CN109705905A - A kind of method and apparatus of low-carbon olefines high-output - Google Patents
A kind of method and apparatus of low-carbon olefines high-output Download PDFInfo
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- CN109705905A CN109705905A CN201711015430.0A CN201711015430A CN109705905A CN 109705905 A CN109705905 A CN 109705905A CN 201711015430 A CN201711015430 A CN 201711015430A CN 109705905 A CN109705905 A CN 109705905A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
The invention discloses a kind of method and apparatus of low-carbon olefines high-output.This method comprises: (1), in the first riser reactor, heavy charge and catalytic cracking catalyst haptoreaction obtain carbon deposited catalyst and the first reaction product, then separate to carbon deposited catalyst and the first reaction product；(2) in the second riser reactor, lightweight material and catalytic cracking catalyst haptoreaction, oil agent mixture after reaction is reacted in a fluidized bed reactor, obtain the second reaction product and carbon deposited catalyst, carbon deposited catalyst is filtered from the second reaction product, fluidized-bed reactor is discharged from fluidized bed lower layer in carbon deposited catalyst；(3) carbon deposited catalyst is regenerated in a regenerator, obtains regenerated catalyst, regenerated catalyst is used as the catalytic cracking catalyst of step (1) and/or step (2).Methods and apparatus of the present invention can significantly improve the yield of low-carbon alkene.
Description
Technical field
The present invention relates to a kind of method and apparatus of low-carbon olefines high-output.
Background technique
The low-carbon alkenes such as propylene, butylene are all very important Organic Chemicals, currently, propylene and butylene main source
In steam cracking technology, catalytic cracking technology, preparing propylene by dehydrogenating propane technology and ammonia from coal alkene technology processed again.In steam heat
In cracking, due to not using catalyst, it is therefore desirable to which the cost of very harsh operating condition, device and operation is very high.
On the other hand, as steam thermal cracking uses new lightweight material, product distribution will will appear variation, such as using ethane as steaming
Vapour cracking stock, with using naphtha, compared with raw material, propane ratio is significantly improved in product, and the yield of propylene and butylene will
It reduces.Catalytic cracking process can produce more propylene and butylene, be that an effectively supplement of steam heat cracking ethylene preparation is arranged
It applies.But with the intensification of crude oil heaviness, in poor quality degree, to Conventional catalytic cracking technique, more stringent requirements are proposed.Due to
Conventional catalytic cracking technology mainly produces gasoline and diesel oil, the low-carbon alkenes such as by-product propylene and butylene, but its yield is not high, is difficult
Meets the needs of market, therefore it is to have very much that exploitation, which is capable of handling heavy raw oil and the catalytic cracking technology of low-carbon olefines high-output,
It is necessary.
A kind of catalyst cracking method for producing propylene is disclosed in CN102690683A.This method uses double lifting leg structure
Type, the first riser reactor use the catalyst containing y-type zeolite and zeolite beta for treatment of heavy hydrocarbon oil, and second
Riser reactor handles light hydrocarbon, uses and selects type zeolite less than 0.7nm containing aperture.This method uses two kinds of differences
Catalyst, and stripping zone and regeneration are distinguished by two independent parts by partition respectively, increase the complexity of device
Degree, not only bad for operation, and the yield of propylene and butylene is not high, is also not directed to race's composition of gasoline.
CN104560149A discloses a kind of catalysis conversion method for producing butylene.This method is provided with 4 reactors altogether,
Other than adding the reactor configuration of fluidized bed using double lifting leg, a fluidized-bed reaction also is provided in the outside of settler
Device, for gasoline fraction in cracking, and reaction product enters riser reactor and continues that cracking reaction, the catalysis after reaction occurs
Agent is recycled in Returning reactor after coke burning regeneration.This method using the mixture containing Y zeolite and β zeolite as catalyst,
Higher propylene and butylene yield can be obtained.
CN105505456A discloses a kind of catalytic cracking unit.The device includes riser reactor, settler and vapour
Device is mentioned, wherein the lower chamber in settler is provided with the sleeve of the up and down aperture coaxial with the settler, riser reactor
Outlet is located in sleeve, and fluidized bed reaction zone can be formed in sleeve, and the catalyst outlet of two cyclone separators is located at by covering
The outer wall of cylinder and the inner wall of settler are formed by space, it is possible to reduce the carbon deposited catalyst convection current separated by cyclone separator
The interference of fluidized bed reactor bed increases the height of fluidized bed bed, to improve the yield of low-carbon alkene.But the device uses
Be single riser reactor, and be not involved with the freshening of gasoline fraction, it is not high so as to cause the yield of low-carbon alkene.
Although the above technology is improved in catalytic cracking process and is achieved in terms of the productivity of low carbon olefin hydrocarbon such as propylene and butylene
Progress, but device operation is more complicated, and the yield of propylene and butylene needs to be further increased.
Summary of the invention
The object of the present invention is to provide a kind of methods of the low-carbon olefines high-output of yield for further increasing propylene and butylene
And device.
The inventors discovered that after lightweight material is reacted in riser reactor and fluidized-bed reactor, to fluidisation
Reaction product obtained in bed reactor is filtered, and can prevent catalyst from leaving fluidized-bed reactor together with oil gas, is tieed up
The reserve of catalyst in fluidized-bed reactor is held, provides suitable condition for reaction, so that the yield of low-carbon alkene is significantly improved,
It has thus completed the present invention.
To achieve the goals above, the present invention provides a kind of method of low-carbon olefines high-output, this method comprises:
(1) in the first riser reactor, heavy charge and catalytic cracking catalyst haptoreaction obtain carbon deposit catalysis
Agent and the first reaction product, then separate carbon deposited catalyst and the first reaction product；
(2) in the second riser reactor, lightweight material and catalytic cracking catalyst haptoreaction, the finish after reaction
Mixture reacts in a fluidized bed reactor, obtains the second reaction product and carbon deposited catalyst, filters from the second reaction product
Fluidized-bed reactor is discharged from fluidized bed lower layer in carbon deposited catalyst, carbon deposited catalyst；
(3) carbon deposited catalyst is regenerated in a regenerator, obtains regenerated catalyst, regenerated catalyst is used as step
(1) and/or the catalytic cracking catalyst of step (2).
Preferably, it includes the second reaction that will be mingled with carbon deposited catalyst that carbon deposited catalyst is filtered from the second reaction product
Product passes through the filter being arranged in above fluidized-bed reactor.
Preferably, method of the invention further includes purging from the top of the filter to the filter, preferably
It is purged using steam.
