone separator 14, in embodiment one, bubble breaking portion 13 is grid.Preferably, grid comprises one or more layers.The concentration that one or more layers grid significantly reduces the solid-phase catalyst particle entering dilute phase pipe 122 is set.More preferably, two-layer or three layers of grid are adopted.On the one hand, grid can bubble crushing, strengthening gas-solid contact and mass transfer, keeps the stable of fluidized-bed layer and uniformity; On the other hand, grid can prevent the interface of bubble between emulsion zone and the dilute-phase zone situation that a large amount of catalyst splashes because bubble crushing causes, and greatly reduces the catalyst granules concentration of the entrance of cyclone separator.
In embodiment one, the distance between adjacent two grids is equal.Multilayer grid is disposed at equal distance in emulsion zone, and the aperture in the broken hole of every layer of grid is identical.Preferably, the percent opening of grid is in the scope of 0.5 ~ 0.9, and wherein, the percent opening of grid is the area in broken hole on grid and the area ratio of grid.
In embodiment one, reactor 10 also comprises cyclone separator 14, cyclone separator 14 is arranged in isolated area 11b, kuppe 12 comprises taper section 121 and dilute phase pipe 122, the opening at the top of the aperture efficiency taper section 121 of the bottom of taper section 121 is large, the bottom of taper section 121 is connected on the inwall of reactor 10, the top of taper section 121 is connected to the bottom of dilute phase pipe 122, the top of dilute phase pipe 122 is connected with the entrance of cyclone separator 14, and taper section 121 is provided with the through hole of the dipleg for dodging cyclone separator 14.Gas product and dilute phase decanting zone of the prior art are kept apart by kuppe 12, and isolated area 11b is for placing the components such as cyclone separator.Space insufflation gas between reactor 10 and kuppe 12, ensures the pressure balance between reaction zone 11a and isolated area 11b.Gas product enters rapidly the cyclone separator 14 be connected with dilute phase pipe 122 by dilute phase pipe 122, reduce the gas product time of staying in reactor 10.In embodiment one, the flow velocity of the gas product in dilute phase pipe 122 is in the scope of 2m/s ~ 15m/s.Preferably, the flow velocity of the gas product in dilute phase pipe 122 is in the scope of 4m/s ~ 12m/s.Preferably, the flow velocity of the gas product in dilute phase pipe 122 is in the scope of 6m/s ~ 10m/s.
In embodiment one, cyclone separator 14 is two stage cyclone separator.The dipleg of cyclone separator 14 gos deep into the reaction zone in reactor 10 by through hole, cyclone separator 14 arranges fell cone or flutter valve.After catalyst fines is separated with gas product by cyclone separator 14, catalyst fines turns back in reaction zone by dipleg, and gas product enters into reactor three-stage cyclone separator 91 by product gas outlet 18 and carries out separation reclaimable catalyst fine powder.
In embodiment one, the isolated thinner reclaimable catalyst fine powder of reactor three-stage cyclone separator 91 enters in reclaimable catalyst fine powder conveying pot 93, is then transported in regenerator 20 by reclaimable catalyst fine powder conveyance conduit 83.Insulation is set in reclaimable catalyst fine powder conveying pot 93 and reclaimable catalyst fine powder conveyance conduit 83, after effectively preventing the temperature of the materials such as steam from reducing generation condensation, causes reclaimable catalyst fine powder and mud to be difficult to conveying.
In embodiment one, the device of methanol-to-olefins also comprises chilling water wash system 94, and chilling water wash system 94 is connected with reactor three-stage cyclone separator 91.Gas product enters separation of olefins flow process through chilling water wash system 94.
In embodiment one, the device of methanol-to-olefins also comprises residual neat recovering system 95, and residual neat recovering system 95 is connected with regenerator three-stage cyclone separator 92.Regenerated flue gas is entrained with regenerated catalyst fines and enters regenerator three-stage cyclone separator 92 from regenerated flue gas outlet 23, the regenerated catalyst fines of the isolated drying of regenerator three-stage cyclone separator 92 is carried out recovery and is re-used from regenerated catalyst fines exit, regenerated flue gas enters residual neat recovering system 95.
