CN103772092A - Reaction device for converting methanol into light olefin - Google Patents
Reaction device for converting methanol into light olefin Download PDFInfo
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- CN103772092A CN103772092A CN201210412567.0A CN201210412567A CN103772092A CN 103772092 A CN103772092 A CN 103772092A CN 201210412567 A CN201210412567 A CN 201210412567A CN 103772092 A CN103772092 A CN 103772092A
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Abstract
The invention relates to a reaction device for converting methanol into light olefin. The reaction device mainly solves the problem that the yield of light olefin is lower in the prior art. The reaction device for converting methanol into light olefin mainly comprises a rapid bed reaction area 2, a coke-burning tank regenerator 22 and a regenerated catalyst lift pipe 16, wherein a product gas outlet 14 is formed at the top of a settler 11; a catalyst outlet is formed at the lower part of the settler 11, and connected with a circulating inclined pipe 6, an external cooler 4 and a stripper 17 respectively; an outlet of the circulating inclined pipe 6 is connected with a 1/3-2/3 reaction area height part away from the bottom of the rapid bed reaction area 2; an outlet end of a to-be-generated inclined pipe 19 is connected with a regenerator coke-burning tank 22; a fume outlet 27 is formed at the top of a settler 29; a catalyst outlet is formed at the lower part of the settler 29; the catalyst outlet is connected with a circulating inclined pipe 36, a degassing tank 24 and an external cooler 33 respectively; and an outlet end of a regenerating inclined pipe 20 is connected with the regenerated catalyst lift pipe 16. With the adoption of the technical scheme, the problem is solved better, so that the reaction device can be used in industrial production of light olefin.
Description
Technical field
The present invention relates to the reaction unit that a kind of methanol conversion is low-carbon alkene.
Background technology
Low-carbon alkene, i.e. ethene and propylene, is two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, but due to the limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people start to greatly develop the technology of alternative materials conversion ethene processed, propylene.Wherein, the important alternative materials of producing for low-carbon alkene of one class is oxygenatedchemicals, such as alcohols (methyl alcohol, ethanol), ethers (dme, methyl ethyl ether), ester class (methylcarbonate, methyl-formiate) etc., these oxygenatedchemicalss can be transformed by coal, Sweet natural gas, biomass equal energy source.Some oxygenatedchemicals can reach fairly large production, as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize the industrial scale of up to a million tonnes.Due to the popularity in oxygenatedchemicals source, add and transform the economy that generates low-carbon alkene technique, so by the technique of oxygen-containing compound conversion to produce olefine (OTO), be particularly subject to increasing attention by the technique of preparing olefin by conversion of methanol (MTO).
In US4499327 patent, silicoaluminophosphamolecular molecular sieve catalyst is applied to preparing olefin by conversion of methanol technique and studies in detail, think that SAPO-34 is the first-selected catalyzer of MTO technique.SAPO-34 catalyzer has very high selectivity of light olefin, and activity is also higher, and can make methanol conversion is reaction times of low-carbon alkene to be less than the degree of 10 seconds, more even reaches in the reaction time range of riser tube.
Technology and reactor that a kind of methanol conversion is low-carbon alkene in US 6166282, are announced, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas speed has reacted, rise to after the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Due to reaction after product gas and catalyzer sharp separation, effectively prevent the generation of secondary reaction.Through analog calculation, compared with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all greatly reduce.But in the method, low-carbon alkene carbon base absorption rate is general all in 77% left and right, has the problem that yield of light olefins is lower.
In CN 1723262, having announced with the multiple riser reaction unit of central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises multiple riser reactors, gas solid separation district, multiple offset components etc., each riser reactor has the port of injecting catalyst separately, be pooled to the disengaging zone of setting, catalyzer and gas product are separated.In the method, low-carbon alkene carbon base absorption rate is general all between 75～80%, has equally the problem that yield of light olefins is lower.
All there is the problem that yield of light olefins is lower in prior art, the present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the lower problem of yield of light olefins existing in prior art, and the reaction unit that a kind of new methanol conversion is low-carbon alkene is provided.This device, for the production of low-carbon alkene, has advantages of that yield of light olefins is higher.
