CN102453543A - Combined process of hydrotreatment and catalytic cracking for residuum - Google Patents
Combined process of hydrotreatment and catalytic cracking for residuum Download PDFInfo
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Abstract
The invention discloses a combined process of hydrotreatment and catalytic cracking for residuum. According to the process, a boiling bed hydrotreatment method is used in hydrotreatment of residuum, and the process comprises the following steps that: liquid phase products obtained after the raw material of residuum undergoes boiling bed hydrotreatment are subjected to fractional distillation so as to obtain light components and heavy components; the light components are used as first-stage charging materials and enter into a catalytic cracking riser reactor from the bottom of the reactor; the heavy components directly enter into a catalytic cracking fractionator and are subjected to fractional distillation together with effluent of a catalytic cracking reaction so as to isolate dry gas, liquefied gas, gasoline fraction, diesel oil fraction, recycle oil and slurry oil, wherein, the recycle oil is used as a second-stage charging material of the riser reactor, and the slurry oil is used as a charging component for delayed coking. Compared to the prior art, the process provided in the invention has the following characteristics: gasoline with a high octane number, diesel oil fraction and liquefied gas with a high added value can be produced; reaction thermal energy is fully utilized, thereby reducing energy consumption in production.
Description
Technical field
The present invention relates to a kind of residual oil lightening method, specifically with residual hydrocracking and catalytic cracking organic assembling, is the process method that raw material is mainly produced high octane gasoline products and diesel oil distillate with residual oil.
Background technology
Along with crude oil becomes heavy day by day, becomes bad, increasing residual oil needs processing treatment.Processing treatment heavy, residual oil will be lower boiling product with its cracking not only, like petroleum naphtha, intermediate oil and vacuum gas oil etc., but also will improve their hydrogen-carbon ratio, and this just need realize through the method for decarburization or hydrogenation.Wherein decarbonization process comprises coking, solvent deasphalting, RFCC etc.; Hydrogenation comprises hydrogen cracking, unifining etc.Hydrogenation method can hydrocracking residual oil, improves the productive rate of liquid product, and can also remove heteroatoms wherein, helps improving the quality of product.But hydrogenation method is the catalysis complete processing, has hydrogenation catalyst inactivation problem, and when especially processing poor quality, heavier hydrocarbon feeds, the catalyst deactivation problem is more serious.At present, in order to reduce heavy, poor residuum cost of processing, increase the oil refining enterprise profit; The technology of processing heavy, poor residuum is main with decarbonization process still, but its poor product quality need be carried out aftertreatment and could be utilized; Wherein deasphalted oil and wax tailings cut especially need carry out hydrotreatment; Could continue to use lighting devices such as catalytic cracking or hydrogen cracking to process, therefore, each oil refining enterprise all has the hydrotreater of deasphalted oil and wax tailings in addition.
The slag oil cracking rate of residual hydrocracking technology is lower, and main purpose is to supply raw materials for downstream raw material lighting device such as devices such as catalytic cracking or coking.Through hydrotreatment; Sulphur, nitrogen, metal impurities content and carbon residue in the poor residuum are obviously reduced; Thereby obtain the charging that lighting device in downstream can be accepted; Especially be mainstream technology with residue fixed-bed hydrotreatment and catalytic cracking combination technique in the CCU, therefore heavy at present, residual hydrogenation modifying process technology.
Existing residual hydrocracking and catalytic cracking combined technique; At first be that residual oil is carried out hydrotreatment, hydrogenated oil is isolated petroleum naphtha and diesel oil distillate, and hydrogenation tail oil is as the RFCC charging; Carry out catalytic cracking reaction; Product is dry gas, liquefied gas, gasoline, diesel oil and coke, and recycle stock carries out the catalysis freshening or loops back residual hydrogenation equipment and the residual hydrocracking raw materials mix is carried out hydrotreatment, and catalytic slurry gets rid of outward or part catalysis freshening or loop back residual hydrogenation equipment.Above-mentioned residual hydrocracking and catalytic cracking combined technique exist yield of gasoline low, and heat energy loss is big, unfavorable factors such as facility investment height.