In embodiment one, the distance between kuppe 12 and emulsion zone is in the scope of 1m ~ 8m.Particularly, the distance between kuppe 12 and emulsion zone refers to the position of beginning undergauge and the distance between emulsion zone and the interface of dilute-phase zone of kuppe 12.Preferably, the distance between kuppe 12 and emulsion zone is in the scope of 2m ~ 6m.More preferably, the distance between kuppe 12 and emulsion zone is in the scope of 3m ~ 5m.
In embodiment one, the position in the vertical direction of regenerator 20 is higher than the position of reactor 10.Regenerated catalyst utilizes gravity from regenerated catalyst outlet 22 by regenerated catalyst road 40 inflow reactor 10.Effectively reduce regenerated catalyst of the prior art like this because of the fine powder amount that wearing and tearing produce in lifting process, thus decrease the consumption of catalyst.Preferably, reactor 10 and regenerator 20 are coaxially arranged.
In prior art, patent " methanol conversion is the device and method of low-carbon alkene " (application number 201210149480.9) proposes and be provided with cooling-stripper between regenerated catalyst outlet and regenerated catalyst inlet, in cooling-stripper, on the one hand, CO, CO of will carrying secretly in regenerated catalyst of cooling-stripper
2, N
2, O
2deng gas stripping out; On the other hand, achieve the cooling of regenerated catalyst, reduce the temperature of the regenerated catalyst entered in reactor, thus decrease the side reactions such as methanol decomposition, reduce CO, CH in gas product
4selective, improve initial reaction phase product distribution.But cooling and stripping are closed in one by cooling-stripper, the adjustment of the chilling temperature of regenerated catalyst is limited to the stripping conditions restriction of regenerated catalyst, is difficult to flexible modulation in a big way.Make the temperature of the regenerated catalyst entered in reactor too high like this, cause initial reaction phase product to distribute and be deteriorated.
In embodiment one, reactor 10 also comprises regenerated catalyst inlet 16 and reclaimable catalyst outlet 17, regenerator 20 comprises reclaimable catalyst entrance 21 and regenerated catalyst outlet 22, reclaimable catalyst outlet 17 is connected by reclaimable catalyst conveyance conduit 30 with reclaimable catalyst entrance 21, regenerated catalyst outlet 22 is connected by regenerated catalyst road 40 with regenerated catalyst inlet 16, the device of methanol-to-olefins also comprises cooler 50 and first stripper 60 of separate setting, cooler 50 is arranged on regenerated catalyst road 40, first stripper 60 is arranged on regenerated catalyst road 40, first stripper 60 is arranged between cooler 50 and regenerated catalyst outlet 22.Cooler 50 and the separate setting of the first stripper 60, ensure that the Srteam Stripping effect of regenerated catalyst, effectively prevent CO, N
2not exclusively enter the situation in reactor 10 Deng gas stripping, effectively prevent and the follow-up olefin separation system of gas product is had an impact.Simultaneously, the temperature of the regenerated catalyst in reactor 10 can be entered according to process conditions flexible modulation in a big way, reduce the temperature of the regenerated catalyst entered in reactor 10, react in the Reaction conditions range optimized, improve the distribution of product.
Preferably, methanol feeding mouth 15 is arranged on the bottom of reactor 10, regenerated catalyst inlet 16 and reclaimable catalyst outlet 17 are all arranged on the sidewall of reactor 10, product gas outlet 18 is arranged on the top of reactor 10, reclaimable catalyst entrance 21, regenerated catalyst outlet 22 and reclaimable catalyst fine powder entrance 25 are arranged on the sidewall of regenerator 20, and regenerated flue gas outlet 23 is at the top of regenerator 20.
In embodiment one, the device of methanol-to-olefins also comprises air supply portion 71e, and regenerator 20 also comprises air intake, and air supply portion 71e is connected with air intake.Air supply portion 71e is for providing compressed air or oxygen-enriched air in regenerator 20.
