CN102875296A - Reaction unit for preparing low-carbon olefins - Google Patents
Reaction unit for preparing low-carbon olefins Download PDFInfo
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- CN102875296A CN102875296A CN2011101934310A CN201110193431A CN102875296A CN 102875296 A CN102875296 A CN 102875296A CN 2011101934310 A CN2011101934310 A CN 2011101934310A CN 201110193431 A CN201110193431 A CN 201110193431A CN 102875296 A CN102875296 A CN 102875296A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The invention relates to a reaction unit for preparing low-carbon olefins, mainly solving the problem of low yield of low-carbon olefins in the prior art. The reaction unit mainly comprises a rapid fluidized bed reaction zone 2, a rough-cut cyclone 4, a disengager 21, a gas-solid distribution zone 7, a downer reaction zone 9, a regenerator 11, and a riser reaction zone 20, wherein the outlet of the riser reaction zone 20 is connected with the disengager 21, the bottom of the disengager is connected with the regenerator 11 through a regeneration standpipe 26, the regenerator 11 is provided with two catalyst outlets, one catalyst outlet is connected with the riser reaction zone 20, the other catalyst outlet is connected with the downer reaction zone 9, the outlet of the downer reaction zone 9 is connected with the rapid fluidized bed reaction zone 2, the outlet of the rapid fluidized bed reaction zone 2 is connected with the rough-cut cyclone 4, a gas-phase outlet pipeline 5 of the rough-cut cyclone 4 is connected with the disengager 21, the dipleg of the rough-cut cyclone 4 is connected with the gas-solid distribution zone 7, and the gas-solid distribution zone 7 is connected with the downer reaction zone 9. The reaction unit disclosed herein well solves the problems and can be used in the industrial production of low-carbon olefins.
Description
Technical field
The present invention relates to a kind of reaction unit of preparing light olefins from methanol.
Technical background
Low-carbon alkene, namely ethene and propylene are 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 because limited supply and the higher price of petroleum resources, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people begin to greatly develop the technology that alternative materials transforms ethene processed, propylene.Wherein, the important alternative materials that is used for low-carbon alkene production 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, such as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize up to a million tonnes industrial scale.Because 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), particularly the technique by preparing olefin by conversion of methanol (MTO) is subject to increasing attention.
In the US4499327 patent silicoaluminophosphamolecular molecular sieve catalyst is applied to preparing olefin by conversion of methanol technique and studies in great detail, think that SAPO-34 is the first-selected catalyzer of MTO technique.The 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 10 seconds degree, more even reach in the reaction time range of riser tube.
Technology and reactor that a kind of methanol conversion is low-carbon alkene have been announced among the US 6166282, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu reaction of gas speed is finished, after rising to the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Because reaction after product gas and catalyzer sharp separation have 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 the low-carbon alkene carbon base absorption rate is general all about 77% in the method, has the lower problem of yield of light olefins.
The multiple riser reaction unit of having announced among the 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.The low-carbon alkene carbon base absorption rate is general all between 75～80% in the method, has equally the lower problem of yield of light olefins.
All there is the lower problem of yield of light olefins in prior art, and 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 that exists in the prior art, and a kind of reaction unit of new preparing light olefins from methanol is provided.This device is used 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 of reaction unit of preparing light olefins from methanol, mainly comprise fast fluidized bed reaction zone 2, slightly revolve 4, settling vessel 21, gas-solid distribution zone 7, down-flow fluidized bed using ECT reaction zone 9, revivifier 11, riser reaction zone 20, riser reaction zone 20 outlets link to each other with settling vessel 21, settling vessel 21 bottoms are provided with catalyst outlet and link to each other with revivifier 11 by regeneration standpipe 26, revivifier 11 has two catalyst outlets, one is passed through regenerator sloped tube 17 and links to each other with riser reaction zone 20, one is passed through regenerator sloped tube 13 and links to each other with down-flow fluidized bed using ECT reaction zone 9, the outlet of down-flow fluidized bed using ECT reaction zone 9 links to each other with fast fluidized bed reaction zone 2, the outlet of fast fluidized bed reaction zone 2 with slightly revolve 4 and link to each other, slightly revolving gaseous phase outlet pipeline 5 links to each other with settling vessel 21, thick spin material leg 6 links to each other with gas-solid distribution zone 7, gas-solid distribution zone 7 bottoms link to each other with down-flow fluidized bed using ECT reaction zone 9, gas-solid distribution zone 7 has catalyst outlet and links to each other with revivifier 11 by inclined tube 10 to be generated, and settling vessel 21 tops have product gas outlet 25.