For addressing the above problem, the technical solution used in the present invention is as follows: the reaction unit that a kind of methanol conversion is low-carbon alkene, mainly comprise fast bed reaction zone 2, burn pot type revivifier 22, regenerated catalyst riser tube 16, 2 bottoms, fast bed reaction zone have feed(raw material)inlet 1 and are connected with external warmer 4 lower oblique tubes 3 with catalyst inlet, top is connected with gas-solid sharp separation equipment 10, gas-solid sharp separation equipment 10 is positioned at settling vessel 11, settling vessel 11 tops have product gas outlet 14, bottom has catalyst outlet, respectively with circulation inclined tube 6, external warmer 4, stripper 17 is connected, circulation inclined tube 6 exports with distance fast bed reaction zone 2 1/3-2/3 reaction zone, the bottom At The Heights of fast bed reaction zone 2 and is connected, stripper 17 bottoms are connected with inclined tube 19 to be generated, inclined tube 19 exit end to be generated are connected with revivifier burning tank 22, burning tank 22 tops are provided with gas-solid sharp separation equipment 30, gas-solid sharp separation equipment 30 is positioned at settling vessel 29 inside, settling vessel 29 tops have exhanst gas outlet 27, bottom has catalyst outlet, respectively with circulation inclined tube 36, degassing vessel 24, external warmer 33 is connected, degassing vessel 24 bottoms are connected with regenerator sloped tube 20, regenerator sloped tube 20 exit end are connected with regenerated catalyst riser tube 16, regenerated catalyst riser tube 16 exit end are entering fast bed reaction zone 2 apart from fast bed reaction zone 2 1/3-2/3 reaction zone, bottom At The Heights.
In technique scheme, described regenerated catalyst riser tube 16 exit end enter the position of fast bed reaction zone 2 and difference of altitude that reclaimable catalyst returns to the position of fast bed reaction zone 2 through circulation inclined tube 6 is less than 1/5 reaction zone height; Described catalyzer comprises SAPO-34 molecular sieve; Described reactor settling vessel 11, revivifier settling vessel 29 inside are respectively equipped with cyclonic separator 12,26; Guiding valve control reclaimable catalyst flow is set on described inclined tube to be generated 19, and guiding valve pressure reduction is greater than 20 kPas; Described stripper 17 stripping media are water vapour, and the degassed medium of degassing vessel 24 is water vapour or nitrogen; Guiding valve control reclaimable catalyst flow is set on described regenerator sloped tube 20, and guiding valve pressure reduction is greater than 20 kPas; Described circulation inclined tube 36 is connected with burning tank 22 bottoms; Described external warmer 33 is connected with burning tank 22 bottoms; Described gas-solid sharp separation equipment 10 and 30 outlets of gas-solid sharp separation equipment arrange slightly revolves.
In the present invention, 16 chargings of regenerated catalyst riser tube comprise C4 hydrocarbon, and in described C4 hydrocarbon, C4 alkene mass content is greater than 75%; Described fast bed reaction zone 2 condition of answering is: temperature of reaction is 400～500 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 1～3 meter per second; Regenerated catalyst riser tube 16 conditions are: temperature of reaction is 530～680 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 4～12 meter per seconds; Revivifier 22 regeneration conditions are: regeneration temperature is 550～700 ℃, and regeneration pressure is counted 0.01～0.3MPa with gauge pressure, and resurgent gases phase linear speed is 1～3 meter per second; The average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%; Described reclaimable catalyst is at least divided into three parts, in massfraction, 20～40% return to the bottom of fast bed reaction zone 2 after heat-obtaining, 20～50% return to fast bed reaction zone 2 apart from fast bed reaction zone 2 1/3-2/3 reaction zone, bottom At The Heights, and 10～60% enter after stripper 17 strippings through inclined tube 19 to be generated and enter and burn pot type revivifier 22 and regenerate; The described pot type revivifier 22 that burns arranges through type external warmer 33 one time; Described fast bed reaction zone 2 temperature outs are higher 5～20 ℃ than bottom temp.
The method of calculation of average coke content of the present invention are that carbon deposit quality on catalyzer is divided by described catalyst quality.Carbon deposit measuring method on catalyzer is as follows: will mix the catalyst mix with carbon deposit comparatively uniformly, then weigh the band C catalyst of 0.1～1 gram, be put in pyrocarbon analyser and burn, by infrared analysis burn generate carbonic acid gas quality, thereby obtain the carbonaceous amount on catalyzer.
