CN102875281A - Method for catalytically converting methanol to low-carbon olefins - Google Patents
Method for catalytically converting methanol to low-carbon olefins Download PDFInfo
- Publication number
- CN102875281A CN102875281A CN2011101934490A CN201110193449A CN102875281A CN 102875281 A CN102875281 A CN 102875281A CN 2011101934490 A CN2011101934490 A CN 2011101934490A CN 201110193449 A CN201110193449 A CN 201110193449A CN 102875281 A CN102875281 A CN 102875281A
- Authority
- CN
- China
- Prior art keywords
- low
- gas
- carbon
- reaction zone
- reaction
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
Abstract
The invention relates to a method for catalytically converting methanol to low-carbon olefins, mainly solving the problem of low yield of low-carbon olefins in the prior art. The method disclosed herein comprises the following steps: (a) letting a raw material mainly comprising methanol enter into a downer reaction zone, contact the raw material with a catalyst, letting the generated gas-phase flow and the catalyst enter into a rough-cut cyclone, letting the gas-phase flow enter into a separation section through a gas-phase outlet of a cyclone separator, separating to obtain low-carbon olefins and a C4 or higher hydrocarbon flow, wherein the gas-phase outlet of the rough-cut cyclone is connected with the inlet of the cyclone separator in a disengager; (b) letting the catalyst separated by the rough-cut cyclone and the cyclone separator enter into a regenerator through a regeneration standpipe, letting a regeneration catalyst enter into a riser reaction zone through a regeneration inclined pipe to contact with the C4 or higher hydrocarbon flow, and letting the generated gas-phase flow and the catalyst enter into a gas-solid distribution zone. The method 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 the method that a kind of methanol oxidation is converted into low-carbon alkene.
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, provides a kind of new methanol oxidation to be converted into the method for low-carbon alkene.The method is used for the production of low-carbon alkene, has the higher advantage of yield of light olefins.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of methanol oxidation is converted into the method for low-carbon alkene, may further comprise the steps: enter the down-flow fluidized bed using ECT reaction zone after the raw material that (a) is mainly methyl alcohol enters the gas-solid distribution zone, contact with the catalyzer that comprises the sial phosphorus molecular sieve, generation comprises low-carbon alkene, the gaseous stream of C 4 olefin and catalyzer enter slightly and revolve, the cyclone inlet of slightly revolving in gaseous phase outlet and the settling vessel is joined, described gaseous stream enters centrifugal station from the cyclonic separator gaseous phase outlet, separates the carbon four above hydrocarbon streams that obtain the low-carbon alkene product and comprise C 4 olefin; (b) slightly revolve with the isolated catalyzer of cyclonic separator and enter revivifier by regeneration standpipe after through sedimentation, stripping, enter riser reaction zone through the catalyzer after the regeneration through regenerator sloped tube, contact with the described carbon four above hydrocarbon streams of C 4 olefin that comprise, the gaseous stream of generation and catalyzer enter the gas-solid distribution zone.
In the technique scheme, the C 4 olefin mass content is greater than 75% in the described carbon four above hydrocarbon streams that comprise C 4 olefin; Described sial phosphorus molecular sieve comprises SAPO-34; Described riser reaction zone reaction conditions is: 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 reaction conditions is: temperature of reaction is 430～530 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 5～10 meter per seconds; The average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%; Described revivifier and settling vessel coaxial arrangement, revivifier are positioned at the settling vessel below; Described gas-solid distribution zone is positioned at described down-flow fluidized bed using ECT reaction zone top, and the gaseous stream and the catalyzer that come from riser reaction zone enter the down-flow fluidized bed using ECT reaction zone with described methanol feedstock after the gas-solid distribution zone is mixed; At least one position that separates at described riser reaction zone axial direction due arranges opening for feed, and institute advances material and comprises methyl alcohol.
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.The gas-solid distribution zone generally is positioned at the descending-bed reactor inlet end, and gas, the solid mixing in this district enter down-flow fluidized bed using ECT by the descending-bed reactor inlet distributor, and its effect is to guarantee descending-bed reactor inlet end gas, the solid distribution all and, raising gas-solid contact efficient.