In embodiment one, the device of methanol-to-olefins also comprises methyl alcohol supply department 71a and setting methanol feeding distributor in reactor 10, and methanol feeding distributor arranges the bottom of reactor 10, and methyl alcohol supply department 71a is connected with methanol feeding mouth 15.Preferably, methanol feeding distributor is board-like distributor or pipe distributor.Methyl alcohol supply department 71a by methyl alcohol through preheating, gasification and overheated after enter reactor 10 from methanol feeding mouth 15 by methanol feeding distributor, react at reaction zone 11a and catalyst exposure.
In embodiment one, the device of methanol-to-olefins also comprises setting the first heat collector 19, first heat collector 19 in reactor 10 and takes superfluous heat away, and the first heat collector 19 can be one or more groups.In unshowned in the drawings embodiment, the first heat collector can be arranged on outside reactor.Certainly, the mode that the heat collector be arranged on outside reactor can be adopted combined with the heat collector arranged in the reactor.
In embodiment one, the device of methanol-to-olefins also comprises the second heat collector 24, second heat collector 24 be connected with regenerator 20 and takes in catalyst regeneration process the heat of releasing surplus away, remains on the temperature stabilization in regenerative process.In embodiment one, the reaction temperature in regenerator 20 is in the scope of 580 DEG C ~ 720 DEG C.Preferably, the reaction temperature in regenerator 20 is in the scope of 620 DEG C ~ 700 DEG C.More preferably, the reaction temperature in regenerator 20 is in the scope of 660 DEG C ~ 680 DEG C.In embodiment one, the second heat collector 24 is arranged on outside regenerator 20.Preferably, the second heat collector 24 is one or more groups.In unshowned in the drawings embodiment, the second heat collector can be arranged on the inside of regenerator, and the second heat collector also can be one or more groups.Certainly, the heat collector be arranged on outside regenerator 20 can be adopted and be arranged on the combined mode of regenerator 20 interior heat collector.
In embodiment one, reactor 10 can be bubbling bed reactor, turbulent fluid bed reactor or fast fluidized bed reactor.Preferably, reactor 10 adopts turbulent fluid bed reactor.
In embodiment one, the device of methanol-to-olefins also comprises the second stripper 31, first guiding valve 32, second stripping gas supply department 71d and gas supply department 71b, second stripper 31 and the first guiding valve 32 are all arranged on reclaimable catalyst conveyance conduit 30, stripping inlet and the reclaimable catalyst of the second stripper 31 export 17 and are connected, the stripping gas entrance of the second stripper 31 is connected with the second stripping gas supply department 71d, the gas outlet of returning of the second stripper 31 is connected on the sidewall of reactor 10, reclaimable catalyst conveyance conduit 30 is provided with gas access, gas supply department 71b is connected with gas access, first guiding valve 32 is between the second stripper 31 and gas access.Reclaimable catalyst, after the second stripper 31 stripping, through the first guiding valve 32, then utilizes the gas of gas supply department 71b to be risen in regenerator 20 by reclaimable catalyst and regenerates.Wherein, the gas that returns of the second stripper 31 directly turns back in reaction zone 11a.In embodiment one, the gas in gas supply department 71b can be compressed air, nitrogen or steam.Preferably, the gas in gas supply department 71b is steam.First guiding valve 32 can control the amount of the reclaimable catalyst entered in regenerator 20.
In embodiment one, the device of methanol-to-olefins also comprises the second guiding valve 41, second guiding valve 41 and is arranged on regenerated catalyst road 40, and the second guiding valve 41 is between cooler 50 and regenerated catalyst inlet 16.Second guiding valve 41 can control the amount of the regenerated catalyst entered in reactor 10.The device of methanol-to-olefins also comprises setting regenerated catalyst distributor in reactor 10, and regenerated catalyst distributor is arranged on regenerated catalyst inlet 16 place.
