CN101440014B - Method for producing light olefins - Google Patents
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- CN101440014B CN101440014B CN2007101779018A CN200710177901A CN101440014B CN 101440014 B CN101440014 B CN 101440014B CN 2007101779018 A CN2007101779018 A CN 2007101779018A CN 200710177901 A CN200710177901 A CN 200710177901A CN 101440014 B CN101440014 B CN 101440014B
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Abstract
The invention relates to a method for producing low-carbon olefin, which comprises the following steps: introducing a heavy raw material into a first reactor for contact reaction with a regenerated catalyst, and introducing oil gas and a catalyst into a second reactor for continuous reaction after the reaction; introducing a light raw material into a third reactor for contact reaction with the regenerated catalyst, separating the oil gas exhausted by the third reactor and a catalyst to be generated, and then introducing the catalyst to be generated into the second reactor; and separating the oil gas exhausted by the third reactor and the catalyst to be generated, then burning and regenerating the catalyst to be generated and returning the catalyst to the first reactor and the third reactor to be used circularly, and introducing the oil gas separated in a second reaction area and a third reaction area into a catalytic cracking separation stabilizing system to obtain a target product of the low-carbon olefin through fractionation. The method can flexibly adjust the operation conditions of light material recycle, optimize the distribution of products, increase the yield of the low-carbon olefin, and reduce hydrogen transfer reactivity in the second reactor.
Description
Technical field
The present invention relates to the catalysis conversion method of hydrocarbon ils under the situation that does not have hydrogen, more particularly, relate to a kind of method that heavy feed stock is converted into low-carbon alkenes such as propylene, ethene.
Background technology
Low-carbon alkene such as ethene, propylene etc. are important Organic Chemicals, and wherein propylene is the synthon of products such as Vestolen PP 7052, vinyl cyanide.Along with increasing rapidly of verivate demands such as Vestolen PP 7052, the demand of propylene is also all being increased year by year.The demand in propylene market, the world is 5,120 ten thousand tons of being increased to 2000 of 1,520 ten thousand tons before 20 years, and average growth rate per annum reaches 6.3%.The demand that expects propylene in 2010 will reach 8,600 ten thousand tons, and average growth rate per annum is about 5.6% therebetween.
The method of producing propylene mainly is steam cracking and catalytic cracking (FCC); Wherein steam cracking is that raw material passes through thermo-cracking production ethene, propylene with lightweight oils such as petroleum naphthas; But the productive rate of propylene is merely about 15 heavy %, and FCC is a raw material with decompressed wax oil BOes such as (VGO) then.At present, 66% propylene is produced the sub product of ethene from steam cracking in the world, and 32% produces the sub product of vapour, diesel oil from refinery FCC, and a small amount of (about 2%) is obtained by dehydrogenating propane and ethene-butylene metathesis reaction.
If petrochemical complex is walked prior steam cracking ethylene preparation, propylene route, will face the shortage of lightweight material oil, inefficiency of production and cost and cross high several big restraining factors.
Catalytic cracking is owing to advantages such as its adaptability to raw material is wide, flexible operation come into one's own day by day.In the U.S., almost 50% of the propylene market demand all derive from FCC apparatus.It is very fast that the catalytic cracking of propylene enhancing improves technical development.
US 6045690 discloses a kind of method of producing low-carbon alkene, and this method is divided into regenerated catalyst more than two strands and gets into downflow reactor, but this method can't fine solution temperature of reactor and the inhomogenous problem of density distribution.
US 4257875 discloses a kind of two-stage catalytic method for transformation, and this method is divided into two strands with regenerated catalyst, gets into two riser reactors respectively, but this method can't solve the inhomogenous problem of temperature of reactor and density distribution equally.
US 4578183 discloses a kind of catalysis conversion method, and this method is divided into two strands with regenerated catalyst in riser tube, and one gets into first reactor drum, and second strand gets into second reactor drum, but there is the dry gas yied problem of higher equally in this method.