And the boiling bed hydrogenation technology adaptability to raw material that is used for heavy oil upgrading is wide, can process various poor residuum raw materials, not restricted by feedstock property, but with fixed bed comparatively speaking, its impurity removal percentage is lower, degree of saturation is poor.Boiling bed hydrogenation handle to generate oil usually with the wax oil cut as catalytically cracked material, and heavy oil carries out processing treatment respectively as the delayed coking raw material, obtains corresponding gasoline, diesel oil distillate, needs kinds of processes to make up and accomplishes.
US 6447671 discloses a kind of combination process process that is used for heavily residuum hydroconversion.Detailed process is: heavy residual oil raw material and hydrogen are mixed into boiling bed hydrogenation cracking reaction district; Logistics obtains lighting end and last running through tripping device behind the hydrocracking reaction, and lighting end gets into distillate fixed bed hydrogenation processing section or directly gets into water distilling apparatus carries out the narrow fraction cutting; Heavy constituent get into heavy oil fixed bed hydrogenation reaction zone after filtering system is removed the catalyst solid residue; Perhaps effusive whole logistics directly get into filtering system from boiling bed hydrogenation cracking reaction district, isolate and get into heavy oil fixed bed hydrogenation processing reaction district behind the catalyst solid material; Reacted all or part of logistics gets into water distilling apparatus, cuts out each lighting end and heavy constituent, and the heavy constituent that wherein obtain get into CCU or loop back heavy-oil hydrogenation and handle or the hydrocracking reaction district.This combination process process just requires according to the charging of device and reacted logistics property carries out the rational Match of processing means, the characteristics of each COMBINED PROCESS is not given full play of.
US 6277270 has introduced and has used fixed bed hydrogenation, boiling bed hydrogenation and catalytic cracking combined technique to handle the technological process of heavy crude hydrocarbon feed.Process description: residual oil raw material obtains decompressed wax oil and vacuum residuum through underpressure distillation, and wherein all or part of entering fixed bed hydrogenation of decompressed wax oil treatment unit reacts, and the hydrogenation wax oil obtains distillate and hydrogenation tail oil (a) through the normal pressure distillation; Wherein vacuum residuum directly or be mixed into the liquid bed device with the part decompressed wax oil and carry out hydrocracking reaction; Generate oil and obtain atmospheric distillate and long residuum (b) through air distillation; Wherein atmospheric distillate entering fixed bed hydrogenation reactor carries out hydrogenation reaction; Long residuum (b) gets into the boiling bed hydrogenation device, or the oily remover etc. that acts as a fuel.This combination process just requires to carry out the use of uniting of device according to the liquid feeding of different device, does not specifically combine polytechnic characteristic, brings into play the sharpest edges of each technology as far as possible.
Summary of the invention
To the deficiency of prior art, the invention provides a kind of residual hydrocracking and catalytic cracking combination process, this method can maximum be produced gasoline and diesel product, and technological process is simple simultaneously, and whole energy consumption is low.
Residual hydrocracking of the present invention and catalytic cracking combination process; Wherein riser reactor is adopted in catalytic cracking; Described riser reactor is provided with the two-stage opening for feed; Wherein first step opening for feed is arranged on the bottom of riser tube, and second stage opening for feed is above first step opening for feed, and the boiling bed residual oil hydroprocessing technique is adopted in residual hydrocracking; This method comprises: residual oil raw material gets into the boiling bed hydrogenation treatment reactor; In the presence of hydrogen and hydrotreating catalyst, carry out hydrogenation reaction; Hydrogenation reaction effluent gas-liquid separation, liquid phase fractionate out light constituent and heavy constituent, and wherein the cut point of light constituent and heavy constituent is 320～380 ℃; Light constituent gets into reactor drum as the charging of the catalytic cracking riser reactor first step by first step opening for feed; Heavy constituent get into separation column by the bottom of catalytic cracking fractionating tower; Heavy constituent get into the entry position of catalytic cracking fractionating tower above catalytic cracking reaction elute entering catalytic cracking fractionating tower entry position; Heavy constituent and catalytic cracking reaction elute are isolated dry gas, liquefied gas, gasoline fraction, diesel oil distillate, recycle stock and slurry oil through fractionation, and wherein recycle stock is as the charging of the catalytic cracking riser reactor second stage; Get into reactor drum by second stage opening for feed, carry out catalytic cracking reaction.
In the inventive method, slurry oil can be used as the delayed coking feed component, handles to coker.