Preferably, method of the invention further includes carrying out cyclonic separation and stripping to filtered second reaction product.
Preferably, the process separated to carbon deposited catalyst and the first reaction product includes cyclonic separation and stripping.
Preferably, the heavy charge be selected from decompressed wax oil, reduced crude, decompression residuum, wax tailings, deasphalted oil,
Furfural treatment raffinates oil, liquefied coal coil, tar sand oil, shale oil, by one in the F-T distillate synthesized or vegetable and animals oils
Kind or more than one mixture.
Preferably, the lightweight material is light gasoline fraction and/or C4 hydrocarbon；Preferably, light gasoline fraction is from described second
The middle part of riser reactor introduces, and C4 hydrocarbon is introduced in the bottom of the second riser reactor.
Preferably, the catalytic cracking catalyst contains cracking activity constituent element, clay and binder, it is preferable that the work
Property constituent element contains Y type molecular sieve, MFI structure molecular sieve and SAPO-34 molecular sieve.
Preferably, in the active component, with the total weight of the active component, the content of Y molecular sieve is 20~90
Weight %, preferably 50~80 weight %, the content of MFI structure molecular sieve are 1~50 weight %, preferably 10~40 weights
% is measured, the content of SAPO-34 molecular sieve is 1~50 weight %, preferably 10~40 weight %.
Preferably, the reaction temperature of first riser is 450~650 DEG C, preferably 500~600 DEG C；Oil ratio is
1~20, preferably 5~15；Reaction time is 0.50~10 second, preferably 1~5 second；
The reaction temperature of second riser is 500~700 DEG C, preferably 550~650 DEG C；Oil ratio is 10~30,
Preferably 15~25；Reaction time is 0.10~1.5 second, preferably 0.3~0.8 second；
The reaction temperature of the fluidized-bed reactor is 500~650 DEG C, preferably 520~580 DEG C；Weight (hourly) space velocity (WHSV) be 2~
15 hours-1, preferably 3~10 hours-1；Density of catalyst is 100~600kg/m3, preferably 200~400kg/m3；The line of oil gas
Speed is 0.3~2m/s, preferably 0.3~1.5m/s.
The present invention also provides a kind of device of low-carbon olefines high-output, which includes: the first riser reactor 1,
Two riser reactors 2, fluidized-bed reactor 3, settler 4, stripper 5 and regenerator 6；First riser reactor 1
It is connected to the settler 4；Second riser reactor 2 is connected to the fluidized-bed reactor；The fluidized-bed reaction
The top of device 3 is provided with filter 34, and the fluidized-bed reactor 3 is connected to the settler 4, and the filter 34 is located at institute
It states between fluidized-bed reactor 3 and the settler 4；The regenerator 6 respectively with first riser reactor 1 and described
The connection of second riser reactor 2.
Preferably, it is equipped with gas around the filter 34 and purges ring 35, the set-up mode of the gas purging ring 35 makes
Gas purging direction be perpendicular to filter surfaces to filter surfaces angle at 45 °.
Preferably, the fluidized-bed reactor 3 is located at the outside of the settler 4.
Preferably, first riser reactor 1 and the second riser reactor 2 be respectively equal diameter riser, etc.
Linear speed riser or variable diameters riser；
The fluidized-bed reactor 3 be selected from fixed fluidized-bed reactor, dispersion fluidized bed reactor, bubbling bed reactor,
The combination of one or more of turbulent bed reactor, fast bed reactor, transport bed reactor and dense-phase fluidized bed reactor.
The present invention is filtered by reaction product obtained in fluid bedreactors, significantly improves low-carbon alkene
Yield.
Detailed description of the invention
Fig. 1 is a kind of schematic diagram of embodiment of method and apparatus provided by the invention.The figure be used to illustrate the present invention,
But it is not thereby limiting the invention.Wherein:
The first riser reactor of 1-,
11- heavy charge pipeline,
12- the first atomizing steam pipeline,
13- freshening cracking masout pipeline,
14- the second atomizing steam pipeline,
15- the first riser reactor pre-lift gas line,
The second riser reactor of 2-,
21-C4 hydrocarbon pipeline,
22- third atomizing steam pipeline,
23- light gasoline fraction pipeline,
The 4th atomizing steam pipeline of 24-,
25- the second riser reactor pre-lift gas line,
3- fluidized-bed reactor,
31- oil gas pipeline,
32- catalyst transport pipeline,
33- the second riser reactor outlet distributor,
34- filter,
35- gas purges ring,
36- purges steam entrance,
4- settler,
41- cyclone separator,
45- reaction oil gas introduces separation system pipeline,
5- stripper,
51- stripping baffles,
6- regenerator,
61- regenerated catalyst line,
62- regenerator stripped vapor pipeline,
63- stripper stripped vapor pipeline,
64- regenerated flue gas pipeline,
Specific embodiment
Detailed description of the preferred embodiments below.It should be understood that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to restrict the invention.
The method of low-carbon olefines high-output provided by the invention includes:
(1) in the first riser reactor, heavy charge and catalytic cracking catalyst haptoreaction obtain carbon deposit catalysis
Agent and the first reaction product, then separate carbon deposited catalyst and the first reaction product；
(2) in the second riser reactor, lightweight material and catalytic cracking catalyst haptoreaction, the finish after reaction
Mixture reacts in a fluidized bed reactor, obtains the second reaction product and carbon deposited catalyst, filters from the second reaction product
Fluidized-bed reactor is discharged from fluidized bed lower layer in carbon deposited catalyst, carbon deposited catalyst；
(3) carbon deposited catalyst is regenerated in a regenerator, obtains regenerated catalyst, regenerated catalyst is used as step
(1) and/or the catalytic cracking catalyst of step (2).
A preferred embodiment of the invention: in the first riser reactor, heavy charge and catalytic cracking
Catalyst haptoreaction, the oil agent mixture after reaction are separated by separator.In the second riser reactor, lightweight is former
Material and catalytic cracking catalyst haptoreaction, oil agent mixture after reaction enters to be connected with the second riser reactor end
The reaction was continued in fluidized-bed reactor, and the carbon deposited catalyst of fluidized bed lower layer is introduced into stripper by delivery pipe, the oil on upper layer
Gas is introduced into separator by delivery pipe, isolates the catalyst granules wherein carried secretly.The separator preferably dispenses fastly
It sets, to by reaction oil gas and carbon deposited catalyst quick separating, preferred fast packing is set to cyclone separator.Pass through fast separating device
By oil gas with react after carbon deposited catalyst be rapidly separated, can reduce dry gas yied, low-carbon alkene is inhibited to convert again after generation.
