CN103772103A - Method for increasing yields of ethylene and propylene in reaction process of preparing olefin by methanol - Google Patents

Method for increasing yields of ethylene and propylene in reaction process of preparing olefin by methanol Download PDF

Info

Publication number
CN103772103A
CN103772103A CN201210412550.5A CN201210412550A CN103772103A CN 103772103 A CN103772103 A CN 103772103A CN 201210412550 A CN201210412550 A CN 201210412550A CN 103772103 A CN103772103 A CN 103772103A
Authority
CN
China
Prior art keywords
reaction zone
reaction
methanol
ethene
ring 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.)
Pending
Application number
CN201210412550.5A
Other languages
Chinese (zh)
Inventor
齐国祯
李晓红
王洪涛
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Priority to CN201210412550.5A priority Critical patent/CN103772103A/en
Publication of CN103772103A publication Critical patent/CN103772103A/en
Pending legal-status Critical Current

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
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective 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
    • 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

Landscapes

  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention relates to a method for increasing yields of ethylene and propylene in a reaction process of preparing olefin by methanol. The method mainly solves the problem that the yields of ethylene and propylene are lower in the prior art. The method comprises the following steps that (1) a reactor is provided, wherein the reactor comprises an annular reaction area and a settlement area, and the annular reaction area comprises an external ring reaction area, a middle ring reaction area and an internal ring reaction area; (2) raw methanol enters the external ring reaction area to be contacted with a catalyst comprising an aluminosilicophosphate molecular sieve; a generated product flow enters a separation working section; a light olefin product, above C4 hydrocarbon and an oxygen-containing compound flow are separated; partial separated catalyst is regenerated; partial separated catalyst returns to the external ring reaction area; (3) the regenerated catalyst enters the internal ring reaction area to be contacted with above C4 hydrocarbon; a generated product enters the middle ring reaction area; and (4) the oxygen-containing compound flow enters the middle ring reaction area. With the adoption of the technical scheme, the problem is solved better, so that the method can be used in industrial production of ethylene and propylene.

