CN102464533B - Method for preparing low-carbon olefin - Google Patents

Method for preparing low-carbon olefin Download PDF

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CN102464533B
CN102464533B CN2010105538597A CN201010553859A CN102464533B CN 102464533 B CN102464533 B CN 102464533B CN 2010105538597 A CN2010105538597 A CN 2010105538597A CN 201010553859 A CN201010553859 A CN 201010553859A CN 102464533 B CN102464533 B CN 102464533B
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carbon
reaction zone
catalyst
low
carbon deposition
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CN102464533A (en
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齐国祯
钟思青
陈伟
俞志楠
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Abstract

The invention relates to a method for preparing low-carbon olefin, mainly aiming at solving the problem of low yield of low-carbon olefin in the prior art. The technical scheme of the invention, which better solves the problem, is as follows: the method for preparing low-carbon olefin mainly comprise the following steps: firstly, a first raw material enters a rapid reaction zone having a gas-phase line speed of 1.0-10.0m/s to be in contact with a catalyst so as to generate a product material flow I containing low-carbon olefin, and form a carbon-deposited catalyst I simultaneously; secondly, the carbon-deposited catalyst I enters a downer reaction zone to be in contact with a second raw material to generate a product material flow II containing low-carbon olefin, and form a carbon-deposited catalyst II simultaneously; thirdly, the carbon-deposited catalyst II enters a riser regenerator for regeneration to form a regenerated catalyst; and fourthly, the regenerated catalyst is divided at least into two parts, wherein one part enters the downer reaction zone, and the other part enters the repaid reaction zone. The method disclosed by the invention can be used in industrial low-carbon olefin production.