In the technique scheme, described riser reaction zone 20 outlets are provided with slightly revolves 23, slightly revolves 23 gaseous phase outlets and links to each other with the entrance of gas-solid cyclone separator 24; Described gas-solid distribution zone 7 is provided with methanol feedstock feeding line 8; Described fast fluidized bed reaction zone 2 tops enter behind riser tube 3 slightly revolves 4; Described regenerator sloped tube 13 links to each other with the bottom of down-flow fluidized bed using ECT reaction zone 9; Describedly slightly revolve the close phase section that gaseous stream that gaseous phase outlet pipeline 5 goes out enters settling vessel 21 through described; Described gas-solid distribution zone 7 is positioned at described down-flow fluidized bed using ECT reaction zone 9 tops, and gaseous stream and catalyzer enter down-flow fluidized bed using ECT reaction zone 9 with raw material after gas-solid distribution zone 7 is mixed.
Among the present invention, 2 chargings of fast fluidized bed reaction zone are mainly methyl alcohol, and riser reaction zone 20 chargings are mainly the above hydrocarbon of C4, and the above hydrocarbon of C4 is from the above hydrocarbon by product of the isolated C4 of centrifugal station, and the C 4 olefin mass content is greater than 75% in the above hydrocarbon stream of C4; Described catalyzer is SAPO-34; Described riser reaction zone 20 reaction conditionss are: temperature of reaction is 500～600 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 4～12 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditionss are: temperature of reaction is 380～460 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 5～10 meter per seconds; Fast bed reaction zone 2 reaction conditionss are: temperature of reaction is 425～500 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 1～3 meter per second; The average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%; The catalyzer of described gas-solid distribution zone 7 is divided into two portions at least, and 20～75% enter down-flow fluidized bed using ECT reaction zone 9,25～80% enters revivifier 11 regeneration, forms regenerated catalyst; Described regenerated catalyst is divided into two portions at least, and 20～60% return down-flow fluidized bed using ECT reaction zone 9,40～80% enters riser reaction zone 20.
The method of calculation of average coke content of the present invention are that carbon deposit quality on the catalyzer is divided by described catalyst quality.Carbon deposit measuring method on the catalyzer is as follows: will mix comparatively uniform catalyst mix with carbon deposit, then the band C catalyst of weighing 0.1～1 gram, be put in the pyrocarbon analyser and burn, the carbonic acid gas quality that generates by infrared analysis burning, thus carbonaceous amount on the catalyzer obtained.
The preparation method of sial phosphorus molecular sieve of the present invention is: at first preparing the molecular sieve presoma, is 0.03～0.6R with the mole proportioning: (Si 0.01～0.98: Al 0.01～0.6: P 0.01～0.6): 2～500H
2O, wherein R represents template, and template is triethylamine, and the constitutive material mixed solution is obtaining after through 1～10 hour crystallization under 100-250 ℃ the temperature; Again, molecular sieve presoma, phosphorus source, silicon source, aluminium source, template, water etc. after at least 0.1 hour, are finally obtained the SAPO molecular sieve at 110～260 ℃ of lower hydrothermal crystallizings according to certain ratio mixing is rear.The molecular sieve of preparation is mixed with the binding agent of required ratio, and through obtaining final SAPO catalyzer after the operation stepss such as spraying drying, roasting, the weight percentage of binding agent in molecular sieve is between 10～90%.
Among the present invention, slightly revolve and refer to be positioned at the elementary cyclonic separator that riser tube or down-flow fluidized bed using ECT outlet can realize the gas-solid sharp separation, because its separation efficiency lower (generally between 70～90%), so those skilled in the art generally is simply referred to as " slightly revolving ".And down-flow fluidized bed using ECT refers to that solid particulate presents the tubular reactor of flow pattern from top to bottom under solid particulate self gravitation or airflow acting force.
