CN102268290B - Catalytic cracking method and device - Google Patents
Catalytic cracking method and device Download PDFInfo
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- CN102268290B CN102268290B CN201010188833.7A CN201010188833A CN102268290B CN 102268290 B CN102268290 B CN 102268290B CN 201010188833 A CN201010188833 A CN 201010188833A CN 102268290 B CN102268290 B CN 102268290B
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Abstract
The invention discloses a catalytic cracking method and device, overcoming the defects of high gas and coke yields and low liquid yield which are caused by secondary cracking in the prior art. The method comprises the following steps: introducing a raw material oil into the lower part of a riser reactor so as to be contacted and reacted with a catalyst from a heat exchanger; carrying out crude separation on oil gas after reaction and a spent catalyst; further separating fine catalyst powder out of the reaction oil gas obtained by separation and then introducing the reaction oil gas without the fine catalyst powder into a fractionating column; carrying out steam stripping on the spent catalyst obtained by separation, and then introducing the spent catalyst subjected to steam stripping into a regenerator for regeneration; and introducing a part of regenerated high temperature reclaiming agent into the riser reactor from different heights of the riser reactor, introducing the other part of regenerated high temperature reclaiming agent into the heat exchanger, and the cooled reclaiming agent is recycled.
Description
Technical field
The invention belongs in the situation that not there is not hydrogen the catalytic cracking field of hydrocarbon ils, particularly a kind of new catalyst cracking method and device.
Background technology
The development of recent domestic catalytic cracking process rapidly, various novel increased low carbon olefine outputs and clean gasoline producing process emerge in an endless stream, but the maximization of economic benefit is the target that enterprise is pursued forever, and low dry gas and coke yield, high liquid are received, it is the fundamental means that catalytic cracking technology is increased economic efficiency always.Each research institution has made fruitful research in this respect both at home and abroad, and the technology of exploitation mainly contains following several:
" X design " (US 5451313) of Uop Inc., this new design has been invented in nineteen ninety-five by Uop Inc., its objective is rising agent oil ratio, be characterized in being provided with between reactor and revivifier a catalyst mix device, spent agent mixes in mixing tank with regenerator, part 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 enters riser tube than next low of revivifier, and catalyst recirculation amount is increased, and agent-oil ratio improves, so thermal response minimizings, catalyzed reaction increase, coke and dry gas yied reduce, gasoline yield increase.But it is very low that this design shortcoming is exactly spent agent activity in mixed catalyst, makes the activity of mixture on the low side, is unfavorable for the cracking of stock oil.
The IsoCat technique of Petrobras company (US 6059958), is characterized in being divided into two strands through the cooling catalyzer of external warmer, and one returns to regenerator bed, another strand with enter riser tube after hot regenerated catalyst mixes and react with stock oil.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 technique can reduce coke and dry gas yied, and two strands of catalyzer of IsoCat technique are regenerated catalyst, and the activity of mixture is higher, is more conducive to catalyzed reaction.But this technique implements comparatively complicated, and mixed catalyst difficult control of temperature.
The disclosed regenerator sloped tube catalyzer of CN 1288933 cooling technology, this method is exactly directly at regenerator sloped tube, a cooling water jecket to be set outward, by water coolant, the regenerated catalyst temperature that enters riser reactor is lowered.Although this method has obtained good effect on pilot plant, dry gas and coke yield are significantly declined, bring very large difficulty in industrial practice the control of temperature of reaction, that is to say that this method seems simply, put into practice difficulty larger.
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, the lower gasoline rising pipe reclaimable catalyst of part relative temperature is introduced to stock oil riser tube catalyzer pre-lift mixing tank simultaneously, after mixing with high temperature regeneration agent, enter stock oil riser tube, so both reduced the finish Contact Temperature of stock oil riser tube, take full advantage of again the remaining activity of gasoline rising pipe reclaimable catalyst, improve agent-oil ratio and the product selectivity of stock oil riser catalytic cracking, reduce dry gas and coke yield, improve propene yield and Propylene Selectivity.Although this technique weak point is that gasoline spent agent remaining activity is higher, compares or have a certain distance with regenerated catalyst.