The oil gas separated is through products such as the isolated cracked gas of subsequent product separation system, gasoline, light oil and heavy oil；Spent agent into
Enter subsequent stripper, the spent agent after stripping is imported after regenerator regenerates by feed-line and returns to the first riser reactor
It is recycled with the second riser reactor.The product separation system is the prior art, and the present invention does not have particular/special requirement.
In the present invention, the heavy charge can be selected from decompressed wax oil, reduced crude, decompression residuum, wax tailings, take off
Coal tar, furfural treatment raffinate oil, liquefied coal coil, tar sand oil, shale oil, by the F-T distillate synthesized or animals and plants
One of oil or more than one mixture.
In the present invention, the lightweight material can be light gasoline fraction and/or C4 hydrocarbon, be preferably enriched in the light vapour of alkene
Oil distillate and/or C4 hydrocarbon.
In the present invention, the light gasoline fraction rich in alkene is selected from the light gasoline fraction that boiling range is 40~120 DEG C, excellent
Selecting boiling range is 40~85 DEG C of light gasoline fraction.The light gasoline fraction includes apparatus of the present invention production (i.e. from institute of the present invention
State product separation system) light gasoline fraction or other devices production light gasoline fraction: other devices production light petrol evaporate
It point can be selected from light FCC gasoline, light coker naphtha, visbreaking light petrol and other oil refining or chemical process produced
One of light gasoline fraction or more than one mixture, the preferred light gasoline fraction of present apparatus production.The injection the
The weight ratio of the heavy charge of the first riser reactor of light gasoline fraction and injection of two riser reactors can be 0.05
~0.20:1, preferably 0.08~0.15:1.The light gasoline fraction is preferably enriched in the light gasoline fraction of alkene, olefin(e) centent
It can be 20~95 weight %, preferably 35~90 weight %, more preferable 50 weight % or more.
In the present invention, the C4 hydro carbons refers to deposit in gaseous form under C 4 fraction room temperature as main component, normal pressure
Low-molecular-weight hydrocarbon, including carbon atom number in molecule be 4 alkane, alkene and alkynes.The C4 hydro carbons includes this
The gaseous hydrocarbon products rich in C 4 fraction of invention device production also may include that other device processes are produced rich in C 4 fraction
Gaseous hydrocarbon, wherein it is preferred that apparatus of the present invention production C 4 fraction.The C4 hydro carbons is preferably enriched in the C 4 fraction of alkene, wherein
The content of C4 alkene is greater than 50 weight %, preferably greater than 60 weight %, preferably more than 70 weight %.The C4 hydrocarbon is evaporated with gasoline
The weight ratio divided is 0~2:1, preferably 0~1.2:1.
In the present invention, the light gasoline fraction and C4 hydrocarbon can introduce the in the same position of the second riser reactor
Two riser reactors can also introduce the second riser reactor in different positions, preferably introduce second in different positions
Riser reactor；The light gasoline fraction and C4 hydrocarbon are anti-in different location the second riser of introducing of the second riser reactor
When answering device, it can be light gasoline fraction in the bottom of the second riser reactor and introduce the second riser reactor, be also possible to
C4 hydrocarbon introduces the second riser reactor in the bottom of the second riser reactor, and preferably C4 hydrocarbon is in the second riser reactor
Bottom introduces the second riser reactor.In the present invention, the lightweight material is split in the second riser reactor with catalysis
Entered and the second riser reactor end phase after changing catalyst haptoreaction by the second riser reactor outlet distributor
The reaction was continued in fluidized-bed reactor even.It is provided with uniform aperture on the distributor, can make from second reactor
Oil agent mixture is even into fluidized-bed reactor, and the flow direction of adjustable oil agent mixture, reduces oil gas and returns
It is mixed.The distributor preferred lower pressure distributor, pressure drop are less than 10kPa.Oil gas after reaction passes through the fluidized-bed reactor
The filter at top, then enters in separator through delivery pipe, isolates the catalyst granules wherein carried secretly.The filter
Catalyst can be reduced and leave fluidized-bed reactor together with oil gas, to maintain the reserve of catalyst in fluidized-bed reactor.
Preferably, it is mounted with that gas purges ring around the filter, catalyst granules blocking catalyst mistake is prevented by gas purging
Filter.Wherein, the gas purging ring is arranged around catalyst filter, can arrange one group of gas purging ring, can also be with cloth
Multiple groups gas purging ring is set, preferably arrangement multiple groups gas purges ring.Gas for purging can be selected from vapor, C1-C4Hydro carbons
Or one of Conventional catalytic cracking dry gas or a variety of, preferred vapor.Gas purging direction is preferably normal to filter
Device surface to filter surfaces angle at 45 °.Preferably, slide valve is arranged in fluidized-bed reactor lower part outlet, passes through slide valve aperture
Catalyst transport speed is controlled, to maintain the reserve of catalyst in fluidized-bed reactor.
In the present invention, it is preferred to which the cracking masout for also obtaining product of the present invention separation system introduces the first riser
It is reacted in reactor, this advantageously reduces dry gas yied and coke yield, and improves low-carbon system especially productivity of propylene.
It is highly preferred that the cracking masout introduces position in the middle and lower reaches of the first riser reactor.The cracking masout is this
The cracking masout that invention product separation system obtains, normal pressure boiling range is between 330~550 DEG C, and preferably its normal pressure boiling range is 350
~530 DEG C.Inject the weight of the heavy charge of the first riser reactor of cracking masout and injection of the first riser reactor
Than for 0.05~0.30:1, preferably 0.10~0.2:1.
In the present invention, the first riser reactor is entered after the heavy charge is preheated to 180~340 DEG C, and is come from
The catalytic cracking catalyst of regenerated catalyst is reacted.Operating condition packet in first riser reactor
Include: reaction temperature is 450~650 DEG C, preferably 500~600 DEG C；Oil ratio (the weight of catalytic cracking catalyst and heavy charge
Measure ratio) it is 1~20, preferably 5~15；Reaction time is 0.50~10 second, preferably 1~5 second；Reactor pressure is (absolutely
Pressure) it is 0.1~0.4MPa, preferably 0.15~0.35MPa；Atomization water vapour accounts for the ratio of heavy charge inlet amount and is preferably
10~30 weight %, preferably 10~20 weight %.
