CN102746891A - Catalytic cracking method and device - Google Patents

Catalytic cracking method and device Download PDF

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Publication number
CN102746891A
CN102746891A CN2011100968273A CN201110096827A CN102746891A CN 102746891 A CN102746891 A CN 102746891A CN 2011100968273 A CN2011100968273 A CN 2011100968273A CN 201110096827 A CN201110096827 A CN 201110096827A CN 102746891 A CN102746891 A CN 102746891A
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China
Prior art keywords
catalyst
oil
heat exchange
main air
regenerator
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CN2011100968273A
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Chinese (zh)
Inventor
闫鸿飞
王龙延
刘昱
孟凡东
樊麦跃
陈曼桥
乔立功
汤海涛
吴辰捷
李秋芝
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China Petroleum and Chemical Corp
Sinopec Luoyang Guangzhou Engineering Co Ltd
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China Petroleum and Chemical Corp
Sinopec Luoyang Petrochemical Engineering Corp
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Priority to CN2011100968273A priority Critical patent/CN102746891A/en
Publication of CN102746891A publication Critical patent/CN102746891A/en
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Abstract

The invention discloses a catalytic cracking method and device. The method is characterized by including 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 on the regenerated catalyst and part of system prevailing wind within the catalyst heat exchanger; and sending the regenerated catalyst to a lower part of the riser reactor to contact and react with raw oil. The method of the invention can increase catalyst-oil ratio of the riser reactor to above 10, reduce total yield of dry gas and coke by 0.8-1.8 percentage, increase total liquid yield of liquefied gas, gasoline and diesel by 1 percentage, and reduce volume content of gasoline olefin by 5-15 percentage.