The preparation method of sial phosphorus molecular sieve of the present invention is: first preparing molecular sieve presoma, is 0.03～0.6R by mole proportioning: (Si 0.01～0.98: Al 0.01～0.6: P 0.01～0.6): 2～500 H
2o, wherein R represents template, and template is triethylamine, and constitutive material mixed solution obtains at the temperature of 100-250 ℃ after the crystallization of 1～10 hour; Again, molecular sieve presoma, phosphorus source, silicon source, aluminium source, template, water etc. are mixed according to certain ratio after at 110～260 ℃ hydrothermal crystallizing after at least 0.1 hour, finally obtain SAPO molecular sieve.The molecular sieve of preparation is mixed with the binding agent of required ratio, after the operation stepss such as, roasting dry through spraying, obtain final SAPO catalyzer, the weight percentage of binding agent in molecular sieve is between 10～90%.
Adopt device of the present invention, in fast bed reaction zone, return to position, the temperature of fast bed reaction zone, the difference of flow by controlling reclaimable catalyst, temperature in fast bed reaction zone, catalyst activity are adjusted to and are applicable to methyl alcohol highly selective and are converted into the condition of low-carbon alkene, reach and improve optionally object of low-carbon alkene assertive evidence.In addition, regenerated catalyst riser tube is set, be that the C4 hydrocarbon generating in low carbon olefin hydrocarbon contacts with high temperature, highly active regenerated catalyst by methanol conversion, C4 hydrocarbon is converted into low-carbon alkene, realize the effect of the pre-carbon distribution of regenerated catalyst simultaneously, further improve the low-carbon alkene assertive evidence selectivity in fast bed reaction zone.Therefore, adopt device of the present invention, reached the object that improves yield of light olefins.
Adopt technical scheme of the present invention: described regenerated catalyst riser tube 16 exit end enter the position of fast bed reaction zone 2 and difference of altitude that reclaimable catalyst returns to the position of fast bed reaction zone 2 through circulation inclined tube 6 is less than 1/5 reaction zone height; Described catalyzer comprises SAPO-34 molecular sieve; Described reactor settling vessel 11, revivifier settling vessel 29 inside are respectively equipped with cyclonic separator 12,26; Guiding valve control reclaimable catalyst flow is set on described inclined tube to be generated 19, and guiding valve pressure reduction is greater than 20 kPas; Described stripper 17 stripping media are water vapour, and the degassed medium of degassing vessel 24 is water vapour or nitrogen; Guiding valve control reclaimable catalyst flow is set on described regenerator sloped tube 20, and guiding valve pressure reduction is greater than 20 kPas; Described circulation inclined tube 36 is connected with burning tank 22 bottoms; Described external warmer 33 is connected with burning tank 22 bottoms; Described gas-solid sharp separation equipment 10 and 30 outlets of gas-solid sharp separation equipment arrange slightly revolves, low-carbon alkene carbon base absorption rate reaches 86.86% weight, exceed and can reach more than 4 percentage points than the low-carbon alkene carbon base absorption rate of prior art, obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of device of the present invention;
In Fig. 1,1 is methanol feed line; 2 is fast bed reaction zone; 3 is reactor external warmer lower oblique tube; 4 is reactor external warmer; 5 is reactor external warmer fluidizing medium; 6 is reactor cycles inclined tube; 7 is the close bed of reactor two; 8 is reactor external warmer heat-eliminating medium; 9 is reactor external warmer gas phase Returning reactor settling vessel; 10 is gas-solid sharp separation equipment; 11 is reactor settling vessel; 12 is cyclonic separator; 13 is reactor collection chamber; 14 is product gas outlet pipeline; 15 is the charging of regenerated catalyst riser tube; 16 is regenerated catalyst riser tube; 17 is stripper; 18 is stripped vapor; 19 is inclined tube to be generated; 20 is regenerator sloped tube; 21 is regeneration air; 22 is burning tank; 23 is degassed medium; 24 is degassing vessel; 25 return to revivifier for degassing vessel gas phase; 26 is revivifier cyclonic separator; 27 is regenerated flue gas outlet line; 28 is revivifier collection chamber; 29 is revivifier settling vessel; 30 is gas-solid sharp separation equipment; 31 return to settling vessel for external catalyst cooler for regenerator gas phase; 32 is external catalyst cooler for regenerator heat-eliminating medium; 33 is external catalyst cooler for regenerator; 34 is external catalyst cooler for regenerator lower oblique tube; 35 is external catalyst cooler for regenerator fluidization steam vapor; 36 is revivifier circulation inclined tube; 37 is the close bed of revivifier two.
