CN102190548B - Method for enhancing yield of light olefins in MTO technology - Google Patents
Method for enhancing yield of light olefins in MTO technology 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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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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 method for enhancing yield of light olefins in MTO technology. The method mainly solves the problem of low yield of light olefins in the prior art, and comprises the following steps that: (1) raw materials containing methanol enter into a first rapid fluidized bed reaction zone and contact with a catalyst containing a silicoaluminophosphate molecular sieve to produce a product flow I containing light olefins and to make the catalyst inactivating; (2) the inactivating catalyst enters into a reactivator for regeneration, the regenerated catalyst enters into a riser reaction zone and contacts with raw materials containing fractions with four or more carbon atoms, the product and catalyst enter into a second rapid fluidized bed reaction zone and contact with raw materials containing fractions with four or more carbon atoms and with a second catalyst coming from the reactivator so as to produce a product flow II containing light olefins and a pre-coked catalyst; (3) after gas-solid separation, the product flow II is mixed with the product flow I, and the mixture is subjected to separation. The technique scheme that pre-coked catalyst returns to the first rapid fluidized bed reaction zone enables effective solving of problems in the prior art and can be used for industrial production of light olefins.
Description
Technical field
The present invention relates to a kind of method of enhancing yield of light olefins in MTO technology.
Technical background
Low-carbon alkene, i.e. ethene and propylene, is two kinds of important basic chemical industry raw materials, its demand is in continuous increase.Usually, ethene, propylene are to produce by petroleum path, but due to the limited supply of petroleum resources and higher price, the cost of being produced ethene, propylene by petroleum resources constantly increases.In recent years, people start to greatly develop the technology of alternative materials conversion ethene processed, propylene.Wherein, the important alternative materials for light olefin production of one class is oxygenatedchemicals, such as alcohols (methyl alcohol, ethanol), ethers (dme, methyl ethyl ether), ester class (methylcarbonate, methyl-formiate) etc., these oxygenatedchemicalss can be transformed by coal, Sweet natural gas, biomass equal energy source.Some oxygenatedchemicals can reach fairly large production, as methyl alcohol, can be made by coal or Sweet natural gas, and technique is very ripe, can realize the industrial scale of up to a million tonnes.Due to the popularity in oxygenatedchemicals source, add and transform the economy that generates light olefin technique, so by the technique of oxygen-containing compound conversion to produce olefine (OTO), be particularly subject to increasing attention by the technique of preparing olefin by conversion of methanol (MTO).
In US4499327 patent, silicoaluminophosphamolecular molecular sieve catalyst is applied to preparing olefin by conversion of methanol technique and studies in detail, think that SAPO-34 is the first-selected catalyzer of MTO technique.SAPO-34 catalyzer has very high light olefin selectivity, and activity is also higher, and can make methanol conversion is reaction times of light olefin to be less than the degree of 10 seconds, more even reaches in the reaction time range of riser tube.
Technology and reactor that a kind of oxygenate conversion is low-carbon alkene in US6166282, are announced, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu of gas speed has reacted, rise to after the fast subregion that internal diameter diminishes rapidly, adopt special gas-solid separation equipment initial gross separation to go out most entrained catalyst.Due to reaction after product gas and catalyzer sharp separation, effectively prevent the generation of secondary reaction.Through analog calculation, compared with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all greatly reduce.
In CN1723262, having announced with the multiple riser reaction unit of central catalyst return is low-carbon alkene technique for oxygenate conversion, this covering device comprises multiple riser reactors, gas solid separation district, multiple offset components etc., each riser reactor has the port of injecting catalyst separately, be pooled to the disengaging zone of setting, catalyzer and gas product are separated.
In Chinese invention patent 200810043971.9, announce a kind of method that improves yield of light olefins, the first top, reaction zone that it is low-carbon alkene in methanol conversion that the method adopts arranges a second reaction zone, and this second reaction zone diameter is greater than the first reaction zone, the residence time with the gas product that increases by the first reaction zone outlet in second reaction zone, make unreacted methyl alcohol, the above hydrocarbon of the dme generating and carbon four continues reaction, reach the object that improves yield of light olefins, the method also comprises that the charging of second reaction zone can be the above hydrocarbon of freshening carbon four through separating.Although the method can improve the yield of low-carbon alkene to a certain extent, but because the first reaction zone catalyzer is out with more carbon distribution, and the above hydrocarbon pyrolysis of carbon four needs higher catalyst activity, therefore in the method, the above hydrocarbon changing effect of the carbon four in second reaction zone is still on the low side.
