CN1333048C - Petroleum hydrocarbon catalytic conversion method - Google Patents
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- CN1333048C CN1333048C CNB200410086225XA CN200410086225A CN1333048C CN 1333048 C CN1333048 C CN 1333048C CN B200410086225X A CNB200410086225X A CN B200410086225XA CN 200410086225 A CN200410086225 A CN 200410086225A CN 1333048 C CN1333048 C CN 1333048C
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Abstract
The present invention relates to a petroleum hydrocarbon catalytic conversion method. A regeneration agent and a carbon agent from a secondary reaction region enter a mixing region to be mutually mixed and upwards flow to enter a first reaction region under the function of a pre-lifting medium in a reactor comprising a mixing region, the first reaction region and the secondary reaction region. Raw material oil and the mixing agent touch and react in the first reaction region, and the formed oil solvent mixture upwards flow to enter the secondary reaction region along the first reaction region and continues to touch and react in the secondary reaction region. Part of the reacting carbon agent is returned to the mixing region to be recycled in the secondary reaction region. Reaction oil gas and the rest reacting catalyst are separated, and the reaction oil gas is conveyed to a subsequent product separation system. The reacting catalyst is recycled after being stripped and regenerated. The petroleum hydrocarbon and the catalyst touch for a long time at low reaction temperature by the method, and accordingly, the present invention has dry gas yield reduction, hydrogen transfer reaction strengthening and olefin content reduction in a gasoline product.
Description
Technical field
The invention belongs to the catalysis conversion method of petroleum hydrocarbon under the situation that does not have hydrogen, more particularly, is a kind of petroleum hydrocarbon catalytic conversion method that improves finish contact effect.
Background technology
Fluid catalytic cracking is in contact with one another in fluidized-bed reactor by petroleum hydrocarbon and catalyzer and realizes.Carrying out along with reaction generates a large amount of sedimentation of coke and form reclaimable catalyst on catalyzer, and reclaimable catalyst is circulated to revivifier, at high temperature with the air catalytic combustion, burn the back and form regenerated catalyst, regenerated catalyst is Returning reactor again, continues to react with fresh feed oil again.The fluidized circulation of catalyzer can be realized by all gases medium.
Although fluid catalytic cracking process is comparatively ripe, people still endeavour to seek new technology with improve the quality of products, yield and selectivity.At present rather noticeable mainly is two aspects: the one, and the recovery of adsorption production on the reclaimable catalyst; The 2nd, the mixing of catalytically cracked stock and regenerated catalyst contacts.Reclaim the yield that product can directly improve product from reclaimable catalyst, the optimization mixing of catalytically cracked stock and catalyzer contacts the yield and the selectivity that then can improve product, and can improve the character of product.
The method that reclaims the adsorption production on the reclaimable catalyst is exactly the lighter hydrocarbons product on the stripping reclaimable catalyst more completely.Complete steam stripped ordinary method is exactly to improve the temperature of the reclaimable catalyst in the stripper.And the raising of the temperature of reclaimable catalyst can be adopted indirect heat exchange on the one hand, can in stripper reclaimable catalyst be mixed mutually with the pyritous regenerated catalyst on the one hand.U.S.Pat.3,821,103 and 2,451,619 have set forth back a kind of method.More complete stripping reclaimable catalyst both can improve the recovery of hydrocarbon product, can also improve the thermal equilibrium of fluidized catalytic cracker, thereby because the intact hydrocarbon of stripping does not burn in revivifier and can influence thermal equilibrium by a large amount of waste heat of generation.
Realize that by the equipment that changes existing apparatus stock oil is a lot of with the method that the catalyzer thorough mixing contacts.U.S.Pat.5,017,343 is exactly an exemplary device, and it mainly improves the mixing of stock oil and catalyzer by the dispersion that improves stock oil.U.S.Pat.4,960,503 by increasing the mixing that a plurality of nozzles improve stock oil and catalyzer in riser reactor.Although these methods have been improved the distribution of stock oil in regenerated catalyst, when a small amount of stock oil contacts with a large amount of catalyzer, will cause the skewness of moment, thereby cause non-selective cracking to increase the weight of, dry gas yied is too much.Local temperature distributing disproportionation when reducing stock oil and catalyst mix, U.S.Pat.4,960,503 have adopted the method with stock oil and thermocatalyst indirect heat exchange, but this method causes the interchanger green coke again easily.