The course of work of the device of methanol-to-olefins is as follows:
Methyl alcohol and catalyst react in reactor 10, gas product and reclaimable catalyst is obtained after reaction, gas product enters cyclone separator 14 products of separated gas and catalyst fines by kuppe 12, gas product after separation enters reactor three-stage cyclone separator 91 from product gas outlet 18 and is separated reclaimable catalyst fine powder further, then gas product enters chilling water wash system, and reclaimable catalyst enters the second stripper 31 from reclaimable catalyst outlet 17.Reclaimable catalyst enters regenerator 20 by reclaimable catalyst conveyance conduit 30 from reclaimable catalyst entrance 21 after stripping, after regenerator 20 regenerates, obtain regenerated catalyst.Regenerated catalyst enters the first stripper 60 from regenerated catalyst outlet 22, then after stripping, enter cooler 50, then enters reactor 10 from regenerated catalyst inlet after supercooling.At this moment, methyl alcohol reacts with regenerated catalyst again.Continue to repeat above-mentioned cyclic process.The reclaimable catalyst fine powder that reactor three-stage cyclone separator 91 is separated is transported in regenerator 20 by reclaimable catalyst fine powder conveyance conduit 83 and regenerates, regenerated catalyst fines after regeneration is separation and recovery in regenerator three-stage cyclone separator 92, and the regenerated catalyst fines after recovery is delivered to catalyst plant and again recycled.
In embodiment one, the device of methanol-to-olefins also comprises the first stripping gas supply department, first stripper 60 comprises stripping gas entrance 61, second returns gas outlet 62, stripping inlet 63 and stripping outlet 64, cooler 50 comprises fluidized gas entrance 51, heat-obtaining outlet 52, water inlet 53, first returns gas outlet 54, cooling entrance 55 and coolant outlet 56, stripping gas entrance 61 is connected with the first stripping gas supply department, stripping inlet 63 is connected with regenerated catalyst outlet 22, stripping outlet 64 is connected with cooling entrance 55, second returns gas outlet 62 returns letter shoot road 81 by first and is connected on the sidewall of regenerator 20, the gas that returns in first stripper 60 turns back to top in regenerator 20.In the first stripper 60, one or more layers grid is set.In embodiment one, the stripping gas in the first stripping gas supply department is fluidisation nitrogen or steam.Preferably, the stripping gas in the first stripping gas supply department is steam.More preferably, the stripping gas in the first stripping gas supply department is superheated steam.Stripping gas in first stripping gas supply department enters in the first stripper 60 by distribution rings, is entered cooler 50 from stripping outlet 64 through steam stripped regenerated catalyst by regenerated catalyst road 40 from cooling entrance 55.Be provided with heat production coil pipe in cooler 50, heat production coil pipe takes heat away, reduces the temperature of regenerated catalyst.
In embodiment one, the device of methanol-to-olefins also comprises fluidized gas supply department 71c, fluidized gas supply department 71c is connected with fluidized gas entrance 51, first returns gas outlet 54 returns letter shoot road 82 by second and is connected to first and returns on letter shoot road 81, and the gas that returns namely in cooler 50 to turn back to top in regenerator 20 again after gas mixes with returning in the first stripper 60.In embodiment one, the fluidized gas in fluidized gas supply department 71c is nitrogen or steam.Preferably, the fluidized gas in fluidized gas supply department 71c is steam.Fluidized gas in fluidized gas supply department 71c enters in cooler 50 by one or more groups distribution rings, liquid heat-obtaining medium enters cooler 50 from water inlet 53, after liquid heat-obtaining medium takes the heat in cooler 50 away, liquid heat-obtaining medium reverts becomes the heat-obtaining medium of gaseous state, and the heat-obtaining medium of gaseous state turns back to drum from heat-obtaining outlet 52.Preferably, heat-obtaining medium is water.The temperature of regenerated catalyst is by regulating the inlet of fluidized gas, and the inlet of fluidized gas is comparatively large, and the fluidizing performance of cooler 50 is good, and heat-obtaining amount is just comparatively large, and the temperature of regenerated catalyst is just lower.Otherwise the temperature of regenerated catalyst is just higher.In unshowned in the drawings embodiment, first returns gas outlet returns letter shoot road by second and is connected on the sidewall of regenerator, and the gas that returns in cooler turns back to top in regenerator.
Because cooler 50 is different with the type of the fluid bed in the first stripper 60, cooler 50 adopts turbulent fluidized bed, and turbulent fluidized bed is convenient to heat transfer and heat-obtaining, and the first stripper 60 adopts bubbling fluidized bed, and bubbling fluidized bed is conducive to stripping.Cooler 50 and the first stripper 60 operate under being provided separately and being conducive to respective condition.
