CN103739430A - Reaction device used for converting methanol into low-carbon olefins - Google Patents

Reaction device used for converting methanol into low-carbon olefins Download PDF

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CN103739430A
CN103739430A CN201210393071.3A CN201210393071A CN103739430A CN 103739430 A CN103739430 A CN 103739430A CN 201210393071 A CN201210393071 A CN 201210393071A CN 103739430 A CN103739430 A CN 103739430A
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reaction
low
zone
breeding blanket
methyl alcohol
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CN103739430B (en
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齐国祯
王洪涛
王华文
盛世春
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

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Abstract

The invention relates to a reaction device used for converting methanol into low-carbon olefins, mainly solving a problem of the low yield of the low-carbon olefins in the prior art. According to the technical scheme adopted b the reaction device, the reaction device mainly comprises a methanol conversion reaction zone 21, a first regeneration zone 10, a second regeneration zone 3 and a hydrocarbon cracking reaction zone 20; a gas solid separation zone 9 is disposed above the upper part of the methanol conversion reaction zone 21 and is connected to a lifting stand pipe 11 through a spent-catalyst inclined pipe 5; the outlet end of the lifting stand pipe 11 is disposed in the first regeneration zone 10; catalyst outlets are disposed in the lower part of the first regeneration zone 11, and are respectively connected to the methanol conversion reaction zone 21, the second regeneration zone 3 and the hydrocarbon cracking reaction zone 20; the upper part of the hydrocarbon cracking reaction zone 20 is provided with a steam stripping zone 26 and a settling zone 28; and the lower part of the steam stripping zone 26 is provided with a catalyst outlet connected to the second regeneration zone 3. By the technical scheme, the problem is solved well and the reaction device can be used in industrial production of the low-carbon olefins.