CN1898362A discloses a kind of method of producing low-carbon alkene and aromatic hydrocarbons, and raw material contacts with catalytic cracking catalyst, is 400～800 ℃, weight hourly space velocity 0.1～750h in temperature of reaction
-1Condition under react; Separate reclaimable catalyst and reaction oil gas; Reclaimable catalyst is Returning reactor after regenerating; This reaction is carried out at two reaction zones at least, in the reaction zone in the first reaction zone downstream, have at least the temperature of reaction of a reaction zone to be higher than the temperature of reaction of first reaction zone, and its weight hourly space velocity is lower than the weight hourly space velocity of first reaction zone.This method is introduced the highly active regenerated catalyst of high temperature at second reaction zone, makes that the hydrogen transfer reactions of second reaction zone is many, has reduced the productive rate of low-carbon alkene.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of productivity of low carbon olefin hydrocarbon higher, produce the method for low-carbon alkene by heavy feed stock.
The method of production low-carbon alkene provided by the invention comprises: heavy feed stock is introduced in first reactor drum, and with the catalytic cracking catalyst contact reacts from revivifier, reaction back oil gas and catalyzer get into second reactor drum and continue reaction; Lightweight material is introduced in the 3rd reactor drum, and with the catalytic cracking catalyst contact reacts from revivifier, the oil gas behind the 3rd reactor reaction separates through gas-solid separation equipment with reclaimable catalyst, and isolated reclaimable catalyst is introduced second reactor drum; Oil gas behind second reactor reaction and reclaimable catalyst are after separating; Isolated reclaimable catalyst in revivifier, after coke burning regeneration recovers activity, returns first reactor drum and the 3rd reactor cycles is used; The isolated oil gas of second reactor drum and the 3rd reactor drum is introduced catalytic cracking separating stable system, obtains purpose product low-carbon alkene through fractionation; Wherein the temperature of reaction of second reactor drum is higher than the temperature of reaction of first reactor drum, and weight hourly space velocity is lower than the weight hourly space velocity of first reactor drum, and the temperature of reaction of the 3rd reactor drum is higher than the temperature of reaction of second reactor drum.
The advantage of method provided by the invention is:
Method provided by the invention can flexible the 3rd reactor operating condition, and the product of optimizing the lightweight material freshening distributes, and increases the yield of low-carbon alkene; Reduce the hydrogen transfer reaction activity in second reactor drum, further increase the yield of low-carbon alkene, especially increase propene yield.
Description of drawings
Fig. 1 is the schematic flow sheet of method provided by the invention;
Fig. 2 is the schematic flow sheet of the method for the low-carbon olefines high-output that adopts in the Comparative Examples.
Embodiment
Method provided by the invention is such practical implementation:
Heavy feed stock being introduced in first reactor drum, contacted with catalytic cracking catalyst from revivifier, is 500～650 ℃, preferred 540～600 ℃ in temperature of reaction, and weight hourly space velocity is 0.1～750h
-1, preferred 1～500h
-1Reaction pressure is that the weight ratio of 0.10～1.0MPa (absolute pressure), catalytic cracking catalyst and raw material is to react under 2～100, preferred 5～50 the condition; Reaction back oil gas and catalyzer get into second reactor drum and continue reaction; The temperature of reaction of second reactor drum is higher 10～100 ℃ than first reactor drum, preferred high 20～60 ℃, and second reactor drum is 1 with the ratio of the weight hourly space velocity of first reactor drum: (1.1～750), preferred 1: (1.1～300); Lightweight material is introduced in the 3rd reactor drum; Contact with catalytic cracking catalyst from revivifier; In temperature of reaction is 600～750 ℃, preferred 650～700 ℃; The residence time is 1～20 second, preferred 1～10 second, and reaction pressure is to react under the weight ratio 4～100, preferred 5～80 condition of 0.10～1.0MPa (absolute pressure), catalyzer and raw material, and the temperature of reaction of the 3rd reactor drum is higher than the temperature of reaction of second reactor drum; Oil gas behind the 3rd reactor reaction separates through gas-solid separation equipment with reclaimable catalyst, and isolated reclaimable catalyst is introduced second reactor drum; Oil gas behind second reactor reaction and reclaimable catalyst are after separating; Isolated reclaimable catalyst in revivifier, after coke burning regeneration recovers activity, returns first reactor drum and the 3rd reactor cycles is used; The isolated oil gas of second reactor drum and the 3rd reactor drum is introduced catalytic cracking separating stable system, obtains purpose product low-carbon alkene through fractionation.