The raw material that is mainly methyl alcohol enters fast bed reaction zone 2, contact with the catalyzer that comprises sial phosphorus molecular sieve, generation comprises low-carbon alkene, the gaseous stream of C4 hydrocarbon and reclaimable catalyst, after cyclonic separator 12 separates, gaseous stream enters centrifugal station through pipeline 14, reclaimable catalyst is at least divided into three parts, first part returns to the bottom of fast bed reaction zone 2 after reactor external warmer 4 heat-obtainings, second section returns to fast bed reaction zone 2 apart from fast bed reaction zone 2 1/3-2/3 reaction zone, bottom At The Heights through reactor cycles inclined tube 6, Part III enters after stripper 17 strippings through inclined tube 19 to be generated and enters and burn pot type revivifier 22 and regenerate, form regenerated catalyst, regenerated catalyst is through degassed, 24 enter regenerated catalyst riser tube 16 through regenerator sloped tube 20 after degassed, contact with the raw material that comprises C4 hydrocarbon, regenerated catalyst riser tube 16 exit end are entering fast bed reaction zone 2 apart from fast bed reaction zone 2 1/3-2/3 reaction zone, bottom At The Heights.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
On reaction unit as shown in Figure 1, purity is that the methyl alcohol of 99.5% (weight) enters fast bed reaction zone, contact with the catalyzer that comprises SAPO-34 molecular sieve, the gaseous stream generating and catalyzer are after gas solid separation, gaseous stream enters centrifugal station, reclaimable catalyst is divided into three parts, in massfraction, 20% returns to the bottom of fast bed reaction zone after heat-obtaining, 20% returns to fast bed reaction zone apart from bottom, fast bed reaction zone 1/3 reaction zone At The Height, 60% enters after stripper stripping and enters and burn the regeneration of pot type revivifier through inclined tube to be generated, reactor settling vessel, revivifier settling vessel inside is respectively equipped with cyclonic separator, regenerated catalyst enters regenerated catalyst riser tube through regenerator sloped tube, contact with the raw material that comprises C4 hydrocarbon, the raw material of the described C4 of comprising hydrocarbon is: in massfraction, 82%C4 hydrocarbon, 18% water vapour, in wherein said C4 hydrocarbon, C4 alkene mass content is 75%.Regenerated catalyst leg outlet end is entering fast bed reaction zone apart from bottom, fast bed reaction zone 1/3 reaction zone At The Height.Fast bed reaction zone reaction conditions is: temperature of reaction is 400 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 1 meter per second; Regenerated catalyst riser tube reaction conditions is: temperature of reaction is 530 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; Revivifier regeneration condition is: regeneration temperature is 550 ℃, and regeneration pressure is counted 0.01MPa with gauge pressure, and resurgent gases phase linear speed is 1 meter per second; The average carbon deposition quantity massfraction of described regenerated catalyst is 0.5%, burn pot type revivifier through type external warmer is set one time, guiding valve control reclaimable catalyst flow is set on inclined tube to be generated, guiding valve pressure reduction is 21 kPas, stripper stripping medium is water vapour, the degassed medium of degassing vessel is water vapour, and fast bed reaction zone temperature out is higher 5.5 ℃ than bottom temp.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 84.78% (weight).
