CN103537235A - Reaction device for preparing low-carbon olefin by using oxy-compounds - Google Patents
Reaction device for preparing low-carbon olefin by using oxy-compounds Download PDFInfo
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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 invention relates to a reaction device for preparing low-carbon olefin by using oxy-compounds, mainly for solving the problem in the prior art that the yield of low-carbon olefin is low. The reaction device for preparing the low-carbon olefin by using oxy-compounds mainly comprises a first fluidized bed reaction area 2, a second fluidized bed reaction area 4, a lifting tube regeneration area 11 and a dense phase bed regeneration area 12, wherein a distribution plate 3 is arranged at the top part of the first fluidized bed reaction area 2; the second first fluidized bed reaction area 4 is arranged above the distribution plate 3; a catalyst outlet is formed in the bottom of the first fluidized bed reaction area 2 and is respectively connected with the first fluidized bed reaction area 2 and the lifting tube regeneration area 11; the inlet end of the lifting tube regeneration area 11 is positioned below the outside of the first fluidized bed reaction area 2; the outlet end of the lifting tube regeneration area 11 is positioned inside the dense phase bed regeneration area 12; a catalyst outlet is formed in the bottom of the dense phase bed regeneration area 12 and is respectively connected with the first fluidized bed reaction area 2 and the lifting tube regeneration area 11; and a regeneration fume outlet 15 is formed in the top part of the dense phase bed regeneration area 12. Due to adoption of the technical scheme, the problem in the prior art is well solved. The reaction device can be applied to industrial production of low-carbon olefin.
Description
Technical field
The present invention relates to a kind of reaction unit of preparing low-carbon olefin from oxygen-containing compounds.
Background technology
Low-carbon alkene, ethene and propylene, be two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, but due to the limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people start to greatly develop the technology that alternative materials transforms ethene processed, propylene.Wherein, the important alternative materials of producing for low-carbon alkene of one class is oxygenatedchemicals, such as alcohols (methyl alcohol, ethanol), ethers (dimethyl ether, ethyl methyl ether), ester class (dimethyl carbonate, methyl formate) etc., these oxygenatedchemicals can be transformed by coal, natural gas, living beings equal energy source.Some oxygenatedchemicals can reach fairly large production, as methyl alcohol, can be made by coal or natural gas, and technique is very ripe, can realize the production scale of up to a million tonnes.Popularity due to oxygenatedchemicals source, add and transform the economy that generates low-carbon alkene technique, so by the technique of oxygen-containing compound conversion to produce olefine (OTO), particularly the technique by preparing olefin by conversion of methanol (MTO) is subject to increasing attention.
In 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 catalyst of MTO technique.SAPO-34 catalyst has very high selectivity of light olefin, and activity is also higher, and can make methanol conversion is reaction time of low-carbon alkene to be less than the degree of 10 seconds, more even reaches in the reaction time range of riser.
Technology and reactor that a kind of methanol conversion is low-carbon alkene in US 6166282, have been 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.Because reaction afterproduct gas is separated fast with catalyst, effectively prevented the generation of secondary response.Through analog computation, to compare with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyst all greatly reduce.But in the method, low-carbon alkene carbon base absorption rate is general all in 77% left and right, has the problem that yield of light olefins is lower.
The multiple riser reaction unit of having announced in CN 1723262 with central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises a plurality of riser reactors, gas solid separation district, a plurality of offset components etc., each riser reactor has the port of injecting catalyst separately, be pooled to the Disengagement zone of setting, catalyst and gas product are separated.In the method, low-carbon alkene carbon base absorption rate is general all between 75～80%, has equally the problem that yield of light olefins is lower.