The reactor drum of described CCU adopts riser reactor; This reactor drum is provided with the two-stage opening for feed, and wherein first step opening for feed is arranged on the bottom of reactor drum, can be charging place of conventional riser reactor; Also can be arranged on any position of riser tube bottom as requested; Second stage opening for feed is arranged on the top of first step opening for feed, accounts for 1/30～1/5 of whole riser tube height apart from the distance of first step opening for feed, is preferably 1/10～1/6.This technical process is specially: light constituent injects as the first step opening for feed of first step charging from the riser reactor bottom; Contact with high-temperature regenerated catalyst from revivifier; The oil gas that cracking reaction generates and the catalyst mixture of deposit coke move up along riser reactor; Mix with the recycle stock that second stage opening for feed from riser reactor gets into, carry out catalytic cracking reaction.
In the inventive method, residual oil raw material comprises long residuum or vacuum residuum or poor residuum, can be the residual oil raw material in other source also, also can contain in part wax tailings, deasphalted oil, the heavy distillate one or several in the residual oil raw material simultaneously.Hydrogenation reaction effluent at first carries out gas-liquid separation; This gas-liquid separation is carried out under the condition identical with the reaction pressure grade; Separate the gas phase that obtains and be mainly hydrogen; Handle the back circulation through selectable depriving hydrogen sulphide and be used for hydrogenation reaction, hydrogenation process need replenish the consumption of new hydrogen with the postreaction process simultaneously.The liquid phase that the hydrogenation reaction effluent solution-air obtains after separating gets into separation column, isolates light constituent and heavy constituent; Wherein light constituent gets into riser reactor by the catalytic cracking riser bottom; Heavy constituent directly get into the catalytic cracking fractionating tower bottom; Carry out fractionation with the catalytic cracking reaction elute, obtain dry gas, liquefied gas, gasoline fraction, diesel oil distillate, recycle stock and slurry oil, wherein recycle stock is as the charging of the catalytic cracking riser reactor second stage; Get into reactor drum by second stage opening for feed, carry out catalytic cracking reaction.
Among the present invention, the boiling bed hydrogenation catalyst that described boiling bed residual oil hydroprocessing technique adopts is the conventional hydrotreating catalyst in this area, and wherein the activity of such catalysts metal can be in nickel, cobalt, molybdenum or the tungsten one or more.Can comprise by weight percentage like the catalyzer composition: nickel or cobalt are 1%～20% (calculating by its oxide compound); Molybdenum or tungsten are 1%～30% (calculating by its oxide compound), and carrier can be in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or the titanium oxide one or more.The shape of catalyzer is extrudate or sphere, and bulk density is 0.4～0.9g/cm
3, particle diameter (spherical diameter or bar shaped diameter) is 0.08～1.2mm, specific surface area is 100～300m
2/ g.The operational condition that boiling bed hydrogenation is handled is generally: reaction pressure 6～30MPa, 400～490 ℃ of temperature of reaction, volume space velocity 0.1～5.0h during liquid
-1, hydrogen to oil volume ratio (under the standard conditions) 200～2000; Preferred operational condition is: reaction pressure 15～20MPa, 420～470 ℃ of temperature of reaction, volume space velocity 0.5～2.0h during liquid
-1Hydrogen to oil volume ratio (under the standard conditions) 400～1000.Described reaction product tripping device can be HP separator or flashing tower, and the temperature of cutting apart of light constituent and heavy constituent is 320～380 ℃, and light constituent mainly comprises gasoline fraction and diesel oil distillate.
The present invention is applicable to normal pressure or vacuum residuum hydrotreatment, is particularly useful for the hydrocracking of heavy hydrocarbon.The actual conditions of residual hydrocracking process can specifically be confirmed according to the requirement of raw material properties and CCU charging.
In the inventive method, catalytic cracking can be adopted this area routine techniques.CCU can be that every covering device should comprise a reactor drum, a revivifier at least more than a cover or overlapped.CCU is provided with separation column, can set respectively by every cover CCU, also can be shared.Catalytic cracking fractionating tower is dry gas, liquefied gas, gasoline, diesel oil distillate, recycle stock and slurry oil with the fractionation of catalytic cracking reaction elute.
