CN102746892A - Catalytic cracking method and device - Google Patents
Catalytic cracking method and device Download PDFInfo
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- CN102746892A CN102746892A CN2011100968292A CN201110096829A CN102746892A CN 102746892 A CN102746892 A CN 102746892A CN 2011100968292 A CN2011100968292 A CN 2011100968292A CN 201110096829 A CN201110096829 A CN 201110096829A CN 102746892 A CN102746892 A CN 102746892A
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Abstract
The invention discloses a catalytic cracking method and device. The method comprises the following steps: introducing raw oil into a lower part of a riser reactor to contact and react with a catalyst from a catalyst heat exchanger; separating oil gas after the reaction from a coked catalyst; introducing separated reaction oil gas into a fractionating tower; carrying out steam stripping on the separated coked catalyst and sending the coked catalyst into a regenerator for regeneration; carrying out heat transfer and cooling on the regenerated catalyst and part of system prevailing wind within the catalyst heat exchanger; sending part of the regenerated catalyst into the riser reactor from different heights of the riser; and sending the other part of the regenerated catalyst into the lower part of the riser reactor. The method can reduce total yield of dry gas and coke by 0.8-2 percentage, increase total liquid yield of liquefied gas, gasoline and diesel by 1.2 percentage, and reduce volume content of gasoline olefin by 5-15 percentage.
Description
Technical field
The invention belongs under the situation that does not have hydrogen the catalytic cracking field of hydrocarbon ils, particularly a kind of catalyst cracking method and device that improves total liquid receipts.
Background technology
When paying attention to environment protection, the maximization of economic benefit is the target that enterprise is pursued forever.And low dry gas and coke yield, high liquid receipts then are the fundamental means that catalytic cracking technology is increased economic efficiency always.In recent years, domestic each research institution has carried out fruitful research aspect the distribution of catalytic cracking product being devoted to improve, and the technology of exploitation mainly contains following several:
US5451313 disclosed " X design ", this new design has been invented in nineteen ninety-five by Uop Inc., its objective is the rising agent oil ratio, improves product and distributes.Be characterized in being provided with a catalyst mix device between reactor drum and the revivifier, spent agent mixes in mixing tank with regenerator, and the partial confounding mixture flows into riser tube and raw material contact reacts, and remaining mixture flows into revivifier and regenerates.The benefit of this structure is the mixture temperature that gets into riser tube than next low of revivifier, and the catalyst recirculation amount is increased, and agent-oil ratio improves, so thermal response minimizings, catalyzed reaction increase, coke and dry gas yied reduction, gasoline yield increase.But it is very low that this design shortcoming is exactly a spent agent activity in the mixed catalyst, makes the active on the low side of mixture, is unfavorable for the cracking of raw oil.
US 6059958, are the IsoCat technology of Petrobras company, are characterized in that one returns regenerator bed with being divided into two strands through external warmer refrigerative catalyzer, and another strand mixes the back and get into riser tube and raw oil reaction with the regenerated catalyst of heat.Obviously, the temperature of mixed regeneration catalyzer is lower than the temperature of conventional regenerated catalyst.Similar with " X design " reason of Uop Inc., IsoCat technology can reduce coke and dry gas yied, and two strands of catalyzer of IsoCat technology are regenerated catalyst, and the activity of mixture is higher, more helps catalyzed reaction.But this technology implements comparatively complicated, and the mixed catalyst difficult control of temperature.
CN 1288933 disclosed regenerator sloped tube catalyzer cooling technologies, this method is exactly that a cooling water jecket directly is set outside regenerator sloped tube, lowers the regenerated catalyst temperature of entering riser reactor through water coolant.Though this method has obtained good effect on pilot plant, dry gas and coke yield are significantly descended, bring very big difficulty in industrial practice, for the control of temperature of reaction, that is to say that this method seems simply, it is bigger to put into practice difficulty.