Adopt method of the present invention, two reaction zones are set, being mainly used in transforming the carbon four above hydrocarbon that the methyl alcohol reaction generates in the riser reaction zone is low-carbon alkene, and it is low-carbon alkene that the down-flow fluidized bed using ECT reaction zone mainly transforms methyl alcohol.Be high temperature, highly active regenerated catalyst in the riser reaction zone, can guarantee higher C 4 olefin transformation efficiency, the high linear speed of riser tube can improve selectivity of light olefin again, and the C 4 olefin scission reaction can be the pre-carbon distribution of regenerated catalyst again in the riser tube simultaneously.And be the catalyzer of pre-carbon distribution in the down-flow fluidized bed using ECT reaction zone, have the higher advantage of selectivity, the raising that the advantage of the approximate plug flow of down-flow fluidized bed using ECT Gas-particle Flows is favourable selectivity of light olefin.In addition, the down-flow fluidized bed using ECT outlet connects slightly revolves, and slightly revolve the entrance that gaseous phase outlet connects cyclonic separator, can guarantee separating as early as possible of gaseous stream and catalyzer, avoid in settling vessel overstand to cause the generation of some side reaction, at the riser reaction zone axial direction due at least one opening for feed is set simultaneously, institute advances material and comprises methyl alcohol, can play the effect that reduces gaseous stream dividing potential drop in the riser tube, thereby reach the purpose that improves selectivity of light olefin.Therefore, adopt method of the present invention, can reach the purpose that improves yield of light olefins.
Adopt technical scheme of the present invention: the C 4 olefin mass content is greater than 75% in the described carbon four above hydrocarbon streams that comprise C 4 olefin; Described sial phosphorus molecular sieve comprises SAPO-34; Described riser reaction zone reaction conditions is: 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 reaction conditions is: temperature of reaction is 430～530 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 5～10 meter per seconds; The average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%; Described revivifier and settling vessel coaxial arrangement, revivifier are positioned at the settling vessel below; Described gas-solid distribution zone is positioned at described down-flow fluidized bed using ECT reaction zone top, and the gaseous stream and the catalyzer that come from riser reaction zone enter the down-flow fluidized bed using ECT reaction zone with described methanol feedstock after the gas-solid distribution zone is mixed; At least one position that separates at described riser reaction zone axial direction due arranges opening for feed, institute advances material and comprises methyl alcohol, the low-carbon alkene carbon base absorption rate reaches 87.91% (weight), exceed than the low-carbon alkene carbon base absorption rate of prior art and can reach more than 5 percentage points, obtained preferably technique effect.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
Among Fig. 1,1 is the regeneration air feed pipeline; 2 is plug valve under the regeneration standpipe; 3 is revivifier; 4 is stripper; 5 is the stripped vapor charging; 6 is regeneration standpipe; 7 is regenerator sloped tube; 8 is the riser tube charging; 9 is riser reaction zone axial direction due opening for feed; 10 is raising section, riser reaction zone bottom; 11 is riser reaction zone; 12 is the revivifier gas-solid cyclone separator; 13 is exhanst gas outlet; 14 is delivering vapor; 15 is product gas outlet; 16 is settling vessel; 17 for slightly revolving; 18 is the down-flow fluidized bed using ECT reaction zone; 19 are the gas-solid distribution zone; 20 is methanol feeding; 21 is cyclonic separator in the settling vessel.
The raw material that is mainly methyl alcohol enters down-flow fluidized bed using ECT reaction zone 18 after pipeline 20 enters gas-solid distribution zone 19, contact with the catalyzer that comprises the sial phosphorus molecular sieve, generation comprises low-carbon alkene, the gaseous stream of C 4 olefin and catalyzer enter and slightly revolve 17, cyclonic separator 21 entrances that slightly revolve in 17 gaseous phase outlets and the settling vessel 16 join, gaseous stream enters centrifugal station from cyclonic separator 21 gaseous phase outlets, separate the carbon four above hydrocarbon streams that obtain the low-carbon alkene product and comprise C 4 olefin, slightly revolve 17 and the isolated catalyzer of cyclonic separator 21 through sedimentations, enter revivifier 3 by regeneration standpipe 6 behind the stripping, enter riser reaction zone 11 through the catalyzer after the regeneration through regenerator sloped tube 7, contact with the described carbon four above hydrocarbon streams of C 4 olefin that comprise, the gaseous stream of generation and catalyzer enter gas-solid distribution zone 19.