In the inventive method, CCU is operated by this area general condition: temperature of reaction is 450～600 ℃, preferably 480～550 ℃; Regeneration temperature is 600～800 ℃, is preferably 650～750 ℃, and the agent weight of oil is than 2～30, preferably 4～10; With 0.1～15.0 second duration of contact of catalyzer, best 0.5～5.0 second; Pressure 0.1～0.5MPa.The catalytic cracking catalyst that is adopted comprises the catalyzer that is generally used for catalytic cracking; Like silica-alumina catalyst, silica-magnesia catalyst, acid-treated carclazyte and X type, Y type, ZSM-5, M type, layer post equimolecular sieve cracking catalyst; Molecular sieve cracking catalyst preferably, this is because molecular sieve cracking catalyst active high, green coke is few; Gasoline yield is high, and transformation efficiency is high.
In the inventive method, the concrete operations condition of residual hydrocracking and catalytic cracking can be obtained through simple experiment according to feedstock property and product quality indicator by the technician.
The invention has the advantages that:
1, in whole combination process; The light constituent that boiling bed residual oil hydrogenation process generates is as the charging of the catalytic cracking riser first step, after the reaction of high-temperature regenerated catalyst short-time contact; Arrive riser tube second stage charging place rapidly; Obtain cooling to a certain degree at this, stoped the generation of secondary reaction, make the gasoline yield maximization.
2, the feedstock property of boiling bed hydrogenation processing is poor, and the boiling bed hydrogenation degree of depth relaxes in addition, and transformation efficiency is lower, and tail oil character is poor, is not good catalytically cracked material.The heavy constituent that the boiling bed hydrogenation process obtains directly get into catalytic cracking fractionating tower and carry out fractionation; These heavy constituent can fractionate out wax oil and heavy oil; Wherein wax oil is included in the recycle stock; Get into CCU by riser tube second stage opening for feed, effectively utilize the catalytic cracking process characteristics, maximum is produced light ends oil; Heavy oil is included in the slurry oil, as the coking raw material component, handles to coker, and the coking raw material of poor residuum is good feed composition relatively.
3, from whole combination process; Only simple and easy fractionating system need be set in the hydrotreater, hydrotreatment generates oil and directly gets into catalyst cracker and separation column, need not establish fresh feed pump; A large amount of heat-exchange equipments have been reduced simultaneously; Greatly reduce the loss of heat, significantly reduced the required energy of fractionation process simultaneously, thereby reduced the energy consumption of whole technological process.
4, the position of hydrogenation heavy constituent entering catalytic cracking fractionating tower is arranged on the top of catalytic cracking reaction elute inlet, helps catalysis generation oil like this and carries out heat exchange with heavy constituent, helps the separation of light constituent.
5, the two-stage charging is adopted in catalytic cracking of the present invention, and wherein the light constituent in the hydrogenated oil gets into reactor drum as first step charging by the riser tube bottom, contacts with high-temperature regenerated catalyst, generates stop bracket gasoline and liquefied gas.Behind charging of the riser tube first step and the catalyst reaction, the rapid desorption of reaction product together gets into air-flow with the catalyzer that has part of coke (catalyst activity at this moment slightly descends); After second stage charging is injected, contact with catalyzer from the first step, carrying out catalytic cracking reaction under the demulcent condition relatively, generation gasoline, diesel oil and gas; In addition, the injection of second stage charging, having stoped the light constituent overcracking is littler molecule, and the purpose product yield is increased.
Description of drawings
Fig. 1 is residual hydrocracking of the present invention and catalytic cracking combinational processing method process flow diagram.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is further explained, but therefore do not limited the present invention.
Technical process of the present invention is described in detail as follows, and CCU adopts riser reactor.