Adopt device of the present invention, three reaction zones are set, it is low-carbon alkene that fast bed reaction zone 2 is mainly used in transforming methyl alcohol, down-flow fluidized bed using ECT reaction zone 9 main transform portion methyl alcohol are dme and low-carbon alkene, and being mainly used in transforming the above hydrocarbon of C4 that the methyl alcohol reaction generates in the riser reaction zone 20 is low-carbon alkene.Be high temperature, highly active regenerated catalyst in the riser reaction zone 20, can guarantee the above olefin conversion of higher C4, the high linear speed of riser tube can improve selectivity of light olefin again, and the reaction of C4 olefin cracking can be the pre-carbon distribution of regenerated catalyst again in the riser tube simultaneously.And fast bed reaction zone 2 forms carbon distribution at catalyzer after conversion methyl alcohol is low-carbon alkene, still has catalytic activity but this part contains the catalyzer of carbon distribution, and having the ability methanol conversion fully is dme, generates simultaneously low-carbon alkene.Owing to be the catalyzer of pre-carbon distribution in the down-flow fluidized bed using ECT reaction zone 9, has the higher advantage of selectivity, the down-flow fluidized bed using ECT Gas-particle Flows has been similar to the favourable raising of the advantage of plug flow selectivity of light olefin.Gaseous stream in the down-flow fluidized bed using ECT reaction zone 9 enters the 2 rear sustainable participation reactions of fast fluidized bed reaction zone, dme and the above hydrocarbon of part C4 can react the generation low-carbon alkene, and unreacted completely the above hydrocarbon of C4 after entering settling vessel 21 close phase sections, continue reaction for low-carbon alkene, final unreacted returns further generation low-carbon alkenes of riser reaction zone 20 after the above hydrocarbon of C4 is separated completely.Therefore, adopt device of the present invention, can reach the purpose that improves yield of light olefins.
Adopt technical scheme of the present invention: described riser reaction zone 20 outlets are provided with slightly revolves 23, slightly revolves 23 gaseous phase outlets and links to each other with the entrance of gas-solid cyclone separator 24; Described gas-solid distribution zone 7 is provided with methanol feedstock feeding line 8; Described fast fluidized bed reaction zone 2 tops enter behind riser tube 3 slightly revolves 4; Described regenerator sloped tube 13 links to each other with the bottom of down-flow fluidized bed using ECT reaction zone 9; Describedly slightly revolve the close phase section that gaseous stream that gaseous phase outlet pipeline 5 goes out enters settling vessel 21 through described; Described gas-solid distribution zone 7 is positioned at described down-flow fluidized bed using ECT reaction zone 9 tops, gaseous stream and catalyzer enter down-flow fluidized bed using ECT reaction zone 9 with raw material after gas-solid distribution zone 7 is mixed, the low-carbon alkene carbon base absorption rate reaches 88.94% (weight), exceed than the low-carbon alkene carbon base absorption rate of prior art and can reach more than 6 percentage points, obtained preferably technique effect.
Description of drawings
Fig. 1 is the schematic flow sheet of device of the present invention.
Among Fig. 1,1 is methanol feed line; 2 is the fast fluidized bed reaction zone; 3 is the undergauge riser tube; 4 for slightly revolving; 5 for slightly revolving the gaseous phase outlet pipeline; 6 is thick spin material leg; 7 are the gas-solid distribution zone; 8 is methanol feed line; 9 is the down-flow fluidized bed using ECT reaction zone; 10 is inclined tube to be generated; 11 is revivifier; 12 is the regenerating medium feeding line; 13 is regenerator sloped tube; 14 is the revivifier negative area; 15 is the revivifier gas-solid cyclone separator; 16 is exhanst gas outlet; 17 is regenerator sloped tube; 18 is the above hydrocarbon feeding line of C4; 19 is the raising section; 20 is riser reaction zone; 21 is settling vessel; 22 is the settling vessel expanding reach; 23 slightly revolve for riser reaction zone outlet; 24 is gas-solid cyclone separator in the settling vessel; 25 is its outlet of product; 26 is regeneration standpipe; 27 stripping medium feeding lines.