In the present invention, the second riser reactor is entered after the lightweight material is preheated to 250~400 DEG C, and is come from
The catalyst of regenerated catalyst is reacted.Operating condition in second riser reactor are as follows: reaction temperature 500
~700 DEG C, preferably 550~650 DEG C；Oil ratio (introduce the second riser reactor catalytic cracking catalyst and C4 hydrocarbon and
The mass ratio of gasoline fraction) it is 10~30, preferably 15~25；Reaction time be 0.10~1.5 second, preferably 0.3~0.8
Second；It is preferably 10~20 weight % that atomization water vapour, which accounts for C4 hydrocarbon and the ratio of gasoline fraction inlet amount,.Reaction oil gas and catalyst
Mixture enters fluidized-bed reactor, the reaction temperature of the fluidized-bed reactor through the outlet distributor of the second riser reactor
Degree is 500~650 DEG C, preferably 520~580 DEG C；Weight (hourly) space velocity (WHSV) is 2~15 hours-1, preferably 3~10 hours-1；Catalyst
Density is 100~600kg/m3, preferably 200~400kg/m3；Material position is the 1/3~4/5 of fluidized-bed reactor height, is preferably flowed
The 1/3~2/3 of fluidized bed reactor height；Oil gas is 0.3~2m/s by the linear velocity of fluidized-bed reactor, preferably 0.3~
1.5m/s；Reactor pressure is 0.1~0.4MPa (absolute pressure), preferably 0.15~0.35MPa.
In the present invention, the catalytic cracking catalyst for introducing the first riser reactor is usually from regenerator
Regenerative agent, due to regenerated needs, the temperature of regenerative agent would generally be higher than 700 DEG C, for this purpose, regenerative agent first carries out taking at heat cooling
Reason, being cooled to temperature is 520~680 DEG C, preferably 550~620 DEG C.
In the present invention, the heavy charge is contacted in the first riser reactor bottom with catalytic cracking catalyst and is gone forward side by side
Row reaction, the mixing temperature after heavy charge is contacted with catalytic cracking catalyst is 520~680 DEG C, preferably 540~610 DEG C.
In the present invention, the catalytic cracking catalyst for introducing the second riser reactor is usually from regenerator
Regenerative agent, due to regenerated needs, the temperature of regenerative agent would generally be higher than 700 DEG C, for this purpose, regenerative agent first carries out taking at heat cooling
Reason, being cooled to temperature is 550~680 DEG C, preferably 580~660 DEG C.
In the present invention, the lightweight material is contacted in the second riser reactor bottom with catalytic cracking catalyst and is gone forward side by side
Row reaction, the mixing temperature after lightweight material is contacted with catalytic cracking catalyst is 540~680 DEG C, preferably 560~630 DEG C.
In the present invention, the catalytic cracking catalyst can contain cracking activity constituent element, clay and binder.It is preferred that
Ground, the active component contain Y type molecular sieve, MFI structure molecular sieve and SAPO-34 molecular sieve.The catalytic cracking catalyst
Dry weight on the basis of, the content of cracking activity constituent element is 20~70 weight %, and preferably 30~50 weight %, clay contains
Amount is 15~60 weight %, and preferably 30~50 weight %, the content of binder is 20~35 weight %, preferably 20~30 weights
Measure %.In the active component, with the total weight of the active component, the content of the Y molecular sieve is 20~90 weights
%, preferably 50~80 weight % are measured, the content of the MFI structure molecular sieve is 1~50 weight %, preferably 10~40 weights
% is measured, the content of the SAPO-34 molecular sieve is 1~50 weight %, preferably 10~40 weight %.The Y type molecular sieve choosing
It is obtained from one of HY, USY, REUSY, REY, REHY, DASY, REDASY or a variety of, or through various metal oxide treateds
Y type molecular sieve.The MFI structure molecular sieve is selected from ZRP zeolite, phosphorous ZRP zeolite (CN1194181A), containing rare earth
ZRP zeolite (CN1052290A), phosphorous and rare earth ZRP zeolite (CN1147420A), phosphorous and alkaline-earth metal ZRP zeolite
(CN1211470A) and one of the ZRP zeolite (CN1465527A) of phosphorous and transition metal or a variety of.The clay choosing
From the various clays that can be used as catalytic component, such as kaolin, montmorillonite, bentonite.The binder is selected from silica solution, aluminium
One or both of colloidal sol and boehmite or three kinds of mixture, wherein preferred binder is Aluminum sol and intends thin water
The double aluminium binder of aluminium stone.Macromolecule reactant can be made to be cracked into gasoline component using Y type molecular sieve, use MFI type molecule
Sieve can make gasoline component be cracked into C3, C4 alkene, C5, C6 cracking of olefins can be made at C2, C3 alkene using SAPO-34 molecular sieve
Hydrocarbon, to improve the yield of the low-carbon alkenes such as propylene, butylene.
In the present invention, the first riser reactor and the second riser reactor can be each independently selected from equal diameter
Riser reactor, etc. one or more of linear speeds riser reactor and variable diameters riser reactor combination.Wherein
First riser reactor and the second riser reactor can be using identical patterns or using different patterns.It is described
Fluidized-bed reactor be selected from fixed fluidized-bed reactor, dispersion fluidized bed reactor, bubbling bed reactor, turbulent bed reactor,
The combination of one or more of fast bed reactor, transport bed reactor and dense-phase fluidized bed reactor.The fluidized bed is anti-
Answering device is barrel type reactor, and the height and diameter ratio of the cylinder are h/d=3~10:1, preferably h/d=5~8:1.
In the present invention, it is preferred to which the fluidized-bed reactor is located at the outside of stripper, pass through catalyst transport pipeline
The catalyst of fluidized bed lower layer is introduced into stripper and is stripped, the conveying of catalyst is controlled by the slide valve in delivery pipe
Speed, to control catalyst inventory and material position in fluidized-bed reactor.The oil gas after reaction is drawn by oil gas pipeline
Enter into separator, isolates the catalyst granules wherein carried secretly.
In method of the invention, the mode of operation and operating condition of regenerator can refer to Conventional catalytic cracking regenerator.
A kind of specific embodiment of device provided by the invention is as described in Figure 1, and described device includes at least reactor portion
Point, stripper section, settler and regenerator section.It is preferred that reactor takes the group formed using double lifting leg and fluidized bed
Reactor configuration is closed, one of riser is mutually arranged in juxtaposition after connecting with fluidized-bed reactor with another riser, described
Fluidized-bed reactor is located at the outside of stripper, and the riser and fluidized-bed reactor cascaded structure further with stripping
Device arranged in series.
In the present invention, the catalytic convention design includes riser reactor 1, riser reactor 2, is attached thereto
The entrance of fluidized-bed reactor 3, settler 4, cyclone separator 41, stripper 5, cyclone separator 41 is located at 4 top of settler,
The catalyst outlet position of cyclone separator 41 makes catalyst therein be able to enter stripper 5, the oil gas of cyclone separator 41
Outlet is connected to after being connected with oil and gas separating system.