The invention will be further elaborated below by embodiment, but be not limited only to present embodiment.
Embodiment
[embodiment 1]
On reaction unit as shown in Figure 1, pure methanol feedstock enters down-flow fluidized bed using ECT reaction zone 18 after pipeline 20 enters gas-solid distribution zone 19, contact with the SAPO-34 catalyzer, generation comprises low-carbon alkene, the gaseous stream of C 4 olefin and catalyzer enter and slightly revolve 17, cyclonic separator 21 entrances that slightly revolve in 17 gaseous phase outlets and the settling vessel 16 join, gaseous stream enters centrifugal station from cyclonic separator 21 gaseous phase outlets, separate the carbon four above hydrocarbon streams that obtain the low-carbon alkene product and comprise C 4 olefin, slightly revolve 17 and the isolated catalyzer of cyclonic separator 21 through sedimentations, enter revivifier 3 by regeneration standpipe 6 behind the stripping, enter riser reaction zone 11 through the catalyzer after the regeneration through regenerator sloped tube 7, contact with the described carbon four above hydrocarbon streams of C 4 olefin that comprise, the gaseous stream of generation and catalyzer enter gas-solid distribution zone 19.The massfraction of molecular sieve is 40% in the SAPO-34 catalyzer, riser tube 11 chargings are to comprise the carbon of C 4 olefin four above hydrocarbon streams, wherein carbon four hydrocarbon classical group become to see Table 1, the C 4 olefin mass content is 75.33%, riser reaction zone 11 reaction conditionss are: temperature of reaction is 500 ℃, 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 reacts 18 reaction conditionss: temperature of reaction is 430 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 5 meter per seconds.The average carbon deposition quantity massfraction of regenerated catalyst is 0.01%, revivifier 3 and settling vessel 16 coaxial arrangement, revivifier 2 is positioned at settling vessel 16 belows, gas-solid distribution zone 19 is positioned at down-flow fluidized bed using ECT reaction zone 18 tops, enters the down-flow fluidized bed using ECT reaction zone from gaseous stream and the catalyzer of riser reaction zone 11 with methanol feedstock after gas-solid distribution zone 19 is mixed.At riser reaction zone 11 axial direction dues an opening for feed is set, it is pure methyl alcohol that material advances in institute, and the methyl alcohol that described axial feed inlet enters and C 4 olefin mass ratio are 1: 2.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 83.68% (weight).
Table 1 carbon four hydrocarbon classical group become to distribute
| Component | Massfraction, % |
| Trimethylmethane | 10.25 |
| Normal butane | 14.42 |
| Anti-2-butylene | 16.75 |
| 1-butylene | 25.17 |
| Iso-butylene | 4.48 |
| Along 2-butylene | 27.05 |
| 1.3-divinyl | 1.88 |
[embodiment 2]
According to embodiment 1 described condition and step, purity is that 81% methanol feedstock (all the other are water) enters down-flow fluidized bed using ECT reaction zone 18 after pipeline 20 enters gas-solid distribution zone 19.Riser tube 11 chargings are to comprise the carbon of C 4 olefin four above hydrocarbon streams, and wherein the C 4 olefin mass content is 88%, and riser reaction zone 11 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 reacts 18 reaction conditionss: temperature of reaction is 530 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 10 meter per seconds.The average carbon deposition quantity massfraction of regenerated catalyst is 0.5%, at riser reaction zone 11 axial direction dues two opening for feeds are set, two opening for feeds lay respectively at apart from riser tube bottom 1/3/, 1/2 reaction zone At The Height, to advance material be that purity is 81% methyl alcohol, the methyl alcohol that described axial feed inlet enters and C 4 olefin mass ratio are 1: 1.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 85.71% (weight).
[embodiment 3]
According to embodiment 1 described condition and step, riser tube 11 chargings are to comprise the carbon of C 4 olefin four above hydrocarbon streams, wherein the C 4 olefin mass content is 88%, riser reaction zone 11 reaction conditionss are: temperature of reaction is 550 ℃, 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 reacts 18 reaction conditionss: temperature of reaction is 465 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 7 meter per seconds.The average carbon deposition quantity massfraction of regenerated catalyst is 0.12%, at riser reaction zone 11 axial direction dues three opening for feeds are set, three opening for feeds lay respectively at apart from riser tube bottom 1/3/, 1/2,2/3 reaction zone At The Height, and the methyl alcohol that described axial feed inlet enters and C 4 olefin mass ratio are 1: 1.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 87.91% (weight).