Description

In methanol-to-olefins reaction process, improve the method for ethene, propene yield
Technical field
The present invention relates to improve in a kind of methanol-to-olefins reaction process the method for ethene, propene yield.
Background technology
Low-carbon alkene, i.e. ethene and propylene, is 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 of alternative materials conversion ethene processed, propylene.Wherein, the important alternative materials of producing for low-carbon alkene of one class is oxygenatedchemicals, such as alcohols (methyl alcohol, ethanol), ethers (dme, methyl ethyl ether), ester class (methylcarbonate, methyl-formiate) etc., these oxygenatedchemicalss can be transformed by coal, Sweet natural gas, biomass equal energy source.Some oxygenatedchemicals can reach fairly large production, as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize the industrial scale of up to a million tonnes.Due to 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), be particularly subject to increasing attention by the technique of preparing olefin by conversion of methanol (MTO).
In US4499327 patent, silicoaluminophosphamolecular molecular sieve catalyst is applied to preparing olefin by conversion of methanol technique and studies in detail, think that SAPO-34 is the first-selected catalyzer of MTO technique.SAPO-34 catalyzer has very high selectivity of light olefin, and activity is also higher, and can make methanol conversion is reaction times of low-carbon alkene to be less than the degree of 10 seconds, more even reaches in the reaction time range of riser tube.
Technology and reactor that a kind of methanol conversion is low-carbon alkene in US6166282, are announced, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas speed has reacted, rise to after the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Due to reaction after product gas and catalyzer sharp separation, effectively prevent the generation of secondary reaction.Through analog calculation, compared with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all greatly reduce.But in the method, yield of light olefins is general all in 77% left and right, has the problem that yield of light olefins is lower.
In CN1723262, having announced with the multiple riser reaction unit of central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises multiple riser reactors, 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, yield of light olefins is general all between 75～80%, has equally the problem that yield of light olefins is lower.
Still there is ethene, shortcoming that propene yield is lower in prior art, the present invention has solved this problem targetedly.
Summary of the invention
Technical problem to be solved by this invention is the lower problem of ethene, propene yield existing in prior art, and a kind of method that improves ethene, propene yield in new methanol-to-olefins reaction process is provided.The method, for the production of ethene, propylene, has advantages of that in product, 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 that improves ethene, propene yield in methanol-to-olefins reaction process, comprise the following steps: (1) provides a kind of reactor, comprise annular reaction district, negative area, described annular reaction district comprises outer shroud reaction zone, middle ring reaction zone, interior ring reaction zone; (2) raw material that is mainly methyl alcohol 50～99% enters outer shroud reaction zone in mass, 1～50% enters middle ring reaction zone, contact with the catalyzer that comprises silicoaluminophosphamolecular molecular sieve, the product stream generating entering centrifugal station after gas solid separation in negative area, isolate low-carbon alkene product, the above hydrocarbon of carbon four, oxygenatedchemicals logistics, in negative area, an isolated catalyzer part is gone regeneration, and a part is returned to outer shroud reaction zone; (3) catalyzer after regeneration enters interior ring reaction zone, contacts with the above hydrocarbon stream of described carbon four, and the product stream of generation enters middle ring reaction zone; (4) described oxygenatedchemicals logistics enters middle ring reaction zone.
In technique scheme, described silicoaluminophosphamolecular molecular sieve is selected from SAPO-34; The outlet of described interior ring reaction zone is arranged in ring reaction zone, in the distance of exit, interior ring reaction zone, encircle in bottom, reaction zone 1/5～2/3 and encircle reaction zone height, interior ring reaction zone entrance is arranged in ring reaction zone, outside, outer shroud reaction zone, and Yu Zhonghuan reaction zone, outer shroud reaction zone communicates by catalyst stream port; The reaction conditions of described outer shroud reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 400～500 ℃, the average coke content of catalyzer are as 1.5～3.5% weight, gas phase linear speed are as 0.5～5.0 meter per second take gauge pressure; The reaction conditions of described middle ring reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 400～500 ℃, gas phase linear speed are as 0.3～2.0 meter per second take gauge pressure; The reaction conditions of described interior ring reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 500～680 ℃, gas phase linear speed are as 2～10.0 meter per seconds take gauge pressure; The average carbon deposition quantity massfraction of catalyzer after described regeneration is 0.01～0.5%; In described negative area, isolated catalyzer 20～60% goes regeneration in mass, and 40～80% return to outer shroud reaction zone; In the above hydrocarbon stream of described carbon four, alkene quality percentage composition is greater than 60%, and oxygenatedchemicals logistics comprises methyl alcohol, dme.