China University Of Petroleum Beijing has proposed Novel multi association control heavy oil MZCC catalytic cracking technology (< < oil Refining Technologies and engineering > > the 12nd phase in 2008), MZCC technology be take the heat that mixes of optimizing heavy oil and regenerator and is promoted the cracking of hydro carbons macromole, reduces dry gas and coke is technique basis, 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, cooled catalyzer mixes with the thermocatalyst that former regenerator sloped tube comes, after mixing, regenerator and the raw material of lesser temps carry out contact reacts, this technology can reduce finish mixing temperature, and rising agent oil ratio is improved product and distributed, but this technology regenerator cooling measure is slightly aobvious complicated, need set up equipment more.
Summary of the invention
The present invention is in order to reduce catalytic cracking unit dry gas and coke yield, improves total liquid and receives, and reduces the SO in content of olefin in gasoline and 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) stock oil enters riser reactor bottom, contacts with the catalyzer from interchanger, reacts;
2) reacted oil gas and reclaimable catalyst carry out roughing out, and isolated reaction oil gas enters separation column after further isolating catalyst fines, and isolated reclaimable catalyst carries out stripping, and the reclaimable catalyst after stripping enters revivifier regeneration.
3) the high temperature regeneration agent part after regeneration enters riser reactor from riser tube different positions; Another part enters interchanger, and the regenerator after cooling enters 1).
Described a kind of catalyst cracking method, the high temperature regeneration agent after some regeneration enters interchanger by outer circulating tube.
Described a kind of catalyst cracking method, the regenerator that enters riser reactor from riser tube different heights be by catalyst transport be responsible for, catalyst transport arm enters riser reactor;
Described a kind of catalyst cracking method, reclaimable catalyst and part system main air and contact and carry out coke burning regeneration from the main air of catalyst heat exchange device.
Described a kind of catalyst cracking method, the high temperature regeneration agent and the heat exchange of FCC system main air counter current contact that after regeneration, enter interchanger, the main air after heat exchange enters revivifier and burns.The main air amount that enters interchanger generally accounts for 20%～100% of the whole main air amounts of FCC, and preferably 30%～90%, be preferably 40%～85%; After interchanger heat exchange, regenerated catalyst temperature is generally 580～670 ℃, preferably 600～660 ℃, is preferably 610～660 ℃.
Described riser reactor axial temperature is approximately equalised, is generally 450～560 ℃, preferably 460～540 ℃, is preferably 470～530 ℃; Reaction times is generally 0.5～5 second, and preferably 1.0～4.5 seconds, best 1.5～4.0 seconds; Agent weight of oil ratio, catalyst recirculation amount, by leg outlet internal circulating load, is generally 3～20, and preferably 5～18, best 8～15; Reaction absolute pressure is generally 0.15～0.40Mpa, and preferably 0.20～0.36Mpa, is preferably 0.22～0.33Mpa; The catalytic amount that is delivered to riser reactor by catalyst transport supervisor, catalyst transport arm is 5～30% of 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 % by weight, and regenerated catalyst micro-activity is generally 55～70.
It is a kind of that described riser reactor charging at least contains 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.
A kind of catalytic cracking unit of the present invention, contain riser reactor, settling vessel, revivifier, interchanger, inclined tube to be generated, outer circulating tube, standpipe, regenerator sloped tube, catalyst transport supervisor, catalyst transport arm, riser reactor top exit is connected with settling vessel entrance, riser reactor bottom is connected with interchanger bottom, settling vessel is connected with revivifier, revivifier is connected with interchanger top, and revivifier is connected with riser reactor.
Described a kind of catalytic cracking unit, revivifier is communicated with interchanger bottom by outer circulating tube.
Described a kind of catalytic cracking unit, revivifier is responsible for by catalyst transport and catalyst transport arm is connected with riser reactor, catalyst transport supervisor be communicated with catalyst transport arm, catalyst transport arm is 1～5, below catalyst transport arm 0.5～10 meter of above stock oil feed entrance point, position that is connected with riser reactor wherein, other catalyst transport arm is connected position far from 4～10 meters of conveying arm positions, below with riser reactor.