All there is the problem that yield of light olefins 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 yield of light olefins existing in prior art, and a kind of reaction unit of new preparing low-carbon olefin from oxygen-containing compounds is provided.This device, for the production of low-carbon alkene, has advantages of that yield of light olefins is higher.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of reaction unit of preparing low-carbon olefin from oxygen-containing compounds, mainly comprise first fluidized bed reaction zone 2, the second fluidized bed reaction zone 4, riser renewing zone 11, dense bed renewing zone 12, first fluidized bed reaction zone 2 tops are provided with distribution grid 3, distribution grid 3 tops are the second fluidized bed reaction zone 4, the second 4 tops, fluidized bed reaction zone is provided with product gas outlet 13, bottom has catalyst outlet, respectively with first fluidized bed reaction zone 2, riser renewing zone 11 is connected, riser renewing zone 11 arrival ends are positioned at the outside below of first fluidized bed reaction zone 2, the port of export is positioned at dense bed renewing zone 12, 40～80% of riser renewing zone 11 height are positioned at first fluidized bed reaction zone 2 and the second fluidized bed reaction zone 3, 12 bottoms, dense bed renewing zone have catalyst outlet, respectively with first fluidized bed reaction zone 2, riser renewing zone 11 is connected, top has regenerated flue gas outlet 15.
In technique scheme, described first fluidized bed reaction zone 11 is fast bed; The catalyst of described the second fluidized bed reaction zone 3 returns to first fluidized bed reaction zone 2 after heat collector 8 heat exchange; The catalyst of described dense bed renewing zone 12 returns to riser renewing zone 11 after heat collector 18 heat exchange; Described distribution grid 3 percent openings are 40～75%.
In the present invention, described catalyst comprises SAPO-34 sial phosphorus molecular sieve; Described first fluidized bed reaction zone 2 reaction conditions are: reaction temperature is 400～500 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 1～3 meter per second; The second fluidized bed reaction zone 3 reaction conditions are: reaction temperature is 420～550 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 0.4～1 meter per second; The average carbon deposition quantity mass fraction of described regenerated catalyst is 0.01～1.5%; The regeneration condition of described riser renewing zone 11 is: reaction temperature is 550～680 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 4～10 meter per seconds; The regeneration condition of dense bed renewing zone 12 is: reaction temperature is 600～700 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and gas phase linear speed is 0.4～1 meter per second; The catalyst of described the second fluidized bed reaction zone 3 is at least divided into two parts, and in mass fraction, 40-80% returns to first fluidized bed reaction zone 2, and 20-60% enters riser renewing zone 11; Described regenerated catalyst is at least divided into two parts, and in mass fraction, 20-60% returns to first fluidized bed reaction zone 2, and 40-80% returns to riser renewing zone 11 after heat-obtaining; Described oxygenatedchemicals is at least one in methyl alcohol or dimethyl ether.
The computational methods of average coke content of the present invention are that carbon deposit quality on catalyst is divided by described catalyst quality.Carbon deposit measuring method on catalyst is as follows: will mix the comparatively uniform catalyst mix with carbon deposit, then weigh the band C catalyst of 0.1～1 gram, be put in pyrocarbon analyzer and burn, the carbon dioxide quality of burning and generating by infrared analysis, thus the carbonaceous amount on catalyst obtained.
The preparation method of sial phosphorus molecular sieve of the present invention is: first preparing molecular sieve presoma, is 0.03～0.6R by mole proportioning: (Si 0.01～0.98: Al 0.01～0.6: P 0.01～0.6): 2～500 H
2o, wherein R represents template, and template is triethylamine, and constitutive material mixed liquor obtains at the temperature of 100-250 ℃ after the crystallization of 1～10 hour; Again, molecular sieve presoma, ,Lv source, ,Gui source, phosphorus source, template, 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 the binding agent of required ratio, after the operating procedures such as, roasting dry through spraying, obtain final SAPO catalyst, the percetage by weight of binding agent in molecular sieve is between 10～90%.
Adopt method of the present invention, two reaction zones are set, first fluidized bed reaction zone 2 under higher linear speed for the most of methyl alcohol of the conversion of high selectivity, and generate low-carbon alkene, the second fluidized bed reaction zone 3 for transforming the above high-carbon hydrocarbon of C4 of unconverted methyl alcohol, generation, and further generates low-carbon alkene under higher temperature, lower linear speed.The coking yield that is low-carbon alkene due to methyl alcohol or dimethyl ether conversion is lower, the present invention adopts the method for riser renewing zone 11 and the 12 series connection two-stage regeneration of dense bed renewing zone, and the 40-80% of riser renewing zone 11 is placed in first fluidized bed reaction zone 2 and the second fluidized bed reaction zone 3, to keep the regeneration temperature of riser, this renovation process can be realized incomplete regen-eration and two kinds of modes of holomorphosis easily, reach the effect that regulates regenerative agent carbon distribution, can improve the yield of low-carbon alkene.
Adopt technical scheme of the present invention: described first fluidized bed reaction zone 11 is fast bed; The catalyst of described the second fluidized bed reaction zone 3 returns to first fluidized bed reaction zone 2 after heat collector 8 heat exchange; The catalyst of described dense bed renewing zone 12 returns to riser renewing zone 11 after heat collector 18 heat exchange; Described distribution grid 3 percent openings are 40～75%, and low-carbon alkene carbon base absorption rate reaches 84.85% (weight), than the low-carbon alkene carbon base absorption rate of prior art, exceed and can reach more than 3 percentage points, have obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of device of the present invention;
In Fig. 1,1 is oxygenate feedstock pipeline; 2 is first fluidized bed reaction zone; 3 is distribution grid; 4 is the second fluidized bed reaction zone; 5 is cyclone separator; 6 is product gas outlet pipeline; 7 is catalyst circulation pipe; 8 is heat collector; 9 is inclined tube to be generated; 10 is riser renewing zone regenerating medium suction line; 11 is riser renewing zone; 12 is dense bed renewing zone; 13 is dense bed renewing zone regenerating medium suction line; 14 is cyclone separator; 15 is regenerated flue gas outlet line; 16 is regenerator sloped tube; 17 is catalyst circulation pipe; 18 is heat collector.
Oxygenatedchemicals enters first fluidized bed reaction zone 2, contact with the catalyst that comprises sial phosphorus molecular sieve, the gaseous stream and the distribution grid 3 of catalyst through first fluidized bed reaction zone 2 tops that generate enter the second fluidized bed reaction zone 4, after gaseous stream and catalyst separation, enter centrifugal station, the catalyst of the second fluidized bed reaction zone 4 is at least divided into two parts, a part is returned to first fluidized bed reaction zone 2, a part enters riser renewing zone 11, then be promoted to dense bed renewing zone 12, form regenerated catalyst, described regenerated catalyst is at least divided into two parts, a part is returned to first fluidized bed reaction zone 2, a part is returned to riser renewing zone 11 after heat-obtaining.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
The specific embodiment
[embodiment 1]
On reaction unit as shown in Figure 1, purity is that 99.5% methyl alcohol enters first fluidized bed reaction zone, contact with SAPO-34 catalyst, the gaseous stream and the distribution grid of catalyst through first fluidized bed reaction zone top that generate enter the second fluidized bed reaction zone, after gaseous stream and catalyst separation, enter centrifugal station, the catalyst of the second fluidized bed reaction zone is divided into two parts, in mass fraction, 40% returns to first fluidized bed reaction zone, 60% enters riser renewing zone, then be promoted to dense bed renewing zone, form regenerated catalyst, regenerated catalyst is divided into two parts, 20% returns to first fluidized bed reaction zone, 80% returns to riser renewing zone after heat-obtaining.The catalyst of the second fluidized bed reaction zone returns to first fluidized bed reaction zone after heat collector heat exchange, and the catalyst of dense bed renewing zone returns to riser renewing zone after heat collector heat exchange, and distribution grid percent opening is 40%.First fluidized bed reaction zone is fast bed, and first fluidized bed reaction zone reaction condition is: reaction temperature is 400 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 1 meter per second; The second fluidized bed reaction zone reaction condition is: reaction temperature is 420 ℃, reaction pressure is counted 0.01MPa with gauge pressure, gas phase linear speed is 0.4 meter per second, the average carbon deposition quantity mass fraction of regenerated catalyst is 0.01%, the regeneration condition of riser renewing zone is: reaction temperature is 550 ℃, reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 4 meter per seconds; The regeneration condition of dense bed renewing zone is: reaction temperature is 600 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 0.4 meter per second.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 82.13% (weight).
[embodiment 2]
According to condition and the step described in embodiment 1, purity is that 99.5% methyl alcohol enters first fluidized bed reaction zone, contact with SAPO-34 catalyst, the gaseous stream and the distribution grid of catalyst through first fluidized bed reaction zone top that generate enter the second fluidized bed reaction zone, after gaseous stream and catalyst separation, enter centrifugal station, the catalyst of the second fluidized bed reaction zone is divided into two parts, in mass fraction, 80% returns to first fluidized bed reaction zone, 20% enters riser renewing zone, then be promoted to dense bed renewing zone, form regenerated catalyst, regenerated catalyst is divided into two parts, 60% returns to first fluidized bed reaction zone, 40% returns to riser renewing zone after heat-obtaining.Distribution grid percent opening is 75%, and first fluidized bed reaction zone reaction condition is: reaction temperature is 500 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 3 meter per seconds; The second fluidized bed reaction zone reaction condition is: reaction temperature is 550 ℃, reaction pressure is counted 0.01MPa with gauge pressure, gas phase linear speed is 1 meter per second, the average carbon deposition quantity mass fraction of regenerated catalyst is 1.5%, the regeneration condition of riser renewing zone is: reaction temperature is 680 ℃, reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 10 meter per seconds; The regeneration condition of dense bed renewing zone is: reaction temperature is 700 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 1 meter per second.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 83.89% (weight).
[embodiment 3]
According to condition and the step described in embodiment 2, the catalyst of the second fluidized bed reaction zone is divided into two parts, in mass fraction, 50% returns to first fluidized bed reaction zone, and 50% enters riser renewing zone, is then promoted to dense bed renewing zone, form regenerated catalyst, regenerated catalyst is divided into two parts, and 50% returns to first fluidized bed reaction zone, and 50% returns to riser renewing zone after heat-obtaining.Distribution grid percent opening is 60%, and first fluidized bed reaction zone reaction condition is: reaction temperature is 470 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 1.5 meter per seconds; The second fluidized bed reaction zone reaction condition is: reaction temperature is 500 ℃, reaction pressure is counted 0.01MPa with gauge pressure, gas phase linear speed is 0.8 meter per second, the average carbon deposition quantity mass fraction of regenerated catalyst is 1.0%, the regeneration condition of riser renewing zone is: reaction temperature is 630 ℃, reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 6 meter per seconds; The regeneration condition of dense bed renewing zone is: reaction temperature is 660 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and gas phase linear speed is 0.8 meter per second.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 84.85% (weight).
[embodiment 4]
According to condition and the step described in embodiment 3, purity is that 99.2% dimethyl ether enters first fluidized bed reaction zone, contact with SAPO-34 catalyst, the gaseous stream and the distribution grid of catalyst through first fluidized bed reaction zone top that generate enter the second fluidized bed reaction zone, after gaseous stream and catalyst separation, enter centrifugal station, the catalyst of the second fluidized bed reaction zone is divided into two parts, in mass fraction, 60% returns to first fluidized bed reaction zone, 40% enters riser renewing zone, then be promoted to dense bed renewing zone, form regenerated catalyst, regenerated catalyst is divided into two parts, 50% returns to first fluidized bed reaction zone, 50% returns to riser renewing zone after heat-obtaining.First fluidized bed reaction zone reaction condition is: reaction temperature is 450 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 1.1 meter per seconds; The second fluidized bed reaction zone reaction condition is: reaction temperature is 500 ℃, reaction pressure is counted 0.3MPa with gauge pressure, gas phase linear speed is 0.6 meter per second, the average carbon deposition quantity mass fraction of regenerated catalyst is 0.1%, the regeneration condition of riser renewing zone is: reaction temperature is 600 ℃, reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; The regeneration condition of dense bed renewing zone is: reaction temperature is 650 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and gas phase linear speed is 0.7 meter per second.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 81.08% (weight).
[embodiment 5]
According to condition and the step described in embodiment 1, methyl alcohol and dimethyl ether be take the ratio that mass ratio is 2:1 and are entered first fluidized bed reaction zone, contact with SAPO-34 catalyst, the gaseous stream and the distribution grid of catalyst through first fluidized bed reaction zone top that generate enter the second fluidized bed reaction zone, after gaseous stream and catalyst separation, enter centrifugal station, the catalyst of the second fluidized bed reaction zone is divided into two parts, in mass fraction, 60% returns to first fluidized bed reaction zone, 40% enters riser renewing zone, then be promoted to dense bed renewing zone, form regenerated catalyst, regenerated catalyst is divided into two parts, 50% returns to first fluidized bed reaction zone, 50% returns to riser renewing zone after heat-obtaining.First fluidized bed reaction zone reaction condition is: reaction temperature is 480 ℃, and reaction pressure is counted 0.15MPa with gauge pressure, and gas phase linear speed is 1.25 meter per seconds; The second fluidized bed reaction zone reaction condition is: reaction temperature is 530 ℃, reaction pressure is counted 0.15MPa with gauge pressure, gas phase linear speed is 0.6 meter per second, the average carbon deposition quantity mass fraction of regenerated catalyst is 0.8%, the regeneration condition of riser renewing zone is: reaction temperature is 650 ℃, reaction pressure is counted 0.15MPa with gauge pressure, and gas phase linear speed is 5 meter per seconds; The regeneration condition of dense bed renewing zone is: reaction temperature is 670 ℃, and reaction pressure is counted 0.15MPa with gauge pressure, and gas phase linear speed is 0.7 meter per second.Reactor product adopts online gas chromatographic analysis, and low-carbon alkene carbon base absorption rate is 84.35% (weight).
[comparative example 1]
According to condition and the step described in embodiment 3, the second fluidized bed reaction zone is not just set, yield of light olefins is 81.27% (weight).
Obviously, adopt device of the present invention, can reach the object that improves yield of light olefins, there is larger technical advantage, can be used in the industrial production of low-carbon alkene.
Claims (5)
1. the reaction unit of a preparing low-carbon olefin from oxygen-containing compounds, mainly comprise first fluidized bed reaction zone (2), the second fluidized bed reaction zone (4), riser renewing zone (11), dense bed renewing zone (12), first fluidized bed reaction zone (2) top is provided with distribution grid (3), distribution grid (3) top is the second fluidized bed reaction zone (4), top, the second fluidized bed reaction zone (4) is provided with product gas outlet (13), bottom has catalyst outlet, respectively with first fluidized bed reaction zone (2), riser renewing zone (11) is connected, riser renewing zone (11) arrival end is positioned at the outside below of first fluidized bed reaction zone (2), the port of export is positioned at dense bed renewing zone (12), 40～80% of riser renewing zone (11) height is positioned at first fluidized bed reaction zone (2) and the second fluidized bed reaction zone (3), bottom, dense bed renewing zone (12) has catalyst outlet, respectively with first fluidized bed reaction zone (2), riser renewing zone (11) is connected, top has regenerated flue gas outlet (15).
2. the reaction unit of preparing low-carbon olefin from oxygen-containing compounds according to claim 1, is characterized in that described first fluidized bed reaction zone (11) is fast bed.
3. the reaction unit of preparing low-carbon olefin from oxygen-containing compounds according to claim 1, is characterized in that the catalyst of described the second fluidized bed reaction zone (3) returns to first fluidized bed reaction zone (2) after heat collector (8) heat exchange.
4. the reaction unit of preparing low-carbon olefin from oxygen-containing compounds according to claim 1, is characterized in that the catalyst of described dense bed renewing zone (12) returns to riser renewing zone (11) after heat collector (18) heat exchange.
5. the reaction unit of preparing low-carbon olefin from oxygen-containing compounds according to claim 1, is characterized in that described distribution grid (3) percent opening is 40～75%.
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| CN103664449A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Method for preparing low carbon olefin through oxygenated chemicals |
| CN113423804A (en) * | 2018-11-27 | 2021-09-21 | 阿卜杜拉国王科技大学 | Zoned fluidization process for catalytic conversion of hydrocarbon feedstocks to petrochemical products |
| CN114130313A (en) * | 2021-11-08 | 2022-03-04 | 清华大学 | C is to be3-C9Fluidized bed continuous reaction regeneration system and method for converting alkane into aromatic hydrocarbon |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103664449A (en) * | 2012-09-05 | 2014-03-26 | 中国石油化工股份有限公司 | Method for preparing low carbon olefin through oxygenated chemicals |
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| CN114130313B (en) * | 2021-11-08 | 2023-03-10 | 清华大学 | C is to be 3 -C 9 Fluidized bed continuous reaction regeneration system and method for converting alkane into aromatic hydrocarbon |
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