The raw material that is mainly methyl alcohol enters fast fluidized bed reaction zone 2, contact with the catalyzer that comprises the sial phosphorus molecular sieve, the gaseous stream that generates and catalyzer enter and slightly revolve 4, gaseous stream enters the close phase section 21 of settling vessel through slightly revolving gaseous phase outlet 5, catalyzer enters gas-solid distribution zone 7 through thick spin material leg 6, the catalyzer of gas-solid distribution zone 7 is divided into two portions at least, a part enters down-flow fluidized bed using ECT reaction zone 9, contact with the raw material that comprises methyl alcohol, the gaseous stream and the catalyzer that generate enter fast bed reaction zone 2, a part enters revivifier 11 regeneration, form regenerated catalyst, described regenerated catalyst is divided into two portions at least, a part is returned down-flow fluidized bed using ECT reaction 9, a part enters riser reaction zone 20, contact with the above hydrocarbon of C4, the gaseous stream and the catalyzer that generate enter described settling vessel 22, enter centrifugal station through the gaseous stream after the gas solid separation, separate and obtain low-carbon alkene product and the above hydrocarbon by product of described C4, the above hydrocarbon by product of C4 enters riser reaction zone 20, and the settling vessel 22 interior catalyzer that go out through gas solid separation enter revivifier 11 regeneration behind stripping.
The invention will be further elaborated below by embodiment, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
On reaction unit as shown in Figure 1, methanol feedstock enters fast fluidized bed reaction zone 2, contact with the SAPO-34 catalyzer, the gaseous stream that generates and catalyzer enter and slightly revolve 4, gaseous stream enters settling vessel 21 close phase sections through slightly revolving gaseous phase outlet 5, catalyzer enters gas-solid distribution zone 7 through thick spin material leg 6, the catalyzer of gas-solid distribution zone 7 is divided into two portions at least, 20% enters down-flow fluidized bed using ECT reaction zone 9, contact with methanol feedstock, the gaseous stream that generates and catalyzer enter fast bed reaction zone 2,80% and enter revivifier 11 regeneration, form regenerated catalyst.Described regenerated catalyst is divided into two portions at least, 20% returns down-flow fluidized bed using ECT reaction zone 9,80% enters riser reaction zone 20, contact with the above hydrocarbon of C4, the gaseous stream and the catalyzer that generate enter described settling vessel 21, enter centrifugal station through the gaseous stream after the gas solid separation, separate obtaining low-carbon alkene product and the above hydrocarbon by product of described C4, the above hydrocarbon by product of C4 enters riser reaction zone 20, and the settling vessel 21 interior catalyzer that go out through gas solid separation enter revivifier 11 regeneration behind stripping.Described riser reaction zone 20 outlets are provided with slightly revolves 23, slightly revolves 23 gaseous phase outlets and links to each other with the entrance of gas-solid cyclone separator 24, and fast fluidized bed reaction zone 2 tops enter behind riser tube 3 slightly revolves 4, and regenerator sloped tube 13 links to each other with the bottom of down-flow fluidized bed using ECT reaction zone 9.The C 4 olefin mass content is 88% in the above hydrocarbon stream of C4, and riser reaction zone 20 reaction conditionss are: temperature of reaction is 500 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 4 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditionss are: temperature of reaction is 380 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 5 meter per seconds; Fast bed reaction zone 2 reaction conditionss are: temperature of reaction is 425 ℃, reaction pressure is counted 0.01MPa with gauge pressure, the gas phase linear speed is 1 meter per second, the average carbon deposition quantity massfraction of regenerated catalyst is 0.01%, described gas-solid distribution zone 7 is positioned at described down-flow fluidized bed using ECT reaction zone 9 tops, and gaseous stream and catalyzer enter down-flow fluidized bed using ECT reaction zone 9 with methanol feedstock after gas-solid distribution zone 7 is mixed.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 84.15% (weight).
[embodiment 2]
According to embodiment 1 described condition and step, the catalyzer of gas-solid distribution zone 7 is divided into two portions at least, 75% enters down-flow fluidized bed using ECT reaction zone 9,25% enters revivifier 11 regeneration, form regenerated catalyst, described regenerated catalyst is divided into two portions at least, 60% returns down-flow fluidized bed using ECT reaction zone 9,40% enters riser reaction zone 20, the C 4 olefin mass content is 75% in the above hydrocarbon stream of C4, riser reaction zone 20 reaction conditionss are: temperature of reaction is 600 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 12 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditionss are: temperature of reaction is 460 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 10 meter per seconds; Fast bed reaction zone 2 reaction conditionss are: temperature of reaction is 500 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 3 meter per seconds, and the average carbon deposition quantity massfraction of regenerated catalyst is 0.5%.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 85.39% (weight).
