CN102875296B - Reaction unit for preparing low-carbon olefins - Google Patents
Reaction unit for preparing low-carbon olefins Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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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, i.e. ethene and propylene, be two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are produced by petroleum path, but due to the limited supply of petroleum resources and higher price, produce ethene by petroleum resources, the cost of propylene constantly increases.In recent years, people start to greatly develop the technology that alternative materials transforms ethene processed, propylene.Wherein, one class important for low-carbon alkene produce alternative materials be 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, and as methyl alcohol, can be obtained by coal or Sweet natural gas, technique is very ripe, can realize the industrial scale of up to a million tonnes.Due to the popularity in oxygenatedchemicals source, add the economy transforming and generate 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).
Be applied to preparing olefin by conversion of methanol technique to silicoaluminophosphamolecular molecular sieve catalyst in US4499327 patent to study 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, methanol conversion can be made to be less than the degree of 10 seconds in reaction times of low-carbon alkene, more even reach in the reaction time range of riser tube.
Technology and reactor that a kind of methanol conversion is low-carbon alkene is disclosed in US 6166282, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas speed has reacted, after rising to the fast subregion that internal diameter diminishes rapidly, special gas-solid separation equipment initial gross separation is adopted 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, needed for this fast fluidized bed reactor internal diameter and catalyzer, reserve all greatly reduces.But in the method, low-carbon alkene carbon base absorption rate is generally all about 77%, there is the problem that yield of light olefins is lower.
The multiple riser reaction unit disclosed in CN 1723262 with central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises multiple riser reactor, 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 generally all between 75 ~ 80%, there is the problem that yield of light olefins is lower equally.
All there is the lower problem of yield of light olefins in prior art, the present invention solves this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the problem that the yield of light olefins that exists in prior art is lower, provides a kind of reaction unit of new preparing light olefins from methanol.This device is used for, in the production of low-carbon alkene, having the advantage that yield of light olefins is higher.
For solving the 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 exports and is connected with settling vessel 21, be provided with catalyst outlet bottom settling vessel 21 to be connected with revivifier 11 by regeneration standpipe 26, revivifier 11 has two catalyst outlets, one is connected with riser reaction zone 20 by regenerator sloped tube 17, one is connected with down-flow fluidized bed using ECT reaction zone 9 by regenerator sloped tube 13, the outlet of down-flow fluidized bed using ECT reaction zone 9 is connected with fast fluidized bed reaction zone 2, the outlet of fast fluidized bed reaction zone 2 with slightly revolve 4 and be connected, slightly revolve gaseous phase outlet pipeline 5 to be connected with settling vessel 21, thick spin material leg 6 is connected with gas-solid distribution zone 7, be connected with down-flow fluidized bed using ECT reaction zone 9 bottom gas-solid distribution zone 7, gas-solid distribution zone 7 is had catalyst outlet and is connected with revivifier 11 by inclined tube 10 to be generated, settling vessel 21 top has product gas outlet 25.
In technique scheme, the outlet of described riser reaction zone 20 is provided with slightly revolves 23, slightly revolves 23 gaseous phase outlets and is connected with the entrance of gas-solid cyclone separator 24; Described gas-solid distribution zone 7 is provided with methanol feedstock feeding line 8; Top, described fast fluidized bed reaction zone 2 enters after riser tube 3 slightly revolves 4; Described regenerator sloped tube 13 is connected with the bottom of down-flow fluidized bed using ECT reaction zone 9; Describedly slightly revolve through described the close phase section that gaseous stream that gaseous phase outlet pipeline 5 goes out enters settling vessel 21; Described gas-solid distribution zone 7 is positioned at above described down-flow fluidized bed using ECT reaction zone 9, and gaseous stream and catalyzer enter down-flow fluidized bed using ECT reaction zone 9 with raw material after gas-solid distribution zone 7 mixes.