[embodiment 2]
According to condition and step [embodiment 1] Suo Shu, purity is that the methyl alcohol of 99.5% (weight) enters fast bed reaction zone, contact with the catalyzer that comprises SAPO-34 molecular sieve, the gaseous stream generating and catalyzer are after gas solid separation, gaseous stream enters centrifugal station, reclaimable catalyst is divided into three parts, in massfraction, 40% returns to the bottom of fast bed reaction zone after heat-obtaining, 50% returns to fast bed reaction zone apart from bottom, fast bed reaction zone 2/3 reaction zone At The Height, 10% enters after stripper stripping and enters and burn the regeneration of pot type revivifier through inclined tube to be generated, regenerated catalyst enters regenerated catalyst riser tube through regenerator sloped tube, contact with the raw material that comprises C4 hydrocarbon, the raw material of the described C4 of comprising hydrocarbon is: in massfraction, 75%C4 hydrocarbon, 25% water vapour, in wherein said C4 hydrocarbon, C4 alkene mass content is 92%.Regenerated catalyst leg outlet end is entering fast bed reaction zone apart from bottom, fast bed reaction zone 2/3 reaction zone At The Height.Fast bed reaction zone reaction conditions is: temperature of reaction is 500 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 3 meter per seconds; Regenerated catalyst riser tube reaction conditions is: temperature of reaction is 680 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 12 meter per seconds; Revivifier regeneration condition is: regeneration temperature is 700 ℃, and regeneration pressure is counted 0.01MPa with gauge pressure, and resurgent gases phase linear speed is 3 meter per seconds; The average carbon deposition quantity massfraction of described regenerated catalyst is 0.01%, and guiding valve control reclaimable catalyst flow is set on inclined tube to be generated, and guiding valve pressure reduction is 40 kPas, and the degassed medium of degassing vessel is nitrogen, and fast bed reaction zone temperature out is higher 20 ℃ than bottom temp.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 85.12% (weight).
[embodiment 3]
According to condition and step [embodiment 2] Suo Shu, purity is that the methyl alcohol of 99.5% (weight) enters fast bed reaction zone, contact with the catalyzer that comprises SAPO-34 molecular sieve, the gaseous stream generating and catalyzer are after gas solid separation, gaseous stream enters centrifugal station, reclaimable catalyst is divided into three parts, in massfraction, 30% returns to the bottom of fast bed reaction zone after heat-obtaining, 40% returns to fast bed reaction zone apart from bottom, fast bed reaction zone 1/2 reaction zone At The Height, 30% enters after stripper stripping and enters and burn the regeneration of pot type revivifier through inclined tube to be generated, regenerated catalyst enters regenerated catalyst riser tube through regenerator sloped tube, contact with the raw material that comprises C4 hydrocarbon.Regenerated catalyst leg outlet end is entering fast bed reaction zone apart from bottom, fast bed reaction zone 2/3 reaction zone At The Height.Fast bed reaction zone reaction conditions is: temperature of reaction is 470 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 1.5 meter per seconds; Regenerated catalyst riser tube reaction conditions is: temperature of reaction is 650 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 7 meter per seconds; Revivifier regeneration condition is: regeneration temperature is 680 ℃, and regeneration pressure is counted 0.01MPa with gauge pressure, and resurgent gases phase linear speed is 1.6 meter per seconds; The average carbon deposition quantity massfraction of described regenerated catalyst is 0.1%, and guiding valve control reclaimable catalyst flow is set on inclined tube to be generated, and guiding valve pressure reduction is 46 kPas, and fast bed reaction zone temperature out is higher 12 ℃ than bottom temp.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 86.86% (weight).
[embodiment 4]
According to condition and step [embodiment 3] Suo Shu, fast bed reaction zone reaction conditions is: temperature of reaction is 486 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 1.25 meter per seconds; Regenerated catalyst riser tube reaction conditions is: temperature of reaction is 630 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; Revivifier regeneration condition is: regeneration temperature is 660 ℃, and regeneration pressure is counted 0.3MPa with gauge pressure, and resurgent gases phase linear speed is 1.3 meter per seconds.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 83.95% (weight).
[comparative example 1]
According to condition and step [embodiment 3] Suo Shu, just first part and second section reclaimable catalyst all directly return to bottom, fast bed reaction zone, and yield of light olefins is 84.76% (weight).
[comparative example 2]
According to condition and step [embodiment 3] Suo Shu, first part and second section reclaimable catalyst all directly return to bottom, fast bed reaction zone, regenerated catalyst riser tube is not set, regenerated catalyst directly returns to bottom, fast bed reaction zone through regenerator sloped tube, and yield of light olefins is 82.45% (weight).