There are many patents to realize the mixing of catalyzer by the direct Returning reactor of reclaimable catalyst is entered the mouth.U.S.Pat.3,679,576 have set forth a kind of like this method, before contacting with raw material, reclaimable catalyst and regenerated catalyst are fed the mixing that a minor diameter short tube is realized catalyzer simultaneously.U.S.Pat.3,888,762 change on this basis slightly, propose stock oil, reclaimable catalyst and regenerated catalyst are fed the mixing that catalyzer is improved in the riser tube bottom simultaneously.U.S.Pat.6616900 draws the oil gas at the middle part of riser tube and separates with catalyzer, band Pd/carbon catalyst wherein returns the riser tube bottom to be mixed with the rising agent oil ratio with regenerated catalyst.These methods have all greatly been improved catalyzer round-robin handiness between FCC apparatus, and shortcoming is still not solve the local excessive cracking problem of stock oil.U.S.Pat.5,346,613 have proposed the mixing that another kind of method solves catalyzer and stock oil with U.S.Pat.5455010 contacts, specifically, exactly reclaimable catalyst and regenerated catalyst are fed mixing section mixing, mixed catalyst is separated into two parts then, and a part is returned riser reactor, and another part then enters revivifier.Mixing section places between revivifier and the reactor.This method deficiency is that facility investment is excessive, the flow process complexity.U.S.Pat.5,451,313 and U.S.Pat.5597537 improve on this basis, mixing section is placed the bottom of riser reactor, regenerated catalyst and a part of reclaimable catalyst mix at mixing section.Mixing section at the riser tube bottom, U.S.Pat.5965012 and U.S.Pat.6183699 are on this basis, introduce the mixture contact reacts of lighter hydrocarbons and regenerated catalyst and spent agent at the end of regenerator sloped tube, thereby can realize the ultrashort contact reacts of light hydrocarbon feedstocks, after reacted oil, agent separation, spent agent is returned mixing section.U.S.Pat.6113776 and U.S.Pat.6616899 are provided with mixing section at the middle part of riser tube, the heat cracking reaction that the hypomere of riser tube carries out gasoline and high-temperature regenerated catalyst obtains low-carbon alkene, and the band charcoal agent of generation mixes at mixing section with the spent agent that stripping stage returns.But the blending means of all these catalyzer for solve raw material and catalyzer at a lower temperature the contact problems of long period be not very effective.
ZL99105903.4 provides a kind of novel reducing riser reactor, and CN1310223 adopts this reducing riser reactor, and the mixing at second reaction zone contacts with catalyzer by hydro carbons, has reduced content of olefin in gasoline.
Summary of the invention
The objective of the invention is to provide on the basis of existing technology a kind of petroleum hydrocarbon catalytic conversion method that improves finish contact effect, make petroleum hydrocarbon under lower temperature of reaction, carry out contacting of long period, thereby reduce olefin(e) centent in dry gas yied, reinforcement hydrogen transfer reactions, the reduction product gasoline with catalyzer.
Petroleum hydrocarbon catalytic conversion method provided by the present invention is as follows: in a reactor that comprises mixing zone, first reaction zone and second reaction zone, make regenerator and enter the mixing zone from the band charcoal agent of second reaction zone and mix under the effect that is incorporated in pre-lifting medium mutually and upwards flow into first reaction zone; Stock oil contacts, reacts with above-mentioned mixture in first reaction zone, and formed finish mixture is along being advanced into second reaction zone on first reaction zone, and touches, reacts in the second reaction zone relaying continued access; The reacted band charcoal of part agent in second reaction zone is returned the mixing zone and is recycled; Separating reaction oil gas and remaining reacted catalyzer, reaction oil gas is delivered to the subsequent product separation system, and reacted catalyzer recycles after stripping, regeneration.