The FDFCC-III Technology that CN 1710029 is disclosed; This technology is developed by Luoyang Petrochemical engineering corporation; FDFCC-III process using double lifting leg is also set up petrol sediment bulb and secondary separation column; Simultaneously that the part relative temperature is lower gasoline rising pipe reclaimable catalyst is introduced raw oil riser tube catalyzer and is promoted mixing tank in advance, mixes the back with the high temperature regeneration agent and gets into the raw oil riser tube, has so both reduced the finish contact temperature of raw oil riser tube; Made full use of the remaining activity of gasoline rising pipe reclaimable catalyst again; Improve the agent-oil ratio and the product selectivity of raw oil riser catalytic cracking, reduce dry gas and coke yield, improve propene yield and propylene selectivity.Though this technology weak point is that gasoline spent agent remaining activity is higher, compares with regenerated catalyst or a certain distance is arranged.
" oil Refining Technologies and engineering " the 12nd phase in 2008 discloses the novel multi-region control heavy oil MZCC of the association catalytic cracking technology that China University Of Petroleum Beijing proposes; The MZCC technology promotes that with the heat that mixes of regenerator the cracking of hydro carbons macromole, minimizing dry gas and coke are the technology basis to optimize heavy oil, has proposed the strong back-mixing of charging, the propelling of reaction advection, the ultrafast separation of product and chemical steam stripped subregion Collaborative Control new concept.This technology is intended a newly-increased root regeneration inclined tube and air-lift unit pipe, and on this newly-increased regenerator sloped tube, catalyst cooler is set, and cooled catalyzer mixes with the thermocatalyst that former regenerator sloped tube comes; The regenerator and the raw material that mix the back lesser temps carry out contact reacts; This technology can reduce the finish mixing temperature, and the rising agent oil ratio is improved product and distributed; But should show complicated slightly by technology regenerator cooling measure, it is more to set up equipment.
Summary of the invention
The present invention is in order to reduce CCU dry gas and coke yield, to improve total liquid and receive, reducing the SO in content of olefin in gasoline and the catalysis flue gas simultaneously
XA kind of new catalyst cracking method that discharges and provide.
A kind of catalyst cracking method of the present invention is characterized in that comprising the steps:
1) raw oil gets into the riser reactor bottom, contacts with catalyzer from the catalyst heat exchange device, reacts;
2) reacted oil gas separates with reclaimable catalyst; Isolated reaction oil gas gets into separation column; Isolated reclaimable catalyst gets into revivifier regeneration behind stripping, regenerator part after the cooling of catalyst heat exchange device gets into riser reactor from the riser tube different heights; Another part returns step 1).
Described a kind of catalyst cracking method, the high temperature regeneration agent after the regeneration directly get into the catalyst heat exchange device and carry out heat exchange.
Described a kind of catalyst cracking method, the cooling regenerator that gets into riser reactor from the riser tube different heights is to get into riser reactor through the catalyst transport arm;
Described a kind of catalyst cracking method, reclaimable catalyst and part system main air and contact from the main air of catalyst heat exchange device and to carry out coke burning regeneration.
Said a kind of catalyst cracking method, high temperature regeneration agent and the main air counter current contact heat exchange of FCC system that the regeneration back gets into the catalyst heat exchange device, the main air after the heat exchange gets into revivifier and burns.The main air amount that gets into interchanger generally accounts for 20%～100% of the whole main air amounts of FCC, is preferably 30%～90%, is preferably 40%～85%; The regenerator temperature is generally 580～670 ℃ after the heat exchange of catalyst heat exchange device, is preferably 600～660 ℃, is preferably 610～660 ℃.
Said riser reactor axial temperature is approximately equalised, and temperature out is generally 450～560 ℃, is preferably 460～540 ℃, is preferably 470～530 ℃; Reaction times was generally 0.5～5 second, was preferably 1.0～4.5 seconds, best 1.5～4.0 seconds; The agent weight of oil is generally 3～20 than (catalyst recirculation amount and inlet amount weight ratio, the catalyst recirculation amount is by riser tube outlet internal circulating load), is preferably 5～18, best 8～15; The reaction absolute pressure is generally 0.15～0.40MPa, is preferably 0.20～0.36MPa, is preferably 0.22～0.33MPa; The catalytic amount that is delivered to riser reactor by the catalyst transport arm is 5～30% of a riser reactor global cycle amount; The regeneration temperature of revivifier is 650～750 ℃, and the carbon content of regenerated catalyst is 0.02～0.2 weight %, and the regenerated catalyst micro-activity is generally 55～70.