[embodiment 3]
According to embodiment 1 described condition and step, the catalyzer of gas-solid distribution zone 7 is divided into two portions at least, 50% enters down-flow fluidized bed using ECT reaction zone 9,50% enters revivifier 11 regeneration, form regenerated catalyst, described regenerated catalyst is divided into two portions at least, 50% returns down-flow fluidized bed using ECT reaction zone 9,50% enters riser reaction zone 20, the C 4 olefin mass content is 92% in the above hydrocarbon stream of C4, riser reaction zone 20 reaction conditionss are: temperature of reaction is 560 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 7 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditionss are: temperature of reaction is 440 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 6.6 meter per seconds; Fast bed reaction zone 2 reaction conditionss are: temperature of reaction is 450 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 1.5 meter per seconds, and the average carbon deposition quantity massfraction of regenerated catalyst is 0.15%.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 88.94% (weight).
[embodiment 4]
According to embodiment 3 described condition and steps, riser reaction zone 20 reaction conditionss are: temperature of reaction is 550 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and the gas phase linear speed is 5 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditionss are: temperature of reaction is 434 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and the gas phase linear speed is 4.5 meter per seconds; Fast bed reaction zone 2 reaction conditionss are: temperature of reaction is 438 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and the gas phase linear speed is 1.2 meter per seconds, and the average carbon deposition quantity massfraction of regenerated catalyst is 0.1%.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 87.01% (weight).
[comparative example 1]
According to embodiment 3 described condition and steps, just riser reaction zone 20 is not set, fast bed reaction zone 2, down-flow fluidized bed using ECT reaction zone 9, settling vessel 21 only are set, yield of light olefins is 83.17% (weight).
[comparative example 2]
According to embodiment 3 described condition and steps, down-flow fluidized bed using ECT reaction 9 just is not set, the gaseous stream of fast bed reaction zone 2 directly enters settling section 21 close mutually sections with catalyzer, and yield of light olefins is 86.28% (weight).
[comparative example 3]
According to embodiment 3 described condition and steps, down-flow fluidized bed using ECT reaction zone 9 and riser reaction zone 20 just are not set, after the catalyzer of fast bed reaction zone 2 and gaseous stream enter settling vessel 21, gas gas-phase objects diffluence centrifugal station, catalyzer returns revivifier, and yield of light olefins is 82.34% (weight).
Obviously, adopt device of the present invention, can reach the purpose that improves yield of light olefins, have larger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (7)
1. the reaction unit of a preparing light olefins from methanol, mainly comprise fast fluidized bed reaction zone (2), slightly revolve (4), settling vessel (21), gas-solid distribution zone (7), down-flow fluidized bed using ECT reaction zone (9), revivifier (11), riser reaction zone (20), riser reaction zone (20) outlet links to each other with settling vessel (21), settling vessel (21) bottom is provided with catalyst outlet and links to each other with revivifier (11) by regeneration standpipe (26), revivifier (11) has two catalyst outlets, one is passed through regenerator sloped tube (17) and links to each other with riser reaction zone (20), one is passed through regenerator sloped tube (13) and links to each other with down-flow fluidized bed using ECT reaction zone (9), the outlet of down-flow fluidized bed using ECT reaction zone (9) links to each other with fast fluidized bed reaction zone (2), the outlet of fast fluidized bed reaction zone (2) with slightly revolve (4) and link to each other, slightly revolving gaseous phase outlet pipeline (5) links to each other with settling vessel (21), thick spin material leg (6) links to each other with gas-solid distribution zone (7), gas-solid distribution zone (7) bottom links to each other with down-flow fluidized bed using ECT reaction zone (9), gas-solid distribution zone (7) has catalyst outlet and links to each other with revivifier (11) by inclined tube to be generated (10), and settling vessel (21) top has product gas outlet (25).
2. the reaction unit of described preparing light olefins from methanol according to claim 1, it is characterized in that described riser reaction zone (20) outlet is provided with slightly revolves (23), slightly revolves (23) gaseous phase outlet and links to each other with the entrance of gas-solid cyclone separator (24).
3. the reaction unit of described preparing light olefins from methanol according to claim 1 is characterized in that described gas-solid distribution zone (7) is provided with methanol feedstock feeding line (8).
4. the reaction unit of described preparing light olefins from methanol according to claim 1, it is characterized in that described fast fluidized bed reaction zone (2) top enters slightly behind riser tube (3) revolves (4).
5. the reaction unit of described preparing light olefins from methanol according to claim 1 is characterized in that described regenerator sloped tube (13) links to each other with the bottom of down-flow fluidized bed using ECT reaction zone (9).