In the present invention, 2 exit of the second riser reactor is equipped with the second riser reactor outlet distribution
Device 33 is provided with uniform aperture on the distributor, can make the oil agent mixture from the second riser reactor 2 uniformly into
In fluidized bed reactor 3, and the flow direction of adjustable oil agent mixture, reduce oil gas back-mixing.The fluidized bed is anti-
It answers and filter 34 is installed at the top of device 3, can prevent catalyst from leaving fluidized-bed reactor 3 together with oil gas, to maintain to flow
The reserve of catalyst in fluidized bed reactor 3.It is mounted with that gas purges ring 35 around the filter 34, is prevented by gas purging
Catalyst granules blocking catalyst filter.The gas purging ring 35 is arranged around filter 34, can arrange one group of gas
Ring is purged, can also arrange that multiple groups gas purges ring, preferably arrangement multiple groups gas purges ring.Gas purging direction is vertical
In 34 surface of catalyst filter to 34 surface of catalyst filter angle at 45 °.
In the present invention, the catalytic convention design further includes regenerator 6, completes catalytic cracking reaction for regenerating
Regenerated catalyst is delivered to riser reactor 1 by regenerated catalyst line 61 and mentioned by catalyst, the regenerator 6
The bottom of riser reactors 2.Wherein, pass through the conveying speed of the adjustable catalyst of valve on catalyst transport pipeline.
In the present invention, the stripper 5 is located at the top of regenerator 6, and the two takes coaxial arrangement.It is described
Regenerator 6 is connected to stripper 5 by spent agent delivery pipe.
In the present invention, fluidized-bed reactor 3 is located at the outside of settler 4, will be fluidized by catalyst transport pipeline 32
The catalyst of bed lower layer, which is introduced into stripper 5, to be stripped, and controls catalyst by speed, to maintain by slide valve aperture
The reserve of catalyst in fluidized-bed reactor 3.The oil gas after reaction is introduced into settler 4 by oil gas pipeline 31,
Isolate the catalyst granules wherein carried secretly.
In the present invention, for freshening cracking masout, the riser reactor 1 further includes freshening cracking masout entrance
13。
1 pair of method provided by the present invention is further detailed with reference to the accompanying drawing, but and is not so limited this hair
It is bright.
After heavy charge is preheated to 180~340 DEG C, through heavy charge feeding line 11 and the first atomizing steam pipeline is come from
After 12 atomizing steam is mixed in a certain ratio, riser reactor 1 is sprayed by nozzle, is 450~650 in reaction temperature
DEG C, preferably 500~600 DEG C；Oil ratio (weight ratio of catalytic cracking catalyst and heavy charge) be 1~20, preferably 5~
15；Reaction time is 0.50~10 second, preferably 1~5 second；Reactor pressure (absolute pressure) is 0.1~0.4MPa, preferably
To enter the regeneration of 1 bottom of the first riser reactor with by regenerated catalyst 61 under conditions of 0.15~0.35MPa
Catalyst is reacted.Oil agent mixture after reaction enters cyclone separator 41 and is separated, and is conveyed by regenerated catalyst
The conveying speed of the adjustable catalyst of valve on pipe 61 controls the inlet amount of regenerated catalyst to adjust oil ratio to appropriate
Range.
C4 hydrocarbon be preheated to 250~400 DEG C after through C4 hydrocarbon pipeline 21 and the atomizing steam from third atomizing steam pipeline 22
After mixing according to a certain percentage, the second riser reactor 2 is sprayed by nozzle and is reacted；Gasoline fraction is preheated to 250~
It is mixed according to a certain percentage through light gasoline fraction pipeline 23 with the atomizing steam from the 4th atomizing steam pipeline 24 after 400 DEG C
Afterwards, the second riser reactor 2 is sprayed by nozzle to be reacted.The operating condition of second riser reactor are as follows: reaction temperature
Degree is 500~700 DEG C, preferably 550~650 DEG C；Oil ratio (introduce the second riser reactor catalytic cracking catalyst with
The mass ratio of C4 hydrocarbon and gasoline fraction) it is 10~30, preferably 15~25；Reaction time be 0.10~1.5 second, preferably 0.3
~0.8 second；It is preferably 10~20 weight % that atomization water vapour, which accounts for C4 hydrocarbon and the ratio of gasoline fraction inlet amount,.Pass through regenerator vapour
The conveying speed for mentioning the adjustable catalyst of valve on steam pipe line 62 controls the inlet amount of regenerated catalyst with regulator oil
Than to range appropriate.Reaction oil gas and catalyst mixture enter fluidized bed through the second riser reactor outlet distributor 33
Reactor, the reaction temperature of the fluidized-bed reactor are 500~650 DEG C, preferably 520~580 DEG C；Weight (hourly) space velocity (WHSV) be 1~
15 hours-1, preferably 3~10 hours-1；Density of catalyst is 100~600kg/m3, preferably 200~400kg/m3；Material position is stream
The 1/3~4/5 of fluidized bed reactor height, preferably the 1/3~2/3 of fluidized-bed reactor height；Oil gas passes through fluidized-bed reactor
Linear velocity be 0.3~2m/s, preferably 0.3~1.5m/s；Reactor pressure is 0.1~0.4MPa (absolute pressure), preferably
For 0.15~0.35MPa.The catalyst of 3 lower layer of fluidized-bed reactor is introduced into stripper 5 by catalyst transport pipeline 32
It is stripped, by the conveying speed of the adjustable catalyst of valve on catalyst transport pipeline 32, controls fluidized-bed reaction
The reserve of catalyst is to range appropriate in device.The oil gas on upper layer, which enters cyclone separator 42 by catalyst filter 34, to carry out
Separation.Reaction oil gas after separation introduces the extraction reactor of separation system pipeline 45 by reaction oil gas and enters subsequent product separation
System (does not mark) in figure.Catalytic cracking production is separated into the production such as cracked gas, gasoline, light oil and heavy oil in product separation system
Object.Cracked gas can be obtained polymerization-grade propylene product after subsequent product is separated, refined and rich in the C 4 fraction of alkene.Gasoline is cut
It is segmented into light, heavy naphtha section, the part or all of Returning reacting system of light petrol converts again, preferably proposes light petrol return second
Riser reactors 2 convert again.Heavy oil is through freshening cracking masout pipeline 13 and the atomizing steam from the second atomizing steam pipeline 14
After being mixed in a certain ratio, the first riser reactor 1 is sprayed by nozzle, this advantageously reduces dry gas yied and coke produces
Rate, and improve low-carbon alkene especially productivity of propylene.