In the method provided by the invention, described heavy feed stock is selected from one or more the mixture in decompressed wax oil, normal pressure wax oil, wax tailings, deasphalted oil, vacuum residuum, long residuum, recycle stock, slurry oil, the diesel oil.Wherein decompressed wax oil, normal pressure wax oil, wax tailings, deasphalted oil, vacuum residuum, long residuum, diesel oil are the full cut or the part cut of not hydrogenation, or be behind the hydrogenation full cut or part cut.When the raw material that gets into reactor drum when being two or more, can get into reactor drum in identical position, also can get in different positions.
In the method provided by the invention, described lightweight material is selected from the hydrocarbon mixture of gasoline and/or C4～C8.Wherein preferred C4～C8 hydrocarbon mixture.
Described gasoline is selected from the catalytic cracking gasoline that obtains in the method provided by the invention, also can be from a kind of in the outer catalytically cracked gasoline of this device, straight-run spirit, coker gasoline, pyrolysis gasoline, pressure gasoline, the hydrogenated gasoline or more than one mixture wherein.
In the method provided by the invention; Described catalyst activity component is selected from mesopore zeolite and optional large pore zeolite; Large pore zeolite is Y type or the HY type zeolite that contains or do not contain rare earth, the ultrastable Y that contains or do not contain rare earth, mesopore zeolite be have the zeolite of MFI structure or the supersiliceous zeolite that makes with other method with five-membered ring structure in one or more.
Said catalyzer is made up of zeolite, inorganic oxide and optional clay, wherein in total catalyst weight, contains zeolite 10～50w%, inorganic oxide 5～90w%, clay 0～70w%.
Described inorganic oxide is selected from silicon-dioxide (SiO as caking agent
2) and/or aluminium sesquioxide (Al
2O
3).
Described clay is selected from kaolin and/or halloysite as matrix (being carrier).
In the method provided by the invention, said first reactor drum is riser tube, upstriker transfer limes, downstriker transfer limes or fluidized-bed reactor, preferred riser reactor or fluidized-bed reactor, more preferably riser reactor; Second reactor drum is a fluidized-bed reactor; The 3rd reactor drum is a riser reactor.The void tower linear speed of described fluidized-bed reactor is 0.2～2.5 meter per second, and density of catalyst is 150～700kg/m
3
In order to realize the fluidization operation, can promote medium and be selected from water vapor or dry gas, preferably water steam at injecting lift medium bottom the reaction zone.The weight ratio of water vapor and raw material is 0.05～1.0.
In the method provided by the invention, described first reactor drum and second reactors in series, second reactor drum is in the downstream of first reactor drum, and the temperature of reaction of second reactor drum is 10～100 ℃ than the temperature of reaction height of first reactor drum, preferred 20～60 ℃.According to those of ordinary skills' general knowledge, the temperature of reaction of tubular reactor such as riser tube is meant temperature out, and the temperature of reaction of bed reactor such as fluidized-bed is meant the bed medial temperature.The weight hourly space velocity of second reactor drum is 1 with the ratio of the weight hourly space velocity of first reactor drum: (1.1～750), preferred 1: (1.1～300).
In the method provided by the invention, described the 3rd reactor drum and first reactor drum and the parallel connection of second reactor drum.The reclaimable catalyst of the 3rd reactor head separates through conventional sedimentation, cyclonic separator with reaction oil gas, and the isolated reclaimable catalyst of the 3rd reactor head gets into the bottom or the middle part of second reactor drum, is that second reactor drum provides heat and catalyzer; Isolated oil gas gets into catalytic cracking fractionation stabilization system.
The isolated reclaimable catalyst of second reactor head is through stripping or Returning reactor behind stripping, the coke burning regeneration not; Isolated oil gas gets into catalytic cracking fractionation stabilization system.Obtain the low-carbon alkene product through fractionation and after other separation systems, described low-carbon alkene is ethene, propylene and optional butylene, and promptly low-carbon alkene is ethene, propylene, perhaps ethene, propylene and butylene.
The method of separating ethene is identical with the method for separating ethene from catalytic cracked dry gas that those of ordinary skills know from reaction oil gas, and the method for separation of propylene and optional butylene is identical with the method for the butylene of choosing wantonly with the separation of propylene from the catalytic cracking liquefied gas that those of ordinary skills know from reaction oil gas.The method of aromatics separation is that the solvent extracting is identical with the method for aromatics separation from steam cracking gasoline that those of ordinary skills know from the pyrolysis gasoline cut fraction of reaction oil gas; Before present method gained catalytic cracking gasoline aromatics separation, can be with the C in this gasoline
5～C
8Separate as recycle stock earlier.