Description

A kind of catalyst cracking method and device
Technical field
The invention belongs under the situation that does not have hydrogen the catalytic cracking field of hydrocarbon ils, the particularly catalyst cracking method of high solvent-oil ratio and device.
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:
US 5451313 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 improve the CCU agent-oil ratio, to reduce CCU dry gas and coke yield, 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 carries out stripping, and the reclaimable catalyst behind the stripping gets into revivifier regeneration, and regenerator and system's main air carry out turning back to step 1) after the heat exchange.
Described system main air is a part or all of system main air.
It is to carry out in the catalyst heat exchange device that described regenerator and system's main air carry out heat exchange.
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 the catalyst heat exchange device generally accounts for 20%～100% of the whole main air amounts of FCC, is preferably 30%～90%, is preferably 40%～85%; Regenerator temperature after the heat exchange of catalyst heat exchange device is generally 580～670 ℃, is preferably 600～660 ℃, is preferably 610～660 ℃.
Described riser reactor 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 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 raw oil 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 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 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; Revivifier links to each other with external warmer through inclined tube, and revivifier links to each other with the catalyst heat exchange device through regeneration standpipe, main air outlet pipe.
The present invention improves existing riser fluid catalytic cracking, through the catalyst heat exchange device is set, makes part or all of system 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, the raw oil thermal response weakens; Dry gas and coke yield significantly descend, 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.
For same raw material, and use with a kind of catalyzer, compare with conventional CCU, beneficial effect of the present invention is:
(1) the riser reactor agent-oil ratio can be increased to more than 10.
(2) device dry gas and coke overall yield descend 0.8～1.8 percentage point, and the total liquid of liquefied gas, gasoline and diesel oil is received and improved more than 1.0 percentage points.
(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 the CCU of a kind of high solvent-oil ratio of the present invention.
Among the figure:
1. reaction oil gas; 2. settling vessel; 3. riser reactor; 4. revivifier; 5. regeneration standpipe; 6. main air outlet pipe; 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. system's main air; 12. external warmer; 13. regeneration standpipe.
Embodiment
CCU of the present invention comprises: riser reactor 3, settling vessel 2, revivifier 4, external warmer 12, catalyst heat exchange device 10, regeneration standpipe 13, main air outlet pipe 6, regeneration standpipe 5, regenerator sloped tube 8.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 13; Revivifier 4 inside are connected with catalyst heat exchange device 10 inside through regeneration standpipe 5, main air outlet pipe 6, and revivifier 4 is connected with external warmer 12 through inclined tube, and catalyst heat exchange device 10 bottoms are connected with riser reactor 3 bottoms through regenerator sloped tube 8.
Raw oil 7 gets into riser reactors 3 bottoms, contact intensification, vaporization and the reaction of completion raw material with catalyzer from catalyst heat exchange device 10.Reacted oil gas and reclaimable catalyst separate through slightly revolving rapidly in the riser tube outlet, and gas gets into settling vessel 2 single stage cyclone separators, further remove the catalyst fines that carries after, reaction oil gas leaves settling vessel 2, gets into separation column and realizes separating.Reclaimable catalyst gets into stripping stage through thick spin material leg, in this and stripped vapor counter current contact, with oil gas entrained in the stripping catalyst.Catalyzer behind the stripping gets into revivifiers 4 through regeneration standpipe 13 and contacts with system main air 11 and from the main air that catalyst heat exchange device 10 is come and burn realization holomorphosis.High temperature regeneration agent after the regeneration gets into catalyst heat exchange device 10 through regeneration standpipe 5, and with part system main air 9 contact heat-exchangings, after abundant heat exchange, the main air after the heat exchange gets into revivifiers 4 through main air outlet pipe 6 and burns.Regenerator after the cooling gets into riser reactor 3 bottoms and raw oil 7 contact reactss, realization response-reprocessing cycle.
The temperature out of riser reactor according to the invention 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 ℃; 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 comprises 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, coal tar.
Embodiment
Embodiment 1 (Comparative Examples)
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 and table 3.
Embodiment 2 (Comparative Examples)
Press embodiment 1, different is that raw oil is the hydrogenation wax oil, and main character is listed in table 1, and treatment capacity is 30 kg/day, and the test catalyst system therefor is a RSC-2006 industry poiser, and the equilibrium catalyst micro-activity is 60, and carbon content is 0.06w%.The main operational condition of riser reactor, product distribute and the main character of product is listed in table 2 and table 3.
Embodiment 3 (Comparative Examples)
Press embodiment 1, different is that raw oil is hydrogenation heavy oil, and main character is listed in table 1, and treatment capacity is 30 kg/day, and the test catalyst system therefor is a MLC-500 industry poiser, and the equilibrium catalyst micro-activity is 63, and carbon content is 0.03w%.The main operational condition of riser reactor, product distribute and the main character of product is listed in table 2 and table 3.
Embodiment 4
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.
Embodiment 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.
Embodiment 6
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.
Table 1 raw oil main character
Project Embodiment 1,4 Embodiment 2,5 Embodiment 3,6
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
Project Embodiment 1 Embodiment 2 Embodiment 3
Raw oil The defeated heavy oil that mixes of pipe The hydrogenation wax oil Hydrogenation heavy oil
Catalyzer CDC RSC-2006 MLC-500
Main operational condition
The riser tube temperature out/℃ 520 500 515
Reaction pressure (gauge pressure)/MPa 0.17 0.18 0.18
Raw material preheating temperature/℃ 220 260 210
The regenerator temperature/℃ 690 690 690
Agent-oil ratio 7.2 6.0 7.2
Reaction times/s 3.19 3.23 2.96
Recycle ratio 0.16 0.06 0.10
Product distribution/weight %
Dry gas 4.23 3.05 3.81
Liquefied gas 15.20 16.67 14.02
Gasoline 39.54 51.25 44.10
Diesel oil 27.14 22.97 25.12
Slurry oil 5.00 0 5.00
Coke 8.39 5.56 7.45
Loss 0.50 0.50 0.50
Add up to 100 100 100
Total liquid is received (liquefied gas+gasoline+diesel oil) 81.88 90.89 83.24
Table 3 product main character
Project Embodiment 1 Embodiment 2 Embodiment 3
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
Project Embodiment 4 Embodiment 5 Embodiment 6
Raw oil The defeated heavy oil that mixes of pipe The hydrogenation wax oil Hydrogenation heavy oil
Catalyzer CDC RSC-2006 MLC-500
Main operational condition
The riser tube temperature out/℃ 520 500 515
Reaction pressure (gauge pressure)/MPa 0.17 0.18 0.18
Raw material preheating temperature/℃ 220 260 220
The regenerator temperature/℃ 650 630 640
Agent-oil ratio 10.3 8.5 9.8
Reaction times/s 2.96 3.02 2.89
Recycle ratio 0.07 0.04 0.05
Product distribution/weight %
Dry gas 2.82 1.82 2.50
Liquefied gas 17.37 19.87 17.26
Gasoline 43.36 55.56 46.21
Diesel oil 23.12 16.96 21.22
Slurry oil 5.00 0 5.00
Coke 7.83 5.29 7.31
Loss 0.50 0.50 0.50
Add up to 100 100 100
Total liquid is received (liquefied gas+gasoline+diesel oil) 83.85 92.39 84.69
Table 5 product main character
Project Embodiment 4 Embodiment 5 Embodiment 6
The gasoline main character
Density (20 ℃)/kg.m -3 723.0 722.3 725.0
Sulphur content/μ g.g -1 670 83 138
Octane value (RON) 93.0 92.2 93.2
Olefin(e) centent/volume % 29.6 18.3 20.8
Benzene content/volume % 0.68 0.65 0.59
Do/℃ 193 200 190
The diesel oil main character
Density (20 ℃)/kg.m -3 926.2 912.9 921.3
Sulphur content/μ g.g -1 6906 1323 2750
Cetane value 27.7 28.0 29.1
SO in the flue gas XContent/mg.m -3 556 406 1189