Compared with prior art, beneficial effect of the present invention is mainly reflected in following aspect: by in the riser reactor bottom mixing zone being set, the band charcoal agent of a part of second reaction zone returned contact mixing with regenerated catalyst, realize an internal recycle of catalyzer, thereby realized that at first reaction zone suboptimization of hydro carbons and catalyzer contacts on the one hand, increase by the first reaction zone agent-oil ratio, and reduce the ratio that the first reaction zone thermally splitting takes place simultaneously.The more important thing is in addition, the also corresponding internal circulating load that increases the second reaction zone catalyzer, strengthened the second reaction zone gas-solid contact efficiency, thereby can make hydro carbons realize that at second reaction zone double optimization contacts with catalyzer, make hydro carbons and catalyzer contacting of longer reaction times at a lower temperature, so the environment that provides a very suitable hydrogen transfer reactions to take place at second reaction zone, thereby dry gas yied reduced, improve product property, reduced the olefin(e) centent of gasoline in the product.
Description of drawings
Fig. 1 is the schematic flow sheet of method provided by the present invention.
Embodiment
The reactor that comprises mixing zone, first reaction zone and second reaction zone of the present invention is the reactor pattern after improving on the conventional FCC riser reactor basis.As shown in Figure 1, can adopt the bottom to be provided with the reducing riser reactor of mixing zone, described reducing riser reactor is the reactor described in the ZL99105903.4; Described first reaction zone is also identical with the partitioned mode described in the ZL99105903.4 with second reaction zone.Reactor of the present invention can also be riser tube+fluidized-bed combined reactor that the bottom is provided with the mixing zone, and wherein, riser tube partly is first reaction zone of the present invention, and fluidized-bed partly is second reaction zone of the present invention.
In reactor of the present invention, the mixing zone is arranged at the bottom of reactor, and its lower end with first reaction zone is fixedly connected and be connected.The aspect ratio of mixing zone is 0.2-5: 1, and preferred 0.5-3: 1.The diameter ratio of the diameter of mixing zone and first reaction zone is 1.2-5: 1, and preferred 1.5-4: 1.
Conventional catalytically cracked material all can be used as stock oil of the present invention, for example, the mixture of one or more in straight-run gas oil, wax tailings, deasphalted oil, hydrofined oil, hydrocracking tail oil, vacuum residuum, the long residuum all can be used as stock oil of the present invention.
The catalyzer that the present invention is suitable for is the catalyzer that is generally used for the FCC process, its active ingredient be selected from Y or HY type zeolite, the ultrastable Y that contains or do not contain rare earth, the ZSM-5 series zeolite that contains or do not contain rare earth or supersiliceous zeolite, β zeolite, the ferrierite with five-membered ring structure a kind of, two or three, also can be the amorphous silicon aluminium catalyzer.
In the method for the invention, the main operational condition of first reaction zone is as follows: temperature of reaction is 450-650 ℃, is preferably 480-580 ℃; Reaction pressure is 130-450 kPa, is preferably 250-400 kPa; The weight ratio of catalyzer and stock oil is 2-15: 1, be preferably 3-10: 1; The weight ratio of water vapor and stock oil is 0-0.12: 1, be preferably 0.01-0.08: 1.The main operational condition of second reaction zone is as follows: temperature of reaction is 450-650 ℃, is preferably 480-580 ℃; Reaction pressure is 130-450 kPa, is preferably 250-400 kPa.
In the method for the invention,, can inject heat-eliminating medium at second reaction zone in order to control the temperature of reaction of second reaction zone better.Described heat-eliminating medium can be selected from: the mixture of the arbitrary proportion of one or more in liquefied gas, raw gasline, stable gasoline, diesel oil, heavy gas oil or the water, also can adopt one or more the mixture of arbitrary proportion in cooled regenerator, half regenerator, spent agent or fresh dose.