The method of calculation of coke content of the present invention are that carbon deposit quality on the catalyzer of certain mass is divided by described catalyst quality.Carbon deposit measuring method on catalyzer is as follows: will mix the catalyst mix with carbon deposit comparatively uniformly, then weigh the band C catalyst of certain mass, be put in pyrocarbon analyser and burn, by infrared analysis burn generate carbonic acid gas quality, thereby obtain the carbonaceous amount on catalyzer.
The preparation method of silicoaluminophosphamolecular molecular sieve of the present invention is: first prepare molecular sieve presoma, be 0.03～0.6R by mole proportioning: (Si 0.01～0.98: Al 0.01～0.6: P 0.01～0.6): 2～500 H2O, wherein R represents template, constitutive material mixed solution obtains at a certain temperature after the crystallization of certain hour; Again, molecular sieve presoma, phosphorus source, silicon source, aluminium source, organic formwork agent, water etc. are mixed according to certain ratio after at 110～260 ℃ hydrothermal crystallizing after at least 0.1 hour, finally obtain SAPO molecular sieve.The molecular sieve of preparation is mixed with a certain proportion of binding agent, after the operation stepss such as, roasting dry through spraying, obtain final SAPO catalyzer, the weight percentage of binding agent in molecular sieve is generally between 10～90%.
Known in the field, in the reaction process that is low-carbon alkene in methanol conversion, on catalyzer, accumulate the selectivity that a certain amount of carbon distribution is conducive to improve low-carbon alkene.Adopt method of the present invention, methanol feedstock enters behind reaction zone, first contacts with reclaimable catalyst, production low-carbon alkene that can highly selective.And the above hydrocarbon olefin(e) centent of carbon four that reaction generates is high, can be used for cracking increased low carbon olefine output.Adopt method of the present invention, allow the above hydrocarbon of carbon four contact high temperature, highly active regenerated catalyst, in the above hydrocarbon of carbon four is converted into low-carbon alkene on regenerated catalyst, on catalyzer, form carbon distribution, then enter middle ring reaction zone, outer shroud reaction zone, play the effect that improves selectivity of light olefin.In addition, the oxygenatedchemicalss such as the dme that reaction generates and unreacted methyl alcohol, from centrifugal station branches away, enter middle ring reaction zone, can on the catalyzer of greater activity, transform completely.Therefore, adopt method of the present invention, can reach the object that improves yield of light olefins.
Adopt technical scheme of the present invention: described silicoaluminophosphamolecular molecular sieve is selected from SAPO-34; The outlet of described interior ring reaction zone is arranged in ring reaction zone, in the distance of exit, interior ring reaction zone, encircle in bottom, reaction zone 1/5～2/3 and encircle reaction zone height, interior ring reaction zone entrance is arranged in ring reaction zone, outside, outer shroud reaction zone, and Yu Zhonghuan reaction zone, outer shroud reaction zone communicates by catalyst stream port; The reaction conditions of described outer shroud reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 400～500 ℃, the average coke content of catalyzer are as 1.5～3.5% weight, gas phase linear speed are as 0.5～5.0 meter per second take gauge pressure; The reaction conditions of described middle ring reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 400～500 ℃, gas phase linear speed are as 0.3～2.0 meter per second take gauge pressure; The reaction conditions of described interior ring reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 500～680 ℃, gas phase linear speed are as 2～10.0 meter per seconds take gauge pressure; The average carbon deposition quantity massfraction of catalyzer after described regeneration is 0.01～0.5%; In described negative area, isolated catalyzer 20～60% goes regeneration in mass, and 40～80% return to outer shroud reaction zone; In the above hydrocarbon stream of described carbon four, alkene quality percentage composition is greater than 60%, and oxygenatedchemicals logistics comprises methyl alcohol, dme, and low-carbon alkene carbon base absorption rate can reach 86.77% weight, has obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of scheme of the present invention.
Fig. 2 is the diagrammatic cross-section of A-B position in Fig. 1.
In Fig. 1,1 is the above hydrocarbon feed charging of carbon four; 2 is interior ring reaction zone; 3 is middle ring reaction zone methanol feeding; 4 is outer shroud reaction zone methanol feeding; 5 is catalyst stream port; 6 is middle ring reaction zone; 7 is regenerator sloped tube; 8 is outer shroud reaction zone; 9 is inclined tube to be generated; 10 is negative area; 11 is gas-solid cyclone separator; 12 is product gas outlet; 13 is outer circulating tube; 14 is middle ring reaction zone oxygenate feedstock.
A raw material part that is mainly methyl alcohol enters outer shroud reaction zone 8, a part enters middle ring reaction zone 6, contact with the catalyzer that comprises silicoaluminophosphamolecular molecular sieve, the product stream generating is the interior centrifugal station that enters after gas solid separation in negative area 10, isolate low-carbon alkene product, the above hydrocarbon of carbon four, oxygenatedchemicals logistics, the interior isolated catalyzer part in negative area 10 is gone regeneration, a part is returned to outer shroud reaction zone 8, catalyzer after regeneration enters interior ring reaction zone 2, contact with the above hydrocarbon stream of described carbon four, the product stream generating enters middle ring reaction zone 6, described oxygenatedchemicals logistics enters middle ring reaction zone 6.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
