CN103539611B - A kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons - Google Patents
A kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons Download PDFInfo
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- CN103539611B CN103539611B CN201210244617.9A CN201210244617A CN103539611B CN 103539611 B CN103539611 B CN 103539611B CN 201210244617 A CN201210244617 A CN 201210244617A CN 103539611 B CN103539611 B CN 103539611B
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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
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Abstract
The present invention discloses a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons, overcome the defect that prior art productivity of low carbon olefin hydrocarbon is low, main reactor (5), auxiliary reactor (11) and revivifier (21) composition, it is connected with the 2nd regenerated catalyst (28) by the 2nd reclaimable catalyst transfer lime (23) between main reactor (5) with revivifier (21), it is connected with the first regenerated catalyst (18) by the first reclaimable catalyst transfer lime (16) between auxiliary reactor (11) with revivifier (21).
Description
Technical field:
The present invention relates to and prepare hydrocarbon technical field from one or several non-hydrocarbon compounds, in particular to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons
Background technology:
Light aromatics based on the light olefin of ethene, propylene, divinyl with based on benzene, toluene, dimethylbenzene is the basic raw material of petrochemical complex. Current ethylene production mainly relies on the tube furnace steam cracking technique of light naphthar raw material. Due to the shortage of crude resources and the raising day by day of price, naphtha resource has more and more seemed not enough, and the production cost of low-carbon alkene is more and more higher. The ethylene production route that positive active development raw material sources are abundanter both at home and abroad, 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 based on the reaction product of ethene, propylene, just be subject to domestic and international attention widely.
It is typical oxygen-containing organic compound by the oxygen-containing organic compound of representative of methyl alcohol or dme, produces primarily of synthetic gas that is coal-based or Sweet natural gas base. The oxygen-containing organic compound being representative in order to methyl alcohol is that raw material production mainly contains the MTO technology of American UOP/Hyro company, Germany's MTP technology of Lurgi company and the methanol-to-olefins DMTO technology of the Dalian Chemistry and Physics Institute of the Chinese Academy of Sciences at present based on the low-carbon alkene technique of ethene and propylene.
The reaction characteristics producing low-carbon alkene technique abbreviation MTO taking methyl alcohol as representing oxygenatedchemicals is that rapid reaction, strong heat release and alcohol agent are lower, carries out reacting and regenerating in the dense fluidized bed bioreactor of continuous print reaction-regeneration. The high-temperature oil gas being rich in the low-carbon alkene such as ethene and propylene that reaction generates, it is necessary to carry out the washing of anxious cold-peace, removes wherein after catalyzer and cooling, is sent to bottom olefin separation system and is separated. The object product of MTO process unit is ethene and propylene, byproduct liquefied gas, C5 +Above component and fuel gas, wherein C4 +Carbon base absorption rate be about 10%. Ethene and the propylene how this part low value product is converted into high added value is the problem of pendulum in face of vast scientific research and engineering design personnel always.
In recent years, MTO has become the focus and emphasis of insider's research. People conduct extensive research from aspects such as work flow, catalyzer, processing condition and device structures and explore, and obtain gratifying achievement, but about how by the byproduct C in MTO process products4 +The ethene and the propylene document report 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 to4��C7Middle 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 alkene2��C8Send into flash trapping stage device, separate C2��C3Light olefin and C4 +Heavy olefin fraction; (2) olefin fraction will be weighed and send into the second-order separation district, separate the 2nd light olefin fraction, C4��C7Middle matter olefin fraction and C7 +Heavy olefin fraction; (3) middle matter olefin fraction is sent into cracking of olefins reactor, make crack materials at least partially be C2��C3Alkene; (4) C that cracking is formed2��C3Alkene some return to the second-order separation district. Another part is drawn out of; (5) the 2nd light olefin fraction that the second-order separation is distinguished some return to flash trapping stage district.
US5914433 patent relates to the technique that OTO produces polymerization-grade alkene. It is characterized in the mixed butene in product and heavy constituent are carried out cracking, thus improves the output of ethene and propylene. Cracking reaction carries out in riser cracking district or independent cracking district, provides handiness to technique. This technique overcomes the equilibrium-limited of silicon aluminium phosphate catalyst, also improve the life-span of catalyzer, it is to increase catalyzer is transforming the stability in district.