In the present invention, fast fluidized bed reaction zone 2 charging is mainly methyl alcohol, and riser reaction zone 20 charging is mainly more than C4 hydrocarbon, and more than C4 hydrocarbon is from centrifugal station isolated more than C4 hydrocarbon by product, and in more than C4 hydrocarbon stream, C 4 olefin mass content is greater than 75%; Described catalyzer is SAPO-34; Described riser reaction zone 20 reaction conditions is: temperature of reaction is 500 ~ 600 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 4 ~ 12 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditions is: temperature of reaction is 380 ~ 460 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 5 ~ 10 meter per seconds; Fast bed reaction zone 2 reaction conditions is: temperature of reaction is 425 ~ 500 DEG C, and reaction pressure counts 0.01 ~ 0.3MPa with gauge pressure, and gas phase linear speed is 1 ~ 3 meter per second; Described regenerated catalyst average product carbon amounts massfraction is 0.01 ~ 0.5%; The catalyzer of described gas-solid distribution zone 7 is at least divided into two portions, and 20 ~ 75% enter down-flow fluidized bed using ECT reaction zone 9,25 ~ 80% enters revivifier 11 and regenerate, and forms regenerated catalyst; Described regenerated catalyst is at least divided into two portions, and 20 ~ 60% return to 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 catalyzer is divided by described catalyst quality.Carbon deposit measuring method on catalyzer is as follows: by the comparatively uniform catalyst mix with carbon deposit of mixing, then the band C catalyst of 0.1 ~ 1 gram is weighed, be put in pyrocarbon analyser and burn, by the carbonic acid gas quality that infrared analysis burning generates, thus obtain the carbonaceous amount on catalyzer.
The preparation method of sial phosphorus molecular sieve of the present invention is: first prepare molecular sieve precursor, is 0.03 ~ 0.6R by mol ratio: (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, constitutive material mixed solution, obtains at the temperature of 100-250 DEG C after the crystallization of 1 ~ 10 hour; Again, after molecular sieve precursor, phosphorus source, silicon source, aluminium source, template, water etc. being mixed according to certain ratio, at 110 ~ 260 DEG C, hydrothermal crystallizing, after at least 0.1 hour, finally obtains SAPO molecular sieve.Mixed with the binding agent of required ratio by the molecular sieve of preparation, after the operation steps such as spraying dry, roasting, 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 riser tube or down-flow fluidized bed using ECT outlet can realize the primary cyclone of gas-solid sharp separation, due to its separation efficiency lower (generally between 70 ~ 90%), therefore 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 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 converting methanol, the main transform portion methyl alcohol in down-flow fluidized bed using ECT reaction zone 9 is dme and low-carbon alkene, and more than the C4 hydrocarbon being mainly used in converting methanol reaction generation in riser reaction zone 20 is low-carbon alkene.Be high temperature, highly active regenerated catalyst in riser reaction zone 20, higher more than C4 olefin conversion can be ensured, the high linear speed of riser tube can improve selectivity of light olefin again, and in riser tube, the reaction of C4 olefin cracking can be again the pre-carbon distribution of regenerated catalyst simultaneously.And fast bed reaction zone 2 is after converting methanol is low-carbon alkene, form carbon distribution on a catalyst, but the catalyzer that this part contains carbon distribution still has catalytic activity, having the ability methanol conversion is completely dme, generates low-carbon alkene simultaneously.Owing to being the catalyzer of pre-carbon distribution in down-flow fluidized bed using ECT reaction zone 9, there is the advantage that selectivity is higher, down-flow fluidized bed using ECT Gas-particle Flows be similar to the advantage of plug flow favourable improve selectivity of light olefin.Gaseous stream in down-flow fluidized bed using ECT reaction zone 9 continues to participate in reaction after entering fast fluidized bed reaction zone 2, dme and the above hydrocarbon of part C4 can react generation low-carbon alkene, and unreacted completely more than C4 hydrocarbon after entering the close phase section of settling vessel 21, continue reaction for low-carbon alkene, final unreacted completely more than C4 hydrocarbon returns to riser reaction zone 20 and generates low-carbon alkene further after separating.Therefore, adopt device of the present invention, the object improving yield of light olefins can be reached.