In the method provided by the invention, described reclaimable catalyst is introduced in the revivifier, with the oxygen-containing medium contact reacts, burns whole or most coke on the reclaimable catalyst, makes that this activity of such catalysts is able to recover.Regenerated catalyst behind coke burning regeneration returns first reactor drum and the 3rd reactor cycles is used.The coke that yet can exist part not burn fully on this regenerated catalyst, this patent is not limit the carbon-bearing amount on the reclaimable catalyst, as long as regenerated catalyst can have suitable activity.
The catalyst regeneration condition of said revivifier is: temperature is 600～800 ℃, and pressure is 0.1～0.6MPa (absolute pressure), and the residence time is 60～720 seconds.
The beneficial effect of method provided by the invention is:
Because gasoline and C4～C8 hydro carbons freshening separately in the 3rd reactor drum, can flexible and operation conditions optimization, the raising productivity of propylene.Because introducing second reactor drum, the spent agent behind the 3rd reactor reaction continues reaction simultaneously; Compare from the regenerated catalyst of revivifier with introducing; Catalyst activity decreases, and under the situation that has improved the second reactor drum potential temperature, has reduced the hydrogen transfer reaction activity in second reactor drum; Can further increase the yield of low-carbon alkene, especially increase propene yield.
Below in conjunction with accompanying drawing method provided by the present invention is further explained, but therefore do not limited the present invention.
Fig. 1 is the schematic flow sheet of the method that provides of this patent.As shown in Figure 1; First reactor A is a riser reactor, and second reactor B is a fluidized-bed reactor, first reactor drum and second reactors in series; The 3rd reactor drum C is a riser reactor, the 3rd reactor drum C and first reactor A and the parallel connection of second reactor B.
Part regenerated catalyst gets into pre lift zone 3 bottoms of the first reactor A bottom through pipeline 1 and valve 2, promotes steam in advance and gets into pre lift zones 3 bottoms through pipeline 4, in the castering action lower edge riser tube that the promotes medium in advance accelerated motion that makes progress; Raw oil, contacts with regenerated catalyst and along the up reaction of riser tube A with the atomizing steam injecting lift pipe A from pipeline 6 through pipeline 5.Oil gas and the catalyzer of riser tube A outlet get into second reactor B together, in the bottom of fluidized-bed B and through the catalyst mix of pipeline 8 and in second reactor B, react.Second reactor drum also can be through pipeline 27 compensation regeneration catalyzer.
A part of in addition regenerated catalyst gets into the bottom of the 3rd reactor drum C pre lift zone 11 through pipeline 9 and valve 10, promotes steam in advance and gets into pre lift zones 11 bottoms through pipeline 14, in the castering action lower edge riser tube that the promotes medium in advance accelerated motion that makes progress; The C4 of this device～C8 hydrocarbon mixture, contacts in the 3rd reactor drum C with regenerated catalyst and to react with the atomizing steam injecting lift pipe C from pipeline 13 through pipeline 12.The oil gas of reactor drum C outlet and catalyzer get into cyclone separator 7 through pipeline 15, isolate catalyzer and get into second reactor B through cyclone separator dipleg and pipeline 8, for it provides catalyzer and heat; Isolated oil gas 18 gets into settling vessel D through managing earlier.
The oil gas and the catalyzer of the outlet of second reactor B also get into settling vessel D through pipeline 16; After cyclone separator separates, catalyst-free almost in the oil gas, this oil gas is through the separation system F at pipeline 19 entering rear portions; Isolate ethene, propylene, C4～C8 hydro carbons, gasoline, diesel oil and slurry oil at separation system F; Slurry oil is through pipeline 5 whole freshenings, and part diesel oil is also through pipeline 5 freshenings, and portion C 4～C8 hydro carbons gets among the 3rd reactor drum C through pipeline 12 and reacts.Contact with water vapor from pipeline 20 at stripping stage 28 through the isolated catalyzer of settling vessel D, stripping goes out the oil gas of catalyst entrainment, and the carbon-bearing catalyzer (being called spent agent) behind the stripping gets into revivifier E through pipeline 21 and valve 22.