Description

The reaction unit that conversion methyl alcohol is low-carbon alkene
Technical field
The present invention relates to a kind of reaction unit that methyl alcohol is low-carbon alkene that transforms.
Background technology
Low-carbon alkene, ethene and propylene, be 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 that alternative materials transforms 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.Popularity due to 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), particularly the technique by preparing olefin by conversion of methanol (MTO) is subject to increasing attention.
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, have been 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 prevented the generation of secondary reaction.Through analog calculation, to compare 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.
The multiple riser reaction unit of having announced in CN 1723262 with central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises a plurality of riser reactors, gas solid separation district, a plurality of 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 conversion methyl alcohol 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: a kind ofly transform the reaction unit that methyl alcohol is low-carbon alkene, mainly comprise the reaction of methanol conversion district 21, the first breeding blanket 10, the second breeding blanket 3, hydrocarbon cracking reaction zone 20, 21 tops, the reaction of methanol conversion district are gas solid separation district 9, gas solid separation district 9 is connected with lifting standpipe 11 by inclined tube 5 to be generated, promote standpipe 11 exit end and be positioned at the first breeding blanket 10, the first 10 tops, breeding blanket is negative area 13, bottom has catalyst outlet, respectively with the reaction of methanol conversion district 21, the second breeding blanket 3, hydrocarbon cracking reaction zone 20 is connected, 20 tops, hydrocarbon cracking reaction zone are provided with 26He negative area, stripping zone 28, 26 bottoms, stripping zone have catalyst outlet and are connected with the second breeding blanket 3, the second breeding blanket 3 exit end are provided with gas-solid sharp separation equipment 4, 4 outlets of gas-solid sharp separation equipment communicate with the first breeding blanket 10.
In technique scheme, 9 tops, described gas solid separation district have product gas outlet 22, and 28 tops, negative area have product gas outlet 30; Described the reaction of methanol conversion district 21 is fast fluidized bed, and hydrocarbon cracking reaction zone 20 is riser tube, and the second breeding blanket 3 is burning tank; Described lifting standpipe 11 outlets are provided with slightly revolves 12; After merging, product gas outlet 22 and product gas outlet 30 enter centrifugal station; 28 inside, 13He negative area, described negative area are respectively equipped with cyclonic separator 14 and 29; 3 bottoms, described the second breeding blanket are provided with feed distributing plate 2; It is air or nitrogen that described lifting standpipe 11 promotes medium; The stripping medium of described stripping zone 26 is water vapour; 13 tops, 10 negative area, top, described the first breeding blanket have exhanst gas outlet 15.
In the present invention, catalyzer comprises SAPO-34 molecular sieve; The reaction of methanol conversion district 21 reaction conditionss are: temperature of reaction is 400～500 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 0.5～3 meter per second; Hydrocarbon cracking reaction zone 20 reaction conditionss are: temperature of reaction is 550～650 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 3～10 meter per seconds; The first breeding blanket 10 reaction conditionss are: regeneration temperature is 550～700 ℃, and gas phase linear speed is 0.4～1 meter per second; The second breeding blanket 3 reaction conditionss are: regeneration temperature is 580～670 ℃, and gas phase linear speed is 1～3 meter per second; The average carbon deposition quantity massfraction of catalyzer after described the first breeding blanket 10 regeneration is 0.01～0.5%; Described hydro carbons comprises C4 alkene, and C4 olefin content is greater than 60%.
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 comparatively uniform catalyst mix with carbon deposit, then weigh the band C catalyst of 0.1～1 gram, be put in pyrocarbon analyser and burn, the carbonic acid gas quality of burning and generating by infrared analysis, thus the carbonaceous amount on catalyzer obtained.
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%.
In the present invention, slightly revolve and refer to and be positioned at the elementary cyclonic separator that the outlet of riser tube or down-flow fluidized bed using ECT can realize gas-solid sharp separation, because its separation efficiency is lower generally between 70～90%, so those skilled in the art is generally simply referred to as " slightly revolving ".And down-flow fluidized bed using ECT refers to that solid particulate presents the bed type of flow pattern from top to bottom under solid particulate self gravitation or airflow acting force.
The inventor finds by research, hydro carbons (as C4 alkene) is cracked into low-carbon alkene needs higher catalyst activity and temperature of reaction, and the carbon distribution character of its generation and methanol conversion be that the carbon distribution that forms in low carbon olefin hydrocarbon is different, need higher coke burning degree.Adopt device of the present invention, two breeding blankets are set, the second breeding blanket is burning tank, for highly efficient regeneration, can burn 60～90% the carbon distribution being produced by hydrocarbon cracking, then the carbon distribution forming in the carbon distribution not burning down and methanol conversion process continues regeneration in the first breeding blanket, and the catalyzer after regeneration offers respectively the reaction of methanol conversion district and hydrocarbon cracking reaction zone is used.By the cracking of hydro carbons, especially the above hydrocarbon of methyl alcohol by-product C4 continue to be converted into low-carbon alkene, effectively improved the yield of low-carbon alkene.Therefore, adopt device of the present invention, can reach the object that improves yield of light olefins.
Adopt technical scheme of the present invention: 9 tops, described gas solid separation district have product gas outlet 22, and 28 tops, negative area have product gas outlet 30; Described the reaction of methanol conversion district 21 is fast fluidized bed, and hydrocarbon cracking reaction zone 20 is riser tube, and the second breeding blanket 3 is burning tank; Described lifting standpipe 11 outlets are provided with slightly revolves 12, after product gas outlet 22 and product gas outlet 30 merge, enters centrifugal station; 28 inside, 13He negative area, described negative area are respectively equipped with cyclonic separator 14 and 29; 3 bottoms, described the second breeding blanket are provided with feed distributing plate 2; It is air or nitrogen that described lifting standpipe 11 promotes medium; The stripping medium of described stripping zone 26 is water vapour; 13 tops, 10 negative area, top, described the first breeding blanket have exhanst gas outlet 15, and low-carbon alkene carbon base absorption rate reaches 86.88% weight, than the low-carbon alkene carbon base absorption rate of prior art, exceeds and can reach more than 3 percentage points, has 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 the second breeding blanket regeneration air pipeline; 2 is the second breeding blanket dispersion plate; 3 is the second breeding blanket; 4 is gas-solid sharp separation equipment; 5 is inclined tube to be generated; 6 promote medium pipeline for promoting standpipe; 7 is catalyst recirculation pipe; 8 is the first breeding blanket regeneration air pipeline; 9 is gas solid separation district; 10 is the first breeding blanket; 11 for promoting standpipe; 12 for slightly revolving; 13 is negative area; 14 is cyclonic separator; 15 is exhanst gas outlet; 16 is hydrocarbon raw material feeding line; 17 is the pipeline that the second breeding blanket catalyst transport is gone to hydrocarbon cracking reaction; 18 is pre-mixing section; 19 is methanol feed line; 20 is hydrocarbon cracking reaction zone; 21Wei the reaction of methanol conversion district; 22 is product gas outlet; 23 is regenerator sloped tube; 24 enter the pipeline of the first breeding blanket for the catalyzer after stripping; 25 is stripped vapor; 26 is stripping zone; 27 for slightly revolving; 28 is negative area; 29 is cyclonic separator; 30 is product gas outlet.
The raw material that is mainly methyl alcohol enters the reaction of methanol conversion district 21, contact with the catalyzer that comprises sial phosphorus molecular sieve, the gaseous stream generating enters centrifugal station, the reclaimable catalyst forming is through inclined tube 5 to be generated, promote standpipe 11 and enter the first breeding blanket 11, a catalyzer part for the first breeding blanket 11 enters the second breeding blanket 10, a part is returned to the reaction of methanol conversion district 21, a part enters hydrocarbon cracking reaction zone 20, the catalyzer of hydrocarbon cracking reaction zone 20 enters the second breeding blanket 3 after stripping, the gaseous stream of the second breeding blanket 3 and catalyzer enter the first breeding blanket 10.
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 99.5% methanol feedstock enters the reaction of methanol conversion district, contact with SAPO-34 molecular sieve catalyst, the gaseous stream generating enters centrifugal station, the reclaimable catalyst forming enters the first breeding blanket through inclined tube to be generated, the catalyzer of the first breeding blanket, in massfraction, 20% returns to the reaction of methanol conversion district through regenerator sloped tube, 40% enters the second breeding blanket, 40% enters hydrocarbon cracking reaction zone, and the catalyzer of hydrocarbon cracking reaction zone is with gaseous stream after separated, and catalyzer enters the second breeding blanket after stripping.The gaseous stream of the second breeding blanket and catalyzer enter the first breeding blanket after gas-solid sharp separation.The reaction of methanol conversion district is fast fluidized bed, and hydrocarbon cracking reaction zone is riser tube, and the second breeding blanket is burning tank, and lifting stand-pipe output is provided with slightly and revolves.The second bottom, breeding blanket is provided with feed distributing plate, and the lifting medium that promotes standpipe is air, and the stripping medium of stripping zone is water vapour, and the first top, negative area, top, breeding blanket has exhanst gas outlet.The reaction of methanol conversion district reaction conditions is: temperature of reaction is 400 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 0.5 meter per second; Hydrocarbon cracking reaction zone reaction conditions is: temperature of reaction is 550 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 3 meter per seconds; The first breeding blanket reaction conditions is: regeneration temperature is 550 ℃, and gas phase linear speed is 0.4 meter per second; The second breeding blanket reaction conditions is: regeneration temperature is 580 ℃, and gas phase linear speed is 1 meter per second, and the average carbon deposition quantity massfraction of catalyzer after the first breeding blanket regeneration is 0.01%, and hydrocarbon cracking reaction zone feeds comprises C4 alkene, and C4 olefin content is 60%.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 81.55% (weight).
 