In the method for the invention, can make reacted spent agent part behind stripping, deliver to the revivifier coke burning regeneration, and the rest part spent agent can directly return second reaction zone behind stripping or without stripping, in order to regulate the operational condition of second reaction zone.
Enumerate two kinds of concrete embodiments below further specifying method provided by the present invention, but therefore the present invention is not subjected to any restriction.
Embodiment A: as shown in Figure 1, the reducing riser reactor for described in the ZL99105903.4 is provided with the mixing zone at this reactor bottom.Its constitutional features is: vertically be followed successively by co-axial each other mixing zone, pre lift zone, first reaction zone, enlarged-diameter from bottom to up second reaction zone, reduced outlet area.The stripper of the sizableness of mixing zone in catalytic cracking unit, coaxial with riser tube, place the bottom of riser tube.The high temperature regeneration agent that comes from revivifier and in the mixing zone, mix, mixture from the band charcoal agent that second reaction zone returns again with the stock oil contact reacts, can the rising agent oil ratio, and reduce dry gas yied; Up, the reaction of above-mentioned mixture and oil gas enters second reaction zone.The mixing zone is returned in the agent of part band charcoal in second reaction zone.Remaining catalyzer and oil gas enter settling vessel through outlet area and carry out gas solid separation, and spent agent at least a portion behind stripping is gone revivifier regeneration, recycles.
Embodiment B:, the mixing zone is set at this reactor bottom for riser tube+fluidized-bed combined reactor (fluidized-bed is positioned at the top of riser tube).Its constitutional features is: vertically be followed successively by co-axial each other mixing zone, riser tube (first reaction zone), fluidized-bed (second reaction zone) from bottom to up.The stripper of mixing zone sizableness in catalytic cracking unit, coaxial with riser tube, place the bottom of riser tube.The high temperature regeneration agent that comes from revivifier and in the mixing zone, mix, mixture from the band charcoal agent that second reaction zone returns again with the stock oil contact reacts, can the rising agent oil ratio, and reduce dry gas yied; Up, the reaction of above-mentioned mixture and reaction oil gas enters second reaction zone.The mixing zone is returned in the agent of part band charcoal in second reaction zone.Remaining catalyzer and oil gas enter settling vessel and carry out gas solid separation, and reclaimable catalyst at least a portion behind stripping is gone revivifier regeneration, recycles.
The concrete operations step of above-mentioned two kinds of embodiments is as follows: temperature is that 650-800 ℃ regenerator enters the mixing zone by regenerator sloped tube; The relatively low band charcoal agent of returning from second reaction zone of temperature, its carbon content is the heavy % of 0.05-0.50, and temperature is 450-620 ℃, also enters the mixing zone through transfer lime, mix with regenerator, the temperature of formed mixture depends on the band charcoal agent that enters the mixing zone and the ratio of regenerator.Generally, entering the band charcoal agent of mixing zone and the weight ratio of regenerator is 0.01-0.8, is preferably 0.01-0.5.The temperature of mixture is 5 00-720 ℃, is preferably 560-640 ℃.In order to make the lower band charcoal agent of regenerator and temperature contact heat transfer better, close operation is mutually preferably kept in the mixing zone, and its density of catalyst requires greater than 100kg/m
3, be preferably 160-400kg/m
3For guaranteeing the close operation mutually of mixing zone, operated by rotary motion fluidizing medium entrance and exit in the mixing zone becomes flexible by injecting fluidizing medium.The fluidizing medium that enters the mixing zone is generally inert material, for example, water vapour, dry gas, nitrogen etc., preferably water steam, its superficial gas velocity are 0.06-0.9m/s.By the fluidizing medium of common pre-lifting medium and mixing zone mixture is delivered to first reaction zone of reactor, makes mixture contact, react with stock oil, catalyzer and stock oil weight ratio are 4-25, are preferably 5-20.Reaction oil gas and mixture of catalysts enter second reaction zone of hole enlargement, draw the agent of part band charcoal to the mixing zone from the beds of second reaction zone.Oil gas and mixture of catalysts come out to carry out gas solid separation after outlet area enters settling vessel from second reaction zone, and the reclaimable catalyst after the separation enters stripping stage, wherein recycle after the regeneration of the reclaimable catalyst behind the part stripping.