In revivifier E, reclaimable catalyst with contact through the air of pipeline 23 with air-distributor 24, burn the coke on the reclaimable catalyst, activity of such catalysts is able to recover, and burns simultaneously to discharge great amount of heat and supply reaction needed.Carry the flue gas of catalyzer and isolate catalyzer through cyclone separator 25, clean flue gas gets into smoke energy recovering system through pipeline 26, to reclaim the heat of flue gas.Regenerated catalyst gets into reactive system through pipeline 1 and pipeline 9 respectively.
Following embodiment will further explain present method, but therefore not limit the present invention.
Used heavy feed stock is decompressed wax oil F1 in embodiment and the Comparative Examples, and its character is as shown in table 1; Used lightweight material is F2, and its character is as shown in table 3.Catalyst system therefor MMC-2 catalyzer, this catalyzer are China Petrochemical Corp.'s Shandong catalyst plant production, and catalyst property is seen table 2.
Comparative Examples
The effect that the method for disclosed production low-carbon alkene and aromatic hydrocarbons is produced low-carbon alkene among the Comparative Examples explanation CN1898362.
The flow process of Comparative Examples is as shown in Figure 2; In medium-sized tester; The series connection of first reactor A and second reactor B, from the regenerated catalyst of revivifier E through the bottom of managing earlier 1, valve 2 is introduced the pre lift zone of first reactor A, in the accelerated motion that makes progress of the lifting lower edge riser reactor of the preparatory lifting medium of introducing through pipeline 4; Raw oil F1 is through pipeline 5 with from the atomizing steam of pipeline 6 injecting lift pipe A together, with the regenerated catalyst contact reacts.The oil gas of first reactor outlet and catalyzer get into and continue reaction in second reactor B, and the regenerator among the revivifier E adds to second reactor bottom through pipeline 27 simultaneously.Oil gas behind second reactor reaction gets among the settling vessel D through pipeline 16 with catalyzer and separates, and isolated spent agent carries out coke burning regeneration through managing earlier among the 21 entering revivifier E; Isolated oil gas gets into shunting stable system F through pipeline 19 to be separated, and separates the product that obtains and distributes through the gas chromatography determination product.Wherein the temperature of reaction of first reactor drum is 600 ℃, and the temperature of reaction of second reactor drum is 580 ℃, and the weight hourly space velocity of first reactor drum is 180hr
-1, the weight hourly space velocity of second reactor drum is 3hr
-1The operational condition of first and second reactor drum and product distribute as shown in table 4.
Embodiment
Embodiment explains the effect of method production low-carbon alkene provided by the invention.
As shown in Figure 1, in medium-sized tester, make an experiment first reactor drum and second reactors in series, the 3rd reactor drum and first reactor drum and the parallel connection of second reactor drum.No diesel oil and slurry oil freshening, raw oil F1 are as the raw material of first reactor drum, and carbon four freshening raw material F2 are as the raw material of the 3rd reactor drum.Wherein, the temperature of reaction of first reactor drum is 560 ℃, and weight hourly space velocity is 180hr
-1The temperature of reaction of second reactor drum is 600 ℃, and weight hourly space velocity is 3hr
-1, second reactor drum is 1: 60 with the ratio of the weight hourly space velocity of first reactor drum.The temperature of reaction of the 3rd reactor drum is 680 ℃, accounts for 24% of entire reaction system response heat for the second reactor drum additional heat.Behind the product separation, wherein have only C 4 olefin to be circulated to the 3rd reactor drum, other recycle stock is circulation not.The operational condition of first, second and third reactor drum and product distribute as shown in table 4.