Main processing step is: (1) oxygenatedchemicals (C1��C4A kind of alcohol or a kind of ether) raw material thinner dilutes, adopts silicon aluminium phosphate catalyst (SAPO-34, SAPO-17 or its mixture) and fluidized-bed reactor, obtain Light olefin products logistics at reaction conditions; (2) ethene, propylene and mixed butene heavy constituent is obtained after stream of light olefins being separated; (3) take out reclaimable catalyst at least partially to go to regenerate; (4) the catalyzer part after regenerating returns 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 2nd product stream, generates extra ethene and propylene; (5) part the 2nd product stream is returned to fluidized bed reaction zone.
The patent CN1803738 of American UOP company discloses and uses mobile technology and independent heavy alkene change step that oxygenatedchemicals is converted into propylene. These patent main points establish two reaction zones, and first moving bed reaction district uses the dual-function catalyst with SAPO and ZSM function, and oil gas product mainly propylene, has a small amount of ethene, butylene and C simultaneously4 +Alkene, C1��C4Stable hydrocarbon, a small amount of aromatic hydrocarbon and water. Liquid hydrocarbon three part of the aqueous phase that be divided into, after the anxious cold separation of reaction oil gas, the steam being rich in propylene, 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, it may also be useful to be different ZSM, SAPO dual-function catalyst of portfolio ratio, temperature of reaction is higher than the first reaction zone more than 15 DEG C, it is intended that by C4 +Conversion of olefines is propylene is the product led, and estimates to be similar to disclosed Atofina company OCPC4+Olefin conversion process catalyzer. What the first reactor generated contains ethene, butylene and C4 +Alkene, C1��C4The gas-phase product of stable hydrocarbon, a small amount of aromatic hydrocarbon is separated further, wherein C4 +Alkene removes the 2nd further conversion of olefines of reactor.
The patent CN1419527 of ExxonMobil company of the U.S. discloses C in a kind of oxygenate conversion reaction4And C4 +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 C4 +Alkene, by the first olefin product stream with at least partly from the catalyzer introducing second reaction zone in the first reaction zone, revivifier introduced by least part of catalyzer in second reaction zone, all catalyzer are at regeneration in-situ regeneration, the first olefin product stream is made to contact with at least part of catalyzer in second reaction zone, C4 +Conversion of olefines becomes light olefin.
The patent US4433188 of BASF company discloses a kind of methyl alcohol/dimethyl ether alkene technology, and this invention adopts silicic acid B catalyst, comprises two-stage reaction and two-phase seperation. Material benzenemethanol/dme contacts with catalyzer in first paragraph reaction zone and catalytic cracking reaction occurs, and product separates C through the first separation system2��C4Alkene and C1��C4Alkane, C5 +Component enters second reaction zone and contacts generation scission reaction with catalyzer, and product, through the 2nd separation system Arene removal component, then returns the first separation system. The principal feature of this patent is circulation C5 +Component is reacted under different conversion zones and condition from raw material.
The patent CN1962573A of Tsing-Hua University discloses 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 characterised in that, the C in the product of low-carbon alkene preparation technology2And C2Following component, C4And C4After above component and object product propylene separation, circulation returns alkene in fluidized-bed catalytic cracking reaction device and turns reaction zone and carry out conversion of olefines, and by control operational condition, highly selective produces propylene. C2 -��C4 +Two bursts of logistics had before returning to olefin reaction district speeds to put on a small quantity, to avoid inert component to accumulate. Correspondingly, it is proposed that can be used as the multicompartment fluidized bed structure of reactor in main reaction region or olefin reaction district. This invention has the advantage that height always received by propylene, selectivity is strong.
In sum, although prior art relate to C in some oxygenate conversion reaction4And C4 +Return smelting method, but also exist and use different catalyst systems, it is necessary to build the C that independent investment is higher4 +Cracking unit, olefin cracking system thermal is uneven, it is necessary to be C specially4 +Heat needed for cracker offer, cracking condition is restricted, and transformation efficiency is lower; Only pay close attention to C in unconverted raw material and product5 +Component, what usually do not relate to butylene returns refining problem; The technology of part product for the purpose of propylene is also had to improve propylene total recovery by by product circulation, but majority adopts the simple form that by product loops back former reactor.