Obviously, adopt device of the present invention, can reach the object that improves yield of light olefins, there is larger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (10)
1. the reaction unit that methanol conversion is low-carbon alkene, mainly comprise fast bed reaction zone (2), burn pot type revivifier (22), regenerated catalyst riser tube (16), bottom, fast bed reaction zone (2) has feed(raw material)inlet (1) and is connected with external warmer (4) lower oblique tube (3) with catalyst inlet, top is connected with gas-solid sharp separation equipment (10), gas-solid sharp separation equipment (10) is positioned at settling vessel (11), settling vessel (11) top has product gas outlet (14), bottom has catalyst outlet, respectively with circulation inclined tube (6), external warmer (4), stripper (17) is connected, circulation inclined tube (6) outlet is connected with 1/3-2/3 reaction zone, bottom, distance fast bed reaction zone (2) At The Height of fast bed reaction zone (2), stripper (17) bottom is connected with inclined tube to be generated (19), inclined tube to be generated (19) exit end is connected with revivifier burning tank (22), burning tank (22) top is provided with gas-solid sharp separation equipment (30), gas-solid sharp separation equipment (30) is positioned at settling vessel (29) inside, settling vessel (29) top has exhanst gas outlet (27), bottom has catalyst outlet, respectively with circulation inclined tube (36), degassing vessel (24), external warmer (33) is connected, degassing vessel (24) bottom is connected with regenerator sloped tube (20), regenerator sloped tube (20) exit end is connected with regenerated catalyst riser tube (16), regenerated catalyst riser tube (16) exit end is entering fast bed reaction zone (2) apart from 1/3-2/3 reaction zone, fast bed reaction zone (2) bottom At The Height.
2. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that described regenerated catalyst riser tube (16) exit end enters the position of fast bed reaction zone (2) and difference of altitude that reclaimable catalyst returns to the position of fast bed reaction zone (2) through circulation inclined tube (6) is less than 1/5 reaction zone height.
3. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that described catalyzer comprises SAPO-34 molecular sieve.
4. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that described reactor settling vessel (11), revivifier settling vessel (29) inside are respectively equipped with cyclonic separator (12), (26).
5. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that, on described inclined tube to be generated (19), guiding valve control reclaimable catalyst flow is set, and guiding valve pressure reduction is greater than 20 kPas.
6. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that described stripper (17) stripping medium is water vapour, and the degassed medium of degassing vessel (24) is water vapour or nitrogen.
7. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that, on described regenerator sloped tube (20), guiding valve control reclaimable catalyst flow is set, and guiding valve pressure reduction is greater than 20 kPas.
8. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that described circulation inclined tube (36) is connected with burning tank (22) bottom.
9. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, is characterized in that described external warmer (33) is connected with burning tank (22) bottom.
10. the reaction unit that methanol conversion is low-carbon alkene according to claim 1, it is characterized in that the outlet of described gas-solid sharp separation equipment (10) and gas-solid sharp separation equipment (30) arranges slightly revolves.
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| CN104478642A (en) * | 2014-11-18 | 2015-04-01 | 神华集团有限责任公司 | Device and method for producing olefin from methanol |
| CN104628506A (en) * | 2013-11-06 | 2015-05-20 | 中国石油化工股份有限公司 | Method for converting methanol to low carbon olefin |
| CN105085130A (en) * | 2014-05-14 | 2015-11-25 | 中国石油化工股份有限公司 | Device for preparing low carbon olefins from oxygen-containing compound by conversion |
| CN105669348A (en) * | 2014-11-20 | 2016-06-15 | 中国石油化工股份有限公司 | Device for preparing low carbon olefins from oxygen-containing compound by conversion |
| CN108080009A (en) * | 2016-11-21 | 2018-05-29 | 中国石油大学(华东) | A kind of alkane isomerization reaction-regenerative device and method |
| CN108079912A (en) * | 2016-11-21 | 2018-05-29 | 中国石油大学(华东) | A kind of reaction unit and its reaction method of alkane catalytic dehydrogenation |
| CN109107615A (en) * | 2017-06-23 | 2019-01-01 | 中国石油大学(华东) | A kind of alkane dehydrogenating catalyst regeneration method and regenerating unit |
| CN110452087A (en) * | 2018-05-08 | 2019-11-15 | 中国石油化工股份有限公司 | The production method of low-carbon alkene |
| CN114177840A (en) * | 2020-09-15 | 2022-03-15 | 中国石油化工股份有限公司 | Reaction system and method for preparing ethylene propylene |
| CN114377620A (en) * | 2020-10-16 | 2022-04-22 | 中国科学院大连化学物理研究所 | Fluidized bed reactor, device and method for preparing low-carbon olefin by using oxygen-containing compound |
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