Table 1 raw oil
| Raw oil | F1 | |
| Density (20 ℃), | g/cm 3 | 0.8966 |
| Kinematic viscosity, | mm 2/s(80℃) | 57.11 |
| Kinematic viscosity, | mm 2/s(100℃) | 29.94 |
| Condensation point, | ℃ | 42 |
| Carbon residue, | m％ | 4.9 |
| Refractive index, | (n D 20) | 1.4852 |
| Elementary composition, m% | ||
| C | 86.47 | |
| H | 13.00 | |
| N | 0.35 | |
| S | 0.17 | |
| Boiling range, ℃ | ||
| Over point | 304 | |
| 5％ | 368 | |
| 10％ | 386 | |
| 30％ | 488 | |
| 50％ | 557(46％) | |
| 70％ | - | |
| 90％ | - | |
| Do | - | |
Table 2 catalyzer
| Catalyzer | C1 |
| Chemical constitution, w% | |
| RE 2O 3 | 0.56 |
| Al 2O 3 | 54.00 |
| Physical properties | |
| Specific surface, m 2/g | 120 |
| Pore volume, cm 3/g | 0.17 |
| Apparent density, g/cm 3 | 0.91 |
| Screening, w% | |
| 0～20μm | 0.8 |
| 0～40μm | 10.4 |
| 0～80μm | 70.8 |
| 0～110μm | 88.5 |
| 0～149μm | 97.8 |
| ＞149μm | 2.2 |
| APS，μm | 64.3 |
| Micro-activity, w% | 60 |
Table 3 raw material F2 C 4 olefin is formed
| Form | w％ |
| Butene-1 | 15.53 |
| Iso-butylene | 43.67 |
| Instead-butylene | 24.02 |
| Suitable-butylene | 16.78 |
Table 4 operational condition and product distribute
| Project | Comparative Examples | Embodiment |
| Catalyzer | C1 | C1 |
| The 3rd reactor feedstocks | - | F2 |
| First reactor feedstocks | F1 | F1 |
| The first reactor feed amount, kg/h | 6 | 6 |
| The first reactor reaction pressure, MPa (absolute pressure) | 0.22 | 0.22 |
| First average reactor temperature, ℃ | 580 | 560 |
| The first reactor drum agent-oil ratio, w/ |
12 | 10 |
| The first reactor drum air speed, hr -1 | 180 | 180 |
| The first reactor drum atomizing steam amount, kg/hr | 1.8 | 1.8 |
| The first reactor feedstocks preheating temperature, ℃ | 330 | 330 |
| Second average reactor temperature, ℃ | 600 | 600 |
| The second reactor drum agent-oil ratio, w/w | 17 | 17 |
| The second reactor drum WHSV air speed, |
3 | 3 |
| The 3rd average reactor temperature, ℃ | - | 680 |
| The 3rd reactor drum freshening carbon four inlet amounies, kg/h | - | 1.2 |
| The 3rd reactor drum freshening carbon four atomizing steam amounts, kg/h | - | 0.12 |
| The 3rd reactor feedstocks preheating temperature, ℃ | - | 150 |
| The 3rd reactor drum agent-oil ratio, w/w | - | 35 |
| The 3rd reactor drum WHSV air speed, hr -1 | - | 3.5 |
| Product distributes, w% | - | |
| Dry gas | 12.3 | 13.2 |
| Liquefied gas | 48.1 | 42.8 |
| Gasoline | 18.5 | 22.1 |
| Diesel oil | 9.5 | 9.7 |
| Slurry oil | 2.1 | 2.1 |
| Coke | 9.5 | 10.1 |
| Amount to | 100.0 | 100.0 |
| Ethylene yield, w% | 7.5 | 8.3 |
| Productivity of propylene, w% | 24.1 | 28.4 |
Can find out from table 4, compare that the propylene of method provided by the invention and yield of ethene are 28.4w% and 8.3w%, improve 4.3 percentage points and 0.8 percentage point respectively with Comparative Examples.
Claims (14)
1. a method of producing low-carbon alkene is characterized in that comprising: heavy feed stock is introduced in catalytic cracking first reactor drum, with the catalytic cracking catalyst contact reacts from revivifier, reacted back oil gas and catalyzer and get into second reactor drum continuation reaction; Lightweight material is introduced in the 3rd reactor drum, and with the catalytic cracking catalyst contact reacts from revivifier, the oil gas behind the 3rd reactor reaction separates through gas-solid separation equipment with reclaimable catalyst, and isolated reclaimable catalyst is introduced second reactor drum; Oil gas behind second reactor reaction and reclaimable catalyst are after separating; Isolated reclaimable catalyst in revivifier, after coke burning regeneration recovers activity, returns first reactor drum and the 3rd reactor cycles is used; The isolated oil gas of second reactor drum and the 3rd reactor drum is introduced catalytic cracking separating stable system, obtains purpose product low-carbon alkene through fractionation; Wherein the temperature of reaction of second reactor drum is higher than the temperature of reaction of first reactor drum, and weight hourly space velocity is lower than the weight hourly space velocity of first reactor drum, and the temperature of reaction of the 3rd reactor drum is higher than the temperature of reaction of second reactor drum.