Summary of the invention:
The object of the present invention is just to provide a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons, overcomes that prior art productivity of low carbon olefin hydrocarbon is low, flow process is complicated, invest high defect.
The present invention provides a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons, it is made up of main reactor 5, auxiliary reactor 11 and revivifier 21, it is characterized in that: be connected with the 2nd regenerated catalyst 28 by the 2nd reclaimable catalyst transfer lime 23 between main reactor 5 with revivifier 21, it is connected with the first regenerated catalyst 18 by the first reclaimable catalyst transfer lime 16 between auxiliary reactor 11 with revivifier 21.
Described a kind of oxygenatedchemicals produces olefin hydrocarbon apparatus, is characterised in that: be also provided with riser reactor 15, and riser reactor 15 is connected with revivifier 21 with auxiliary reactor 11 by the first regenerated catalyst 18.
Described a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons, is characterised in that: be also provided with riser reactor 15, riser reactor 15 is connected with revivifier 21 with main reactor 5 by the first regenerated catalyst 18.
Described main reactor 5 and auxiliary reactor 11 are provided with outlet, and outlet is connected with separation system.
Auxiliary reactor reclaimable catalyst stripping stage 13 it is provided with bottom described auxiliary reactor 11.
Described auxiliary reactor reclaimable catalyst stripping stage 13 top is connected with bottom auxiliary reactor 11, and bottom is connected with revivifier 21 by the first reclaimable catalyst transfer lime 16.
It is respectively equipped with the first reclaimable catalyst stripping stage 2 and regenerated catalyst stripping stage 17 bottom described main reactor 5 and revivifier 21, first reclaimable catalyst stripping stage 2 top is connected with bottom main reactor 5, bottom is connected with revivifier 21 by the 2nd reclaimable catalyst transfer lime 23, regenerated catalyst stripping stage 17 top is connected with revivifier 21, and bottom is connected with the first regenerated catalyst 18 by the 2nd regenerated catalyst 28 respectively and is connected with auxiliary reactor 11 with reactor 5.
Described main reactor 5, auxiliary reactor 11 and revivifier 21 inside are provided with the 2nd cyclonic separator 6 and the first cyclonic separator 20.
Described auxiliary reactor 11 and riser reactor 15 are provided with C4��C8Hydrocarbon entrance.
Described main reactor 5 is provided with heat collector 4, it is preferable that interior heat collector 4.
Described main reactor 5, auxiliary reactor 11, revivifier 21 are the one among fluidized-bed, bubbling bed, fast fluidized bed, it is preferable that turbulent bed.
Described revivifier 21 is provided with heat collector 22, it is preferable that external warmer 22.
Compared with prior art, the present invention is a kind of utilizes the device of oxygenatedchemicals producing olefinic hydrocarbons to have 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 C4��C8It is thermo-negative reaction that hydrocarbon transforms, and temperature of reaction is higher, and agent/material is bigger, and catalyst recirculation mode is parallel operation, it is ensured that oxygenatedchemicals and C4��C8Hydrocarbon reacts respectively under the operational condition optimized;
(2) C that this device is produced4��C8Hydrocarbon can carry out back refining, it is also possible to does not return refining, and device operation understands;
(3) owing to adopting auxiliary reactor, ethene+propene yield improves 4��6 percentage points;
(4) oxygenatedchemicals and C4��C8Hydrocarbon reaction catalyzer used is a kind of catalyzer, shares a revivifier, reduces revivifier height and reduce investment outlay.
Below in conjunction with the drawings and specific embodiments, the present invention is described further. But it does not limit the scope of the invention.
Accompanying drawing explanation
A kind of device schematic diagram utilizing oxygenatedchemicals producing olefinic hydrocarbons of Fig. 1 the present invention.
Fig. 2 is the device schematic diagram that another kind of the present invention utilizes oxygenatedchemicals producing olefinic hydrocarbons.
Wherein:
1. guiding valve to be generated, 2. the first reclaimable catalyst stripping stage, 3. oxygenatedchemicals, 4. heat collector, 5. main reactor, 6. the 2nd cyclonic separator, 7. main reactor reaction oil gas, 9. auxiliary reactor reaction oil gas, 10. auxiliary reactor cyclonic separator, 11. auxiliary reactors, 12.C4��C8Hydrocarbon, 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. the 2nd reclaimable catalyst transfer limes, 24. first guiding valves to be generated, 25. the 2nd guiding valves to be generated, 26. first regeneration guiding valves, 27. the 2nd regeneration guiding valves, 28. the 2nd regenerated catalyst.