Described riser reactor charging contains a kind of in long residuum, vacuum residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle stock, slurry oil, crude oil, shale oil, synthetic oil, the coal tar at least.
A kind of CCU of the present invention; Contain riser reactor, settling vessel, regeneration standpipe, revivifier, external warmer, regeneration standpipe, main air outlet pipe, catalyst heat exchange device, regenerator sloped tube, the catalyst transport person in charge, catalyst transport arm; The riser reactor top exit is connected with the settling vessel inlet; The riser reactor bottom is connected with catalyst heat exchange device bottom, and settling vessel is connected with revivifier, and revivifier is connected with external warmer; Revivifier is connected with catalyst heat exchange device top, and the catalyst heat exchange device is connected with riser reactor.
Described a kind of CCU; The catalyst heat exchange device is responsible for through regenerator sloped tube, catalyst transport and the catalyst transport arm is connected with riser reactor; Catalyst transport is responsible for and is connected with riser reactor through the catalyst transport arm; The catalyst transport arm is 1～5; Below catalyst transport arm 0.5～10 meter above the raw oil feed entrance point, position that links to each other with riser reactor wherein, other catalyst transport arm link to each other with riser reactor the position far from the below 4～10 meters of conveying arm positions.
Described a kind of CCU; The riser reactor bottom links to each other with the catalyst heat exchange device through regenerator sloped tube; The settling vessel stripping stage links to each other with revivifier through regeneration standpipe, and revivifier links to each other with catalyst heat exchange device top through regeneration standpipe, main air outlet pipe.
The present invention improves existing riser fluid catalytic cracking, at first through the catalyst heat exchange device is set, makes part or all of main air in the catalyst heat exchange device, carry out heat exchange with the high temperature regeneration agent that revivifier comes; The main air temperature that gets into revivifier is raise; Reduced the regenerator temperature that gets into the riser reactor bottom on the other hand, finish contact temperature is reduced, raw oil heat cracking reaction degree weakens; Dry gas and coke yield decline to a great extent, and total liquid is received obviously and improved; The agent-oil ratio of riser reactor also significantly improves simultaneously, and the raising of agent-oil ratio more helps the carrying out of catalyzed reaction, helps the improvement that product distributes, and can reduce the olefin(e) centent of gasoline simultaneously.Agent-oil ratio increases, and the catalyst recirculation amount significantly improves, and because of containing certain MOX in the catalyzer, the catalyst recirculation amount of raising is equivalent to play the effect of more sulfur transfer additives, therefore can obviously reduce SOx content in the catalysis flue gas.
Secondly, the present invention proposes isothermal riser tube notion, through the catalyst transport person in charge, arm segmentation injecting lift pipe different heights zone, for the reaction additional heat, riser tube is axially distributed through the regenerator after will lowering the temperature on a small quantity near isothermal.Generally, the catalytic cracking reaction aggregate performance is thermo-negative reaction, and along with the increase of riser tube height, reaction is constantly carried out, and the temperature of catalyzer can continue to descend.Charging mixing section above nozzle; Jet phase (representative mist of oil) and the particle distributional pattern of (representative catalyzer) mutually are unfavorable for that very two alternate contacts are even; The position that the jet phase concentration is big, the concentration of particle phase is little, is not complementary; Particle is bad with jet concentration distribution coupling mutually, and being influences the well major cause of uniform contact of finish two phases.And the present invention can solve the well problem of uniform contact of charging mixing section finish two phases preferably.To lower the temperature on a small quantity regenerator segmentation injecting lift pipe different heights zone of the present invention axially distributes riser tube near isothermal.Charging mixing section above the raw oil feed entrance point; Mend the catalyzer of going into and suitably to improve the less zone of particle phase concentration; Jet and particle phase concentration are complementary; Realize finish two phase uniform contact, suppress the heat cracking reaction that the particle phase concentration takes place than the zonule, promote the carrying out of catalyzed reaction; Mend the regenerator of going in other zone of riser tube and can be the reaction additional heat, improve riser tube inner catalyst average activity simultaneously, guarantee that catalyzed reaction continues to carry out, product is distributed be able to optimize.
For same raw material, and use with a kind of catalyzer, compare with conventional CCU, beneficial effect of the present invention is:
(1) device dry gas and coke overall yield descend 0.8～2.0 percentage point, and the total liquid of liquefied gas, gasoline and diesel oil is received and improved more than 1.2 percentage points.