Fig. 2 shows the structure of the embodiment two of the device of the methanol-to-olefins of the application, and device and the difference of embodiment one of the methanol-to-olefins of embodiment two are that the first stripper 60 is arranged on different positions.In embodiment one, the first stripper 60 is arranged between cooler 50 and regenerated catalyst outlet 22.And in embodiment two, the first stripper 60 is arranged on the inwall of regenerator 20.The total height of regenerator 20 and reactor 10 can be reduced like this, reduce device gross investment.
In embodiment two, because the first stripper 60 is arranged on the inside of regenerator 20 near inwall place, stripping outlet 64 overlaps with regenerated catalyst outlet 22, first returns gas outlet 54 returns letter shoot road 82 by second and is connected on the sidewall of regenerator 20, and the gas that returns in cooler 50 turns back to top in regenerator 20.
Fig. 3 shows the structure of the embodiment three of the device of the methanol-to-olefins of the application, and device and the difference of embodiment one of the methanol-to-olefins of embodiment three are that the first stripper 60 is arranged on different positions.In embodiment one, the first stripper 60 is arranged between cooler 50 and regenerated catalyst outlet 22.And in embodiment three, the first stripper 60 is arranged between cooler 50 and regenerated catalyst inlet 16.
In embodiment three, second returns gas outlet 62 returns letter shoot road 81 by first and is connected on the sidewall of regenerator 20.Certainly, second return gas outlet 62 and also can return letter shoot road 81 by first and be connected to fluidized gas entrance 51 place.Such regenerated catalyst first cools stripping again, the first stripper 60 stripping gas out can be utilized as the fluidizing agent of part, reduce the consumption of the fluidizing agent of cooler 50, thus the energy consumption of saveall.
In embodiment three, because the first stripper 60 is arranged between cooler 50 and regenerated catalyst inlet 16, regenerated catalyst outlet 22 is connected with cooling entrance 55, coolant outlet 56 is connected with stripping inlet 63, stripping outlet 64 is connected with regenerated catalyst inlet 16, first returns gas outlet 54 returns letter shoot road 82 by second and is connected on the sidewall of regenerator 20, and the gas that returns in cooler 50 turns back to top in regenerator 20.
Present invention also provides a kind of method of methanol-to-olefins, embodiment according to the method for the methanol-to-olefins of the application comprises the following steps: make the methyl alcohol in reactor 10 and/or dimethyl ether and regenerated catalyst produce gas product in reaction zone 11a haptoreaction, the method of methyl alcohol and/or dimethyl ether alkene is further comprising the steps of: in reaction zone 11a, pass through bubble breaking portion 13 bubble crushing to strengthen gas-solid contact, and gas product enters cyclone separator 14 by kuppe 12 and generates accessory substance with ethene suppressing, propylene generation secondary response; The gas product separated in reactor 10 enters in reactor three-stage cyclone separator 91 and proceeds to be separated, the reclaimable catalyst fine powder separated in reactor three-stage cyclone separator 91 enters in regenerator 20 and regenerates, and the reclaimable catalyst fine powder after regeneration reclaims from regenerator three-stage cyclone separator 92.Bubble breaking portion 13 can broken air pocket, improves gas-solid contact effect, gives full play to the catalytic activity of catalyst, make reaction zone 11a fluidized-bed layer more stable.Such bubble breaking portion 13 can reduce the catalyst that the interface between emulsion zone in reaction zone 11a and dilute-phase zone causes due to air pocket fragmentation and splash, significantly reduce the concentration of the catalyst granules entering cyclone separator, reduce the load of cyclone separator, efficiently avoid the problem that cyclone separator runs agent, improve the efficiency of cyclone separator, thus effectively improve the selective of the low-carbon alkene such as ethene, propylene of the device of methanol-to-olefins, improve economic benefit.The gas product that reactor 10 is separated enters into reactor three-stage cyclone separator 91 and proceeds to be separated, and the reclaimable catalyst fine powder that reactor three-stage cyclone separator 91 is separated enters into regenerator 20 and regenerates.The regenerated catalyst fines of the drying after regeneration enters into regenerator three-stage cyclone separator 92, reclaims the regenerated catalyst fines of the isolated drying of regenerator three-stage cyclone separator 92.Dry regenerated catalyst fines is convenient to handling and conveying, thus recycles catalyst fines, effectively reduces the catalyst operating cost of the device of methanol-to-olefins.Said structure efficiently solves the problem that low carbon selectivity is low, catalyst runs agent and catalyst consumption is high.