Spent agent after the separation of cyclone separator 41 enters stripper 5 and is stripped.Stripped vapor is stripped through stripper
Steam pipe line 63 injects in stripper, and with carbon deposited catalyst counter current contacting, reaction oil gas entrained by carbon deposited catalyst to the greatest extent may be used
Energy ground stripping is clean, and the stripped vapor in stripper can be directly entered settler 4, through cyclone separator together with other oil gas
Separation system pipeline 45 is introduced by reaction oil gas after 41 separation and draws reactor.Catalyst after stripping in stripper enters again
Coke burning regeneration is carried out in raw device 6.Oxygen-containing gas such as air injects regenerator 6, regenerated flue gas through regenerator stripped vapor pipeline 62
It is drawn in the headspace of regenerator 6 through regenerated flue gas pipeline 64.Catalyst after regeneration is through regenerated catalyst line 61
The first riser reactor 1 is returned respectively and the second riser reactor 2 is recycled.
During above-mentioned specific embodiment, mentioned by the first riser reactor pre-lift gas line 15 and second
Riser reactors pre-lift gas line 25 introduces pre- mention to the first riser reactor 1 and the second riser reactor 2 respectively
Rise medium.The pre-lift medium is can be selected from vapor, C known to those skilled in the art1-C4Hydro carbons or Conventional catalytic are split
Change one of dry gas or a variety of, preferably vapor.
It is mounted with catalyst filter at the top of fluidized-bed reactor in device provided by the invention, catalyst can be reduced
Fluidized-bed reactor is left together with oil gas, to maintain the reserve of catalyst in fluidized-bed reactor, it is suitable to provide for reaction
Condition.Higher hydrocarbon conversion ability, higher productivity of low carbon olefin hydrocarbon can achieve using method provided by the invention, simultaneously
The gasoline rich in aromatic hydrocarbons can also be produced.
The following examples illustrate the present invention further, but content not thereby limiting the invention.
In the embodiment of the present invention and comparative example, gaseous product is carried out using petrochemical analysis method RIPP 77-90 method
Test measures coke content using petrochemical analysis method RIPP 107-90 method, and organic liquid product composition uses SH/T
The fraction cut point of the measurement of 0558-1993 method, gasoline and diesel oil is respectively 221 DEG C and 343 DEG C, and light aromatics uses in gasoline
Petrochemical analysis method RIPP 82-90 measurement.
Below in an example, the conversion ratio of feedstock oil and the yield of cracked product are calculated according to the following formula:
RIPP petrochemical analysis method of the present invention is selected from " petrochemical egineering analysis method (RIPP test methods) ",
Yang Cui is surely equal to be compiled, Science Press, and 1990.
Reagent used below is except as expressly described chemically pure reagent.
Y type molecular sieve used is produced by Shandong catalyst plant, the industrial trade mark are as follows:
DASY, physical parameter are as follows: lattice constant 2.443nm, Na2O content is 0.85 weight %；
SAPO-34 molecular sieve used is produced by Shandong catalyst plant；
MFI structure molecular sieve used is produced by Shandong catalyst plant, the industrial trade mark are as follows:
ZRP-1: wherein SiO2/Al2O3=30, Na2The content of O is 0.17 weight %, rare earth oxide RE2O3Content be
1.4 weight %, wherein the content of lanthana is 0.84 weight %, and the content of cerium oxide is 0.18 weight %, other rare-earth oxidations
The content of object is 0.38 weight %.
Raw material used in embodiment and comparative example is heavy raw material A, and specific nature is shown in Table 1.In embodiment and comparative example
A kind of homemade catalyst is used, the active component of the catalyst is Y molecular sieve (DASY), ZRP molecular sieve and SAPO-34 divide
Son sieve, is denoted as CAT-1, specific preparation process for the catalyst are as follows: by DASY molecular sieve, ZRP molecular sieve and SAPO-34 molecular sieve
It is uniformly mixed, deionized water mashing is added, stirs evenly, obtain the molecular sieve pulp that solid content is 20~40 weight %；Then it will stick
Soil, binder and deionized water are mixed with beating, and are stirred evenly, and the carrier pulp that solid content is 15~25 weight % is obtained；It finally will be equal
The carrier pulp after molecular sieve pulp and homogeneous after matter is mixed with beating, and is then successively spray-dried, washed, filtered and done
It is dry, obtain catalyst CAT-1.The specific nature of CAT-1 is shown in Table 2.By catalyst in 790 DEG C, 100% vapor item before test
Aging 14 hours under part.
Embodiment 1
Test carries out on medium-sized tester.The device includes two riser reactors and a fluidized-bed reaction
Device.First riser reactor internal diameter is 16mm, and length 3800mm, the internal diameter of the second riser reactor is 16mm, height
For 3200mm, in one fluidized-bed reactor of the second riser reactor terminal tandem, the internal diameter of fluidized-bed reactor is 64mm,
Height is 500mm.Heavy charge A introduces the first riser reactor bottom, connects with the regenerated catalyst CAT-1 from regenerator
It touches and reacts, the oil gas and catalyst after reaction are separated by cyclone separator, and catalyst enters again after entering stripper
Raw device regeneration, the catalyst after regeneration return to riser reactor and are recycled, and oil gas introduces fractionating system and separated.Fractionation
Obtained light gasoline fraction (40~150 DEG C of boiling range, olefin(e) centent be 65 weight %) introduce in the middle part of second riser reactor away from
Position from the second riser reactor bottom 1500mm contacts with the regenerated catalyst CAT-1 from regenerator and occurs anti-
It answers, the oil gas and catalyst after conversion are into the reaction was continued with the concatenated fluidized-bed reactor of the second riser reactor, fluidisation
The catalyst of bed lower layer is introduced into stripper by feed-line to be stripped, and the oil gas on upper layer is defeated by passing through after filter
It send pipeline to introduce cyclone separator, isolates the catalyst granules wherein carried secretly.Catalyst enters regenerator after entering stripper
Regeneration, the catalyst after regeneration return to riser reactor and are recycled, and oil gas introduces fractionating system and separated.The light vapour
The mass ratio of oil distillate and heavy charge A are 0.1:1.Reaction condition and it the results are shown in Table 3.