(2) the riser reactor agent-oil ratio can be increased to more than 10.
(3) the gasoline olefin volume content can reduce by 5～15 percentage points.
(4) SOx content reduces more than 30% in the catalysis flue gas.
Utilize accompanying drawing and embodiment that the present invention is further explained below, but do not limit the scope of the invention.
Description of drawings
Fig. 1 is the synoptic diagram of a kind of CCU of the present invention.
Wherein: 1. reaction oil gas, 2. settling vessel, 3. riser reactor, 4. revivifier, 5. catalyst transport arm, 6. catalyst transport is responsible for, 7. raw oil, 8. regenerator sloped tube; 9. get into system's main air of catalyst heat exchange device; 10. catalyst heat exchange device, 11. regeneration standpipes, 12 system's main airs, 13. main air outlet pipes, 14. external warmers, 15. regeneration standpipes.
Embodiment
As shown in Figure 1, CCU of the present invention comprises: riser reactor 3, settling vessel 2, revivifier 4, external warmer 14, catalyst heat exchange device 10, regeneration standpipe 15, main air outlet pipe 13, regeneration standpipe 11, regenerator sloped tube 8, catalyst transport are responsible for 6,3 catalyst transport arms 5.The top exit of riser reactor 3 is connected with settling vessel 2; The bottom is connected with catalyst heat exchange device 10 through regenerator sloped tube 8; Settling vessel 2 stripping stages are connected with revivifier 4 through regeneration standpipe 15; Revivifier 4 inside are connected with catalyst heat exchange device 10 inside through regeneration standpipe 11, main air outlet pipe 13, and revivifier 4 is connected with external warmer 14 through inclined tube, and catalyst heat exchange device 10 bottoms are connected with riser reactor 3 bottoms through regenerator sloped tube 8; Catalyst heat exchange device 10 is responsible for 6 through catalyst transport and is connected with 3 catalyst transport arms 5, and the catalyst transport person in charge 6 is connected with riser reactor 3 through 3 catalyst transport arms 5.The present invention is below catalyst transport arm 5 0.5～10 meter above raw oil 7 feed entrance points, position that links to each other with riser reactor 3, other catalyst transport arm 5 link to each other with riser reactor 3 position far from the below 4～10 meters of conveying arm 5 positions.
The axial temperature of riser reactor according to the invention is approximately equalised, and temperature out is generally 450～560 ℃, is preferably 460～550 ℃, is preferably 470～540 ℃; Reaction times was generally 0.5～5 second, was preferably 1.0～4.5 seconds, best 1.5～4.0 seconds; Agent-oil ratio is generally 3～20, is preferably 5～18, is preferably 7～15; The reaction absolute pressure is generally 0.15～0.40MPa, is preferably 0.20～0.36MPa, is preferably 0.22～0.33MPa; Advance catalyst heat exchange device heat exchange main air amount and generally account for 20%～100% of whole main air amounts, be preferably 30%～90%, be preferably 40%～85%; The regenerator temperature is generally 580～670 ℃ after the heat exchange of catalyst heat exchange device, is preferably 600～660 ℃, is preferably 610～660 ℃.Total catalyst internal circulating load by catalyst transport is responsible for, arm is delivered to riser reactor is 5～30% of a riser reactor global cycle amount; The regeneration temperature of revivifier is 650～750 ℃, and the carbon content of regenerated catalyst is 0.02～0.2 weight %, and micro-activity is generally 55～70.The riser reactor charging is at least a in long residuum, vacuum residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle stock, slurry oil, crude oil, shale oil, synthetic oil, the coal tar.
Embodiment
On common riser catalytic cracking testing apparatus, make an experiment, raw oil mixes heavy oil for pipe is defeated, and main character is listed in table 1; Treatment capacity is 30 kg/day; The test catalyst system therefor is a CDC industry poiser, and the equilibrium catalyst micro-activity is 62, and carbon content is 0.05w%.The main operational condition of riser reactor, product distribute and the main character of product is listed in table 2,3.
On FCC tests device of the present invention as shown in Figure 1, make an experiment, treatment capacity is 30 kg/day, and raw oil, catalyzer are identical with embodiment 1, and the main operational condition of riser reactor, product distribute and the main character of product is listed in table 4 and table 5.