[embodiment 2]
According to condition and the step [embodiment 1] Suo Shu, the catalyzer of the first breeding blanket, in massfraction, 20% returns to the reaction of methanol conversion district through regenerator sloped tube, and 40% enters the second breeding blanket, and 40% enters hydrocarbon cracking reaction zone, the lifting medium that promotes standpipe is nitrogen, the reaction of methanol conversion district 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; Hydrocarbon cracking reaction zone reaction conditions is: temperature of reaction is 650 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; The first breeding blanket reaction conditions is: regeneration temperature is 700 ℃, and gas phase linear speed is 1 meter per second; The second breeding blanket reaction conditions is: regeneration temperature is 670 ℃, and gas phase linear speed is 3 meter per seconds, and the average carbon deposition quantity massfraction of catalyzer after the first breeding blanket regeneration is 0.5%, and hydrocarbon cracking reaction zone feeds comprises C4 alkene, and C4 olefin content is 76%.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 84.75% (weight).
 
[embodiment 3]
According to condition and the step [embodiment 1] Suo Shu, the catalyzer of the first breeding blanket, in massfraction, 30% returns to the reaction of methanol conversion district through regenerator sloped tube, 50% enters the second breeding blanket, and 20% enters hydrocarbon cracking reaction zone, and the reaction of methanol conversion district reaction conditions is: temperature of reaction is 480 ℃, reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 1.5 meter per seconds; Hydrocarbon cracking reaction zone reaction conditions is: temperature of reaction is 610 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; The first breeding blanket reaction conditions is: regeneration temperature is 650 ℃, and gas phase linear speed is 0.6 meter per second; The second breeding blanket reaction conditions is: regeneration temperature is 680 ℃, and gas phase linear speed is 1.8 meter per seconds, and the average carbon deposition quantity massfraction of catalyzer after the first breeding blanket regeneration is 0.1%, and hydrocarbon cracking reaction zone feeds comprises C4 alkene, and C4 olefin content is 76%.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 86.88% (weight).
 
[embodiment 4]
According to condition and step [embodiment 3] Suo Shu, the reaction of methanol conversion district reaction conditions is: temperature of reaction is 480 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 1.5 meter per seconds; Hydrocarbon cracking reaction zone reaction conditions is: temperature of reaction is 610 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; The first breeding blanket reaction conditions is: regeneration temperature is 650 ℃, and gas phase linear speed is 0.5 meter per second; The second breeding blanket reaction conditions is: regeneration temperature is 680 ℃, and gas phase linear speed is 1.5 meter per seconds, and the average carbon deposition quantity massfraction of catalyzer after the first breeding blanket regeneration is 0.1%, and hydrocarbon cracking reaction zone feeds comprises C4 alkene, and C4 olefin content is 76%.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 84.95% (weight).
 