Adopt technical scheme of the present invention: the outlet of described riser reaction zone 20 is provided with slightly revolves 23, slightly revolves 23 gaseous phase outlets and is connected with the entrance of gas-solid cyclone separator 24; Described gas-solid distribution zone 7 is provided with methanol feedstock feeding line 8; Top, described fast fluidized bed reaction zone 2 enters after riser tube 3 slightly revolves 4; Described regenerator sloped tube 13 is connected with the bottom of down-flow fluidized bed using ECT reaction zone 9; Describedly slightly revolve through described the close phase section that gaseous stream that gaseous phase outlet pipeline 5 goes out enters settling vessel 21; Described gas-solid distribution zone 7 is positioned at above described down-flow fluidized bed using ECT reaction zone 9, gaseous stream and catalyzer enter down-flow fluidized bed using ECT reaction zone 9 with raw material after gas-solid distribution zone 7 mixes, 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, achieve 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 fluidized bed reaction zone; 3 is undergauge riser tube; 4 for slightly to revolve; 5 for slightly to revolve gaseous phase outlet pipeline; 6 is thick spin material leg; 7 is gas-solid distribution zone; 8 is methanol feed line; 9 is down-flow fluidized bed using ECT reaction zone; 10 is inclined tube to be generated; 11 is revivifier; 12 is regenerating medium feeding line; 13 is regenerator sloped tube; 14 is revivifier negative area; 15 is revivifier gas-solid cyclone separator; 16 is exhanst gas outlet; 17 is regenerator sloped tube; 18 is more than C4 hydrocarbon feeding line; 19 is raising section; 20 is riser reaction zone; 21 is settling vessel; 22 is settling vessel expanding reach; 23 slightly revolve for riser reaction zone exports; 24 is gas-solid cyclone separator in settling vessel; 25 is its outlet of product; 26 is regeneration standpipe; 27 stripping fluid feeding lines.
The raw material being mainly methyl alcohol enters fast fluidized bed reaction zone 2, with the catalyst exposure comprising sial phosphorus molecular sieve, the gaseous stream generated 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 at least divided into two portions, a part enters down-flow fluidized bed using ECT reaction zone 9, with the contact raw comprising methyl alcohol, the gaseous stream generated and catalyzer enter fast bed reaction zone 2, a part enters revivifier 11 and regenerates, form regenerated catalyst, described regenerated catalyst is at least divided into two portions, a part returns down-flow fluidized bed using ECT reaction 9, a part enters riser reaction zone 20, contact with more than C4 hydrocarbon, the gaseous stream generated and catalyzer enter described settling vessel 22, gaseous stream after gas solid separation enters centrifugal station, separation obtains low-carbon alkene product and described more than C4 hydrocarbon by product, more than C4 hydrocarbon by product enters riser reaction zone 20, the catalyzer gone out through gas solid separation in settling vessel 22 enters revivifier 11 and regenerates after stripping.
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, methanol feedstock enters fast fluidized bed reaction zone 2, with SAPO-34 catalyst exposure, the gaseous stream generated and catalyzer enter and slightly revolve 4, gaseous stream enters the close phase section of settling vessel 21 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 at least divided into two portions, 20% enters down-flow fluidized bed using ECT reaction zone 9, contact with methanol feedstock, the gaseous stream generated and catalyzer enter fast bed reaction zone 2,80% and enter revivifier 11 and regenerate, and form regenerated catalyst.Described regenerated catalyst is at least divided into two portions, 20% returns to down-flow fluidized bed using ECT reaction zone 9,80% enters riser reaction zone 20, contact with more than C4 hydrocarbon, the gaseous stream generated and catalyzer enter described settling vessel 21, and the gaseous stream after gas solid separation enters centrifugal station, are separated and obtain low-carbon alkene product and described more than C4 hydrocarbon by product, more than C4 hydrocarbon by product enters riser reaction zone 20, and the catalyzer gone out through gas solid separation in settling vessel 21 enters revivifier 11 and regenerates after stripping.The outlet of described riser reaction zone 20 is provided with slightly revolves 23, and slightly revolve 23 gaseous phase outlets and be connected with the entrance of gas-solid cyclone separator 24, top, fast fluidized bed reaction zone 2 enters after riser tube 3 slightly revolves 4, and regenerator sloped tube 13 is connected with the bottom of down-flow fluidized bed using ECT reaction zone 9.In more than C4 hydrocarbon stream, C 4 olefin mass content is 88%, and riser reaction zone 20 reaction conditions is: temperature of reaction is 500 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditions is: temperature of reaction is 380 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; Fast bed reaction zone 2 reaction conditions is: temperature of reaction is 425 DEG C, reaction pressure counts 0.01MPa with gauge pressure, gas phase linear speed is 1 meter per second, regenerated catalyst average product carbon amounts massfraction is 0.01%, described gas-solid distribution zone 7 is positioned at above described down-flow fluidized bed using ECT reaction zone 9, and gaseous stream and catalyzer enter down-flow fluidized bed using ECT reaction zone 9 with methanol feedstock after gas-solid distribution zone 7 mixes.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 84.15% (weight).