On FCC tests device of the present invention as shown in Figure 1, make an experiment, treatment capacity is 30 kg/day, and raw oil, catalyzer are identical with embodiment 2, and the main operational condition of riser reactor, product distribute and the main character of product is listed in table 4 and table 5.
On FCC tests device of the present invention as shown in Figure 1, make an experiment, treatment capacity is 30 kg/day, and raw oil, catalyzer are identical with embodiment 3, and the main operational condition of riser reactor, product distribute and the main character of product is listed in table 4 and table 5.
The main character of table 1 raw oil
| | Embodiment | 1,4 | |
|
|
| The raw oil title | The defeated heavy oil that mixes of pipe | The hydrogenation wax oil | Hydrogenation heavy oil | ||
| Density (20 ℃)/kg.m -3 | 923.6 | 896.8 | 918.2 | ||
| Carbon residue/% | 3.50 | 0.46 | 3.92 | ||
| Molecular weight | 450 | 451 | 500 | ||
| Boiling range/℃ | |||||
| IBP | 320 | 369 | 167 | ||
| 10％ | 375 | 413 | 265 | ||
| 30％ | / | 468 | 451 | ||
| 50％ | 450 | 519 | / | ||
| 70％ | / | 566 | / | ||
| 90％ | 589 | / | / | ||
| C/ weight % | 86.65 | 86.81 | 86.84 | ||
| H/ weight % | 12.25 | 13.08 | 12.53 | ||
| S/ weight % | 0.65 | 0.0863 | 0.291 | ||
| N/ weight % | 0.14 | 0.0147 | 0.145 | ||
| Group composition/weight % | |||||
| Stable hydrocarbon | 54.26 | 53.69 | 70.40 | ||
| Aromatic hydrocarbons | 32.10 | 45.70 | 17.80 | ||
| Colloid+bituminous matter | 13.64 | 0.60 | 12.80 | ||
| Metal content/μ g.g -1 | |||||
| Ni | 4.4 | 0.1 | 4.4 | ||
| V | 9.0 | 0.1 | 4.0 | ||
| Fe | 1.7 | 1.1 | 2.6 | ||
| Na | 1.5 | ＜0.05 | ＜0.05 |
Main operational condition of table 2 and product distribute
Table 3 product main character
| | Embodiment | 1 | |
|
| The gasoline main character | ||||
| Density (20 ℃)/kg.m -3 | 718.0 | 725.0 | 722.1 | |
| Sulphur content/μ g.g -1 | 830 | 98 | 159 | |
| Octane value (RON) | 92.6 | 91.3 | 92.3 | |
| Olefin(e) centent/volume % | 43.6 | 24.5 | 30.4 | |
| Benzene content/volume % | 0.60 | 0.68 | 0.51 | |
| Do/℃ | 191 | 200 | 191 | |
| The diesel oil main character | ||||
| Density (20 ℃)/kg.m -3 | 921.3 | 902.5 | 913.6 | |
| Sulphur content/μ g.g -1 | 6700 | 1090 | 2550 | |
| Cetane value | 29.0 | 30.5 | 31.1 | |
| SO in the flue gas XContent/mg.m -3 | 1035 | 656 | 2120 |
Main operational condition of table 4 and product distribute
Table 5 product main character
| | Embodiment | 4 | |
|
| The gasoline main character | ||||
| Density (20 ℃)/kg.m -3 | 720.0 | 727.3 | 724.2 | |
| Sulphur content/μ g.g -1 | 668 | 75 | 130 | |
| Octane value (RON) | 93.3 | 92.4 | 93.5 | |
| Olefin(e) centent/volume % | 29.5 | 18.0 | 20.2 | |
| Benzene content/volume % | 0.70 | 0.65 | 0.58 | |
| Do/℃ | 195 | 200 | 191 | |
| The diesel oil main character | ||||
| Density (20 ℃)/kg.m -3 | 926.0 | 913.1 | 921.0 | |
| Sulphur content/μ g.g -1 | 6865 | 1300 | 2720 | |
| Cetane value | 27.3 | 27.1 | 28.9 | |
| SO in the flue gas XContent/mg.m -3 | 550 | 398 | 1200 |
Claims (11)
1. a catalyst cracking method is characterized in that comprising the steps:
1) raw oil gets into the riser reactor bottom, contacts with catalyzer from the catalyst heat exchange device, reacts;
2) reacted oil gas separates with reclaimable catalyst; Isolated reaction oil gas gets into separation column; Isolated reclaimable catalyst gets into revivifier regeneration behind stripping, regenerator part after the cooling of catalyst heat exchange device gets into riser reactor from the riser tube different heights; Another part returns step 1).
2. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: described regenerator is after catalyst heat exchange device heat exchange cooling; A part gets into riser reactor through the catalyst transport arm from the riser tube different heights, and another part gets into the riser reactor bottom through regenerator sloped tube.
3. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: part system main air gets into revivifier after catalyst heat exchange device and regenerated catalyst heat exchange.
4. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: the catalytic amount of being sent into riser reactor by the catalyst transport arm is 5～30 weight % of riser reactor global cycle amount, in riser reactor catalyzer global cycle amount.
5. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: the system's main air amount that gets into the catalyst heat exchange device accounts for 20%～100% of the whole main air amounts of FCC; In system's main air TV, the regenerator temperature is 580～670 ℃ after the heat exchange of catalyst heat exchange device.
6. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: system's main air amount of said entering catalyst heat exchange device accounts for 30%～90% of the whole main air amounts of FCC; In system's main air TV, the regenerator temperature is 600～660 ℃ after the heat exchange of catalyst heat exchange device.
7. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: said riser reactor temperature out is 450～560 ℃, and the reaction times was generally 0.5～5 second, and agent weight of oil ratio is 3～20, and the reaction absolute pressure is 0.15～0.40MPa.
8. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: said riser reactor temperature out is 460～540 ℃; It is 1.0～4.5 seconds that reaction times is generally, and agent weight of oil ratio is 5～18, and the reaction absolute pressure is generally 0.20～0.36MPa.
9. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: said raw oil is at least a in long residuum, vacuum residuum, straight-run gas oil, wax tailings, deasphalted oil, hydrogenation tail oil, recycle stock, slurry oil, crude oil, shale oil, synthetic oil, the coal tar.
10. CCU; Comprise riser reactor, settling vessel, regeneration standpipe, revivifier, external warmer, regeneration standpipe, main air outlet pipe, regenerator sloped tube, the catalyst transport person in charge; The riser reactor top exit is connected with the settling vessel inlet; The riser reactor bottom is connected with catalyst heat exchange device bottom, and settling vessel is connected with revivifier, and revivifier is connected with external warmer.It is characterized in that: also comprise catalyst heat exchange device and catalyst transport arm; Catalyst heat exchange device one end is communicated with revivifier; The other end is communicated with riser reactor, and catalyst transport arm one end is communicated with the catalyst heat exchange device, and the other end is communicated with riser reactor.
11. according to the described a kind of CCU of claim 10; It is characterized in that: the catalyst transport arm is 1～5; Below catalyst transport arm 0.5～10 meter above the raw oil feed entrance point, position that links to each other with riser reactor wherein, other catalyst transport arm link to each other with riser reactor the position far from the below 4～10 meters of conveying arm positions.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4960503A (en) * | 1988-11-21 | 1990-10-02 | Uop | Heating FCC feed in a backmix cooler |
| CN1928023A (en) * | 2006-09-06 | 2007-03-14 | 中国石油化工集团公司 | Lift leg catalytic cracking method and apparatus |
| CN101575534A (en) * | 2009-06-16 | 2009-11-11 | 中国石油化工集团公司 | Device and method for reducing the temperature of catalytic cracking regenerated catalyst |
-
2011
- 2011-04-19 CN CN2011100968292A patent/CN102746892A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4960503A (en) * | 1988-11-21 | 1990-10-02 | Uop | Heating FCC feed in a backmix cooler |
| CN1928023A (en) * | 2006-09-06 | 2007-03-14 | 中国石油化工集团公司 | Lift leg catalytic cracking method and apparatus |
| CN101575534A (en) * | 2009-06-16 | 2009-11-11 | 中国石油化工集团公司 | Device and method for reducing the temperature of catalytic cracking regenerated catalyst |
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Application publication date: 20121024 |