Embodiment 2
According to the method for embodiment 1, C4 hydrocarbon (olefin(e) centent be 60 weight %) that fractionation obtains is introduced the unlike
Two riser reactor bottoms, not in the middle part of the second riser reactor introducing light gasoline fraction, C4 hydrocarbon and from regenerator
Regenerated catalyst CAT-1 contact and react.The mass ratio of the C 4 fraction and heavy charge A are 0.1:1.Reaction condition
And it the results are shown in Table 3.
Embodiment 3
According to the method for embodiment 1, unlike fractionation obtain light gasoline fraction (40~150 DEG C of boiling range, olefin(e) centent
The position of the second riser reactor of distance bottom 1500mm in the middle part of the second riser reactor, C4 hydrocarbon are introduced for 65 weight %)
(olefin(e) centent is 60 weight %) introduces the second riser reactor bottom, connects with the regenerated catalyst CAT-1 from regenerator
It touches and reacts, the ratio of light gasoline fraction and C4 hydrocarbon is 1:1.The light gasoline fraction and C 4 fraction mixture and heavy are former
The mass ratio for expecting A is 0.1:1.Reaction condition and it the results are shown in Table 3.
Embodiment 4
According to the method for embodiment 3, the difference is that being mentioned at the first riser reactor of distance outlet 1500mm to first
Riser reactors introduce cracking masout (boiling range of cracking masout is 350~500 DEG C), and the cracking masout is with heavy charge A's
Mass ratio is 0.1:1.Reaction condition and it the results are shown in Table 3.
Comparative example 1
Test carries out on medium-sized tester, which includes a riser reactor and a fluidized-bed reaction
Device.Riser reactor internal diameter is 16mm, length 3200mm, in one fluidized-bed reaction of riser reactor terminal tandem
The internal diameter of device, fluidized-bed reactor is 64mm, is highly 500mm.Heavy charge A introduces riser reactor bottom, and comes from
The regenerated catalyst CAT-1 of regenerator is contacted and is reacted, the oil gas and catalyst after conversion enter fluidized-bed reactor after
Continuous to be reacted, the oil gas and catalyst after reaction are separated by cyclone separator, and catalyst enters regeneration after entering stripper
Device regeneration, the catalyst after regeneration return to riser reactor and are recycled, and oil gas introduces fractionating system and separated.React item
Part and it the results are shown in Table 4.
Comparative example 2
Test carries out on medium-sized tester.The device includes two riser reactors.First riser reactor
Internal diameter is 16mm, and it is highly 3800mm that the internal diameter of length 3200mm, the second riser reactor, which are 16mm,.Heavy charge A draws
Enter the first riser reactor bottom, contacts and react with the regenerated catalyst CAT-1 from regenerator, the oil after conversion
Gas and catalyst are separated by cyclone separator, and catalyst enters regenerator regeneration, the catalyst after regeneration after entering stripper
It returns to riser reactor to be recycled, oil gas introduces fractionating system and separated.It is fractionated obtained light gasoline fraction (boiling range 40
~150 DEG C, olefin(e) centent is 65 weight %) introduce the second riser reactor of distance bottom in the middle part of the second riser reactor
The position of 1500mm contacts and reacts with the regenerated catalyst CAT-1 from regenerator, oil gas and catalyst after conversion
It is separated by cyclone separator, catalyst enters regenerator regeneration after entering stripper, and the catalyst after regeneration returns to riser
Reactor cycles use, and oil gas introduces fractionating system and separated.The mass ratio of the light gasoline fraction and heavy charge A is
0.1:1.Reaction condition and it the results are shown in Table 4.
Comparative example 3
According to the method for comparative example 1, the difference is that exporting at 1500mm apart from riser reactor to promotion tube reaction
Device introduces cracking masout (boiling range of cracking masout is 350~500 DEG C), and the mass ratio of the cracking masout and heavy charge A is
0.05:1.Reaction condition and it the results are shown in Table 4.
Comparative example 4
According to the method for comparative example 2, unlike fractionation obtain light gasoline fraction (40~150 DEG C of boiling range, olefin(e) centent
The position of the second riser reactor of distance bottom 1500mm in the middle part of the second riser reactor, C4 hydrocarbon are introduced for 65 weight %)
(olefin(e) centent is 60 weight %) introduces the second riser reactor bottom, connects with the regenerated catalyst CAT-1 from regenerator
It touches and reacts, the ratio of light gasoline fraction and C4 hydrocarbon is 1:1.The light gasoline fraction and C 4 fraction mixture and heavy are former
The mass ratio for expecting A is 0.1:1.Reaction condition and it the results are shown in Table 4.
Comparative example 5
According to the method for embodiment 1, unlike, the oil gas on fluidized bed upper layer does not pass through filter, but directly logical
It crosses feed-line and introduces cyclone separator.Reaction condition and it the results are shown in Table 3.
Higher propylene, fourth can be obtained using method provided by the invention it is found that compare with comparative example with table 4 by table 3
The productivity of low carbon olefin hydrocarbon such as alkene, while the gasoline rich in aromatic hydrocarbons can also be produced.
Table 1
| Project | Heavy charge A |
| Density (20 DEG C)/(kg/m3) | 938.2 |
| Viscosity (80 DEG C)/(mm2/s) | 20.17 |
| Viscosity (100 DEG C)/(mm2/s) | 10.56 |
| Carbon residue mass fraction/% | 0.15 |
| Element quality composition/% | |
| C | 86.82 |
| H | 12.16 |
| S | 0.386 |
| N | 0.18 |
| Quality race composition/% | |
| Saturated hydrocarbons | 71.2 |
| Aromatic hydrocarbons | 22.3 |
| Colloid | 6.4 |
| Asphalitine | 0.1 |
| Metal quality composition/(mg/kg) | |
| Fe | 1.3 |
| Ni | <0.1 |
| V | <0.1 |
| Na | 2.3 |
| Ca | 0.3 |
| Boiling range/DEG C | |
| Initial boiling point | 257 |
| 10% | 371 |
| 30% | 414 |
| 50% | 441 |
| 70% | 465 |
| 90 | 505 |
| The end point of distillation | 521 |
Table 2
| Project | CAT-1 |
| Element composition/% (w) | |
| Al2O3 | 73.3 |
| SiO2 | 27.6 |
| Micro-activity/% (W) | 65 |
| Specific surface area/(m2/g) | 136 |
| Pore volume/(ml/g) | 0.29 |
| Heap ratio/(g/ml) | 0.86 |
| Particle diameter distribution | |
| 0-20μm | 2.9 |
| 0-40μm | 11.3 |
| 0-80μm | 62.6 |
| 0-105μm | 79.3 |
| 105 μm of > | 20.7 |
Table 3
Table 4
The preferred embodiment of the present invention has been described above in detail, and still, the present invention is not limited thereto.In skill of the invention
In art conception range, can with various simple variants of the technical solution of the present invention are made, including each technical characteristic with it is any its
Its suitable method is combined, and it should also be regarded as the disclosure of the present invention for these simple variants and combination, is belonged to
Protection scope of the present invention.