Therefore, need a kind of novel method, make the above hydrocarbon of carbon four object that is converted into low-carbon alkene how as far as possible to reach, finally reach the object that improves yield of light olefins and process economy.The present invention has solved the problems referred to above targetedly.
Summary of the invention
Technical problem to be solved by this invention is the not high problem of yield of light olefins existing in prior art, and a kind of method of new enhancing yield of light olefins in MTO technology is provided.The method, for the production of low-carbon alkene, has advantages of the more high and low carbon olefin production technique of yield of light olefins better economy.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of method of enhancing yield of light olefins in MTO technology, mainly comprise the following steps: (1) comprises that the raw material of methyl alcohol enters the first fast fluidized bed reaction zone, contact with comprising silicoaluminophosphamolecular molecular sieve catalyst, generation comprises the product stream I of low-carbon alkene, forms the catalyzer of inactivation simultaneously; (2) catalyzer of described inactivation enters revivifier regeneration, the catalyzer of having regenerated enters riser reaction zone, contact with the raw material that comprises carbon four above hydrocarbon, the product and the catalyzer that generate enter the second fast fluidized bed reaction zone, contact with the second strand of catalyzer that comprises the raw material of carbon four above hydrocarbon and come from revivifier, generation comprises the product stream II of low-carbon alkene, forms the catalyzer of pre-carbon deposit simultaneously; (3) described product stream II is mixed into centrifugal station with product stream I after gas solid separation, and the catalyzer of described pre-carbon deposit returns to the first fast bed reaction zone.
In technique scheme, described silicoaluminophosphamolecular molecular sieves is selected from least one in SAPO-5, SAPO-11, SAPO-18, SAPO-20, SAPO-34, SAPO-44, SAPO-56, and preferred version is SAPO-34; Temperature of reaction in described the first fast bed reaction zone is 400～500 ℃, preferred version is 430～480 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and preferred version is 0.1～0.2MPa, linear gas velocity is 0.8～2.5 meter per second, and preferred version is 1.0～1.5 meter per seconds; Temperature of reaction in riser reaction zone is 510～650 ℃, preferred version is 550～600 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and preferred version is 0.1～0.2MPa, linear gas velocity is 3.0～10.0 meter per seconds, and preferred version is 5.0～7.0 meter per seconds; Temperature of reaction in the second fast bed reaction zone is 500～630 ℃, preferred version is 530～580 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and preferred version is 0.1～0.2MPa, linear gas velocity is 0.8～2.0 meter per second, and preferred version is 1.0～1.5 meter per seconds; The carbon deposition quantity of the catalyzer of described pre-carbon deposit is 0.1～1.8% weight, and preferred version is 0.5～1.2% weight.
The preparation method of silicoaluminophosphamolecular 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, constitutive material mixed solution obtains at a certain temperature after the crystallization of certain hour; Again, molecular sieve presoma, phosphorus source, silicon source, aluminium source, organic formwork agent, water etc. are mixed according to certain ratio after at 110～260 ℃ hydrothermal crystallizing after at least 0.1 hour, finally obtain SAPO molecular sieve.
The molecular sieve of preparation is mixed with a certain proportion of binding agent, after the operation stepss such as, roasting dry through spraying, obtain final SAPO catalyzer, the weight percentage of binding agent in molecular sieve is generally between 10～90%.
In the method for the invention, be provided with three reaction zones, the first fast bed reaction zone is relatively independent, for preparing olefin by conversion of methanol, riser reaction zone and the series connection of the second fast bed reaction zone, for transforming the above hydrocarbon of carbon four and methyl alcohol or dme etc. for reaction, reach the object that improves feed stock conversion and yield of light olefins.Wherein, the second fast bed reaction zone linear speed significantly reduces, guarantee the enough reaction times, and one high activated catalyst after completing with regeneration contacts, the above hydrocarbon of maximized conversion carbon four is low-carbon alkene, and the parameter such as its material level, temperature of reaction can independently control, and catalyzer in riser reaction zone is directly from revivifier, the activity of the temperature of carrying and catalyzer self is all higher, is conducive to the conversion of the above hydrocarbon of carbon four to low-carbon alkene.In addition, regenerated catalyst by riser reaction zone and the second fast bed reaction zone after, after reaction, can accumulate a certain amount of carbon deposit, the inventor finds by research, the above hydrocarbon of carbon four is converted into a certain amount of carbon distribution being accumulated on catalyzer in low carbon olefin hydrocarbon and is conducive to improve the selectivity that methanol conversion is low-carbon alkene, so return with the catalyzer of a certain amount of carbon distribution behind the first fast bed reaction zone when this part, can obviously improve the selectivity of light olefin in the first fast bed reaction zone.Simultaneously, because the above hydrocarbon pyrolysis of carbon four is that low-carbon alkene is strong endothermic reaction, the heat of the catalyst entrainment after therefore having reacted in riser reaction zone and the second fast bed reaction zone declines, return behind the first fast bed reaction zone, the heat-obtaining load that has alleviated the first fast bed reaction zone, has effectively utilized heat.Therefore, adopt described method of the present invention, both effectively improved the yield of object product low-carbon alkene, optimized again energy distribution and utilization.
Adopt technical scheme of the present invention: described silicoaluminophosphamolecular molecular sieves is selected from least one in SAPO-5, SAPO-11, SAPO-18, SAPO-20, SAPO-34, SAPO-44, SAPO-56; Temperature of reaction in described the first fast bed reaction zone is 400～500 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 0.8～2.5 meter per second; Temperature of reaction in riser reaction zone is 510～650 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 3.0～10.0 meter per seconds; Temperature of reaction in the second fast bed reaction zone is 500～630 ℃, and reaction pressure is counted 0.01～0.3MPa with gauge pressure, and linear gas velocity is 0.8～2.0 meter per second; The carbon deposition quantity of the catalyzer of described pre-carbon deposit is 0.1～1.8% weight, and selectivity of light olefin can reach 90.33% weight, has obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of the method for the invention.
In Fig. 1,1 is the first fast bed reaction zone bottom feed; 2 is the first fast bed reaction zone; 3 is gas-solid sharp separation equipment; 4 is stripping stage; 5 return to the line of pipes of the first fast bed reaction zone for stripping stage catalyzer; 6 is reclaimable catalyst inclined tube; 7 is the first fast bed reaction zone external warmer; 8 is gas-solid cyclone separator; 9 is reactor gas solid separation district; 10 is collection chamber; 11 is reactor product outlet line; 12 is revivifier gas solid separation district; 13 is regenerating medium source line; 14 is revivifier breeding blanket; 15 is external catalyst cooler for regenerator; 16 is revivifier gas-solid cyclone separator; 17 is regenerated flue gas outlet line; 18 is regenerated catalyst inclined tube; 19 is riser reaction zone charging; 20 is buffering mixing zone, bottom, riser reaction zone; 21 is riser reaction zone; 22 is the second fast bed reaction zone outlet gas-solid separation equipment; 23 is the second fast bed reaction zone feeds; 24 is second strand of regenerated catalyst line; 25 is the second fast bed reaction zone.
Raw material enters in the first fast bed reaction zone 2 through feeding line 1, contact with molecular sieve catalyst, reaction generates the product stream I that contains low-carbon alkene, after gas-solid sharp separation equipment 3, enters gas solid separation district 9, and decaying catalyst enters revivifier regeneration from reclaimable catalyst inclined tube 6.Catalyzer after having regenerated enters the catalyzer buffer zone 20 of 21 bottoms, riser reaction zone from regenerated catalyst inclined tube 18, after contacting with from the raw material of pipeline 19, enter riser reaction zone 21, the product that riser reaction zone 21 exports and catalyzer enter in the second fast bed reaction zone 25, again contact with comprising the raw material of carbon four above hydrocarbon and second strand of regenerated catalyst from pipeline 24, generate low-carbon alkene product stream II, after gas-solid separator 22 separates, in product introduction reactor disengaging zone 9, after mixing with product stream I, enter centrifugal station from outlet line 11.In the second fast bed reaction zone 25, reacted catalyzer returns the first fast bed reaction zone 2 from pipeline 5.
Below by embodiment, the invention will be further elaborated, but be not limited only to the present embodiment.
Embodiment
[embodiment 1]
In reaction unit as shown in Figure 1, the first fast bed reaction zone medial temperature is 480 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 1.5 meter per seconds; Riser reaction zone medial temperature is 550 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 5.0 meter per seconds; The second fast bed reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 0.8 meter per second.The carbon deposition quantity of pre-carbon deposition catalyst is 0.5% weight.The first fast bed reaction zone bottom feed is pure methyl alcohol, and charging is 2 kgs/hr, and catalyzer is SAPO-34, wherein SiO in molecular sieve
2: Al
2o
3: P
2o
5=0.1: 1: 1, in catalyzer, binder content was 60%.Riser reaction zone bottom feed is mixed c 4, C 4 olefin content 87%, the second fast bed reaction zone bottom feed is identical with riser reaction zone bottom feed, keep the stability of catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 87.64% weight.
[embodiment 2]
According to the condition described in embodiment 1, the first fast bed reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.2MPa with gauge pressure, and linear gas velocity is 2.5 meter per seconds; Riser reaction zone medial temperature is 650 ℃, and reaction pressure is counted 0.2MPa with gauge pressure, and linear gas velocity is 10.0 meter per seconds; The second fast bed reaction zone medial temperature is 630 ℃, and reaction pressure is counted 0.2MPa with gauge pressure, and linear gas velocity is 2.0 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 1.8% weight.Riser reaction zone bottom feed is mixed c 4, C 4 olefin content 58%, and the stability of maintenance catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 85.55% weight.
[embodiment 3]
According to the condition described in embodiment 1, the first fast bed reaction zone medial temperature is 400 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and linear gas velocity is 0.8 meter per second; Riser reaction zone medial temperature is 600 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and linear gas velocity is 3.0 meter per seconds; The second fast bed reaction zone medial temperature is 530 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and linear gas velocity is 1.0 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 0.1% weight.The stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 85.80% weight.
[embodiment 4]
According to the condition described in embodiment 1, the first fast bed reaction zone medial temperature is 430 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 1.0 meter per seconds; Riser reaction zone medial temperature is 510 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 7.0 meter per seconds; The second fast bed reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 1.5 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 1.2% weight.The stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 86.97% weight.
[embodiment 5]
According to the condition described in embodiment 1, the first fast bed reaction zone linear gas velocity is 1.2 meter per seconds; Riser reaction zone medial temperature is 600 ℃; The second fast bed reaction zone medial temperature is 580 ℃.The carbon deposition quantity of pre-carbon deposition catalyst is 0.8% weight.Riser reaction zone bottom feed is mixed c 4, C 4 olefin content 95%, and the stability of maintenance catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 88.95% weight.
[embodiment 6]
According to the condition described in embodiment 5, riser reaction zone bottom feed is mixed c 4, C 4 olefin content 75%, the second fast bed reaction zone bottom feed is mixed c 4, C 4 olefin content 95%, the stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 88.84% weight.
[embodiment 7]
According to the condition described in embodiment 5, the second fast bed reaction zone bottom feed is mixed c 4 and methyl alcohol, and the olefin(e) centent in mixed c 4 is 95%, and the weight ratio of mixed c 4 and methyl alcohol is 5: 1.The stability that keeps catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 90.33% weight.
[embodiment 8～11]
According to the condition described in embodiment 1, just change the type of molecular sieve in catalyzer, experimental result is in table 1.
Table 1
| Parameter | Molecular sieve type | Yield of light olefins, % (weight) |
| |
SAPO-20 | 80.11 |
| |
SAPO-18 | 86.96 |
| Embodiment 10 | SAPO-56 | 69.37 |
| |
SAPO-34+SAPO-18 (weight ratio is 2: 1) | 88.22 |
[embodiment 12]
According to the condition described in embodiment 1, SiO in molecular sieve
2: Al
2o
3: P
2o
5=0.2: 1: 1, in catalyzer, binder content was 70%, light olefin carbon base absorption rate is 85.18% (weight).
[comparative example 1]
According to the condition described in embodiment 1, do not establish riser reaction zone and the second fast bed reaction zone, regenerated catalyst directly turns back to the bottom of the first fast bed reaction zone, and low-carbon alkene carbon base absorption rate is 79.5% weight.
Obviously, adopt method of the present invention, can reach the object that improves yield of light olefins, there is larger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (1)
1. a method for enhancing yield of light olefins in MTO technology, comprises the following steps:
Raw material enters in the first fast bed reaction zone (2) through feeding line (1), contact with molecular sieve catalyst, reaction generates the product stream I that contains low-carbon alkene, after gas-solid sharp separation equipment (3), enter gas solid separation district (9), decaying catalyst enters revivifier regeneration from reclaimable catalyst inclined tube (6), catalyzer after having regenerated enters the catalyzer buffer zone (20) of bottom, riser reaction zone (21) from regenerated catalyst inclined tube (18), after contacting with the raw material coming from pipeline (19), enter riser reaction zone (21), product and the catalyzer of riser reaction zone (21) outlet enter in the second fast bed reaction zone (25), again contact with the second strand of regenerated catalyst that comprises the raw material of carbon four above hydrocarbon and come from pipeline (24), generate low-carbon alkene product stream II, after gas-solid separator (22) separates, in product introduction reactor disengaging zone (9), after mixing with product stream I, enter centrifugal station from outlet line (11), in the second fast bed reaction zone (25), reacted catalyzer returns the first fast bed reaction zone (2) from pipeline (5),
Described the first fast bed reaction zone medial temperature is 480 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 1.5 meter per seconds; Riser reaction zone medial temperature is 550 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 5.0 meter per seconds; The second fast bed reaction zone medial temperature is 500 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 0.8 meter per second, and the carbon deposition quantity of pre-carbon deposition catalyst is 0.5% weight; The first fast bed reaction zone bottom feed is pure methyl alcohol, and charging is 2 kgs/hr, and catalyzer is SAPO-34, wherein SiO in molecular sieve
2: Al
2o
3: P
2o
5=0.1: 1: 1, in catalyzer, binder content was 60%; Riser reaction zone bottom feed is mixed c 4, C 4 olefin content 87%, the second fast bed reaction zone bottom feed is identical with riser reaction zone bottom feed, keep the stability of catalyst flow control, reactor outlet product adopts online gas chromatographic analysis, and yield of light olefins reaches 87.64% weight.
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| CN103539608B (en) * | 2012-07-12 | 2016-08-03 | 中国石油化工股份有限公司 | The method of preparing low carbon olefin hydrocarbon with methanol |
| CN103664438B (en) * | 2012-09-05 | 2015-12-09 | 中国石油化工股份有限公司 | The method of preparing light olefins from methanol |
| CN103664441B (en) * | 2012-09-05 | 2015-09-09 | 中国石油化工股份有限公司 | By the method for preparing low-carbon olefin by using methanol |
| CN103739418B (en) * | 2012-10-17 | 2016-07-13 | 中国石油化工股份有限公司 | Improve the method for yield of light olefins in preparing light olefins from methanol technique |
| AU2014368547B2 (en) * | 2013-12-20 | 2018-06-21 | Basf Se | Catalyst and process for the conversion of oxygenates to olefins |
| CN111423302B (en) * | 2019-01-09 | 2023-09-19 | 国家能源投资集团有限责任公司 | Method and device for preparing olefin from methanol |
| CN114377624B (en) * | 2020-10-16 | 2024-03-19 | 中国科学院大连化学物理研究所 | Coke regulation reactor, device for preparing low-carbon olefin from oxygen-containing compound and application |
| CN115304442A (en) * | 2021-05-08 | 2022-11-08 | 国家能源投资集团有限责任公司 | Preparation of C from methanol 2 -C 3 Process and apparatus for olefins |
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| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
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| CN101333141A (en) * | 2008-07-08 | 2008-12-31 | 中国石油化工股份有限公司 | Reaction device for conversing methanol or dimethyl ether to be low carbon olefin |
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|---|---|---|---|---|
| US4499327A (en) * | 1982-10-04 | 1985-02-12 | Union Carbide Corporation | Production of light olefins |
| US6166282A (en) * | 1999-08-20 | 2000-12-26 | Uop Llc | Fast-fluidized bed reactor for MTO process |
| CN101195554A (en) * | 2006-12-07 | 2008-06-11 | 中国石油化工股份有限公司 | Method for producing low carbon olefin hydrocarbon with C4 hydrocarbon |
| CN101333141A (en) * | 2008-07-08 | 2008-12-31 | 中国石油化工股份有限公司 | Reaction device for conversing methanol or dimethyl ether to be low carbon olefin |
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