In fluidized bed reaction as shown in Figure 1, purity is that 99.5% methanol feedstock 50% enters outer shroud reaction zone in mass, 50% enters middle ring reaction zone, contact with the catalyzer of SAPO-34 molecular sieve, the product stream generating entering centrifugal station after gas solid separation in negative area, isolate low-carbon alkene product, the above hydrocarbon of carbon four, oxygenatedchemicals logistics, in negative area, isolated catalyzer 20% goes regeneration in mass, 80% returns to outer shroud reaction zone, catalyzer after regeneration enters interior ring reaction zone, contact with the above hydrocarbon stream of carbon four, the product stream generating enters middle ring reaction zone, oxygenatedchemicals logistics also enters middle ring reaction zone.The outlet of interior ring reaction zone is arranged in ring reaction zone, in the distance of exit, interior ring reaction zone, encircle in bottom, reaction zone 1/5 and encircle reaction zone height, interior ring reaction zone entrance is arranged in ring reaction zone, outside, outer shroud reaction zone, and Yu Zhonghuan reaction zone, outer shroud reaction zone communicates by catalyst stream port.The reaction conditions of outer shroud reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 400 ℃, the average coke content of catalyzer are as 1.5% weight, gas phase linear speed are as 0.5 meter per second take gauge pressure; The reaction conditions of described middle ring reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 400 ℃, gas phase linear speed are as 0.3 meter per second take gauge pressure; The reaction conditions of interior ring reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 500 ℃, gas phase linear speed are as 2 meter per seconds take gauge pressure.The average carbon deposition quantity massfraction of catalyzer after regeneration is 0.01%, and in the above hydrocarbon stream of carbon four, alkene quality percentage composition is 60%, and in oxygenatedchemicals logistics, middle methyl alcohol, dme quality percentage composition are 85%.The low-carbon alkene carbon base absorption rate of reactor outlet is 81.69% (weight).
[embodiment 2]
According to condition and step described in embodiment 1, purity is that 99.5% methanol feedstock 99% enters outer shroud reaction zone in mass, 1% enters middle ring reaction zone, in negative area, isolated catalyzer 60% goes regeneration in mass, 40% returns to outer shroud reaction zone, encircles in bottom, reaction zone 2/3 and encircle reaction zone height in the distance of exit, interior ring reaction zone.The reaction conditions of outer shroud reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 500 ℃, the average coke content of catalyzer are as 3.5% weight, gas phase linear speed are as 5.0 meter per seconds take gauge pressure; The reaction conditions of described middle ring reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 500 ℃, gas phase linear speed are as 2.0 meter per seconds take gauge pressure; The reaction conditions of interior ring reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 680 ℃, gas phase linear speed are as 10.0 meter per seconds take gauge pressure.The average carbon deposition quantity massfraction of catalyzer after regeneration is 0.5%, and in the above hydrocarbon stream of carbon four, alkene quality percentage composition is 88%, and in oxygenatedchemicals logistics, middle methyl alcohol, dme quality percentage composition are 91%.The low-carbon alkene carbon base absorption rate of reactor outlet is 84.18% (weight).
[embodiment 3]
According to condition and step described in embodiment 1, purity is that 99.5% methanol feedstock 85% enters outer shroud reaction zone in mass, 15% enters middle ring reaction zone, in negative area, isolated catalyzer 70% goes regeneration in mass, 30% returns to outer shroud reaction zone, encircles in bottom, reaction zone 1/2 and encircle reaction zone height in the distance of exit, interior ring reaction zone.The reaction conditions of outer shroud reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 480 ℃, the average coke content of catalyzer are as 3.0% weight, gas phase linear speed are as 2.0 meter per seconds take gauge pressure; The reaction conditions of described middle ring reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 500 ℃, gas phase linear speed are as 1.0 meter per seconds take gauge pressure; The reaction conditions of interior ring reaction zone is: reaction pressure is counted 0.01MPa, medial temperature as 650 ℃, gas phase linear speed are as 6.0 meter per seconds take gauge pressure.The average carbon deposition quantity massfraction of catalyzer after regeneration is 0.1%, and in the above hydrocarbon stream of carbon four, alkene quality percentage composition is 92%, and in oxygenatedchemicals logistics, middle methyl alcohol, dme quality percentage composition are 93%.The low-carbon alkene carbon base absorption rate of reactor outlet is 86.77% (weight).
[embodiment 4]
According to condition and step described in embodiment 3, just change outer shroud, middle ring, interior ring reaction zone pressure and count 0.3MPa with gauge pressure.The low-carbon alkene carbon base absorption rate of reactor outlet is 83.99% (weight).
[comparative example 1]
According to condition and step described in embodiment 3, middle ring reaction zone is not just set, the low-carbon alkene carbon base absorption rate of reactor outlet is 84.25% (weight).
[comparative example 2]
According to condition and step described in embodiment 3, He Neihuan reaction zone, middle ring reaction zone is not just set, reaction zone is directly returned in the above hydrocarbon stream of carbon four and oxygenatedchemicals logistics, and the low-carbon alkene carbon base absorption rate of reactor outlet is 81.46% (weight).
[comparative example 3]
According to condition and step described in embodiment 3, He Neihuan reaction zone, middle ring reaction zone is not just set, the above hydrocarbon stream of carbon four and oxygenatedchemicals logistics are not returned, and the low-carbon alkene carbon base absorption rate of reactor outlet is 79.67% (weight).
Obviously, adopt method of the present invention, can reach the object that improves ethene, propylene carbon base absorption rate, there is larger technical superiority, can be used in the industrial production of ethene, propylene.

Claims (10)

1. a method that improves ethene, propene yield in methanol-to-olefins reaction process, comprises the following steps:
(1) provide a kind of reactor, comprise annular reaction district, negative area, described annular reaction district comprises outer shroud reaction zone, middle ring reaction zone, interior ring reaction zone;
(2) raw material that is mainly methyl alcohol 50～99% enters outer shroud reaction zone in mass, 1～50% enters middle ring reaction zone, contact with the catalyzer that comprises silicoaluminophosphamolecular molecular sieve, the product stream generating entering centrifugal station after gas solid separation in negative area, isolate low-carbon alkene product, the above hydrocarbon of carbon four, oxygenatedchemicals logistics, in negative area, an isolated catalyzer part is gone regeneration, and a part is returned to outer shroud reaction zone;
(3) catalyzer after regeneration enters interior ring reaction zone, contacts with the above hydrocarbon stream of described carbon four, and the product stream of generation enters middle ring reaction zone;
(4) described oxygenatedchemicals logistics enters middle ring reaction zone.
2. the method that improves according to claim 1 ethene, propene yield in methanol-to-olefins reaction process, is characterized in that described silicoaluminophosphamolecular molecular sieve is selected from SAPO-34.
3. improve according to claim 1 the method for ethene, propene yield in methanol-to-olefins reaction process, it is characterized in that the outlet of described interior ring reaction zone is arranged in ring reaction zone, in the distance of exit, interior ring reaction zone, encircle in bottom, reaction zone 1/5～2/3 and encircle reaction zone height, interior ring reaction zone entrance is arranged in ring reaction zone, outside, outer shroud reaction zone, and Yu Zhonghuan reaction zone, outer shroud reaction zone communicates by catalyst stream port.
4. the method that improves according to claim 1 ethene, propene yield in methanol-to-olefins reaction process, is characterized in that the reaction conditions of described outer shroud reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 400～500 ℃, the average coke content of catalyzer are as 1.5～3.5% weight, gas phase linear speed are as 0.5～5.0 meter per second take gauge pressure.
5. the method that improves according to claim 1 ethene, propene yield in methanol-to-olefins reaction process, is characterized in that the reaction conditions of described middle ring reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 400～500 ℃, gas phase linear speed are as 0.3～2.0 meter per second take gauge pressure.
6. the method that improves according to claim 1 ethene, propene yield in methanol-to-olefins reaction process, is characterized in that the reaction conditions of described interior ring reaction zone is: reaction pressure is counted 0.01～0.3MPa, medial temperature as 500～680 ℃, gas phase linear speed are as 2～10.0 meter per seconds take gauge pressure.
7. the method that improves according to claim 1 ethene, propene yield in methanol-to-olefins reaction process, is characterized in that the average carbon deposition quantity massfraction of catalyzer after described regeneration is 0.01～0.5%.
8. improve according to claim 1 the method for ethene, propene yield in methanol-to-olefins reaction process, it is characterized in that in described negative area, isolated catalyzer 20～60% goes regeneration in mass, 40～80% return to outer shroud reaction zone.
9. the method that improves according to claim 1 ethene, propene yield in methanol-to-olefins reaction process, is characterized in that in the above hydrocarbon stream of described carbon four, alkene quality percentage composition is greater than 60%.
10. the method that improves according to claim 1 ethene, propene yield in methanol-to-olefins reaction process, is characterized in that oxygenatedchemicals logistics comprises methyl alcohol, dme.
CN201210412550.5A 2012-10-25 2012-10-25 Method for increasing yields of ethylene and propylene in reaction process of preparing olefin by methanol Pending CN103772103A (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201210412550.5A CN103772103A (en) 2012-10-25 2012-10-25 Method for increasing yields of ethylene and propylene in reaction process of preparing olefin by methanol

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201210412550.5A CN103772103A (en) 2012-10-25 2012-10-25 Method for increasing yields of ethylene and propylene in reaction process of preparing olefin by methanol

Publications (1)

Publication Number Publication Date
CN103772103A true CN103772103A (en) 2014-05-07

Family

ID=50564936

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201210412550.5A Pending CN103772103A (en) 2012-10-25 2012-10-25 Method for increasing yields of ethylene and propylene in reaction process of preparing olefin by methanol

Country Status (1)

Country Link
CN (1) CN103772103A (en)

Citations (4)

* Cited by examiner, † Cited by third party
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
CN102102025A (en) * 2009-12-17 2011-06-22 中国石油大学(北京) Heavy oil serial/parallel multi-area catalytic cracking method and device
CN103739425A (en) * 2012-10-17 2014-04-23 中国石油化工股份有限公司 Reaction device used for increasing the yields of ethylene and propylene in process of preparing olefins from methanol

Patent Citations (4)

* Cited by examiner, † Cited by third party
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
CN102102025A (en) * 2009-12-17 2011-06-22 中国石油大学(北京) Heavy oil serial/parallel multi-area catalytic cracking method and device
CN103739425A (en) * 2012-10-17 2014-04-23 中国石油化工股份有限公司 Reaction device used for increasing the yields of ethylene and propylene in process of preparing olefins from methanol

Similar Documents

Publication Publication Date Title
CN102464529B (en) Method for increasing yield of low-carbon olefins
CN102464532B (en) Method for preparing low-carbon olefins
CN103739420B (en) Improve the method for yield of light olefins
CN102463079B (en) Reaction device for producing low-carbon olefin from methanol
CN102464528B (en) Method for increasing yields of ethylene and propylene
CN102464526B (en) Method for producing low-carbon olefins from methanol
CN103772089A (en) Reaction device for improving yield of ethylene and propylene
CN103772088B (en) Improve the method for ethene, propene yield
CN103739425B (en) For improving the reaction unit of ethene, propene yield in methanol-to-olefins reaction process
CN102464534B (en) Method for producing low-carbon olefins from methanol
CN102295504B (en) Method for preparing low-carbon olefin by using methanol
CN103664450B (en) Improve the method for yield of light olefins
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
CN103664442B (en) With methyl alcohol and ethanol for the method for low-carbon alkene prepared by raw material
CN103664449A (en) Method for preparing low carbon olefin through oxygenated chemicals
CN103539609B (en) Production method of low-carbon olefin
CN102875291B (en) Method for producing low-carbon olefins from methanol
CN103739427B (en) Reaction device for producing low-carbon olefins from methanol
CN103772105A (en) Reaction device for improving yield of light olefins
CN103739430A (en) Reaction device used for converting methanol into low-carbon olefins
CN103772091A (en) Method for manufacturing low-carbon alkene from methanol
CN102875305B (en) Method for preparing low carbon olefins from methanol
CN102464530B (en) Method for catalytically converting methanol into low-carbon olefins
CN103772103A (en) Method for increasing yields of ethylene and propylene in reaction process of preparing olefin by 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
C02 Deemed withdrawal of patent application after publication (patent law 2001)
WD01 Invention patent application deemed withdrawn after publication

Application publication date: 20140507