[embodiment 2]
According to the condition described in embodiment 1 and step, the catalyzer of gas-solid distribution zone 7 is at least divided into two portions, 75% enters down-flow fluidized bed using ECT reaction zone 9,25% enters revivifier 11 regenerates, form regenerated catalyst, described regenerated catalyst is at least divided into two portions, 60% returns to down-flow fluidized bed using ECT reaction zone 9,40% enters riser reaction zone 20, in more than C4 hydrocarbon stream, C 4 olefin mass content is 75%, riser reaction zone 20 reaction conditions is: temperature of reaction is 600 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 12 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditions is: temperature of reaction is 460 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; Fast bed reaction zone 2 reaction conditions is: temperature of reaction is 500 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 3 meter per seconds, and regenerated catalyst average product carbon amounts massfraction is 0.5%.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 85.39% (weight).
[embodiment 3]
According to the condition described in embodiment 1 and step, the catalyzer of gas-solid distribution zone 7 is at least divided into two portions, 50% enters down-flow fluidized bed using ECT reaction zone 9,50% enters revivifier 11 regenerates, form regenerated catalyst, described regenerated catalyst is at least divided into two portions, 50% returns to down-flow fluidized bed using ECT reaction zone 9,50% enters riser reaction zone 20, in more than C4 hydrocarbon stream, C 4 olefin mass content is 92%, riser reaction zone 20 reaction conditions is: temperature of reaction is 560 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 7 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditions is: temperature of reaction is 440 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 6.6 meter per seconds; Fast bed reaction zone 2 reaction conditions is: temperature of reaction is 450 DEG C, and reaction pressure counts 0.01MPa with gauge pressure, and gas phase linear speed is 1.5 meter per seconds, and regenerated catalyst average product carbon amounts massfraction is 0.15%.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 88.94% (weight).
[embodiment 4]
According to the condition described in embodiment 3 and step, riser reaction zone 20 reaction conditions is: temperature of reaction is 550 DEG C, and reaction pressure counts 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; Down-flow fluidized bed using ECT reaction zone 9 reaction conditions is: temperature of reaction is 434 DEG C, and reaction pressure counts 0.3MPa with gauge pressure, and gas phase linear speed is 4.5 meter per seconds; Fast bed reaction zone 2 reaction conditions is: temperature of reaction is 438 DEG C, and reaction pressure counts 0.3MPa with gauge pressure, and gas phase linear speed is 1.2 meter per seconds, and regenerated catalyst average product carbon amounts massfraction is 0.1%.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 87.01% (weight).
[comparative example 1]
According to the condition described in embodiment 3 and step, just do not arrange riser reaction zone 20, only arrange fast bed reaction zone 2, down-flow fluidized bed using ECT reaction zone 9, settling vessel 21, yield of light olefins is 83.17% (weight).
[comparative example 2]
According to the condition described in embodiment 3 and step, just do not arrange down-flow fluidized bed using ECT reaction 9, the gaseous stream of fast bed reaction zone 2 and catalyzer directly enter the close phase section of settling section 21, and yield of light olefins is 86.28% (weight).