Below in conjunction with accompanying drawing method provided by the present invention is given further instruction, but therefore the present invention is not subjected to any restriction.
As shown in Figure 1, this reactor comprises mixing zone 3, first reaction zone 6 and second reaction zone 8.Regenerator through regenerator sloped tube 4 with through catalyzer inclined tube 5, the mixing zone, mixed by the band charcoal agent of the relatively lower temp that guiding valve 18 control returns from second reaction zone to contact, the mixture that formation temperature is relatively low, the pre-medium that promotes enters the mixing zone through pipeline 1, under the effect of pre-lifting medium, make the catalyzer in the mixing zone enter first reaction zone 6 through pre lift zone 2.Heavy hydrocarbon feeds oil after the preheating enters first reaction zone through pipeline 7, contacts, reacts with mixture, and the finish mixture that is generated goes upward to second reaction zone 8.The band charcoal agent of returning from stripping stage 13 through catalyzer inclined tube 9, be subjected to guiding valve 19 controls also to enter second reaction zone, in second reaction zone, contact, react with mixture of catalysts with up oil gas.Reacted oil gas and catalyzer enter settling vessel 11 through outlet area 10, carry out gas solid separation by cyclonic separator 12 in settling vessel, and the oil gas after the separation removes the separation system (not shown).Be advanced into stripping stage 13 under the spent agent after reaction oil gas separates, wherein the agent of part band charcoal is returned through catalyzer inclined tube 9, remaining band charcoal agent through inclined tube 14 to be generated, be subjected to guiding valve 16 controls to enter revivifier 15 regeneration.Catalyzer after the regeneration through regenerator sloped tube 4, be subjected to guiding valve 17 control to return riser tube to recycle.
The following examples will be further specified the present invention, but not thereby limiting the invention.Employed catalyzer of embodiment and raw material oil properties are listed in table 1 and table 2 respectively.Catalyzer in the table 1 is produced by China PetroChemical Corporation's Shandong catalyst plant.
Embodiment
Present embodiment explanation: adopt method provided by the invention to carry out the resulting product of hydrocarbon ils catalytic conversion reaction and distribute and the product property situation.
The flow process of kitty cracker as shown in Figure 1, preheating material oil is through first reaction zone of pipeline 7 injecting reactors, contact, react with the mixture in this reaction zone, described mixture is to be mixed in the mixing zone by the charcoal agent of return from second reaction zone 495 ℃ bands and the 700 ℃ of regenerators ratio in 0.05: 1, and bed density is 300kg/m in the mixing zone
3The first reaction zone temperature of reaction is 545 ℃, and the reaction times is 1 second, agent-oil ratio 5.5: 1.Be advanced into second reaction zone on oil gas and the mixture of catalysts, return a part of reclaimable catalyst from stripping stage and enter second reaction zone, the ratio of the mass rate of spent agent is 0.1: 1 in the mass rate of the spent agent that returns and the stripping stage.Second reaction zone temperature is 495 ℃, and the reaction times is 3.8 seconds.Reactor head pressure is 0.2 MPa, reaction product, spent agent separate in settling vessel, reaction product isolated obtains gaseous product and product liquid, and spent agent enters stripping stage, a part of spent agent behind the stripping returns second reaction zone, the rest part spent agent goes revivifier regeneration, and the mixing zone of the catalyzer Returning reactor after the regeneration recycles.Test conditions, test-results are listed in table 3, and gasoline property is listed in table 4.