6. the reaction unit of described preparing light olefins from methanol according to claim 1 is characterized in that describedly slightly revolving the close phase section that gaseous stream that gaseous phase outlet pipeline (5) goes out enters settling vessel (21) through described.
7. the reaction unit of described preparing light olefins from methanol according to claim 1, it is characterized in that described gas-solid distribution zone (7) is positioned at described down-flow fluidized bed using ECT reaction zone (9) top, gaseous stream and catalyzer enter down-flow fluidized bed using ECT reaction zone (9) with raw material after gas-solid distribution zone (7) is mixed.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2015081489A1 (en) | 2013-12-03 | 2015-06-11 | 中国科学院大连化学物理研究所 | Method for preparing a light olefin using an oxygen-containing compound |
| WO2015081484A1 (en) | 2013-12-03 | 2015-06-11 | 中国科学院大连化学物理研究所 | Method for preparing a light olefin using an oxygen-containing compound, and device for use thereof |
| WO2015081494A1 (en) | 2013-12-03 | 2015-06-11 | 中国科学院大连化学物理研究所 | Reaction device for preparing light olefins from methanol and/or dimethyl ether |
| CN105218288B (en) * | 2014-07-03 | 2017-05-17 | 中国石油化工股份有限公司 | High-efficiency rapid gas-solid separation and settlement method for methanol-to-olefin |
| CN106914191A (en) * | 2017-03-25 | 2017-07-04 | 青岛京润石化设计研究院有限公司 | The hydrocarbons fluidised-bed reaction method of methyl alcohol system |
| 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 |
| CN110540861A (en) * | 2018-05-28 | 2019-12-06 | 中国石油化工股份有限公司 | Catalytic cracking process and system |
| WO2022077458A1 (en) * | 2020-10-16 | 2022-04-21 | 中国科学院大连化学物理研究所 | Coke-control reactor, device for preparing low-carbon olefins from oxygen-containing compound and use thereof |
| RU2812664C1 (en) * | 2020-10-16 | 2024-01-31 | Далянь Инститьют Оф Кемикал Физикс, Чайниз Академи Оф Сайенсез | Reactor for control of coke content, as well as device and method for obtaining low-carbon olefins from oxygen-containing compound |
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| US9725375B2 (en) | 2013-12-03 | 2017-08-08 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Method for preparing a light olefin with an oxygen-containing compound |
| WO2015081484A1 (en) | 2013-12-03 | 2015-06-11 | 中国科学院大连化学物理研究所 | Method for preparing a light olefin using an oxygen-containing compound, and device for use thereof |
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| WO2015081489A1 (en) | 2013-12-03 | 2015-06-11 | 中国科学院大连化学物理研究所 | Method for preparing a light olefin using an oxygen-containing compound |
| US9827544B2 (en) | 2013-12-03 | 2017-11-28 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Reaction device for preparing light olefins from methanol and/or dimethyl ether |
| CN105218288B (en) * | 2014-07-03 | 2017-05-17 | 中国石油化工股份有限公司 | High-efficiency rapid gas-solid separation and settlement method for methanol-to-olefin |
| CN106914191A (en) * | 2017-03-25 | 2017-07-04 | 青岛京润石化设计研究院有限公司 | The hydrocarbons fluidised-bed reaction method of methyl alcohol system |
| CN110540861A (en) * | 2018-05-28 | 2019-12-06 | 中国石油化工股份有限公司 | Catalytic cracking process and system |
| CN110540861B (en) * | 2018-05-28 | 2021-11-16 | 中国石油化工股份有限公司 | Catalytic cracking process and system |
| 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 |
| WO2022077458A1 (en) * | 2020-10-16 | 2022-04-21 | 中国科学院大连化学物理研究所 | Coke-control reactor, device for preparing low-carbon olefins from oxygen-containing compound and use thereof |
| RU2812664C1 (en) * | 2020-10-16 | 2024-01-31 | Далянь Инститьют Оф Кемикал Физикс, Чайниз Академи Оф Сайенсез | Reactor for control of coke content, as well as device and method for obtaining low-carbon olefins from oxygen-containing compound |
| JP7449414B2 (en) | 2020-10-16 | 2024-03-13 | 中国科学院大▲連▼化学物理研究所 | Coke control reactor, equipment and applications for producing light olefins from oxygenated compounds |
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