In the present embodiment, gas product is further comprising the steps of after cyclone separator is separated: the reclaimable catalyst separated in reactor 10 enters in regenerator 20 and regenerates, and enters in reactor 10 after the regenerated catalyst cooling after regeneration.The temperature of the regenerated catalyst entered in reactor 10 can be reduced like this, react in the Reaction conditions range optimized, improve the distribution of product.
Tested under identical regeneration temperature, identical reaction temperature and identical reaction pressure with the device of the methanol-to-olefins of embodiment three with embodiment one, embodiment two by the device of methanol-to-olefins of the prior art, experimental condition and result of the test are as table 1.
The test data of the device of the methanol-to-olefins of the device of table 1 methanol-to-olefins of the prior art and embodiment one, embodiment two and embodiment three contrasts
As can be drawn from Table 1, the device of the methanol-to-olefins of embodiment one, embodiment two and embodiment three is compared with prior art, the gas product of the device of the methanol-to-olefins of embodiment one, embodiment two and embodiment three all shortened in the time of staying of dilute phase reaction zone, the temperature of the regenerated catalyst in the device of methanol-to-olefins reduces, flexible modulation can also be carried out, and ethene+Propylene Selectivity obviously increases, the selective obvious reductions of accessory substance such as ethane, propane and methane.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, for a person skilled in the art, the present invention can have various modifications and variations.Within the spirit and principles in the present invention all, any amendment done, equivalent replacement, improvement etc., all should be included within protection scope of the present invention.
Claims (12)
1. a device for methyl alcohol and/or dimethyl ether alkene, comprising:
Reactor (10), comprise by lower from upper reaction zone (11a) and isolated area (11b), described reactor (10) also comprises product gas outlet (18);
Kuppe (12), is arranged in described isolated area (11b), and described reactor (10) is separated into described reaction zone (11a) and described isolated area (11b) by described kuppe (12);
Regenerator (20), comprises regenerated flue gas outlet (23);
Reactor three-stage cyclone separator (91), comprise gas product entrance (911) and reclaimable catalyst fine powder outlet (912), described gas product entrance (911) is connected with described product gas outlet (18);
Regenerator three-stage cyclone separator (92), comprise regenerated flue gas entrance (921) and regenerated catalyst fines outlet (922), described regenerated flue gas entrance (921) exports (23) and is connected with described regenerated flue gas
It is characterized in that,
Described regenerator (20) also comprises reclaimable catalyst fine powder entrance (25), described reclaimable catalyst fine powder entrance (25) and described reclaimable catalyst fine powder are exported (912) and are connected by reclaimable catalyst fine powder conveyance conduit (83), and described reclaimable catalyst fine powder conveyance conduit (83) is provided with the reclaimable catalyst fine powder conveying pot (93) for carrying reclaimable catalyst fine powder;
The device of described methyl alcohol and/or dimethyl ether alkene also comprises bubble breaking portion (13), described bubble breaking portion (13) is arranged in described reaction zone (11a), the circumferential edge of described bubble breaking portion (13) is connected on the inwall of described reactor (10), and described bubble breaking portion (13) is provided with multiple broken hole.
2. the device of methyl alcohol according to claim 1 and/or dimethyl ether alkene, it is characterized in that, described reactor (10) also comprises methanol feeding mouth (15), and the position in the vertical direction of described bubble breaking portion (13) is higher than the position of described methanol feeding mouth (15).
3. the device of methyl alcohol according to claim 2 and/or dimethyl ether alkene, is characterized in that, described bubble breaking portion (13) is grid.
4. the device of methyl alcohol according to claim 3 and/or dimethyl ether alkene, is characterized in that, described grid comprises one or more layers.