Described a kind of catalytic cracking unit, riser reactor bottom is connected with interchanger by regenerator sloped tube, and revivifier is connected with settling vessel stripping stage by inclined tube to be generated, and revivifier is connected with interchanger top by standpipe,
The present invention is by arranging interchanger, make part or all of main air carry out heat exchange with the high temperature regeneration agent that revivifier comes in interchanger, make on the one hand the main air temperature that enters revivifier raise, reduced on the other hand the regenerator temperature that enters riser reactor bottom, reduce finish Contact Temperature, stock oil heat cracking reaction degree weakens, and dry gas and coke yield decline to a great extent, and total liquid is received and improved; Due to the agent-oil ratio raising of riser reactor, contribute to the carrying out of catalyzed reaction, be conducive to the improvement that product distributes, can reduce the olefin(e) centent of gasoline simultaneously.Agent-oil ratio increases, and catalyst recirculation amount significantly improves, and because containing certain metal oxide in 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 catalysis flue gas.
The present invention, by by a small amount of high temperature regeneration agent, through catalyst transport supervisor, arm segmentation injecting lift pipe different heights region, is reaction additional heat, proposes isothermal riser tube concept, makes riser tube axially approach isothermal and distributes.Generally, 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 continuous decrease.Charging mixing section above nozzle, the jet phase that represents mist of oil and the distributional pattern that represents granules of catalyst phase be unfavorable for very much two alternate contact even, the position that jet phase concentration is large, the concentration of Particle Phase is little, do not match, Particle Phase mates bad with the concentration distribution of jet phase, being affects the well major cause of uniform contact of finish two-phase.And the present invention can solve the well problem of uniform contact of charging mixing section finish two-phase preferably.The present invention, by a small amount of high temperature regeneration agent segmentation injecting lift pipe different heights region, makes riser tube axially approach isothermal and distributes.Charging mixing section above stock oil feed entrance point, the catalyzer filling into can suitably improve the region that Particle Phase concentration is less, jet phase and Particle Phase concentration are matched, realize finish two-phase uniform contact, suppress the heat cracking reaction that Particle Phase concentration occurs compared with zonule, promote the carrying out of catalyzed reaction; The regenerator filling in other region of riser tube can be reaction additional heat, improves riser tube inner catalyst average activity simultaneously, guarantees that catalyzed reaction continues to carry out, and product is distributed and optimized.
Compare with conventional catalytic cracking unit, in the situation that raw material is identical with catalyzer, beneficial effect of the present invention is:
(1) riser reactor agent-oil ratio can be increased to more than 10.
(2) device dry gas and coke overall yield decline 0.8～1.5 percentage point, and the total liquid of liquefied gas, gasoline and diesel oil is received and improved more than 1 percentage point.
(3) gasoline olefin volume content can reduce by 5～15 percentage points.
(4) in catalysis flue gas, SOx content reduces more than 30%.
Utilize the drawings and specific embodiments to be further detailed the present invention below, but do not limit the scope of the invention.
Accompanying drawing explanation
Fig. 1 is the device schematic diagram that the present invention realizes a kind of catalyst cracking method.
1-reaction oil gas; 2-settling vessel; 3-inclined tube to be generated; 4-main air A; 5-catalyst transport supervisor;
6-riser reactor; 7-catalyst transport arm; 8-stock oil; 9-regenerator sloped tube; 10-main air B; 11-interchanger; 12-outer circulating tube; 13-standpipe; 14-revivifier; 15-flue gas
Embodiment
As shown in Figure 1: a kind of catalyst cracking method of the present invention, concrete steps are:
1) stock oil 8 enters riser reactor 6 bottoms, contacts with the catalyzer from interchanger 11, reacts;
2) reacted oil gas and reclaimable catalyst carry out roughing out in settling vessel 2, isolated reaction oil gas 1 enters follow-up separation column after further isolating catalyst fines, isolated reclaimable catalyst carries out stripping in settling vessel 2 bottoms, and the reclaimable catalyst after stripping enters revivifier 14 and regenerates.