[embodiment 4]
According to embodiment 1 described condition and step, riser tube 11 chargings are to comprise the carbon of C 4 olefin four above hydrocarbon streams, wherein the C 4 olefin mass content is 92%, riser reaction zone 11 reaction conditionss are: temperature of reaction is 570 ℃, 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 reacts 18 reaction conditionss: temperature of reaction is 475 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and the gas phase linear speed is 6 meter per seconds.The average carbon deposition quantity massfraction of regenerated catalyst is 0.06%, at riser reaction zone 11 axial direction dues three opening for feeds are set, three opening for feeds lay respectively at apart from riser tube bottom 1/3/, 1/2,2/3 reaction zone At The Height, and the methyl alcohol that described axial feed inlet enters and C 4 olefin mass ratio are 1: 1.Reactor product adopts online gas chromatographic analysis, and the low-carbon alkene carbon base absorption rate is 85.29% (weight).
[comparative example 1]
According to embodiment 3 described condition and steps, just riser reaction zone 11 axial feed inlets are not set, all methanol feedstocks all enter down-flow fluidized bed using ECT reaction zone 18, and yield of light olefins is 86.98% (weight).
[comparative example 2]
According to embodiment 3 described condition and steps, just down-flow fluidized bed using ECT reaction 18 districts export and slightly revolve 17 gaseous phase outlet and cyclonic separator 21 and do not join, and yield of light olefins is 87.07% (weight).
[comparative example 3]
According to embodiment 3 described condition and steps, down-flow fluidized bed using ECT reaction zone 18 just is not set, methanol feedstock enters riser reaction zone 11 from pipeline 8, the carbon that the comprises C 4 olefin four above hydrocarbon streams that generate do not enter riser reaction zone 11, riser reaction zone 11 outlets are joined with settling vessel 16, and yield of light olefins is 82.87% (weight).
Obviously, adopt method 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 (8)
1. a methanol oxidation is converted into the method for low-carbon alkene, may further comprise the steps:
(a) after entering the gas-solid distribution zone, the raw material that is mainly methyl alcohol enters the down-flow fluidized bed using ECT reaction zone, contact with the catalyzer that comprises the sial phosphorus molecular sieve, generation comprises that the gaseous stream of low-carbon alkene, C 4 olefin and catalyzer enter slightly and revolves, the cyclone inlet of slightly revolving in gaseous phase outlet and the settling vessel is joined, described gaseous stream enters centrifugal station from the cyclonic separator gaseous phase outlet, separates the carbon four above hydrocarbon streams that obtain the low-carbon alkene product and comprise C 4 olefin;
(b) slightly revolve with the isolated catalyzer of cyclonic separator and enter revivifier by regeneration standpipe after through sedimentation, stripping, enter riser reaction zone through the catalyzer after the regeneration through regenerator sloped tube, contact with the described carbon four above hydrocarbon streams of C 4 olefin that comprise, the gaseous stream of generation and catalyzer enter the gas-solid distribution zone.
2. described methanol oxidation is converted into the method for low-carbon alkene according to claim 1, it is characterized in that the C 4 olefin mass content is greater than 75% in the described carbon four above hydrocarbon streams that comprise C 4 olefin.
3. described methanol oxidation is converted into the method for low-carbon alkene according to claim 1, it is characterized in that described sial phosphorus molecular sieve comprises SAPO-34.
4. described methanol oxidation is converted into the method for low-carbon alkene according to claim 1, it is characterized in that described riser reaction zone reaction conditions is: temperature of reaction is 500～600 ℃, 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 reaction conditions is: temperature of reaction is 430～530 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 5～10 meter per seconds.
5. described methanol oxidation is converted into the method for low-carbon alkene according to claim 1, it is characterized in that the average carbon deposition quantity massfraction of described regenerated catalyst is 0.01～0.5%.
6. described methanol oxidation is converted into the method for low-carbon alkene according to claim 1, it is characterized in that described revivifier and settling vessel coaxial arrangement, and revivifier is positioned at the settling vessel below.