[comparative example 1]
According to condition and the step [embodiment 3] Suo Shu, a breeding blanket is only set, 40% of the regenerated catalyst of this breeding blanket returns to the reaction of methanol conversion district, 60% enters hydrocarbon cracking reaction zone, the average carbon deposition quantity massfraction of regenerated catalyst is 0.1%, and yield of light olefins is 83.92% (weight).
 
[comparative example 2]
Condition and step according to [embodiment 3] Suo Shu, only arrange a breeding blanket, and hydrocarbon cracking reaction zone is not set, and the catalyzer after regeneration all returns to the reaction of methanol conversion district, and yield of light olefins is 82.50% (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. one kind transforms the reaction unit that methyl alcohol is low-carbon alkene, mainly comprise the reaction of methanol conversion district (21), the first breeding blanket (10), the second breeding blanket (3), hydrocarbon cracking reaction zone (20), top, the reaction of methanol conversion district (21) is gas solid separation district (9), gas solid separation district (9) is connected with lifting standpipe (11) by inclined tube to be generated (5), promote standpipe (11) exit end and be positioned at the first breeding blanket (10), top, the first breeding blanket (10) is negative area (13), bottom has catalyst outlet, respectively with the reaction of methanol conversion district (21), the second breeding blanket (3), hydrocarbon cracking reaction zone (20) is connected, top, hydrocarbon cracking reaction zone (20) is provided with stripping zone (26) and negative area (28), bottom, stripping zone (26) has catalyst outlet and is connected with the second breeding blanket (3), the second breeding blanket (3) exit end is provided with gas-solid sharp separation equipment (4), gas-solid sharp separation equipment (4) outlet communicates with the first breeding blanket (10).
2. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that top, described gas solid separation district (9) has product gas outlet (22), top, negative area (28) has product gas outlet (30).
3. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that described the reaction of methanol conversion district (21) is for fast fluidized bed, hydrocarbon cracking reaction zone (20) are riser tube, and the second breeding blanket (3) are burning tank.
4. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that described lifting standpipe (11) outlet is provided with slightly revolves (12).
5. transform according to claim 2 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that entering centrifugal station after described product gas outlet (22) and product gas outlet (30) merge.
6. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that described negative area (13) and inside, negative area (28) are respectively equipped with cyclonic separator (14) and (29).
7. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that bottom, described the second breeding blanket (3) is provided with feed distributing plate (2).
8. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that it is air or nitrogen that described lifting standpipe (11) promotes medium.
9. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, the stripping medium that it is characterized in that described stripping zone (26) is water vapour.
10. transform according to claim 1 the reaction unit that methyl alcohol is low-carbon alkene, it is characterized in that top, negative area, top, described the first breeding blanket (10) (13) has exhanst gas outlet (15).
CN201210393071.3A 2012-10-17 2012-10-17 Converting methanol is the reaction unit of low-carbon alkene Active CN103739430B (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105268381A (en) * 2014-07-03 2016-01-27 中国石油化工股份有限公司 Downer reaction-regeneration device used for preparation of olefin from methanol and reaction method thereof
CN110117214A (en) * 2019-05-29 2019-08-13 正大能源材料(大连)有限公司 A kind of device and method of methanol Efficient Conversion producing light olefins

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102190550A (en) * 2010-03-03 2011-09-21 中国石油化工股份有限公司 Production method of low-carbon olefin
CN102464523A (en) * 2010-11-17 2012-05-23 中国石油化工股份有限公司 Method for producing light olefins
CN102463138A (en) * 2010-11-17 2012-05-23 中国石油化工股份有限公司 Two-stage regeneration method for SAPO-34 catalysts

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102190550A (en) * 2010-03-03 2011-09-21 中国石油化工股份有限公司 Production method of low-carbon olefin
CN102464523A (en) * 2010-11-17 2012-05-23 中国石油化工股份有限公司 Method for producing light olefins
CN102463138A (en) * 2010-11-17 2012-05-23 中国石油化工股份有限公司 Two-stage regeneration method for SAPO-34 catalysts

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105268381A (en) * 2014-07-03 2016-01-27 中国石油化工股份有限公司 Downer reaction-regeneration device used for preparation of olefin from methanol and reaction method thereof
CN110117214A (en) * 2019-05-29 2019-08-13 正大能源材料(大连)有限公司 A kind of device and method of methanol Efficient Conversion producing light olefins
CN110117214B (en) * 2019-05-29 2021-11-23 正大能源材料(大连)有限公司 Device and method for preparing low-carbon olefin by efficiently converting methanol

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