Claims (14)
1. a kind of method of low-carbon olefines high-output, which is characterized in that this method comprises:
(1) in the first riser reactor, heavy charge and catalytic cracking catalyst haptoreaction, obtain carbon deposited catalyst and
Then first reaction product separates carbon deposited catalyst and the first reaction product；
(2) in the second riser reactor, lightweight material and catalytic cracking catalyst haptoreaction, the finish mixing after reaction
Object reacts in a fluidized bed reactor, obtains the second reaction product and carbon deposited catalyst, filters carbon deposit from the second reaction product
Fluidized-bed reactor is discharged from fluidized bed lower layer in catalyst, carbon deposited catalyst；
(3) carbon deposited catalyst is regenerated in a regenerator, obtains regenerated catalyst, regenerated catalyst be used as step (1) and/
Or the catalytic cracking catalyst of step (2).
2. according to the method described in claim 1, wherein, it includes that will be mingled with that carbon deposited catalyst is filtered from the second reaction product
Second reaction product of carbon deposited catalyst passes through the filter being arranged in above fluidized-bed reactor.
3. according to the method described in claim 2, wherein, this method further includes from the top of the filter to the filter
It is purged, it is preferable to use steam is purged.
4. method described in any one of -3 according to claim 1, wherein this method further includes to filtered second reaction
Product carries out cyclonic separation and stripping.
5. according to the method described in claim 1, wherein, the process packet that carbon deposited catalyst and the first reaction product are separated
Include cyclonic separation and stripping.
6. the method according to claim 1, wherein the heavy charge is selected from decompressed wax oil, reduced crude, decompression residuum, coke
Change wax oil, deasphalted oil, furfural treatment are raffinated oil, liquefied coal coil, tar sand oil, shale oil, the distillate synthesized by F-T
Or one of vegetable and animals oils or more than one mixture.
7. the method according to claim 1, wherein the lightweight material is light gasoline fraction and/or C4 hydrocarbon；Preferably, light vapour
Oil distillate is introduced from the middle part of second riser reactor, and C4 hydrocarbon is introduced in the bottom of the second riser reactor.
8. the method according to claim 1, wherein the catalytic cracking catalyst contains cracking activity constituent element, clay and bonding
Agent, it is preferable that the active component contains Y type molecular sieve, MFI structure molecular sieve and SAPO-34 molecular sieve.
9. method according to claim 8, wherein in the active component, with the total weight of the active component, Y molecule
The content of sieve is 20~90 weight %, preferably 50~80 weight %, and the content of MFI structure molecular sieve is 1~50 weight %, excellent
The content for being selected as 10~40 weight %, SAPO-34 molecular sieves is 1~50 weight %, preferably 10~40 weight %.
10. the method according to claim 1, wherein
The reaction temperature of first riser is 450~650 DEG C, preferably 500~600 DEG C；Oil ratio is 1~20, preferably
It is 5~15；Reaction time is 0.50~10 second, preferably 1~5 second；
The reaction temperature of second riser is 500~700 DEG C, preferably 550~650 DEG C；Oil ratio is 10~30, preferably
It is 15~25；Reaction time is 0.10~1.5 second, preferably 0.3~0.8 second；
The reaction temperature of the fluidized-bed reactor is 500~650 DEG C, preferably 520~580 DEG C；Weight (hourly) space velocity (WHSV) is 2~15 small
When-1, preferably 3~10 hours-1；Density of catalyst is 100~600kg/m3, preferably 200~400kg/m3；The linear velocity of oil gas
For 0.3~2m/s, preferably 0.3~1.5m/s.
11. a kind of device of low-carbon olefines high-output, which is characterized in that the device includes: the first riser reactor (1), second
Riser reactor (2), fluidized-bed reactor (3), settler (4), stripper (5) and regenerator (6)；First riser
Reactor (1) is connected to the settler (4)；Second riser reactor (2) is connected to the fluidized-bed reactor；Institute
It states and is provided with above fluidized-bed reactor (3) filter (34), the fluidized-bed reactor (3) and the settler (4) are even
Logical, the filter (34) is between the fluidized-bed reactor (3) and the settler (4)；The regenerator (6) is respectively
It is connected to first riser reactor (1) and second riser reactor (2).
12. device according to claim 11, wherein be equipped with gas purging ring (35), institute around the filter (34)
State gas purging ring (35) set-up mode make gas purging direction be perpendicular to filter surfaces to filter surfaces at
45° angle.
13. device according to claim 11, wherein the fluidized-bed reactor (3) is located at the outer of the settler (4)
Portion.
14. device described in any one of 1-13 according to claim 1, wherein first riser reactor (1) and
Two riser reactors (2) be respectively equal diameter riser, etc. linear speeds riser or variable diameters riser；
The fluidized-bed reactor (3) is selected from fixed fluidized-bed reactor, dispersion fluidized bed reactor, bubbling bed reactor, rapids
The combination of one or more of dynamic bed reactor, fast bed reactor, transport bed reactor and dense-phase fluidized bed reactor.
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| CN112680248B (en) * | 2019-10-18 | 2022-02-08 | 中国石油化工股份有限公司 | Catalytic conversion method and device for producing more light olefins |
| CN111748371A (en) * | 2020-07-15 | 2020-10-09 | 中国石油化工股份有限公司 | Catalytic cracking method and catalytic cracking device for double-reactor double-catalyst |
| CN111748371B (en) * | 2020-07-15 | 2022-03-22 | 中国石油化工股份有限公司 | Catalytic cracking method and catalytic cracking device for double-reactor double-catalyst |
| CN112322334A (en) * | 2020-10-21 | 2021-02-05 | 中国石油大学(北京) | Multi-zone coupling control multistage catalytic cracking method and device based on raw material properties |
| CN112322325A (en) * | 2020-10-21 | 2021-02-05 | 中国石油大学(北京) | Multi-bed-layer partition cooperative control multi-stage catalytic cracking method according to raw material types |
| CN112322324A (en) * | 2020-10-21 | 2021-02-05 | 中国石油大学(北京) | Multi-zone coupling control multistage catalytic cracking method and device based on raw material types |
| CN112322338A (en) * | 2020-10-21 | 2021-02-05 | 中国石油大学(北京) | Multi-zone coupling control multistage catalytic cracking method and device based on raw material types |
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