7. described methanol oxidation is converted into the method for low-carbon alkene according to claim 1, it is characterized in that described gas-solid distribution zone is positioned at described down-flow fluidized bed using ECT reaction zone top, the gaseous stream and the catalyzer that come from riser reaction zone enter the down-flow fluidized bed using ECT reaction zone with described methanol feedstock after the gas-solid distribution zone is mixed.
8. described methanol oxidation is converted into the method for low-carbon alkene according to claim 1, it is characterized in that at least one position that described riser reaction zone axial direction due separates opening for feed being set, and institute advances material and comprises methyl alcohol.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110193449.0A CN102875281B (en) | 2011-07-12 | 2011-07-12 | Method for catalytically converting methanol to low-carbon olefins |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110193449.0A CN102875281B (en) | 2011-07-12 | 2011-07-12 | Method for catalytically converting methanol to low-carbon olefins |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102875281A true CN102875281A (en) | 2013-01-16 |
| CN102875281B CN102875281B (en) | 2015-05-13 |
Family
ID=47476843
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201110193449.0A Active CN102875281B (en) | 2011-07-12 | 2011-07-12 | Method for catalytically converting methanol to low-carbon olefins |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102875281B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN112705127A (en) * | 2019-10-24 | 2021-04-27 | 中国石油化工股份有限公司 | Reactor and method for producing low-carbon olefin |
Citations (3)
| 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 |
| 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 |
| CN101270023B (en) * | 2008-04-11 | 2011-04-27 | 中国石油化工股份有限公司 | Method for improving yield of light olefin hydrocarbon |
-
2011
- 2011-07-12 CN CN201110193449.0A patent/CN102875281B/en active Active
Patent Citations (3)
| 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 |
| 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 |
| CN101270023B (en) * | 2008-04-11 | 2011-04-27 | 中国石油化工股份有限公司 | Method for improving yield of light olefin hydrocarbon |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN112705127A (en) * | 2019-10-24 | 2021-04-27 | 中国石油化工股份有限公司 | Reactor and method for producing low-carbon olefin |
| CN112705127B (en) * | 2019-10-24 | 2022-11-01 | 中国石油化工股份有限公司 | Reactor and method for producing low-carbon olefin |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102875281B (en) | 2015-05-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102875296B (en) | Reaction unit for preparing low-carbon olefins | |
| CN103772092A (en) | Reaction device for converting methanol into light olefin | |
| CN103739420A (en) | Method of increasing the yield of low-carbon olefins | |
| CN102190542B (en) | The coupling process of methanol-to-olefins and carbon more than four hydrocarbon catalytic pyrolysis | |
| CN102463079B (en) | Reaction device for producing low-carbon olefin from methanol | |
| CN102464526B (en) | Method for producing low-carbon olefins from methanol | |
| CN102875281B (en) | Method for catalytically converting methanol to low-carbon olefins | |
| CN103739419B (en) | The method of preparing light olefins from methanol | |
| CN103739428A (en) | Device for producing low-carbon olefins from methanol | |
| CN103772091B (en) | By the method for preparing low carbon olefin hydrocarbon with methanol | |
| CN102875291B (en) | Method for producing low-carbon olefins from methanol | |
| CN102875293B (en) | Reaction unit for catalytic conversion of methanol to low-carbon olefins | |
| CN103772089A (en) | Reaction device for improving yield of ethylene and propylene | |
| CN103739430A (en) | Reaction device used for converting methanol into low-carbon olefins | |
| CN103739427B (en) | Reaction device for producing low-carbon olefins from methanol | |
| CN102875305B (en) | Method for preparing low carbon olefins from methanol | |
| CN103664449A (en) | Method for preparing low carbon olefin through oxygenated chemicals | |
| CN103664439B (en) | By the device of preparing low-carbon olefin by using methanol | |
| CN103664441B (en) | By the method for preparing low-carbon olefin by using methanol | |
| CN103772105A (en) | Reaction device for improving yield of light olefins | |
| CN103539609B (en) | Production method of low-carbon olefin | |
| CN103664451A (en) | Low-carbon olefine production device | |
| CN102875304A (en) | Method for preparing low carbon olefins from methanol and naphtha | |
| CN103772104B (en) | The reaction unit of preparing light olefins from methanol | |
| CN102875292B (en) | By the reaction unit of preparing low carbon olefin hydrocarbon with methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |