CN103539611A - Device for preparing olefins by using oxygen-containing compounds - Google Patents
Device for preparing olefins by using oxygen-containing compounds Download PDFInfo
- Publication number
- CN103539611A CN103539611A CN201210244617.9A CN201210244617A CN103539611A CN 103539611 A CN103539611 A CN 103539611A CN 201210244617 A CN201210244617 A CN 201210244617A CN 103539611 A CN103539611 A CN 103539611A
- Authority
- CN
- China
- Prior art keywords
- reactor
- revivifier
- oxygenatedchemicals
- utilizes
- communicated
- 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
-
- 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 discloses a device for preparing olefins by using oxygen-containing compounds, which overcomes the deficiency that the low carbon olefin yield in the prior art is low. The device consists of a main reactor (5), an assistant reactor (11) and a regenerator (21), wherein the main reactor (5) is communicated with the regenerator (21) through a second to-be-regenerated catalyst conveying pipe (23) and a second regenerated catalyst conveying pipe (28), and the assistant reactor (11) is communicated with the regenerator (21) through a first to-be-regenerated catalyst conveying pipe (16) and a first regenerated catalyst conveying pipe (18).
Description
Technical field:
The present invention relates to prepare hydrocarbon technical field from one or several non-hydrocarbon compounds, particularly a kind of device that utilizes oxygenatedchemicals to produce alkene
Background technology:
Take ethene, propylene, divinyl is that main light olefin and the benzene,toluene,xylene of take are that main light aromatics is the basic raw material of petrochemical complex.Ethylene production mainly relies on the tube furnace steam cracking technique of light naphthar raw material at present.Due to the shortage of crude resources and the raising day by day of price, it is not enough that naphtha resource has more and more seemed, the production cost of low-carbon alkene is more and more higher.The domestic and international positive abundanter ethylene production route of active development raw material sources, organic oxygen-containing compound raw material is through the katalysis of metal-modified SAPO type aperture phosphorus pure aluminium silicate Zn-Al-P-Si-oxide molecular sieve, can generate that to take ethene, propylene be main reaction product, just be subject to both domestic and externally paying attention to widely.
The oxygen-containing organic compound that methyl alcohol or dme be representative of take is typical oxygen-containing organic compound, mainly by synthetic gas coal-based or Sweet natural gas base, is produced.The oxygen-containing organic compound that is representative in order to methyl alcohol is that raw material production be take ethene and propylene and mainly contained at present the MTO technology of American UOP/Hyro company, the MTP technology of German Lurgi company and the methanol-to-olefins DMTO technology of the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences as main low-carbon alkene technique.
Take methyl alcohol as representing that the reaction characteristics of oxygenatedchemicals preparing low-carbon olefins technique abbreviation MTO is that rapid reaction, strong heat release and alcohol agent are lower, reacts and regenerates in the dense fluidized bed bioreactor of continuous reaction-regeneration.The high-temperature oil gas that is rich in the low-carbon alkenes such as ethene and propylene that reaction generates, need to carry out chilling and washing, removes wherein after catalyzer and cooling, is sent to bottom olefin separation system and carries out separation.The object product of MTO process unit is ethene and propylene, byproduct liquefied gas, C
5 +above component and fuel gas, wherein C
4 +carbon base absorption rate be 10% left and right.How this part low value product is converted into ethene and the propylene of high added value, be the problem of pendulum in face of vast scientific research and project planner always.
In recent years, MTO has become the focus and emphasis of insider's research.People conduct extensive research and explore from aspects such as work flow, catalyzer, processing condition and device structures, obtain gratifying achievement, but relevant how by the byproduct C in MTO process products
4 +the ethene and the propylene bibliographical information that are converted into high added value are few.
US20040102667 relates to the technology that OTO technique improves ethene and productivity of propylene.Adopt silicon aluminium phosphate catalyst.The C that product is isolated to
4～C
7middle matter olefin fraction carries out cracking in an independent cracking of olefins reactor.Key step is: (1) will be rich in the charging C of alkene
2～C
8send into flash trapping stage device, separate C
2～C
3light olefin and C
4 +heavy olefin fraction; (2) weight olefin fraction is sent into the second-order separation district, separate the second light olefin cut, C
4～C
7middle matter olefin fraction and C
7 +heavy olefin fraction; (3) middle matter olefin fraction is sent into cracking of olefins reactor, making the cracking of at least a portion raw material is C
2～C
3alkene; (4) C that cracking forms
2～C
3some gets back to the second-order separation district alkene.Another part is drawn out of; (5) some turns back to flash trapping stage district the second light olefin cut that the second-order separation is distinguished.
US5914433 patent relates to the technique that OTO produces polymerization-grade alkene.Be characterized in the mixed butene in product and heavy constituent to carry out cracking, thus the output of raising ethene and propylene.Cracking reaction in riser cracking district or the independent zone of cracking carry out, to technique, provide handiness.This technique has overcome the equilibrium-limited of silicon aluminium phosphate catalyst, has also improved the life-span of catalyzer, has improved the stability of catalyzer at zone of transformation.
Main processing step is: (1) oxygenatedchemicals (C
1～C
4a kind of alcohol or a kind of ether) raw material dilutes with thinner, adopts silicon aluminium phosphate catalyst (SAPO-34, SAPO-17 or its mixture) and fluidized-bed reactor, obtains light olefin product stream under reaction conditions; (2) ethene, propylene and mixed butene heavy constituent will be obtained after stream of light olefins separation; (3) taking out at least a portion reclaimable catalyst goes to regenerate; (4) the catalyzer part after regeneration turns back to fluidized bed reaction zone, and another part mixes with a certain amount of mixed butene and heavy constituent, enters cracking case and obtains the second product stream, generates extra ethene and propylene; (5) part the second product stream is turned back to fluidized bed reaction zone.
The patent CN1803738 of American UOP company has disclosed use mobile technology and has independently weighed alkene change step oxygenatedchemicals has been converted into propylene.These patent main points are to establish two reaction zones, and first moving bed reaction district is used the dual-function catalyst with SAPO and ZSM function, and oil gas product is mainly propylene, has a small amount of ethene, butylene and C simultaneously
4 +alkene, C
1～C
4stable hydrocarbon, a small amount of aromatic hydrocarbon and water.After the separation of reaction oil gas chilling, be divided into liquid hydrocarbon three parts that are rich in the steam of propylene, the water that comprises unreacted methyl alcohol and newly-generated oxygenatedchemicals, alkene, stable hydrocarbon, aromatic hydrocarbons.Recovery part water generation reaction is as the absorption agent of reaction raw materials.Second reaction zone is also moving-bed, use be the different ZSM of portfolio ratio, SAPO dual-function catalyst, temperature of reaction is higher more than 15 ℃ than the first reaction zone, object is by C
4 +conversion of olefines is that propylene is main product, estimates to be similar to the disclosed Atofina OCP C of company
4+conversion of olefines process catalyst.The first reactor generates contains ethene, butylene and C
4 +alkene, C
1～C
4the gas-phase product of stable hydrocarbon, a small amount of aromatic hydrocarbon is further separated, wherein C
4 +alkene removes the further conversion of olefines of the second reactor.
The patent CN1419527 of U.S. ExxonMobil company has disclosed C in a kind of oxygenate conversion reaction
4and C
4 +logistics, to the control method of the conversion of light product, is that oxygenate feedstock contacts with aluminium phosphate catalyst in the first reaction zone of reactor assembly, produces the first olefin product stream, and this first olefin product stream comprises light olefin and C
4 +alkene, by the first olefin product stream with at least partly from the catalyzer introducing second reaction zone in the first reaction zone, at least part of catalyzer in second reaction zone is introduced revivifier, all catalyzer are at regeneration in-situ regeneration, in second reaction zone, make the first olefin product stream contact with at least part of catalyzer, C
4 +conversion of olefines becomes light olefin.
The patent US4433188 of BASF AG has disclosed a kind of methanol/dimethyl ether alkene technology processed, and this invention adopts borosilicate catalyzer, comprises two-stage reaction and two sections of separation.Material benzenemethanol/dme contacts with catalyzer catalytic cracking reaction occurs in first paragraph reaction zone, and product separates C through the first separation system
2～C
4alkene and C
1～C
4alkane, C
5 +component enters second reaction zone and contacts generation scission reaction with catalyzer, and product, through the second separation system Arene removal component, then returns to the first separation system.The principal feature of this patent is circulation C
5 +component reacts under different conversion zones and condition from raw material.
The patent CN1962573A of Tsing-Hua University has disclosed method and the reactor of catalytic cracking for producing propylene using fluid bed, and this invention belongs to alcohol, ether cracking propylene technical field, it is characterized in that, the C in low-carbon alkene preparation technology's product
2and C
2following component, C
4and C
4after above component and object product propylene separation, circulation turns back in fluid catalytic cracking reaction unit alkene and turns reaction zone and carry out conversion of olefines, and by red-tape operati condition, highly selective is produced propylene.C
2 -, C
4 +two bursts of logistics had and speed on a small quantity to put before returning to olefin reaction district, to avoid inert component accumulation.Correspondingly, proposed can be used as the multicompartment fluidized bed structure of reactor in main reaction region or olefin reaction district.This invention has advantages of that the total receipts of propylene are high, selectivity is strong.
In sum, although related to C in some oxygenate conversion reaction in prior art
4and C
4 +freshening method, but also exist and use different catalyst systems, need to build the independently higher C of output investment ratio
4 +cracking unit, olefin cracking system thermal is uneven, and needing is specially C
4 +cracker provides required heat, and cracking condition is restricted, and transformation efficiency is lower; Only pay close attention to C in unconverted raw material and product
5 +component, the common freshening problem that does not relate to butylene; The technology that the propylene of partly take is in addition object product is circulated and is improved propylene total recovery by by product, but most employing loops back by product the simple forms of former reactor.
Summary of the invention:
Object of the present invention is just to provide a kind of device that utilizes oxygenatedchemicals to produce alkene, overcomes that prior art productivity of low carbon olefin hydrocarbon is low, flow process is complicated, invest high defect.
The invention provides a kind of device that utilizes oxygenatedchemicals to produce alkene, by main reactor 5, auxiliary reactor 11 and revivifier 21, formed, it is characterized in that: between main reactor 5 and revivifier 21, by the second reclaimable catalyst transfer lime 23 and the second regenerated catalyst 28, be communicated with, between auxiliary reactor 11 and revivifier 21, by the first reclaimable catalyst transfer lime 16 and the first regenerated catalyst 18, be communicated with.
Described a kind of oxygenatedchemicals is produced olefin hydrocarbon apparatus, is characterised in that: be also provided with riser reactor 15, riser reactor 15 is communicated with auxiliary reactor 11 and revivifier 21 by the first regenerated catalyst 18.
Described a kind of device that utilizes oxygenatedchemicals to produce alkene, is characterised in that: be also provided with riser reactor 15, riser reactor 15 is communicated with main reactor 5 and revivifier 21 by the first regenerated catalyst 18.
Described main reactor 5 and auxiliary reactor 11 are provided with outlet, and outlet is communicated with separation system.
Described auxiliary reactor 11 bottoms are provided with auxiliary reactor reclaimable catalyst stripping stage 13.
Described auxiliary reactor reclaimable catalyst stripping stage 13 tops are communicated with auxiliary reactor 11 bottoms, and bottom is communicated with revivifier 21 by the first reclaimable catalyst transfer lime 16.
Described main reactor 5 and revivifier 21 bottoms are respectively equipped with the first reclaimable catalyst stripping stage 2 and regenerated catalyst stripping stage 17, the first reclaimable catalyst stripping stage 2 tops are communicated with main reactor 5 bottoms, bottom is communicated with revivifier 21 by the second reclaimable catalyst transfer lime 23, regenerated catalyst stripping stage 17 tops are communicated with revivifier 21, and bottom is communicated with and is communicated with reactor 5 and auxiliary reactor 11 by the second regenerated catalyst 28 and the first regenerated catalyst 18 respectively.
Described main reactor 5, auxiliary reactor 11 and revivifier 21 inside are provided with the second cyclonic separator 6 and the first cyclonic separator 20.
Described auxiliary reactor 11 and riser reactor 15 are provided with C
4～C
8hydrocarbon entrance.
Described main reactor 5 is provided with heat collector 4, preferably interior heat collector 4.
Described main reactor 5, auxiliary reactor 11, revivifier 21 are a kind of among fluidized-bed, bubbling bed, fast fluidized bed, preferably turbulent bed.
Described revivifier 21 is provided with heat collector 22, preferably external warmer 22.
Compared with prior art, a kind of device that utilizes oxygenatedchemicals to produce alkene of the present invention has following advantage:
(1) the oxygenatedchemicals scission reaction described in the present invention is thermopositive reaction, and temperature of reaction is lower, and agent/expect is smaller, and C
4～C
8it is thermo-negative reaction that hydrocarbon transforms, and temperature of reaction is higher, and agent/material is larger, and catalyst recirculation mode is parallel operation, guarantees oxygenatedchemicals and C
4～C
8hydrocarbon reacts respectively under the operational condition of optimizing;
(2) C that this device is produced
4～C
8hydrocarbon can carry out freshening, also freshening not, and device operation understands;
(3) owing to adopting auxiliary reactor, ethene+propene yield improves 4～6 percentage points;
(4) oxygenatedchemicals and C
4～C
8hydrocarbon reaction catalyzer used is a kind of catalyzer, shares a revivifier, has reduced revivifier height and has reduced investment outlay.
Below in conjunction with the drawings and specific embodiments, the present invention is described further.But do not limit the scope of the invention.
Accompanying drawing explanation
A kind of device schematic diagram that utilizes oxygenatedchemicals to produce alkene of Fig. 1 the present invention.
Fig. 2 is that another kind of the present invention utilizes oxygenatedchemicals to produce the device schematic diagram of alkene.
Wherein:
1. guiding valve to be generated, 2. the first reclaimable catalyst stripping stage, 3. oxygenatedchemicals, 4. heat collector, 5. main reactor, 6. the second cyclonic separator, 7. main reactor reaction oil gas, 9. auxiliary reactor reaction oil gas, 10. auxiliary reactor cyclonic separator, 11. auxiliary reactors, 12.C
4～C
8hydrocarbon, 13. auxiliary reactor reclaimable catalyst stripping stages, 14. first reclaimable catalyst transfer limes, 15. riser reactors, 16. reclaimable catalyst transfer lime 2,17. regenerated catalyst stripping stages, 18. first regenerated catalyst, 19. regenerated flue gas, 20. first cyclonic separators, 21. revivifiers, 22. external warmers, 23. second reclaimable catalyst transfer limes, 24. first guiding valves to be generated, 25. second guiding valves to be generated, 26. first regeneration guiding valves, 27. second regeneration guiding valves, 28. second regenerated catalyst.
Embodiment
Be illustrated in figure 1 a kind of device that utilizes oxygenatedchemicals to produce alkene of the present invention, comprise auxiliary reactor 11, main reactor 5 and revivifier 21, between auxiliary reactor 11, main reactor 5, be provided with the first reclaimable catalyst transfer lime 14 and by the first reclaimable catalyst transfer lime 14, auxiliary reactor 11 and main reactor 5 be communicated with.Oxygenatedchemicals 3 enters main reactor 5 bottoms with gas phase form, contact with the high-temperature regenerated catalyst from revivifier 21, there is strong exothermal reaction, resultant of reaction carries out catalyst separating through main reactor cyclonic separator 6, the reaction gas 7 that is rich in the low-carbon alkenes such as ethene and propylene after separating catalyst is by main reactor 5 Base top contacts, deliver to rear portion chilling water wash system, pass through chilling, washing further reduces the temperature of reaction gas, the catalyst fines simultaneously carrying in washing reaction gas, by washing, the most of water in reaction gas is carried out to separation, then deliver to the separation of olefins unit at rear portion.In separation of olefins unit, reaction gas is carried out to separation, the object product ethene and the propylene that obtain go out device, C
4～C
8hydrocarbon 12 is as auxiliary reactor charging.
The reclaimable catalyst of the carbon distribution after separation enters main reactor stripping stage 2 strippings, remove the reaction gas that reclaimable catalyst carries, reclaimable catalyst after stripping, through guiding valve 1 to be generated and reclaimable catalyst transfer lime 23, enters revivifier 21 under the conveying of nitrogen, at the interior coke burning regeneration of revivifier 21.Catalyzer after regeneration enters revivifier stripping stage 17 strippings, and the regenerated catalyst after stripping divides two-way ，Yi road through regeneration guiding valve 27, regeneration transfer lime 28, enters main reactor 5 and recycles; Another road enters into auxiliary reactor 11 through regeneration guiding valve 26, regeneration transfer lime 18 and riser tube right of ownership 15, and catalyst recirculation is used.
C
4～C
8hydrocarbon 12 enters auxiliary reactor 11 bottoms after heat exchange, in auxiliary reactor 11, directly contacts with the high-temperature regenerated catalyst from revivifier 21, at catalyst surface, carries out rapidly thermo-negative reaction; Or a minute two-way ，Yi road enters auxiliary reactor 11 bottoms, another road enters riser reactor 15 bottoms and high-temperature regenerated catalyst contact reacts from revivifier 21, and the reaction effluent of riser reactor 15 enters auxiliary reactor 11; The reaction gas 9 of auxiliary reactor 11 is drawn after auxiliary reactor cyclonic separator 10 is removed carried secretly catalyzer, mix with reaction gas 7 from main reactor 5 tops or deliver to respectively rear olefin separation system and carry out separatedly, obtaining the object products such as ethene and propylene.
In auxiliary reactor 11, after reaction, the reclaimable catalyst of carbon distribution enters stripping stage 13 strippings to be generated, remove the reaction gas that reclaimable catalyst carries, reclaimable catalyst after stripping is through guiding valve 25 to be generated and reclaimable catalyst transfer lime 16, under the conveying of nitrogen, enter revivifier 21, in revivifier 21, contact coke burning regeneration with main air.Catalyzer after regeneration enters revivifier stripping stage 17 strippings, and the regenerated catalyst after stripping, through regeneration guiding valve 26, regeneration transfer lime 18, riser reactor 15, enters auxiliary reactor 11 and recycles.
As shown in Figure 2, a kind of device schematic diagram that utilizes oxygenatedchemicals to produce alkene, comprise main reactor 5, auxiliary reactor 11 and a revivifier 21, riser reactor 15 forms, between main reactor 5 and revivifier 21, by the second reclaimable catalyst transfer lime 23 and the second regenerated catalyst 28, be communicated with, between auxiliary reactor 11 and revivifier 21, by the first reclaimable catalyst transfer lime 16 and the first regenerated catalyst 18, be communicated with, riser reactor 15 is communicated with auxiliary reactor 11 and revivifier 21 by the first regenerated catalyst 18.
Oxygenatedchemicals 3 enters main reactor 5 bottoms with gas phase form, contact with the high-temperature regenerated catalyst from revivifier 21, there is strong exothermal reaction, resultant of reaction carries out catalyst separating through main reactor cyclonic separator 6, the reaction gas 7 that is rich in the low-carbon alkenes such as ethene and propylene after separating catalyst is by main reactor 5 Base top contacts, deliver to rear portion chilling water wash system, pass through chilling, washing further reduces the temperature of reaction gas, the catalyst fines simultaneously carrying in washing reaction gas, by washing, the most of water in reaction gas is carried out to separation, then deliver to the separation of olefins unit at rear portion.In separation of olefins unit, reaction gas is carried out to separation, the object product ethene and the propylene that obtain go out device, C
4～C
8hydrocarbon is as the charging of auxiliary reactor 11 and riser reactor.
The reclaimable catalyst of the carbon distribution after separation enters main reactor stripping stage 2 strippings, remove the reaction gas that reclaimable catalyst carries, reclaimable catalyst after stripping, through guiding valve 1 to be generated and reclaimable catalyst transfer lime 23, enters revivifier 21 under the conveying of nitrogen, at the interior coke burning regeneration of revivifier 21.Catalyzer after regeneration enters revivifier stripping stage 17 strippings, and the regenerated catalyst after stripping, through regeneration guiding valve 27, regeneration transfer lime 28, enters main reactor 5 and recycles.
C
4～C
8hydrocarbon 12 enters auxiliary reactor 11 bottoms after heat exchange, in auxiliary reactor 11, directly contacts with the high-temperature regenerated catalyst from revivifier 21, at catalyst surface, carries out rapidly thermo-negative reaction; Or a minute two-way ，Yi road enters auxiliary reactor 11 bottoms, another road enters riser reactor 15 bottoms and high-temperature regenerated catalyst contact reacts from revivifier 21, and the reaction effluent of riser reactor 15 enters auxiliary reactor 11; The reaction gas 9 of auxiliary reactor 11 is drawn after auxiliary reactor cyclonic separator 10 is removed carried secretly catalyzer, mix with reaction gas 7 from main reactor 5 tops or deliver to respectively rear olefin separation system and carry out separatedly, obtaining the object products such as ethene and propylene.
In auxiliary reactor 11, after reaction, the reclaimable catalyst of carbon distribution enters stripping stage 13 strippings to be generated, remove the reaction gas that reclaimable catalyst carries, reclaimable catalyst after stripping is through guiding valve 25 to be generated and reclaimable catalyst transfer lime 16, under the conveying of nitrogen, enter revivifier 21, in revivifier 21, contact coke burning regeneration with main air.Catalyzer after regeneration enters revivifier stripping stage 17 strippings, and the regenerated catalyst after stripping, through regeneration guiding valve 26, regeneration transfer lime 18, riser reactor 15, enters auxiliary reactor 11 and recycles.
The regenerated flue gas of revivifier 21 after cyclonic separator 20 is removed the catalyzer carrying, is delivered to residual neat recovering system and is reclaimed after heat, by smoke stack emission atmosphere after double slide valve, step-down orifice plate.
Oxygenatedchemicals 3 enters main reactor 5 bottoms with gas phase form, contact with the high-temperature regenerated catalyst from revivifier 21, there is strong exothermal reaction, resultant of reaction carries out catalyst separating through main reactor cyclonic separator 6, the reaction gas 7 that is rich in the low-carbon alkenes such as ethene and propylene after separating catalyst is by main reactor 5 Base top contacts, deliver to rear portion chilling water wash system, pass through chilling, washing further reduces the temperature of reaction gas, the catalyst fines simultaneously carrying in washing reaction gas, by washing, the most of water in reaction gas is carried out to separation, then deliver to the separation of olefins unit at rear portion.In separation of olefins unit, reaction gas is carried out to separation, the object product ethene and the propylene that obtain go out device, C
4～C
8hydrocarbon is as auxiliary reactor charging.
The reclaimable catalyst of the carbon distribution after separation enters main reactor stripping stage 2 strippings, remove the reaction gas that reclaimable catalyst carries, reclaimable catalyst after stripping, through guiding valve 1 to be generated and reclaimable catalyst transfer lime 23, enters revivifier 21 under the conveying of nitrogen, at the interior coke burning regeneration of revivifier 21.Catalyzer after regeneration enters revivifier stripping stage 17 strippings, and the regenerated catalyst after stripping, through regeneration guiding valve 27, regeneration transfer lime 28, enters main reactor 5 and recycles.
The regenerated flue gas 19 of revivifier 21 after cyclonic separator 20 is removed the catalyzer carrying, is delivered to residual neat recovering system and is reclaimed after heat, by smoke stack emission atmosphere after guiding valve, step-down orifice plate.
Oxygenatedchemicals 3 enters main reactor 5 bottoms with gas phase form, contact with the high temperature reclaimable catalyst from revivifier 21, there is strong exothermal reaction, resultant of reaction carries out separation through main reactor cyclonic separator 6, after separation, be rich in the low-carbon alkene reaction gases 7 such as ethene and propylene by main reactor 5 Base top contacts, and by auxiliary reactor 11 reaction gas 9 out, mix or deliver to respectively the separation of olefins unit at rear portion.In separation of olefins unit, reaction gas is carried out to separation, the object product ethene and the propylene that obtain go out device, C
4～C
8hydrocarbon 12 enters auxiliary reactor 11 bottoms after heat exchange, in auxiliary reactor 11, directly contacts with the high-temperature regenerated catalyst from revivifier 21, at catalyst surface, carries out rapidly thermo-negative reaction; Or a minute two-way ，Yi road enters auxiliary reactor 11 bottoms, another road enters riser reactor 15 bottoms and high-temperature regenerated catalyst contact reacts from revivifier 21, and the reaction effluent of riser reactor 15 enters auxiliary reactor 11; The reaction gas 9 of auxiliary reactor 11 is drawn after auxiliary reactor cyclonic separator 10 is removed carried secretly catalyzer, mix with reaction gas 7 from main reactor 5 tops or deliver to respectively rear olefin separation system and carry out separatedly, obtaining the object products such as ethene and propylene.
The reclaimable catalyst of the carbon distribution after separation enters main reactor stripping stage 2 strippings, remove the reaction gas that reclaimable catalyst carries, reclaimable catalyst after stripping, through guiding valve 1 to be generated and reclaimable catalyst transfer lime 23, enters revivifier 21 under the conveying of nitrogen, at the interior coke burning regeneration of revivifier 21.Catalyzer after regeneration enters revivifier stripping stage 17 strippings, and the regenerated catalyst after stripping, through regeneration guiding valve 26, regeneration transfer lime 18, riser reactor 15, enters auxiliary reactor 11 and recycles.
In auxiliary reactor 11, after reaction, the reclaimable catalyst of carbon distribution enters stripping stage 13 strippings to be generated, remove the reaction gas that reclaimable catalyst carries, the all or part of main reactor 5 that enters of reclaimable catalyst after stripping, or minute two-way, one tunnel is through guiding valve 25 to be generated and reclaimable catalyst transfer lime 16, under the conveying of nitrogen, enter revivifier 21, in revivifier 21, contact coke burning regeneration with main air and recycle.One tunnel, through guiding valve 24 to be generated and reclaimable catalyst transfer lime 14, is delivered to main reactor 5 and is recycled under the conveying of steam.
The regenerated flue gas of revivifier 21 after cyclonic separator 20 is removed the catalyzer carrying, is delivered to residual neat recovering system and is reclaimed after heat, by smoke stack emission atmosphere after double slide valve, step-down orifice plate.
Main reactor 5, auxiliary reactor 11, revivifier 21 are fluidized-bed pattern, can be bubbling bed, turbulent bed or fast bed streaming mode, preferably Turbulent Fluidization operational stage.Main reactor 5 is established interior heat collector and/or external warmer, preferably establishes interior heat collector 4, and heat-obtaining medium can be oxygen-containing compound material 3 or water etc.Revivifier 21 is established interior heat collector and/or external warmer 22, to take revivifier away, burns superfluous heat.Revivifier 21 can be realized incomplete regen-eration and holomorphosis operation.
Claims (17)
1. a device that utilizes oxygenatedchemicals to produce alkene, by main reactor (5), auxiliary reactor (11) and revivifier (21), formed, it is characterized in that: between main reactor (5) and revivifier (21), by the second reclaimable catalyst transfer lime (23) and the second regenerated catalyst (28), be communicated with, between auxiliary reactor (11) and revivifier (21), by the first reclaimable catalyst transfer lime (16) and the first regenerated catalyst (18), be communicated with.
2. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: be also provided with riser reactor (15), riser reactor (15) is communicated with auxiliary reactor (11) and revivifier (21) by the first regenerated catalyst (18).
3. according to a kind of device that utilizes oxygenatedchemicals to produce alkene described in claim 1 and 2, be characterised in that: described riser reactor (15) is communicated with main reactor (5) and revivifier 21 by the first regenerated catalyst (18).
4. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: described main reactor (5) and auxiliary reactor (11) are provided with outlet, outlet is communicated with separation system.
5. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: described auxiliary reactor (11) bottom is provided with auxiliary reactor reclaimable catalyst stripping stage (13).
6. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: described auxiliary reactor reclaimable catalyst stripping stage (13) top is communicated with auxiliary reactor (11) bottom, and bottom is communicated with revivifier (21) by the first reclaimable catalyst transfer lime (16).
7. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: described main reactor (5) and revivifier (21) bottom are respectively equipped with the first reclaimable catalyst stripping stage (2) and regenerated catalyst stripping stage (17).
8. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: the first described reclaimable catalyst stripping stage (2) top is communicated with main reactor (5) bottom, and bottom is communicated with revivifier (21) by the second reclaimable catalyst transfer lime (23).
9. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: described regenerated catalyst stripping stage (17) top is communicated with revivifier (21), bottom is communicated with and is communicated with reactor (5) and auxiliary reactor (11) by the second regenerated catalyst (28) and the first regenerated catalyst (18) respectively.
10. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, be characterised in that: described main reactor (5), auxiliary reactor (11) and revivifier (21) inside are provided with the second cyclonic separator (6) and the first cyclonic separator (20).
11. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, is characterised in that: described auxiliary reactor (11), riser reactor (15) are equipped with C
4～C
8hydrocarbon entrance.
12. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, is characterised in that: described main reactor (5) is provided with heat collector (4).
13. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, is characterised in that: described main reactor (5) is provided with interior heat collector (4).
14. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, is characterised in that: described revivifier (21) is provided with heat collector (22).
15. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, is characterised in that: described revivifier (21) is provided with external warmer (22).
16. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, is characterised in that: described main reactor (5), auxiliary reactor (11) and revivifier (21) are a kind of among fluidized-bed, bubbling bed, fast fluidized bed.
17. according to a kind of device that utilizes oxygenatedchemicals to produce alkene claimed in claim 1, is characterised in that: described main reactor (5), auxiliary reactor (11) and revivifier (21) are turbulent bed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210244617.9A CN103539611B (en) | 2012-07-09 | 2012-07-09 | A kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210244617.9A CN103539611B (en) | 2012-07-09 | 2012-07-09 | A kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103539611A true CN103539611A (en) | 2014-01-29 |
| CN103539611B CN103539611B (en) | 2016-06-08 |
Family
ID=49963524
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210244617.9A Active CN103539611B (en) | 2012-07-09 | 2012-07-09 | A kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103539611B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107043317A (en) * | 2017-04-26 | 2017-08-15 | 神华集团有限责任公司 | Methanol-to-olefins device and method |
| CN107081116A (en) * | 2017-04-26 | 2017-08-22 | 神华集团有限责任公司 | Methanol-to-olefins device and method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4433188A (en) * | 1981-09-09 | 1984-02-21 | Basf Aktiengesellschaft | Preparation of olefins from methanol and/or dimethyl ether |
| US20040102667A1 (en) * | 2002-11-21 | 2004-05-27 | Vora Bipin V. | Process for enhanced olefin production |
| US20070167662A1 (en) * | 2003-09-19 | 2007-07-19 | Duplan Jean L | Method for the direct conversion of a charge containing olefins comprising a minimum of four or five carbon atoms, for producing propylene |
| CN101633593A (en) * | 2008-07-26 | 2010-01-27 | 中国石化集团洛阳石油化工工程公司 | Conversion method of C4 and heavier components |
| CN101891576A (en) * | 2010-07-12 | 2010-11-24 | 兆威兴业有限公司 | Process and device for preparing low-carbon olefin by methanol and/or dimethyl ether |
| CN102276402A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Combined reaction apparatus for producing low-carbon olefin |
| CN102276386A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Production method of light olefins |
-
2012
- 2012-07-09 CN CN201210244617.9A patent/CN103539611B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4433188A (en) * | 1981-09-09 | 1984-02-21 | Basf Aktiengesellschaft | Preparation of olefins from methanol and/or dimethyl ether |
| US20040102667A1 (en) * | 2002-11-21 | 2004-05-27 | Vora Bipin V. | Process for enhanced olefin production |
| US20070167662A1 (en) * | 2003-09-19 | 2007-07-19 | Duplan Jean L | Method for the direct conversion of a charge containing olefins comprising a minimum of four or five carbon atoms, for producing propylene |
| CN101633593A (en) * | 2008-07-26 | 2010-01-27 | 中国石化集团洛阳石油化工工程公司 | Conversion method of C4 and heavier components |
| CN102276402A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Combined reaction apparatus for producing low-carbon olefin |
| CN102276386A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Production method of light olefins |
| CN101891576A (en) * | 2010-07-12 | 2010-11-24 | 兆威兴业有限公司 | Process and device for preparing low-carbon olefin by methanol and/or dimethyl ether |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107043317A (en) * | 2017-04-26 | 2017-08-15 | 神华集团有限责任公司 | Methanol-to-olefins device and method |
| CN107081116A (en) * | 2017-04-26 | 2017-08-22 | 神华集团有限责任公司 | Methanol-to-olefins device and method |
| CN107043317B (en) * | 2017-04-26 | 2020-05-01 | 神华集团有限责任公司 | Device and method for preparing olefin from methanol |
| CN107081116B (en) * | 2017-04-26 | 2020-05-01 | 神华集团有限责任公司 | Device and method for preparing olefin from methanol |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103539611B (en) | 2016-06-08 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101633593B (en) | Conversion method of C4 and heavier components | |
| CN101165017B (en) | Production increasing method for propylene | |
| CN102463086B (en) | Reaction device for co-producing low-carbon olefin and p-xylene | |
| CN103539598B (en) | A kind of oxygenatedchemicals produces the method for low-carbon alkene | |
| CN101165026B (en) | Method for producing ethylene and propylene from methanol and dimethyl ether | |
| JP6189544B2 (en) | Process for producing lower olefins from oxygen-containing compounds | |
| CN102320912B (en) | Method for maximizing total ethylene and propylene yield in process of preparing low-carbon olefin by oxygen compound conversion | |
| US8735639B2 (en) | Preparing a light-olefin containing product stream from an oxygenate-containing feed steam using reactors directing a flow of a fluidized dual-function catalyst system | |
| CN110117214A (en) | A kind of device and method of methanol Efficient Conversion producing light olefins | |
| CN111807916B (en) | Device for producing low-carbon olefin by efficient oxygen-containing compound | |
| JP2017501989A (en) | Method for producing lower olefin from oxygen-containing compound and apparatus used therefor | |
| CN101165025A (en) | Method for producing ethylene and propylene from methanol or dimethyl ether | |
| CN101195554B (en) | Method for producing low carbon olefin hydrocarbon with C4 hydrocarbon | |
| CN104177210B (en) | The method of alcohol ether compound coproduction alkene and aromatic hydrocarbons | |
| CN103539610B (en) | A kind of oxygenatedchemicals produces olefin hydrocarbon apparatus | |
| CN111875465B (en) | Method for producing low-carbon olefin by oxygen-containing compound | |
| CN102268286A (en) | C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device | |
| CN103539611B (en) | A kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons | |
| CN103553863B (en) | Method and system for preparing propylene by using methanol | |
| CN101165027B (en) | Method for producing ethylene and propylene from oxygen-containing compounds | |
| CN103539616B (en) | A kind of oxygenatedchemicals olefins process | |
| CN111871343A (en) | Device for producing low-carbon olefin by using oxygen-containing compound | |
| CN101165023B (en) | Method for increasing selectivity and yield of ethylene and propylene | |
| CN111875464B (en) | Method for producing low-carbon olefin by high-efficiency oxygen-containing compound | |
| CN107266279A (en) | A kind of method by oxygenatedchemicals preparing low-carbon olefins |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |