CN102190540B - Method for producing propylene - Google Patents
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- CN102190540B CN102190540B CN2010101164814A CN201010116481A CN102190540B CN 102190540 B CN102190540 B CN 102190540B CN 2010101164814 A CN2010101164814 A CN 2010101164814A CN 201010116481 A CN201010116481 A CN 201010116481A CN 102190540 B CN102190540 B CN 102190540B
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- 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 producing propylene, and the method is mainly used for solving the problem of low propylene yield in the prior art. The method mainly comprises the following steps: (1) feeding a first raw material containing methanol into a first rapid fluidized bed reaction zone to be contacted with a catalyst comprising a molecular sieve, thus generating a product materialflow I comprising ethylene, propylene and over-C4 hydrocarbon and simultaneously forming an inactivated catalyst; (2) feeding the inactivated catalyst into a regenerator for regeneration, feeding theformed regenerated catalyst into a riser pipe reaction zone so as to be contacted with a second raw material, and feeding the generated product and the catalyst into a second rapid fluidized bed reaction zone to be contacted with a third raw material, thus generating a product material flow II comprising the propylene and simultaneously forming a catalyst with pre-deposited carbon; and (3) mixingthe product material flow II subjected to gas-solid separation with the product material flow I, then feeding into a separation station, and returning the catalyst with the pre-deposited carbon back to the first rapid fluidized bed reaction zone, wherein the activity index of the regenerated catalyst is 0.8-1.0, the second raw material comprises C1-C3 alkane and over-C5 hydrocarbon, and the thirdraw material comprises ethylene and C4 olefin. By using the technical scheme, the problem is well solved, thus the method can be used in industrial production of low-carbon olefin.
Description
Technical field
The present invention relates to a kind of production method of propylene.
Technical background
Propylene is important basic chemical industry raw material, and its demand is in continuous increase.Usually, propylene is to produce by petroleum path, but because the limited supply of petroleum resources and higher price, the cost of being produced propylene by petroleum resources constantly increases.In recent years, people begin to greatly develop the preparing propylene transformed technology of alternative materials.Wherein, the important alternative materials that is used for light olefin production of one class is oxygenatedchemicals, for example 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 technology is very ripe, can realize up to a million tonnes industrial scale.Because the popularity in oxygenatedchemicals source is added and is transformed the economy that generates light olefin technology, so be subjected to increasing attention by the technology of oxygen-containing compound conversion to produce olefine (OTO).
In the US4499327 patent silicoaluminophosphamolecular molecular sieves catalyzer is applied to methanol conversion olefin process processed and studies in great detail, think that SAPO-34 is the first-selected catalyzer of MTO technology.The SAPO-34 catalyzer has very high light olefin selectivity, and activity is also higher, and can make methanol conversion is the degree that was less than in reaction times of light olefin 10 seconds, more even reach in the reaction time range of riser tube.
Announced among the US6166282 that a kind of oxygenate conversion is technology and the reactor of low-carbon alkene, adopt fast fluidized bed reactor, gas phase is after the lower Mi Xiangfanyingqu reaction of gas speed is finished, after rising to 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 after product gas and catalyzer sharp separation have effectively prevented the generation of secondary reaction.Through analog calculation, to compare with traditional bubbling fluidization bed bioreactor, this fast fluidized bed reactor internal diameter and the required reserve of catalyzer all significantly reduce.
Announced among the CN1723262 that it is low-carbon alkene technology that the multiple riser reaction unit that has central catalyst return is used 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 disengaging zone of setting, catalyzer and product gas are separated.
In Chinese invention patent 200810043971.9, announced a kind of method that improves yield of light olefins, it is that the first reaction zone top of low-carbon alkene arranges second reaction zone that this method adopts in methanol conversion, and this second reaction zone diameter is greater than first reaction zone, to increase the residence time of product gas in second reaction zone of first reaction zone outlet, make unreacted methanol, the dme that generates and carbon four above hydrocarbon continue reaction, reach the purpose that improves yield of light olefins, this method comprises that also the charging of second reaction zone can be the freshening carbon four above hydrocarbon through separating.Though this method can improve the head trip of low-carbon alkene to a certain extent, but because the catalyzer that first reaction zone comes out has had more carbon distribution, and the carbon four above hydrocarbon pyrolysiss need higher catalyst activity, so the carbon four above hydrocarbon changing effects in second reaction zone are still on the low side in this method.
Announced a kind of method of methanol production propylene among EP0448000 and the EP0882692, methyl alcohol at first is converted into DME and water, then mixture is transported to first reactor, and adds steam in this reactor.In first reactor methyl alcohol with (or) dme or its mixture contact with catalyzer and react, catalyzer adopts the special-purpose ZSM-5 catalyzer that contains ZnO and CdO, 280～570 ℃ of temperature of reaction, pressure 0.01～0.1MPa, preparing with propylene is the product of main hydro carbons.Heavier product such as C
5 +Hydrocarbon continues to react the hydro carbons that is converted into based on propylene in second reactor, sends separator back to after cooling.Product is compressed, can obtain purity after further refining is 97% chemical grade propylene.But adopt a plurality of fixed-bed reactor in this technology, because the activity of such catalysts restriction therefore need frequent blocked operation, and the heat-obtaining problem is also very complicated.
Therefore, need a kind of novel method, with producing more propylene as much as possible, improve the economy of production of propylene technology.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 propene yield that exists in the prior art, and a kind of production method of new propylene is provided.This method is used for the production of low-carbon alkene, has that propene yield is higher, a production of propylene process economy advantage preferably.
For addressing the above problem, the technical solution used in the present invention is as follows: a kind of production method of propylene, mainly may further comprise the steps: (1) comprises that first raw material of methyl alcohol enters the first fast fluidized bed reaction zone, contact with the catalyzer that comprises molecular sieve, generation comprises the product stream I of ethene, propylene, the above hydrocarbon of C4, forms the catalyzer of inactivation simultaneously; (2) catalyzer of described inactivation enters revivifier regeneration, the regenerated catalyst that forms enters riser reaction zone, contact with second raw material, the product and the catalyzer that generate enter the second fast fluidized bed reaction zone, contact with the 3rd raw material, generation comprises the product stream II of propylene, 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 the first fast bed reaction zone; Wherein, described regenerated catalyst activity index is 0.8～1.0, and described second raw material is for comprising C1～C3 alkane, the above hydrocarbon of C5, and described the 3rd raw material is for comprising ethene, C4 alkene.
In the technique scheme, at least a in SAPO-5, SAPO-11, SAPO-18, SAPO-20, SAPO-34, SAPO-44, SAPO-56, ZSM-5, ZSM-34 of described molecular screening, preferred version is selected from least a among SAPO-34, the ZSM-5, and most preferably scheme is selected from SAPO-34; Described regenerated catalyst activity index is 0.9～1.0; Described second raw material is at least a in ethene, propane, the above hydrocarbon of C5, also comprises methyl alcohol or dme in described the 3rd raw material; Temperature of reaction in the described first fast bed reaction zone is 380～460 ℃, preferred version is 400～440 ℃, 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 the 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 450～630 ℃, preferred version is 470～550 ℃, 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 0.3～1.8% weight, and preferred version is 0.5～1.2% weight.
Low-carbon alkene refers to ethene and propylene among the present invention.
The regenerated catalyst activity index is used for embodying the regeneration level of decaying catalyst, be benchmark with the live catalyst, the amount that transforms methyl alcohol with each catalyzer under the rigid condition is carried out relatively, and method of calculation are: regenerated catalyst activity index=(quantity of methyl alcohol that live catalyst transforms under quantity of methyl alcohol/certain condition that regenerated catalyst transforms under the certain condition) * 100%.
Be provided with three reaction zones in the method for the invention, the first fast bed reaction zone is relatively independent, be used for methanol conversion alkene processed, riser reaction zone and the series connection of the second fast bed reaction zone are used for transforming low-carbon alkanes, ethene, carbon four above hydrocarbon and unreacted methanol or dme etc., reach the purpose that improves feed stock conversion and propene yield.Wherein, the second fast bed reaction zone linear speed significantly reduces, guaranteed the enough reaction times, maximized conversion ethene, carbon four above hydrocarbon and unreacted methanol or dme are propylene, and parameter such as its material level, temperature of reaction can independently be controlled, and riser reaction zone in catalyzer directly from revivifier, the activity index of the temperature of carrying and catalyzer self is all higher, is conducive to low-carbon alkanes and carbon five above hydrocarbon to the conversion of low-carbon alkene.In addition, regenerated catalyst by riser reaction zone and the second fast bed reaction zone after, can accumulate a certain amount of carbon deposit after the reaction, the inventor is by discovering, a certain amount of carbon distribution is conducive to improve the selectivity that methanol conversion is low-carbon alkene, so after this part catalyzer that has an a certain amount of carbon distribution returns the first fast bed reaction zone, can obviously improve the selectivity of light olefin in the first fast bed reaction zone.Simultaneously, because being the reaction of propylene, low-carbon alkanes cracking, the carbon four above hydrocarbon pyrolysiss and ethene and C 4 olefin disproportionation be thermo-negative reaction, therefore the heat of the catalyst entrainment after riser reaction zone and the reaction of the second fast bed reaction zone are finished descends, after returning the first fast bed reaction zone, alleviate the heat-obtaining load of the first fast bed reaction zone, effectively utilized heat.Therefore, adopt described method of the present invention, both effectively improved the yield of purpose product low-carbon alkene, optimized energy distribution and utilization again.
Adopt technical scheme of the present invention: at least a in SAPO-5, SAPO-11, SAPO-18, SAPO-20, SAPO-34, SAPO-44, SAPO-56, ZSM-5, ZSM-34 of described molecular screening; Described second raw material is at least a in ethene, propane, the above hydrocarbon of C5, also comprises methyl alcohol or dme in described the 3rd raw material; Temperature of reaction in the described first fast bed reaction zone is 380～460 ℃, 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 the 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 450～630 ℃, 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 0.3～1.8% weight, and low-carbon alkene carbon back yield reaches 90.27% weight, and wherein propylene carbon back yield is 70.34%, has obtained better technical effect.
Description of drawings
Fig. 1 is the schematic flow sheet of the method for the invention.
Among Fig. 1,1 is the first fast bed reaction zone bottom feed; 2 is the first fast bed reaction zone; 3 are gas-solid sharp separation equipment; 4 is stripping stage; 5 return the line of pipes of the first fast bed reaction zone for the stripping stage catalyzer; 6 is the 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 the reactor product outlet line; 12 is revivifier gas solid separation district; 13 is the regenerating medium source line; 14 is the revivifier breeding blanket; 15 is the revivifier external warmer; 16 is the revivifier gas-solid cyclone separator; 17 is the regenerated flue gas outlet line; 18 is the regenerated catalyst inclined tube; 19 is the riser reaction zone charging; 20 is buffering mixing zone, riser reaction zone bottom; 21 is riser reaction zone; 22 is 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, and through entering gas solid separation district 9 behind the gas-solid sharp separation equipment 3, decaying catalyst enters revivifier regeneration from reclaimable catalyst inclined tube 6.Catalyzer after regeneration is finished enters the catalyzer buffer zone 20 of riser reaction zone 21 bottoms from regenerated catalyst inclined tube 18, with enter riser reaction zone 21 after second raw material from pipeline 19 contacts, product and the catalyzer of riser reaction zone 21 outlets enter in the second fast bed reaction zone 25, contact with the 3rd raw material again, generate low-carbon alkene product stream II, after gas-solid separator 22 separates, product enters in the reactor disengaging zone 9, mixes the back with product stream I and enters centrifugal station from outlet line 11.Reacted catalyzer returns the first fast bed reaction zone 2 from pipeline 5 in the second fast bed reaction zone 25.
The invention will be further elaborated below by embodiment, but be not limited only to present embodiment.
Embodiment
[embodiment 1]
In reaction unit as shown in Figure 1, the first fast bed reaction zone medial temperature is 460 ℃, and reaction pressure is counted 0.1MPa with gauge pressure, and linear gas velocity is 1.5 meter per seconds; The 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 470 ℃, 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, charging is 2 kilograms/hour, and catalyzer is SAPO-34, and second raw material is ethane and pentane, weight ratio is 1: 4, the 3rd raw material is ethene and C 4 olefin, and weight ratio is 1.5: 1, and the regenerated catalyst activity index is 0.95, the stability that keeps catalyst flow control, the reactor outlet product adopts online gas chromatographic analysis, and low-carbon alkene carbon back yield reaches 88.72% weight, and wherein propylene carbon back yield is 66.31%.
[embodiment 2]
According to embodiment 1 described condition, the first fast bed reaction zone medial temperature is 440 ℃, and reaction pressure is counted 0.2MPa with gauge pressure, and linear gas velocity is 2.5 meter per seconds; The 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.Second raw material is propane and mixes carbon five, weight ratio is 1: 4, the alkane content that mixes in the carbon five is 79% (weight), the 3rd raw material is ethene and mixed c 4, and weight ratio is 1.5: 1, and the olefin(e) centent in the mixed c 4 is 88%, the stability that keeps catalyst flow control, the reactor outlet product adopts online gas chromatographic analysis, and low-carbon alkene carbon back yield reaches 86.92% weight, and wherein propylene carbon back yield is 68.03%.
[embodiment 3]
According to embodiment 1 described condition, the first fast bed reaction zone medial temperature is 380 ℃, and reaction pressure is counted 0.01MPa with gauge pressure, and linear gas velocity is 0.8 meter per second; The riser reaction zone medial temperature is 510 ℃, 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 450 ℃, 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 1.2% weight.Second raw material is ethane, propane, pentane, hexane, weight ratio is 1: 2: 4: 2, the 3rd raw material is ethene, butene-2, methyl alcohol, weight ratio is 1: 1: 0.2, the stability that keeps catalyst flow control, the reactor outlet product adopts online gas chromatographic analysis, and low-carbon alkene carbon back yield reaches 83.23% weight, and wherein propylene carbon back yield is 62.41%.
[embodiment 4]
According to embodiment 1 described condition, the first fast bed reaction zone medial temperature is 400 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 1.0 meter per seconds; The riser reaction zone medial temperature is 600 ℃, 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 550 ℃, and reaction pressure is counted 0.3MPa with gauge pressure, and linear gas velocity is 1.5 meter per seconds.Second raw material is ethane, propane and carbon five above hydrocarbon mixtures, weight ratio is 1: 4: 2, alkane content in the carbon five above hydrocarbon mixtures is 43% (weight), the 3rd raw material is ethene, butene-1, dme, weight ratio is 1: 1: 0.2, keeps the stability of catalyst flow control, and the reactor outlet product adopts online gas chromatographic analysis, low-carbon alkene carbon back yield reaches 85.28% weight, and wherein propylene carbon back yield is 65.73%.
[embodiment 5]
According to embodiment 1 described condition, the first fast bed reaction zone medial temperature is 425 ℃, and reaction pressure is counted 0.15MPa with gauge pressure, and linear gas velocity is 1.5 meter per seconds; The riser reaction zone medial temperature is 600 ℃, and reaction pressure is counted 0.15MPa with gauge pressure, and linear gas velocity is 6.0 meter per seconds; The second fast bed reaction zone medial temperature is 530 ℃, and reaction pressure is counted 0.15MPa with gauge pressure, and linear gas velocity is 1.3 meter per seconds.The carbon deposition quantity of pre-carbon deposition catalyst is 1.05% weight.Second raw material be ethane, propane and, weight ratio is 1: 4: 8, alkane content in the carbon five above hydrocarbon mixtures is 18% (weight), the 3rd raw material is ethene and mixed c 4, and weight ratio is 1.5: 1, and the olefin(e) centent in the mixed c 4 is 91%, the stability that keeps catalyst flow control, the reactor outlet product adopts online gas chromatographic analysis, and low-carbon alkene carbon back yield reaches 89.37% weight, and wherein propylene carbon back yield is 70.22%.
[embodiment 6]
According to embodiment 5 described conditions, just changing the regenerated catalyst activity index is 0.8, keeps the stability of catalyst flow control, and the reactor outlet product adopts online gas chromatographic analysis, low-carbon alkene carbon back yield reaches 86.21% weight, and wherein propylene carbon back yield is 65.91%.
[embodiment 7]
According to embodiment 2 described conditions, in the second raw material charging, sneak into water vapour, the weight ratio of water vapour and second raw material is 1: 3, sneak into water vapour in the 3rd raw material, the weight ratio of water vapour and second raw material is 1: 3, and pre-carbon deposition catalyst carbon deposition quantity is 0.3% (weight), the stability that keeps catalyst flow control, the reactor outlet product adopts online gas chromatographic analysis, and low-carbon alkene carbon back yield reaches 87.45% weight, and wherein propylene carbon back yield is 68.47%.
[embodiment 8～14]
According to embodiment 1 described condition, just change the type of molecular sieve in the catalyzer, experimental result sees Table 1.
Table 1
| Parameter | Molecular sieve type | Yield of light olefins, % (weight) | Propylene carbon back yield, % (weight) |
| Embodiment 8 | SAPO-20 | 81.64 | 61.50 |
| |
SAPO-18 | 85.32 | 64.67 |
| |
SAPO-56 | 67.85 | 47.34 |
| Embodiment 11 | ZSM-5 | 84.57 | 67.41 |
| |
ZSM-34 | 78.32 | 59.21 |
| |
SAPO-34+ZSM-5 (weight ratio is 2: 1) | 86.83 | 63.29 |
| |
SAPO-34+SAPO-18 (weight ratio is 2: 1) | 87.92 | 65.78 |
[embodiment 15]
According to embodiment 5 described conditions, just changing the regenerated catalyst activity index is 0.9, keeps the stability of catalyst flow control, and the reactor outlet product adopts online gas chromatographic analysis, low-carbon alkene carbon back yield reaches 87.81% weight, and wherein propylene carbon back yield is 67.29%.
[embodiment 16]
According to embodiment 5 described conditions, just changing the regenerated catalyst activity index is 0.99, keeps the stability of catalyst flow control, and the reactor outlet product adopts online gas chromatographic analysis, low-carbon alkene carbon back yield reaches 90.27% weight, and wherein propylene carbon back yield is 70.34%.
[comparative example 1]
According to embodiment 1 described condition, 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 back yield is 79.68% weight, and wherein propylene carbon back yield is 41.96%.
Obviously, adopt method of the present invention, can reach the purpose that improves yield of light olefins, have bigger technical superiority, can be used in the industrial production of low-carbon alkene.
Claims (6)
1. the production method of a propylene mainly may further comprise the steps:
(1) first raw material that comprises methyl alcohol enters the first fast fluidized bed reaction zone, contacts with the catalyzer that comprises molecular sieve, generates the product stream I that comprises ethene, propylene, the above hydrocarbon of C4, forms the catalyzer of inactivation simultaneously;
(2) catalyzer of described inactivation enters revivifier regeneration, the regenerated catalyst that forms enters riser reaction zone, contact with second raw material, the product and the catalyzer that generate enter the second fast fluidized bed reaction zone, contact with the 3rd raw material, generation comprises the product stream II of propylene, 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 the first fast fluidized bed reaction zone;
Wherein, described regenerated catalyst activity index is 0.8～1.0, and described second raw material is at least a in propane, the above hydrocarbon of C5, and described the 3rd raw material is for comprising ethene, C4 alkene;
Temperature of reaction in the described first fast fluidized bed reaction zone is 380～460 ℃, 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 the 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 fluidized bed reaction zone is 450～630 ℃, 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 0.3～1.8% weight.
2. according to the production method of the described propylene of claim 1, it is characterized in that at least a in SAPO-5, SAPO-11, SAPO-18, SAPO-20, SAPO-34, SAPO-44, SAPO-56, ZSM-5, ZSM-34 of described molecular screening; Also comprise methyl alcohol or dme in described the 3rd raw material; Described regenerated catalyst activity index is 0.9～1.0.
3. according to the production method of the described propylene of claim 2, it is characterized in that at least a in SAPO-34, ZSM-5 of described molecular screening.
4. according to the production method of the described propylene of claim 3, it is characterized in that described molecular screening is from SAPO-34.
5. according to the production method of the described propylene of claim 1, it is characterized in that the temperature of reaction in the described first fast fluidized bed reaction zone is 400～440 ℃, reaction pressure is counted 0.1～0.2MPa with gauge pressure, and linear gas velocity is 1.0～1.5 meter per seconds; Temperature of reaction in the riser reaction zone is 550～600 ℃, and reaction pressure is counted 0.1～0.2MPa with gauge pressure, and linear gas velocity is 5.0～7.0 meter per seconds; Temperature of reaction in the second fast fluidized bed reaction zone is 470～550 ℃, and reaction pressure is counted 0.1～0.2MPa with gauge pressure, and linear gas velocity is 1.0～1.5 meter per seconds.
6. according to the production method of the described propylene of claim 1, the carbon deposition quantity that it is characterized in that the catalyzer of described pre-carbon deposit is 0.5～1.2% weight.
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| CN103664442B (en) * | 2012-09-05 | 2015-08-12 | 中国石油化工股份有限公司 | With methyl alcohol and ethanol for the method for low-carbon alkene prepared by raw material |
| CN103772104B (en) * | 2012-10-25 | 2015-11-18 | 中国石油化工股份有限公司 | The reaction unit of preparing light olefins from methanol |
| 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 |
| CN114479914A (en) * | 2021-12-31 | 2022-05-13 | 内蒙古伊泰煤基新材料研究院有限公司 | Method for removing oxygen-containing compounds in Fischer-Tropsch synthetic oil |
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| CN101279875A (en) * | 2007-04-04 | 2008-10-08 | 中国石油化工股份有限公司 | Method for increasing production of ethylene and propone |
| CN101333141B (en) * | 2008-07-08 | 2012-05-30 | 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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