3) the high temperature regeneration agent part after regeneration enters riser reactor 6 from riser tube 6 different heights; Another part enters interchanger 11, and the regenerator after cooling enters 1).
Be illustrated in figure 1 the device of realizing a kind of catalyst cracking method of the present invention, comprise: riser reactor 6, settling vessel 2, revivifier 14, interchanger 11, inclined tube to be generated 3, outer circulating tube 12, standpipe 13, regenerator sloped tube 9, catalyst transport supervisor 5, catalyst transport arm 7.The top exit of riser reactor 6 is connected with settling vessel 2, riser reactor 6 bottoms are connected with interchanger 11 by regenerator sloped tube 9, by inclined tube 3 to be generated, settling vessel 2 stripping stages are connected with revivifier 14, revivifier 14 is inner to be communicated with interchanger 11 by standpipe 13, revivifier 14 outsides are connected with interchanger 11 bottoms by outer circulating tube 12, interchanger 11 bottoms are connected with riser reactor 6 bottoms by regenerator sloped tube 9, revivifier 14 is responsible for 5 by catalyst transport and is connected with catalyst transport arm 7, catalyst transport supervisor 5 is connected with riser reactor 6 by catalyst transport arm 7.Catalyst transport arm 7 of the present invention can arrange 1～5, below catalyst transport arm 7 0.5～10 meter of above stock oil 8 feed entrance points, position that is connected with riser reactor 6 wherein, other catalyst transport arm 7 is connected position far from 4～10 meters of conveying arm 7 positions, below with riser reactor 6.
Embodiment 1 is comparative example
On conventional riser catalytic cracking test device, test, charging is the defeated mixing heavy oil of pipe, and main character is listed in table 1, treatment capacity is 30 kg/day, test used catalyst is CDC industry poiser, and the micro-activity of equilibrium catalyst is 62, and carbon content is 0.05 % by weight.The main operational condition of riser reactor, product distribute and the main character of product is listed in table 2 and table 3.
Press embodiment 1, difference is that charging is hydrogenation wax oil, and main character is listed in table 1, and treatment capacity is 30 kg/day, and test used catalyst is RSC-2006 industry poiser, and the micro-activity of equilibrium catalyst is 60, and carbon content is 0.06%.The main operational condition of riser reactor, product distribute and the main character of product is listed in table 2 and table 3.
Press embodiment 1, difference is that charging is hydrogenation heavy oil, and main character is listed in table 1, and treatment capacity is 30 kg/day, and test used catalyst is MLC-500 industry poiser, and equilibrium catalyst micro-activity is 63, and carbon content is 0.03 % by weight.The main operational condition of riser reactor, product distribute and the main character of product is listed in table 2 and table 3.