5. the device of methyl alcohol according to claim 1 and/or dimethyl ether alkene, it is characterized in that, described reactor (10) also comprises cyclone separator (14), described cyclone separator (14) is arranged in described isolated area (11b), described kuppe (12) comprises taper section (121) and dilute phase pipe (122), described in the aperture efficiency of the bottom of described taper section (121), the opening at the top of taper section (121) is large, the bottom of described taper section (121) is connected on the inwall of described reactor (10), the top of described taper section (121) is connected to the bottom of described dilute phase pipe (122), the top of described dilute phase pipe (122) is connected with the entrance of described cyclone separator (14), described taper section (121) is provided with the through hole of the dipleg for dodging described cyclone separator (14).
6. the device of methyl alcohol according to claim 1 and/or dimethyl ether alkene, is characterized in that,
Described reactor (10) also comprises regenerated catalyst inlet (16) and reclaimable catalyst outlet (17);
Described regenerator (20) comprises reclaimable catalyst entrance (21) and regenerated catalyst outlet (22), described reclaimable catalyst outlet (17) is connected by reclaimable catalyst conveyance conduit (30) with described reclaimable catalyst entrance (21), and described regenerated catalyst outlet (22) is connected by regenerated catalyst road (40) with described regenerated catalyst inlet (16);
The device of described methyl alcohol and/or dimethyl ether alkene also comprises cooler (50) and first stripper (60) of separate setting, described cooler (50) is arranged on described regenerated catalyst road (40), and described first stripper (60) is arranged on described regenerated catalyst road (40) or described first stripper (60) is arranged on the inwall of described regenerator (20).
7. the device of methyl alcohol according to claim 6 and/or dimethyl ether alkene, is characterized in that, described first stripper (60) is arranged between described cooler (50) and described regenerated catalyst outlet (22).
8. the device of methyl alcohol according to claim 6 and/or dimethyl ether alkene, is characterized in that, described first stripper (60) is arranged between described cooler (50) and described regenerated catalyst inlet (16).
9. the device of methyl alcohol according to claim 1 and/or dimethyl ether alkene, is characterized in that, the position in the vertical direction of described regenerator (20) is higher than the position of described reactor (10).
10. the device of methyl alcohol according to claim 9 and/or dimethyl ether alkene, is characterized in that, described reactor (10) and described regenerator (20) are coaxially arranged.
The method of 11. 1 kinds of methyl alcohol and/or dimethyl ether alkene, comprises the following steps: make the methyl alcohol in reactor (10) and/or dimethyl ether and regenerated catalyst produce gas product in reaction zone (11a) haptoreaction,
It is characterized in that, the method for described methyl alcohol and/or dimethyl ether alkene is further comprising the steps of:
In described reaction zone (11a), pass through bubble breaking portion (13) bubble crushing to strengthen gas-solid contact, described gas product enters cyclone separator (14) by kuppe (12) and generates accessory substance with ethene suppressing, propylene generation secondary response;
The gas product separated in described reactor (10) enters in reactor three-stage cyclone separator (91) and proceeds to be separated, the reclaimable catalyst fine powder separated in described reactor three-stage cyclone separator (91) enters in regenerator (20) and regenerates, and the reclaimable catalyst fine powder after regeneration reclaims from regenerator three-stage cyclone separator (92).
The method of 12. methyl alcohol according to claim 11 and/or dimethyl ether alkene, it is characterized in that, described gas product is further comprising the steps of after described cyclone separator (14) is separated: the reclaimable catalyst separated in described reactor (10) enters in described regenerator (20) and regenerates, and enters in described reactor (10) after the regenerated catalyst cooling after regeneration.
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| CN104478643A (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 |
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| CN106563498A (en) * | 2016-11-03 | 2017-04-19 | 神华集团有限责任公司 | Method and device for cyclically utilizing methanol-to-olefin fine catalyst powder |
| CN108404818A (en) * | 2018-02-01 | 2018-08-17 | 国家能源投资集团有限责任公司 | Methanol to olefins reaction system |
| 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 |
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| CN104478643A (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 |
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| CN104474978B (en) | 2016-08-24 |
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