[comparative example 3]
According to the condition described in embodiment 3 and step, just down-flow fluidized bed using ECT reaction zone 9 and riser reaction zone 20 are not set, after the catalyzer of fast bed reaction zone 2 and gas gas-phase objects flow to 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, the object improving yield of light olefins can be reached, there is 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), first slightly revolves (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 is connected with settling vessel (21), settling vessel (21) bottom is provided with catalyst outlet and is connected with revivifier (11) by regeneration standpipe (26), revivifier (11) has two catalyst outlets, one is connected with riser reaction zone (20) by regenerator sloped tube (17), one is connected with down-flow fluidized bed using ECT reaction zone (9) by regenerator sloped tube (13), the outlet of down-flow fluidized bed using ECT reaction zone (9) is connected with fast fluidized bed reaction zone (2), the outlet of fast fluidized bed reaction zone (2) is slightly revolved (4) and is connected with first, slightly revolve gaseous phase outlet pipeline (5) to be connected with settling vessel (21), thick spin material leg (6) is connected with gas-solid distribution zone (7), gas-solid distribution zone (7) bottom is connected with down-flow fluidized bed using ECT reaction zone (9), gas-solid distribution zone (7) is had catalyst outlet and is connected with revivifier (11) by inclined tube to be generated (10), settling vessel (21) top has product gas outlet (25), wherein said low-carbon alkene is ethene and propylene, describedly slightly revolve for being positioned at riser tube or down-flow fluidized bed using ECT outlet realizes the primary cyclone of gas-solid sharp separation, separation efficiency is between 70 ~ 90%.
2. the reaction unit of preparing light olefins from methanol according to claim 1, it is characterized in that described riser reaction zone (20) outlet is provided with second and slightly revolves (23), second slightly revolves (23) gaseous phase outlet is connected with the entrance of gas-solid cyclone separator (24).
3. the reaction unit of 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 preparing light olefins from methanol according to claim 1, is characterized in that described fast fluidized bed reaction zone (2) top enters first and slightly revolves (4) after riser tube (3).
5. the reaction unit of preparing light olefins from methanol according to claim 1, is characterized in that described regenerator sloped tube (13) is connected with the bottom of down-flow fluidized bed using ECT reaction zone (9).
6. the reaction unit of preparing light olefins from methanol according to claim 1, is characterized in that describedly slightly revolving through described the close phase section that gaseous stream that gaseous phase outlet pipeline (5) goes out enters settling vessel (21).
7. the reaction unit of 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) mixes.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9718743B2 (en) | 2013-12-03 | 2017-08-01 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Method for preparing a light olefin using an oxygen-containing compound, and device for use thereof |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| RU2636077C1 (en) | 2013-12-03 | 2017-11-20 | Далянь Инститьют Оф Кемикал Физикс, Чайниз Академи Оф Сайенсез | Reactive device for obtaining light olefins from methanol and/or dimethyl ether |
| SG11201604429VA (en) | 2013-12-03 | 2016-07-28 | Dalian Chemical Physics Inst | Method for preparing a light olefin using an oxygen-containing compound |
| 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 |
| 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 |
| 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 |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
| CN101164687A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Multi-reaction-area combination type reactor |
| CN101279877A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for increasing yield of ethylene and propone in conversion process of oxocompound |
| CN101348404A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Method for improving ethylene and propene yield in methyl alcohol or dimethyl ether conversion process |
-
2011
- 2011-07-12 CN CN201110193431.0A patent/CN102875296B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
| CN101164687A (en) * | 2006-10-20 | 2008-04-23 | 中国石油化工股份有限公司 | Multi-reaction-area combination type reactor |
| CN101279877A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for increasing yield of ethylene and propone in conversion process of oxocompound |
| CN101348404A (en) * | 2007-07-18 | 2009-01-21 | 中国石油化工股份有限公司 | Method for improving ethylene and propene yield in methyl alcohol or dimethyl ether conversion process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9718743B2 (en) | 2013-12-03 | 2017-08-01 | Dalian Institute Of Chemical Physics, Chinese Academy Of Sciences | Method for preparing a light olefin using an oxygen-containing compound, and device for use thereof |
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