Embodiment
It is illustrated in figure 1 a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons of the present invention, comprise auxiliary reactor 11, main reactor 5 and revivifier 21, between auxiliary reactor 11, main reactor 5, it is provided with the first reclaimable catalyst transfer lime 14 by the first reclaimable catalyst transfer lime 14, auxiliary reactor 11 is connected with main reactor 5. oxygenatedchemicals 3 enters main reactor 5 bottom with gas phase, 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 being rich in the low-carbon alkene such as ethene and propylene after separating catalyst is by main reactor 5 Base top contact, deliver to rear portion quenched water and wash system, logical over-quenching, washing reduces the temperature of reaction gas further, the catalyst fines simultaneously carried in washing reaction gas, by washing, the most of water in reaction gas is separated, then the separation of olefins unit at rear portion is delivered to. in separation of olefins unit, being separated by reaction gas, the object product ethene obtained and propylene go out device, C4��C8Hydrocarbon 12 is as auxiliary reactor charging.
The reclaimable catalyst of the long-pending carbon after separation enters main reactor stripping stage 2 stripping, 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, coke burning regeneration in revivifier 21. Catalyzer after regeneration enters revivifier stripping stage 17 stripping, and the regenerated catalyst after stripping divides two-way, and a 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 uses.
C4��C8Hydrocarbon 12 enters bottom auxiliary reactor 11 after heat exchange, directly contacts with the high-temperature regenerated catalyst from revivifier 21 in auxiliary reactor 11, carries out rapidly thermo-negative reaction at catalyst surface; Or point two-way, a road enters bottom auxiliary reactor 11, another road enter bottom riser reactor 15 with the high-temperature regenerated catalyst contact reacts from revivifier 21, the reaction effluent of riser reactor 15 enters auxiliary reactor 11; The reaction gas 9 of auxiliary reactor 11 is drawn after the catalyzer that auxiliary reactor cyclonic separator 10 removes entrained with, mix with the reaction gas 7 from main reactor 5 top or deliver to rear olefin separation system respectively and be separated, obtain the object product such as ethene and propylene.
In auxiliary reactor 11, after reaction, the reclaimable catalyst of long-pending carbon enters stripping stage 13 stripping 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 wind. Catalyzer after regeneration enters revivifier stripping stage 17 stripping, 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 utilizing oxygenatedchemicals producing olefinic hydrocarbons, comprise main reactor 5, auxiliary reactor 11 and a revivifier 21, riser reactor 15 forms, it is connected with the 2nd regenerated catalyst 28 by the 2nd reclaimable catalyst transfer lime 23 between main reactor 5 with revivifier 21, being connected with the first regenerated catalyst 18 by the first reclaimable catalyst transfer lime 16 between auxiliary reactor 11 with revivifier 21, riser reactor 15 is connected with revivifier 21 with auxiliary reactor 11 by the first regenerated catalyst 18.
Oxygenatedchemicals 3 enters main reactor 5 bottom with gas phase, 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 being rich in the low-carbon alkene such as ethene and propylene after separating catalyst is by main reactor 5 Base top contact, deliver to rear portion quenched water and wash system, logical over-quenching, washing reduces the temperature of reaction gas further, the catalyst fines simultaneously carried in washing reaction gas, by washing, the most of water in reaction gas is separated, then the separation of olefins unit at rear portion is delivered to. in separation of olefins unit, being separated by reaction gas, the object product ethene obtained and propylene go out device, C4��C8Hydrocarbon is as the charging of auxiliary reactor 11 and riser reactor.
The reclaimable catalyst of the long-pending carbon after separation enters main reactor stripping stage 2 stripping, 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, coke burning regeneration in revivifier 21. Catalyzer after regeneration enters revivifier stripping stage 17 stripping, and the regenerated catalyst after stripping, through regeneration guiding valve 27, regeneration transfer lime 28, enters main reactor 5 and recycles.