Description

The method for preparing low-carbon alkene
Technical field
The present invention relates to a kind of method for preparing low-carbon alkene.
Technical background
Low-carbon alkene, ethene and propylene, be two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, but, due to the limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people start to greatly develop the technology that alternative materials transforms ethene processed, propylene.Wherein, the important alternative materials 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, as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize the industrial scale of up to a million tonnes.Popularity due to the 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 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, can make the reaction times that methanol conversion is low-carbon alkene be less than the degree of 10 seconds, more even reaches in the reaction time range of riser tube.
Technology and reactor that to have announced a kind of methanol conversion in US6166282 be low-carbon alkene, adopt fast fluidized bed reactor, gas phase is after in gas speed, lower Mi Xiangfanyingqu has reacted, 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.Due to reaction after product gas and catalyzer sharp separation, effectively prevented the generation of secondary reaction.Through analog calculation, with traditional bubbling fluidization bed bioreactor, to compare, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all greatly reduce.But there is the problem that yield of light olefins is lower in the method.
The multiple riser reaction unit of having announced in CN1723262 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.There is the problem that yield of light olefins is lower equally in the method.
All there is the problem that yield of light olefins is lower 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 existed in prior art, and a kind of new method for preparing low-carbon alkene is provided.The method, 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 method for preparing low-carbon alkene, mainly comprise the following steps: (1) first raw material enters the rapid reaction zone that the gas phase linear speed is 1.0～10.0 meter per seconds, with catalyzer, contact, generation comprises the product stream I of low-carbon alkene, forms carbon deposition catalyst I simultaneously; (2) described carbon deposition catalyst I enters the down-flow fluidized bed using ECT reaction zone, with the second raw material, contacts, and generates the product stream II that comprises low-carbon alkene, forms carbon deposition catalyst II simultaneously; (3) described carbon deposition catalyst II enters riser regenerator regeneration, forms regenerated catalyst; (4) described regenerated catalyst at least is divided into two portions, and a part enters the down-flow fluidized bed using ECT reaction zone, and a part enters described rapid reaction zone.
In technique scheme, described catalyzer is selected from least one in SAPO-34 or ZSM-5, and preferred version is SAPO-34; Described the first raw material comprises at least one of methyl alcohol or carbon four above hydrocarbon, and the second raw material comprises at least one in methyl alcohol or ethanol; Described product stream I and product stream II share a set of separation process; In described rapid reaction zone, reaction conditions is: temperature of reaction is 400～550 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 2.0～7.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 400～550 ℃, and reaction pressure is counted 001～0.3MPa with gauge pressure, and the gas phase linear speed is 4.0～12.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 600～700 ℃, and the gas phase linear speed is 4.0～10.0 meter per seconds, and regenerating medium is air; Described regenerated catalyst at least is divided into two portions, and 20～80% enter the down-flow fluidized bed using ECT reaction zone, and 20～80% enter described rapid reaction zone; The carbon deposition quantity massfraction of described carbon deposition catalyst I is 1.0～4.5%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 1.2～5.5%.
Down-flow fluidized bed using ECT of the present invention refers to the top-down type of reactor of Gas-particle Flows direction.
Adopt method of the present invention, two reaction zones are set, wherein can be by the low-carbon alkene that is converted into of raw material highly selective in rapid reaction zone, this raw material can be selected methyl alcohol or the above hydrocarbon of carbon four, the above hydrocarbon of described carbon four can be from the by product produced in the preparing olefin by conversion of methanol process, and, in the down-flow fluidized bed using ECT reaction zone, except reaching the purpose of producing light olefins with high selectivity under the state that is close to plug flow, can realize improving the purpose of coking yield simultaneously.Therefore, scheme of the present invention can realize improving the purpose of yield of light olefins.
Adopt technical scheme of the present invention: described catalyzer is selected from least one in SAPO-34 or ZSM-5; Described the first raw material comprises at least one of methyl alcohol or carbon four above hydrocarbon, and the second raw material comprises at least one in methyl alcohol or ethanol; Described product stream I and product stream II share a set of separation process; In described rapid reaction zone, reaction conditions is: temperature of reaction is 400～550 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 2.0～7.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 400～550 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 4.0～12.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 600～700 ℃, and the gas phase linear speed is 4.0～10.0 meter per seconds, and regenerating medium is air; Described regenerated catalyst at least is divided into two portions, and 20～80% enter the down-flow fluidized bed using ECT reaction zone, and 20～80% enter described rapid reaction zone; The carbon deposition quantity massfraction of described carbon deposition catalyst I is 1.0～4.5%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 1.2～5.5%, and yield of light olefins reaches 38.26% (weight), than the low-carbon alkene carbon base absorption rate of prior art, exceeds and can reach 5 percentage points, has obtained technique effect preferably.
The accompanying drawing explanation
The schematic flow sheet that Fig. 1 is the method for the invention;
In Fig. 1,1 is the first material feeding tube line; 2 is the pre-mixing district; 3 is stripping medium feeding line; 4 is inclined tube to be generated; 5 is the regenerating medium feeding line; 6 is the pre-lift district; 7 is riser regenerator; 8 enter the first settling vessel pipeline for product stream II; 9 is rapid reaction zone; 10 is gas-solid cyclone separator; 11 is the second material feeding tube line; 12 is the second settling vessel; 13 is the down-flow fluidized bed using ECT reaction zone; 14 is regenerated catalyst; 15 is down-flow fluidized bed using ECT top gas-solid distribution zone; 16 is carbon deposition catalyst I transfer lime; 17 is stripping medium feeding line; 18 is regenerated catalyst; 19 is degassed medium feeding line; 20 is degas zone; 21 is the first settling vessel; 22 is gas-solid cyclone separator; 23 is the products export pipeline; 24 slightly revolve for riser regenerator exports; 25 is the revivifier settling vessel; 26 is gas-solid cyclone separator; 27 is the exhanst gas outlet pipeline; 28 is stripping zone.
The first raw material enters rapid reaction zone 9 from pipeline 1, with catalyzer, contact, generation comprises the product stream I of low-carbon alkene, form carbon deposition catalyst I simultaneously, product stream I enters centrifugal station through gas solid separation by pipeline 23, carbon deposition catalyst I enters down-flow fluidized bed using ECT reaction zone 13 through stripping zone 28 strippings by transfer lime 16, with the second raw material from pipeline 11, contact, generation comprises the product stream II of low-carbon alkene, form carbon deposition catalyst II simultaneously, product stream II enters in the first settling vessel 21 through gas solid separation by pipeline 8, with product stream I, merge, carbon deposition catalyst II enters riser regenerator 7 regeneration through stripping by inclined tube 4 to be generated, the regenerated catalyst formed at least is divided into two portions, a part enters down-flow fluidized bed using ECT reaction zone 13 through pipeline 18, a part enters described rapid reaction zone 9 through pipeline 14.
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, catalyzer adopts SAPO-34, the first raw material adopts the methanol feeding that purity is 99.5%, and the second raw material adopts the methanol feeding that purity is 99.5%, and the first raw material charging mass rate is 3: 1 with the ratio of the second raw material charging mass rate.The rapid reaction zone reaction conditions is: temperature of reaction is 470 ℃, and reaction pressure is counted 01MPa with gauge pressure, and the gas phase linear speed is 3.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 500 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and the gas phase linear speed is 6.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 660 ℃, and the gas phase linear speed is 7.0 meter per seconds, and regenerating medium is air.Regenerated catalyst is divided into two portions, and 50% enters the down-flow fluidized bed using ECT reaction zone, and 50% enters rapid reaction zone, and the carbon deposition quantity massfraction of carbon deposition catalyst I is 3.0%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 4.2%, the product stream II of down-flow fluidized bed using ECT reaction zone discharges after merging with product stream I after stripping in product outlet line 23, reactor product adopts online gas chromatographic analysis, and yield of light olefins is 34.81% (weight).
[embodiment 2]
According to the described condition of embodiment 1 and step, just the second raw material is the ethanol charging that purity is 99.7%, and in the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 400 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and the gas phase linear speed is 4.5 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 600 ℃, and the gas phase linear speed is 5.0 meter per seconds, and regenerated catalyst is divided into two portions, and 20% enters the down-flow fluidized bed using ECT reaction zone, and 80% enters rapid reaction zone, and the carbon deposition quantity massfraction of carbon deposition catalyst I is 2.8%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 3.3%, the product stream II of down-flow fluidized bed using ECT reaction zone discharges after merging with product stream I after stripping in product outlet line 23, reactor product adopts online gas chromatographic analysis, and yield of light olefins is 35.97% (weight).
[embodiment 3]
According to the described condition of embodiment 1 and step, just the first raw material adopts the above hydrocarbon of carbon four that centrifugal station is separated, wherein the C 4 olefin mass content is 89%, the second raw material adopts the methanol feeding that purity is 99.5%, and the first raw material charging mass rate is 1: 5 with the ratio of the second raw material charging mass rate.The rapid reaction zone reaction conditions is: temperature of reaction is 500 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 2.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 450 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and the gas phase linear speed is 12.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 650 ℃, and the gas phase linear speed is 8.0 meter per seconds, and regenerating medium is air.The carbon deposition quantity massfraction of carbon deposition catalyst I is 1.1%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 4.5%, the product stream II of down-flow fluidized bed using ECT reaction zone discharges after merging with product stream I after stripping in product outlet line 23, reactor product adopts online gas chromatographic analysis, and yield of light olefins is 36.32% (weight).
[embodiment 4]
According to the described condition of embodiment 3 and step, just the rapid reaction zone reaction conditions is: temperature of reaction is 550 ℃, and the gas phase linear speed is 7.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 485 ℃, and the gas phase linear speed is 8.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 700 ℃, and the gas phase linear speed is 10.0 meter per seconds.Regenerated catalyst is divided into two portions, and 30% enters the down-flow fluidized bed using ECT reaction zone, and 70% enters rapid reaction zone, and the carbon deposition quantity massfraction of carbon deposition catalyst I is 1.2%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 5.2%, the product stream II of down-flow fluidized bed using ECT reaction zone discharges after merging with product stream I after stripping in product outlet line 23, reactor product adopts online gas chromatographic analysis, and yield of light olefins is 37.09% (weight).
[embodiment 5]
According to the described condition of embodiment 4 and step, just the rapid reaction zone reaction conditions is: temperature of reaction is 550 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and the gas phase linear speed is 1.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 500 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and the gas phase linear speed is 4.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 650 ℃, and the gas phase linear speed is 4.0 meter per seconds.Regenerated catalyst is divided into two portions, and 30% enters the down-flow fluidized bed using ECT reaction zone, and 70% enters rapid reaction zone, and the carbon deposition quantity massfraction of carbon deposition catalyst I is 2.3%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 5.5%, the product stream II of down-flow fluidized bed using ECT reaction zone discharges after merging with product stream I after stripping in product outlet line 23, reactor product adopts online gas chromatographic analysis, and yield of light olefins is 34.59% (weight).
[embodiment 6]
According to the described condition of embodiment 4 and step, just catalyzer is adopted as ZSM-5, and silica alumina ratio is that 40, the first raw material charging mass rates are 2: 5 with the ratio of the second raw material charging mass rate.The rapid reaction zone reaction conditions is: temperature of reaction is 530 ℃, and the gas phase linear speed is 10.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 445 ℃, and the gas phase linear speed is 5.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 600 ℃, and the gas phase linear speed is 4.0 meter per seconds.Regenerated catalyst is divided into two portions, and 80% enters the down-flow fluidized bed using ECT reaction zone, and 20% enters rapid reaction zone, and the carbon deposition quantity massfraction of carbon deposition catalyst I is 1.5%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 2.6%, and reactor product adopts online gas chromatographic analysis, and yield of light olefins is 38.26% (weight).
[embodiment 7]
According to the described condition of embodiment 4 and step, just the rapid reaction zone reaction conditions is: temperature of reaction is 500 ℃, the gas phase linear speed is 1.0 meter per seconds, regenerated catalyst is divided into two portions, 50% enters the down-flow fluidized bed using ECT reaction zone, 50% enters rapid reaction zone, and the carbon deposition quantity massfraction of carbon deposition catalyst I is 1.3%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 4.3%, and reactor product adopts online gas chromatographic analysis, and yield of light olefins is 37.16% (weight).
[comparative example 1]
According to the described condition of embodiment 1 and step, the down-flow fluidized bed using ECT reaction zone just is not set, yield of light olefins is 33.24% (weight).
[comparative example 2]
According to the described condition of embodiment 3 and step, rapid reaction zone just is not set, yield of light olefins is 32.51% (weight).
Obviously, adopt method of the present invention, can reach the purpose that improves yield of light olefins, there is larger technical superiority, can be used in the industrial production of low-carbon alkene.