2. according to the method for claim 1, it is characterized in that the reaction conditions in described first reactor drum is: temperature of reaction is 500～650 ℃, and weight hourly space velocity is 0.1～750h
-1, the reaction absolute pressure is the weight ratio 2～100 of 0.10～1.0MPa, catalytic cracking catalyst and raw material; The temperature of reaction of second reactor drum is higher 10～100 ℃ than the temperature of reaction of first reactor drum, and the weight hourly space velocity of second reactor drum is 1 with the ratio of the weight hourly space velocity of first reactor drum: (1.1～750).
3. according to the method for claim 2, the reaction conditions that it is characterized in that described first reactor drum is that temperature of reaction is 540～600 ℃, and weight hourly space velocity is 1～500h
-1, the weight ratio 5～50 of catalytic cracking catalyst and raw material.
4. according to the method for claim 2, it is characterized in that the temperature of reaction of described second reactor drum is higher 20～60 ℃ than the temperature of reaction of first reactor drum; The ratio of the weight hourly space velocity of the weight hourly space velocity of second reactor drum and first reactor drum is 1: (1.1～300).
5. according to the method for claim 1, it is characterized in that the operational condition of described the 3rd reactor drum is: temperature of reaction is 600～750 ℃, and the residence time is 1～20 second, the weight ratio 4～100 of reaction absolute pressure 0.10～1.0MPa, catalyzer and raw material.
6. according to the method for claim 5, it is characterized in that the operational condition of described the 3rd reactor drum is: temperature of reaction is 650～700 ℃, and the residence time is 1～10 second, and the weight ratio of catalyzer and raw material is 5～80.
7. according to the method for claim 1, it is characterized in that described heavy feed stock is selected from one or more the mixture in decompressed wax oil, normal pressure wax oil, wax tailings, deasphalted oil, vacuum residuum, long residuum, recycle stock, slurry oil, the diesel oil.
8. according to the method for claim 1, it is characterized in that described lightweight material is selected from gasoline and/or C4～C8 hydrocarbon mixture.
9. according to the method for claim 8, it is characterized in that described lightweight material is selected from the hydrocarbon mixture of C4～C8.
10. according to the method for claim 1, it is characterized in that described catalyzer contains zeolite, inorganic oxide and optional clay,, contain zeolite 10～50w%, inorganic oxide 5～90w%, clay 0～70w% in total catalyst weight.
11. according to the method for claim 10, it is characterized in that described catalyst activity component is selected from Y type or HY type zeolite, the ultrastable Y that contains or do not contain rare earth that contains or do not contain rare earth, the zeolite with MFI structure or the supersiliceous zeolite that makes with other method with five-membered ring structure in one or more catalyzer.
12., it is characterized in that described first reactor drum is riser tube, upstriker transfer limes, downstriker transfer limes or fluidized-bed reactor according to the method for claim 1; Described second reactor drum is a fluidized-bed reactor; Described the 3rd reactor drum is a riser reactor.
13., it is characterized in that described first reactor drum is riser reactor or fluidized-bed reactor according to the method for claim 12.
14., it is characterized in that described first reactor drum is a riser reactor according to the method for claim 12.
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| CN105349172B (en) * | 2014-08-20 | 2017-03-01 | 中国石油化工股份有限公司 | The catalytic cracking method of feed naphtha |
| CN109704903B (en) * | 2017-10-25 | 2021-09-07 | 中国石油化工股份有限公司 | Method for producing more propylene and light aromatic hydrocarbon |
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| CN112745899B (en) * | 2019-10-30 | 2023-01-13 | 中国石油化工股份有限公司 | Catalytic conversion method and catalytic conversion device for producing low-carbon olefins |
| CN111807919B (en) * | 2020-07-09 | 2023-04-25 | 青岛京润石化设计研究院有限公司 | Method and device for preparing ethylene and propylene by catalytic conversion of petroleum hydrocarbon |
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| CN114763315B (en) * | 2021-01-11 | 2024-05-17 | 中国石油化工股份有限公司 | Catalytic conversion method for preparing low-carbon olefin |
| CN113004936B (en) * | 2021-03-01 | 2022-10-18 | 润和催化剂股份有限公司 | Method, device and reaction system for producing low-carbon olefin by using petroleum hydrocarbon |
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