C4��C8Hydrocarbon 12 enters bottom auxiliary reactor 11 after heat exchange, directly contacts with the high-temperature regenerated catalyst from revivifier 21 in auxiliary reactor 11, carries out rapidly thermo-negative reaction at catalyst surface; Or point two-way, a road enters bottom auxiliary reactor 11, another road enter bottom riser reactor 15 with the high-temperature regenerated catalyst contact reacts from revivifier 21, the reaction effluent of riser reactor 15 enters auxiliary reactor 11; The reaction gas 9 of auxiliary reactor 11 is drawn after the catalyzer that auxiliary reactor cyclonic separator 10 removes entrained with, mix with the reaction gas 7 from main reactor 5 top or deliver to rear olefin separation system respectively and be separated, obtain the object product such as ethene and propylene.
In auxiliary reactor 11, after reaction, the reclaimable catalyst of long-pending carbon enters stripping stage 13 stripping 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 wind. Catalyzer after regeneration enters revivifier stripping stage 17 stripping, 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 removing, through cyclonic separator 20, the catalyzer carried, after delivering to residual neat recovering system recovery heat after double slide valve, step-down orifice plate, by smoke stack emission air.
Oxygenatedchemicals 3 enters main reactor 5 bottom with gas phase, 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 being rich in the low-carbon alkene such as ethene and propylene after separating catalyst is by main reactor 5 Base top contact, deliver to rear portion quenched water and wash system, logical over-quenching, washing reduces the temperature of reaction gas further, the catalyst fines simultaneously carried in washing reaction gas, by washing, the most of water in reaction gas is separated, then the separation of olefins unit at rear portion is delivered to. in separation of olefins unit, being separated by reaction gas, the object product ethene obtained and propylene go out device, C4��C8Hydrocarbon is as auxiliary reactor charging.
The reclaimable catalyst of the long-pending carbon after separation enters main reactor stripping stage 2 stripping, 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, coke burning regeneration in revivifier 21. Catalyzer after regeneration enters revivifier stripping stage 17 stripping, 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 removing, through cyclonic separator 20, the catalyzer carried, after delivering to residual neat recovering system recovery heat after guiding valve, step-down orifice plate, by smoke stack emission air.
Oxygenatedchemicals 3 enters main reactor 5 bottom with gas phase, contact with the high temperature reclaimable catalyst from revivifier 21, there is strong exothermal reaction, resultant of reaction is separated through main reactor cyclonic separator 6, it is rich in the low-carbon alkene reaction gas such as ethene and propylene 7 by main reactor 5 Base top contact after separation, mixes with by auxiliary reactor 11 reaction gas 9 out or deliver to the separation of olefins unit at rear portion respectively. In separation of olefins unit, being separated by reaction gas, the object product ethene obtained and propylene go out device, C4��C8Hydrocarbon 12 enters bottom auxiliary reactor 11 after heat exchange, directly contacts with the high-temperature regenerated catalyst from revivifier 21 in auxiliary reactor 11, carries out rapidly thermo-negative reaction at catalyst surface; Or point two-way, a road enters bottom auxiliary reactor 11, another road enter bottom riser reactor 15 with the high-temperature regenerated catalyst contact reacts from revivifier 21, the reaction effluent of riser reactor 15 enters auxiliary reactor 11; The reaction gas 9 of auxiliary reactor 11 is drawn after the catalyzer that auxiliary reactor cyclonic separator 10 removes entrained with, mix with the reaction gas 7 from main reactor 5 top or deliver to rear olefin separation system respectively and be separated, obtain the object product such as ethene and propylene.
The reclaimable catalyst of the long-pending carbon after separation enters main reactor stripping stage 2 stripping, 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, coke burning regeneration in revivifier 21. Catalyzer after regeneration enters revivifier stripping stage 17 stripping, 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 long-pending carbon enters stripping stage 13 stripping to be generated, remove the reaction gas that reclaimable catalyst carries, reclaimable catalyst after stripping is all or part of enters main reactor 5, or point 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 wind recycle. One tunnel, through guiding valve 24 to be generated and reclaimable catalyst transfer lime 14, is delivered to main reactor 5 under the conveying of steam and is recycled.
The regenerated flue gas of revivifier 21, after removing, through cyclonic separator 20, the catalyzer carried, after delivering to residual neat recovering system recovery heat after double slide valve, step-down orifice plate, by smoke stack emission air.
Main reactor 5, auxiliary reactor 11, revivifier 21 are fluidized-bed pattern, it is possible to be bubbling bed, turbulent bed or fast bed streaming mode, it is preferable that turbulent flow fluidization operational stage. Main reactor 5 establishes interior heat collector and/or external warmer, it is preferable that establish interior heat collector 4, and heat-obtaining medium can be oxygen-containing compound material 3 or water etc. Revivifier 21 establishes interior heat collector and/or external warmer 22, burns superfluous heat to take revivifier away. Revivifier 21 can realize incomplete regen-eration and holomorphosis operation.
Claims (15)
1. one kind utilizes the device of oxygenatedchemicals producing olefinic hydrocarbons, by main reactor (5), auxiliary reactor (11) and revivifier (21) composition, it is characterized in that: be connected with the 2nd regenerated catalyst (28) by the 2nd reclaimable catalyst transfer lime (23) between main reactor (5) with revivifier (21), it is connected with the first regenerated catalyst (18) by the first reclaimable catalyst transfer lime (16) between auxiliary reactor (11) with revivifier (21), also it is provided with riser reactor (15), riser reactor (15) is connected with revivifier (21) with auxiliary reactor (11) by the first regenerated catalyst (18), or riser reactor (15) is connected with revivifier (21) with auxiliary reactor (11) by the first regenerated catalyst (18).
2. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, being characterised in that: described main reactor (5) and auxiliary reactor (11) are provided with outlet, outlet is connected with separation system.
3. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, it is characterised in that: described auxiliary reactor (11) bottom is provided with auxiliary reactor reclaimable catalyst stripping stage (13).
4. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, it is characterised in that: described auxiliary reactor reclaimable catalyst stripping stage (13) top is connected with auxiliary reactor (11) bottom, and bottom is connected with revivifier (21) by the first reclaimable catalyst transfer lime (16).
5. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, it is 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).
6. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, it is characterised in that: the first described reclaimable catalyst stripping stage (2) top is connected with main reactor (5) bottom, and bottom is connected with revivifier (21) by the 2nd reclaimable catalyst transfer lime (23).
7. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, being characterised in that: described regenerated catalyst stripping stage (17) top is connected with revivifier (21), bottom is connected with the first regenerated catalyst (18) by the 2nd regenerated catalyst (28) respectively and is connected with auxiliary reactor (11) with reactor (5).
8. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, it is characterised in that: described main reactor (5) inside is provided with the 2nd cyclonic separation (6), auxiliary reactor (11) inside is provided with auxiliary reactor cyclonic separator (10), and revivifier (21) inside is provided with the first cyclonic separator (20).
9. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, it is characterised in that: described auxiliary reactor (11), riser reactor (15) are equipped with C4��C8Hydrocarbon entrance.
10. according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, it is characterised in that: described main reactor (5) is provided with heat collector (4).
11., according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, are characterised in that: described main reactor (5) is provided with interior heat collector (4).
12., according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, are characterised in that: described revivifier (21) is provided with heat collector (22).
13., according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, are characterised in that: described revivifier (21) is provided with external warmer (22).
14., according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, are characterised in that: described main reactor (5), auxiliary reactor (11) and revivifier (21) are fluidized-bed, one among bubbling bed, fast fluidized bed.
15., according to a kind of device utilizing oxygenatedchemicals producing olefinic hydrocarbons according to claim 1, are characterised in that: described main reactor (5), auxiliary reactor (11) and revivifier (21) are turbulent bed.
Priority Applications (1)
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| 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 |
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| US4433188A (en) * | 1981-09-09 | 1984-02-21 | Basf Aktiengesellschaft | Preparation of olefins from methanol and/or dimethyl ether |
| 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 |
| 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 |
| 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 |
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| US7317133B2 (en) * | 2002-11-21 | 2008-01-08 | Uop Llc | Process for enhanced olefin production |
| FR2859994B1 (en) * | 2003-09-19 | 2005-10-28 | Inst Francais Du Petrole | PROCESS FOR THE DIRECT CONVERSION OF A CHARGE COMPRISING FOUR AND / OR FIVE ATOMIC CARBON OLEFINS FOR THE PRODUCTION OF PROPYLENE |
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| US4433188A (en) * | 1981-09-09 | 1984-02-21 | Basf Aktiengesellschaft | Preparation of olefins from methanol and/or dimethyl ether |
| 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 |
| 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 |
| 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 |
| 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 |
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