Comparative Examples
Adopt the reducing riser reactor described in the ZL99105903.4 to test, raw materials used oil and catalyzer are same as the previously described embodiments.But the reactor that is adopted in this Comparative Examples is not provided with the mixing zone, does not return the agent of band charcoal from second reaction zone yet and mixes with regenerator.Spent agent is not returned second reaction zone in addition from stripping stage yet.The reaction times of first reaction zone is 1 second, and agent-oil ratio is 4.5: 1.The second reaction zone reaction times was 3.5 seconds.The same embodiment of other condition.Test-results is listed in table 3, and gasoline property is listed in table 4.
Table 1
| Trade names | ZCM-7 |
| Zeolite type | USY |
| Chemical constitution, heavy % | |
| Aluminum oxide | 46.4 |
| Sodium oxide | 0.22 |
| Ferric oxide | 0.32 |
| Apparent density, kilogram/rice 3 | 690 |
| Pore volume, milliliter/gram | 0.38 |
| Specific surface area, rice 2/ gram | 164 |
| Abrasion index is when weighing % -1 | - |
| Size composition, heavy % | |
| 0～40 micron | 4.8 |
| 40～80 microns | 47.9 |
| ＞80 microns | 47.3 |
Table 2
| Density (20 ℃), kilogram/rice 3 | 890.5 |
| Kinematic viscosity (100 ℃), millimeter 2/ second | 5.08 |
| Carbon residue, heavy % | 0.7 |
| Condensation point, ℃ | 40 |
| Total nitrogen, heavy % | 0.16 |
| Sulphur, heavy % | 0.53 |
| Carbon, heavy % | 85.00 |
| Hydrogen, heavy % | 12.62 |
| Heavy metal content, PPM | |
| Nickel | 0.16 |
| Vanadium | 0.15 |
| Sodium | 0.45 |
| Boiling range, ℃ | |
| Initial boiling point | 278 |
| 10％ | 385 |
| 30％ | 442 |
| 50％ | 499 |
| 70％ | -- |
| 90％ | -- |
| Final boiling point | -- |
Table 3
| Embodiment | Comparative Examples | |
| Temperature of reaction, ℃ | ||
| First reaction zone | 545 | 545 |
| Second reaction zone | 495 | 495 |
| Reaction times, second | 5.3 | 5.0 |
| First reaction zone | 1.0 | 1.0 |
| Second reaction zone | 3.8 | 3.5 |
| Outlet area | 0.5 | 0.5 |
| Agent-oil ratio | 5.5 | 4.5 |
| Water-oil ratio | 0.05 | 0.05 |
| Products distribution, heavy % | ||
| Dry gas | 1.54 | 1.83 |
| Liquefied gas | 16.65 | 16.11 |
| Gasoline | 47.28 | 46.86 |
| Solar oil | 23.04 | 23.44 |
| Heavy gas oil | 7.42 | 7.77 |
| Coke | 3.95 | 3.88 |
| Loss | 0.12 | 0.11 |
Table 4
| Embodiment | Comparative Examples | |
| Gasoline property | ||
| RON | 88.6 | 90.0 |
| MON | 80.0 | 79.0 |
| Sulphur, ppm | 45 | 93 |
| Nitrogen, ppm | 0.4 | 29 |
| Aromatic hydrocarbons, heavy % | 26.0 | 24.01 |
| Alkene, heavy % | 12.9 | 26.24 |
| Alkane, heavy % | 53.9 | 42.45 |
| Normal paraffin | 5.2 | 5.15 |
| Isoparaffin | 49.7 | 37.3 |
| Naphthenic hydrocarbon, heavy % | 7.2 | 7.3 |
Claims (10)
1, a kind of petroleum hydrocarbon catalytic conversion method, it is characterized in that: comprise the mixing zone at one, in the reactor of first reaction zone and second reaction zone, make regenerator and enter the mixing zone and mix under the effect that is incorporated in pre-lifting medium mutually and upwards flow into first reaction zone from the band charcoal agent of second reaction zone, stock oil contacts with above-mentioned mixture in first reaction zone, reaction, the temperature of reaction of first reaction zone is 450-650 ℃, reaction pressure is 130-450 kPa, the weight ratio of catalyzer and stock oil is 2-15: 1, the weight ratio of water vapor and stock oil is 0-0.12: 1, formed finish mixture is along being advanced into second reaction zone on first reaction zone, and touch in the second reaction zone relaying continued access, reaction, the temperature of reaction of second reaction zone is 450-650 ℃, and reaction pressure is 130-450 kPa; The reacted band charcoal of part agent in second reaction zone is returned the mixing zone and is recycled; Separating reaction oil gas and remaining reacted catalyzer, reaction oil gas is delivered to the subsequent product separation system, and reacted catalyzer recycles after stripping, regeneration.