On catalytic cracking test device of the present invention, testing as shown in Figure 1, treatment capacity is 30 kg/day, and charging, 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 catalytic cracking test device of the present invention, testing as shown in Figure 1, treatment capacity is 30 kg/day, and charging, 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 catalytic cracking test device of the present invention, testing as shown in Figure 1, treatment capacity is 30 kg/day, and charging, 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 riser reactor charging
| | Embodiment | 1 and 4 | |
|
| Stock oil title | Manage defeated mixing heavy oil | 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/ % by weight | 86.65 | 86.81 | 86.84 | |
| H/ % by weight | 12.25 | 13.08 | 12.53 | |
| S/ % by weight | 0.65 | 0.0863 | 0.291 | |
| N/ % by weight | 0.14 | 0.0147 | 0.145 | |
| Group composition/% by 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 |
The main operational condition of table 2 and product distribute
| Project | Embodiment 1 | |
|
| Stock oil | Manage defeated mixing heavy oil | Hydrogenation wax oil | Hydrogenation heavy oil |
| Catalyzer | CDC | RSC-2006 | MLC-500 |
| Main operational condition | |||
| Outlet temperature of riser/℃ | 520 | 500 | 515 |
| Riser tube middle part temperature/℃ | 535 | 515 | 530 |
| Finish mixing temperature/℃ | 550 | 530 | 545 |
| Reaction pressure (gauge pressure)/Mpa | 0.17 | 0.18 | 0.18 |
| Raw material preheating temperature/℃ | 220 | 260 | 210 |
| 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/% by weight | |||
| Dry gas | 4.23 | 3.05 | 3.81 |
| Liquefied gas | 15.20 | 16.67 | 14.02 |
| Gasoline | 39.54 | 51.25 | 43.80 |
| Diesel oil | 27.14 | 22.97 | 24.82 |
| Slurry oil | 5.00 | 0 | 6.00 |
| Coke | 8.39 | 5.56 | 7.05 |
| 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 | 82.64 |
Table 3 product main character
| Project | Embodiment 1 | |
|
| 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 |
| 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 flue gas XContent/mg.m -3 | 1035 | 656 | 2120 |
The main operational condition of table 4 and product distribute
| | Embodiment | 4 | |
|
| Stock oil | Manage defeated mixing heavy oil | Hydrogenation wax oil | Hydrogenation heavy oil | |
| Catalyzer | CDC | RSC-2006 | MLC-500 | |
| Main operational condition | ||||
| Outlet temperature of riser/℃ | 535 | 515 | 530 | |
| Riser tube middle part temperature/℃ | 535 | 515 | 530 | |
| Finish mixing temperature/℃ | 535 | 515 | 530 | |
| Reaction pressure (gauge pressure)/Mpa | 0.17 | 0.18 | 0.18 | |
| Raw material preheating temperature/℃ | 220 | 260 | 210 | |
| Regenerator temperature/℃ | 630 | 620 | 630 | |
| Agent-oil ratio | 12.1 | 8.5 | 12.3 | |
| Reaction times/s | 2.95 | 3.15 | 2.78 | |
| Recycle ratio | 0.05 | 0.03 | 0.04 | |
| Product distribution/% by weight | ||||
| Dry gas | 2.95 | 1.87 | 2.45 | |
| Liquefied gas | 17.35 | 20.05 | 17.31 | |
| Gasoline | 43.62 | 55.64 | 46.46 | |
| Diesel oil | 22.70 | 16.65 | 21.03 | |
| Slurry oil | 5.00 | 0 | 5.00 | |
| Coke | 7.88 | 5.29 | 7.25 | |
| Loss | 0.50 | 0.50 | 0.50 | |
| Add up to | 100 | 100 | 100 | |
| Total liquid is received (liquefied gas+gasoline+diesel oil) | 83.67 | 92.34 | 84.80 |
Table 5 product main character
| | Embodiment | 4 | |
|
| Gasoline main character | ||||
| Density (20 ℃)/kg.m -3 | 721.0 | 727.9 | 725.3 | |
| Sulphur content/μ g.g -1 | 673 | 77 | 135 | |
| Octane value (RON) | 93.3 | 92.3 | 93.3 | |
| Olefin(e) centent/volume % | 29.8 | 18.1 | 20.6 | |
| Benzene content/volume % | 0.72 | 0.77 | 0.58 | |
| Do/℃ | 191 | 200 | 191 | |
| Diesel oil main character | ||||
| Density (20 ℃)/kg.m -3 | 926.2 | 914.1 | 922.0 | |
| Sulphur content/μ g.g -1 | 6900 | 1310 | 2790 | |
| Cetane value | 27.2 | 27.0 | 28.7 | |
| SO in flue gas XContent/mg.m -3 | 560 | 416 | 1290 |
Claims (10)
1. a catalyst cracking method, is characterized in that comprising the steps:
1) stock oil enters riser reactor bottom, with the catalyzer contact reacts from interchanger, riser reactor axial temperature is to be 450～560 ℃, and the reaction times is 0.5～5 second, agent weight of oil ratio is 3～20, and reaction absolute pressure is 0.15～0.40MPa;
2) reacted oil gas and reclaimable catalyst carry out roughing out, and isolated reaction oil gas enters separation column after further isolating catalyst fines, and isolated reclaimable catalyst carries out stripping, and the reclaimable catalyst after stripping enters revivifier regeneration;
3) the high temperature regeneration agent part after regeneration is responsible for by catalyst transport, catalyst transport arm enters riser reactor from riser tube different heights, by catalyst transport, be responsible for, the catalytic amount that catalyst transport arm is delivered to riser reactor is 5～30% of riser reactor global cycle amount, another part enters high temperature regeneration agent and the heat exchange of FCC system main air counter current contact of interchanger, the main air amount that enters interchanger accounts for 20 volume %～100 volume % of the whole main air amounts of FCC, after heat exchange, regenerated catalyst temperature is 580～670 ℃, regenerator after cooling enters 1).
2. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the high temperature regeneration agent after another part regeneration enters interchanger by outer circulating tube.
3. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: reclaimable catalyst and part system main air and contact and carry out coke burning regeneration from the main air of catalyst heat exchange device.
4. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: the main air amount that enters interchanger accounts for 40 volume %～85 volume % of the whole main air amounts of FCC, and after heat exchange, regenerated catalyst temperature is 610～660 ℃.
5. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: riser reactor axial temperature is to be 460～540 ℃, and the reaction times is 1.0～4.5 seconds, and agent weight of oil ratio is 5～18, and reaction absolute pressure is 0.20～0.36MPa.
6. according to a kind of catalyst cracking method claimed in claim 1, it is characterized in that: riser reactor axial temperature is to be 470～530 ℃, and the reaction times is 1.5～4.0 seconds, and agent weight of oil ratio is 8～15, and reaction absolute pressure is 0.20～0.36Mpa.
7. according to any catalyst cracking method described in claim 1 to 6, it is characterized in that: described stock oil is at least one 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, coal tar.
8. a catalytic cracking unit, contain riser reactor (6), settling vessel (2), revivifier (14), interchanger (11), inclined tube to be generated (3), standpipe (13), regenerator sloped tube (9), catalyst transport supervisor (5), catalyst transport arm (7), riser reactor (6) top exit is connected with settling vessel (2) entrance, riser reactor (6) bottom is connected with interchanger (11) bottom, settling vessel (2) is communicated with revivifier (14), revivifier (14) is communicated with interchanger (11) top, revivifier (14) is responsible for (5) by catalyst transport and catalyst transport arm (7) is communicated with riser reactor (6).
9. according to a kind of catalytic cracking unit claimed in claim 8, it is characterized in that: revivifier (14) is communicated with interchanger (11) by outer circulating tube (12).
10. according to a kind of catalytic cracking unit claimed in claim 8, it is characterized in that: catalyst transport supervisor be communicated with catalyst transport arm, catalyst transport arm is 1～5, below catalyst transport arm 0.5～10 meter of above stock oil feed entrance point, position that is connected with riser reactor, catalyst transport arm is 2 or during more than 2, the distance between catalyst transport arm is 4～10 meters.
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|---|---|---|---|---|
| US6059958A (en) * | 1997-07-17 | 2000-05-09 | Petroleo Brasileiro S.A.-Petrobras | Process for the fluid catalytic cracking of heavy feedstocks |
| CN1288933A (en) * | 1999-09-17 | 2001-03-28 | 中国石油化工集团公司 | Warming method for pipeline of heavy oil catalytic cracking regenerating agent |
| CN1340593A (en) * | 2000-08-30 | 2002-03-20 | 中国石油化工股份有限公司 | Contact method for catalytic cracking of oil |
| CN1340595A (en) * | 2000-08-30 | 2002-03-20 | 中国石油化工股份有限公司 | Feeding method for catalytic cracking of hydrocarbon oil |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant after: China Petrochemical Group Corp. Co-applicant after: Luoyang Petrochemical Engineering Corporation /SINOPEC Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Applicant before: China Petrochemical Group Corp. Co-applicant before: Luoyang Petrochemical Engineering Co., China Petrochemical Group |
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