Claims (5)

1. a method for preparing low-carbon alkene mainly comprises the following steps:
(1) first raw material enters the rapid reaction zone that the gas phase linear speed is 1.0～10.0 meter per seconds, with catalyzer, contacts, and generates the product stream I that comprises low-carbon alkene, forms carbon deposition catalyst I simultaneously;
(2) described carbon deposition catalyst I enters the down-flow fluidized bed using ECT reaction zone, with the second raw material, contacts, and generates the product stream II that comprises low-carbon alkene, forms carbon deposition catalyst II simultaneously;
(3) described carbon deposition catalyst II enters riser regenerator regeneration, forms regenerated catalyst;
(4) described regenerated catalyst at least is divided into two portions, and a part enters the down-flow fluidized bed using ECT reaction zone, and a part enters described rapid reaction zone;
Wherein, described the first raw material comprises at least one of methyl alcohol or carbon four above hydrocarbon, and the second raw material comprises at least one in methyl alcohol or ethanol; In described rapid reaction zone, reaction conditions is: temperature of reaction is 400～550 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 2.0～7.0 meter per seconds; In the down-flow fluidized bed using ECT reaction zone, reaction conditions is: temperature of reaction is 400～550 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and the gas phase linear speed is 4.0～12.0 meter per seconds; In revivifier, regeneration condition is: regeneration temperature is 600～700 ℃, and the gas phase linear speed is 4.0～10.0 meter per seconds, and regenerating medium is air; The carbon deposition quantity massfraction of described carbon deposition catalyst I is 1.0～4.5%; The carbon deposition quantity massfraction of carbon deposition catalyst II is 1.2～5.5%.
2. prepare according to claim 1 the method for low-carbon alkene, it is characterized in that described catalyzer is selected from least one in SAPO-34 or ZSM-5.
3. prepare according to claim 2 the method for low-carbon alkene, it is characterized in that described catalyzer is selected from SAPO-34.
4. prepare according to claim 1 the method for low-carbon alkene, it is characterized in that described product stream I and product stream II share a set of separation process.
5. prepare according to claim 1 the method for low-carbon alkene, it is characterized in that described regenerated catalyst at least is divided into two portions, 20～80% weight enter the down-flow fluidized bed using ECT reaction zone, and 20～80% weight enter described rapid reaction zone.
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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101239871A (en) * 2007-02-07 2008-08-13 中国石油化工股份有限公司 Method for increasing selectivity of low-carbon olefins in methanol or dimethyl ether converting process
CN101260014A (en) * 2008-04-24 2008-09-10 中国石油化工股份有限公司 Method for producing low-carbon olefins from oxygen-containing compound

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101239871A (en) * 2007-02-07 2008-08-13 中国石油化工股份有限公司 Method for increasing selectivity of low-carbon olefins in methanol or dimethyl ether converting process
CN101260014A (en) * 2008-04-24 2008-09-10 中国石油化工股份有限公司 Method for producing low-carbon olefins from oxygen-containing compound

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