2,, it is characterized in that described reactor is reducing riser reactor or riser tube+fluidized-bed combined reactor according to the method for claim 1.
3, according to the method for claim 1, it is characterized in that described mixing zone is arranged at the bottom of reactor, and fixedly connected with the lower end of first reaction zone, the aspect ratio of mixing zone is 0.2-5: 1, and the diameter ratio of the diameter of mixing zone and first reaction zone is 1.2-5: 1.
4, according to the method for claim 1, it is characterized in that described second reaction zone injects heat-eliminating medium, and heat-eliminating medium is selected from: the mixture of the arbitrary proportion of one or more in liquefied gas, raw gasline, stable gasoline, diesel oil, heavy gas oil or the water, or one or more the mixture of arbitrary proportion in cooled regenerator, half regenerator, spent agent or fresh dose.
5,, it is characterized in that described reacted spent agent part delivers to the revivifier coke burning regeneration behind stripping, and directly return second reaction zone behind remaining spent agent stripping or without stripping according to the method for claim 1.
6, according to the method for claim 1, it is characterized in that described mixing zone keep close mutually the operation, its density of catalyst is greater than 100kg/m
3
7,, it is characterized in that the density of catalyst in the described mixing zone is 160-400kg/m according to the method for claim 6
3
8, according to the method for claim 1, it is characterized in that describedly entering the band charcoal agent of mixing zone and the weight ratio of regenerator is 0.01-0.8, the temperature of mixture is 500-720 ℃ in the mixing zone.
9, according to the method for claim 8, it is characterized in that describedly entering the band charcoal agent of mixing zone and the weight ratio of regenerator is 0.01-0.5, the temperature of mixture is 560-640 ℃.
10, according to the method for claim 1, the carbon content that it is characterized in that the described band charcoal agent of being returned by second reaction zone is the heavy % of 0.05-0.50, and its temperature is 450-620 ℃.
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| CN101205475B (en) * | 2006-12-22 | 2012-01-25 | 中国石油化工股份有限公司 | Hydrocarbons catalytic conversion method for preparing low olefin-content gasoline |
| CN102453500A (en) * | 2010-10-21 | 2012-05-16 | 中国石油化工股份有限公司 | Catalytic cracking method and equipment for hydrocarbon oil |
| CN110724550B (en) * | 2018-07-16 | 2021-04-06 | 中国石油化工股份有限公司 | Method and system for catalytic cracking by adopting fast fluidized bed |
| CN110724553B (en) * | 2018-07-16 | 2021-04-06 | 中国石油化工股份有限公司 | Method and system for catalytic cracking by adopting dilute phase conveying bed and rapid fluidized bed |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6113776A (en) * | 1998-06-08 | 2000-09-05 | Uop Llc | FCC process with high temperature cracking zone |
| CN1310223A (en) * | 2001-01-18 | 2001-08-29 | 中国石油化工股份有限公司 | Catalytic converting process for producing low-alkene gasoline and high-yield diesel oil |
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6113776A (en) * | 1998-06-08 | 2000-09-05 | Uop Llc | FCC process with high temperature cracking zone |
| CN1310223A (en) * | 2001-01-18 | 2001-08-29 | 中国石油化工股份有限公司 | Catalytic converting process for producing low-alkene gasoline and high-yield diesel oil |
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