Claims (11)

1. a catalyst cracking method is characterized in that, comprises 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 carries out stripping, and the reclaimable catalyst behind the stripping gets into revivifier regeneration, and regenerator and system's main air carry out turning back to step 1) after the heat exchange.
2. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: described reclaimable catalyst and part system main air reach main air from the catalyst heat exchange device and contact and regenerate.
3. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: the said and system's main air regenerator heat exchange accounts for 20%～100% of the whole main air amounts of FCC, with the whole main air amount of FCC volumeter.
4. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: the said and system's main air regenerator heat exchange accounts for 40%～85% of the whole main air amounts of FCC, with the whole main air amount of FCC volumeter.
5. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: it is to carry out in the catalyst heat exchange device that described regenerator and system's main air carry out heat exchange.
6. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: the regenerator temperature after heat exchange is 580～670 ℃.
7. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: the regenerator temperature after heat exchange is 600～660 ℃.
8. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: described riser reactor temperature out is 450～560 ℃; Reaction times was generally 0.5～5 second; Agent weight of oil ratio is 3～20, and the reaction absolute pressure is generally 0.15～0.40MPa, and the regeneration temperature of revivifier is 650～750 ℃.
9. according to the described a kind of catalyst cracking method of claim 1; It is characterized in that: described riser reactor temperature out is 460～540 ℃; Reaction times is 1.0～4.5 seconds; Agent weight of oil ratio is 5～18, and the reaction absolute pressure is generally 0.20～0.36MPa, and the regeneration temperature of revivifier is 650～750 ℃.
10. according to the described a kind of catalyst cracking method of claim 1, it is characterized in that: described raw oil 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.
11. CCU; Comprise riser reactor, settling vessel, regeneration standpipe, revivifier, external warmer, regeneration standpipe, main air outlet pipe, regenerator sloped tube; 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 the catalyst heat exchange device, catalyst heat exchange device one end is communicated with revivifier, and the other end is communicated with regenerator sloped tube.
CN2011100968273A 2011-04-19 2011-04-19 Catalytic cracking method and device Pending CN102746891A (en)

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Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4960503A (en) * 1988-11-21 1990-10-02 Uop Heating FCC feed in a backmix cooler
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

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4960503A (en) * 1988-11-21 1990-10-02 Uop Heating FCC feed in a backmix cooler
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