Residual oil raw material 1; The back of boosting is mixed into boiling bed hydrogenation treatment reactor 2 with recycle hydrogen 5, through contacting with hydrotreating catalyst, removes impurity such as part metals in the raw oil, sulphur, nitrogen; Reduce the carbon residue of raw material simultaneously, satisfy the charging requirement of downstream catalytic cracking unit as far as possible.Hydrotreating reactor 2 outlet reaction effluents 3 get into HP separator 4 and carry out gas-liquid separation; Isolated gaseous stream carries out being recycled to after the laggard recycle compressor 8 of processing such as depriving hydrogen sulphide boosts hydrotreating reactor 2 inlets; The new hydrogen that replenishes also can be introduced after recycle compressor 8; Isolated liquid phase stream gets into fractionation plant 6 through pipeline 16 and carries out fractionation, obtains light constituent and heavy constituent; Isolated light constituent carries out catalytic cracking reaction through pipeline 7 by the bottom that first step opening for feed gets into catalytic cracking riser 9; Heavy constituent, are isolated wax oil (being included in the recycle stock) and are returned catalytic unit as second stage charging to catalytic cracking fractionating tower 15 through pipeline 18, and heavy oil (being included in the slurry oil) gets into coker and handles; Catalytic cracking reaction elute 10 gets into the separation column 15 of catalytic unit, isolates gas 11, gasoline 12, diesel oil 13, recycle stock 14 and slurry oil 17; Wherein gas 11, gasoline 12, diesel oil 13 dischargers, recycle stock 14 gets into riser reactor 9 by second stage opening for feed, carries out catalytic cracking reaction; Slurry oil 17 gets into coker and handles.
Following embodiment will further specify method provided by the invention, but therefore not limit the present invention.Reaction is on small-sized lifting tubular type CCU and pilot scale boiling bed residual oil hydrotreater, to carry out.Used raw oil is to subtract slag in the sand in embodiment and the Comparative Examples, and its character is listed in table 1.The type of used catalyst for hydrotreatment of residual oil and volume are identical in embodiment and the Comparative Examples, the boiling bed hydrogenation catalyst that process of the test is used as microspheroidal with the molybdenum-nickel catalyzator of aluminum oxide as carrier, wherein contain MoO in the catalyzer
3Be 15wt%, containing NiO is 4wt%, and the bulk density of catalyzer is 0.75g/cm
3, specific surface area is 240m
2/ g, the granules of catalyst mean diameter is 0.6mm.Among the present invention, wt% is the prime number mark.
Catalytic cracking catalyst used in embodiment and the Comparative Examples is identical, and fresh dose consists of: 95wt%LBO-16 olefine lowering catalyst+5wt%LBO-A boosting of octane rating auxiliary agent (LBO-16 and LBO-A are the catalytic cracking catalyst of Lanzhou Petrochemical Company Development and Production).
Comparative Examples
This Comparative Examples adopts conventional boiling bed residual oil hydrogenation and catalystic cracking method, and promptly residual oil carries out hydrogenation reaction at hydrotreater, and reaction product isolated obtains gas and hydrogenated oil.The hydrogenated oil of gained together gets into CCU and carries out cracking reaction, and one way is passed through, and product is gasoline, diesel oil, gas, and the above cut of catalytic cracking recycle oil loops back residual hydrogenation equipment and handles.Table 2, table 3, table 4 are respectively processing condition, product distributes and main products character.
Embodiment
This embodiment adopts boiling bed residual oil hydrotreatment provided by the invention and catalytic cracking combination method; Flow process is seen Fig. 1; Wherein the hydrotreatment liquid product fractionates out light constituent and heavy constituent; Its cut point is 350 ℃, and second stage opening for feed is above first step charging, and the distance first opening for feed height accounts for 1/10 of riser tube height overall.Table 2, table 3, table 4 are respectively processing condition, product distributes and main products character.
Comparing result shows; It is light constituent and heavy constituent that residual hydrogenation is generated oil content; Get into riser reactor from the two-stage opening for feed respectively and carry out catalytic cracking reaction; Together get into catalyst cracker with the full cut of residual hydrogenation generation oil and compare, liquefied gas, gasoline, diesel oil total recovery are 83.9wt%, exceed 17.5 percentage points than Comparative Examples.Coke yield has descended 2.7 percentage points, and dry gas yied has descended 1.9 percentage points.The inventive method can satisfy the enterprise that hopes the raising the output stop bracket gasoline well.
Table 1 raw oil character
Table 2 hydrotreatment and catalytic cracking process condition
Annotate: volume space velocity is to fresh residual oil raw material during * liquid.
Table 3 product distributes
| Title | Comparative Examples | Embodiment | Difference |
| The catalytic cracking product distributes: wt% | |||
| Dry gas | 4.6 | 2.7 | -1.9 |
| Liquefied gas | 9.5 | 12.1 | +2.6 |
| Gasoline | 36.2 | 46.2 | +10.0 |
| Diesel oil | 18.3 | 23.2 | +4.9 |
| Slurry oil | 22.2 | 9.3 | -12.9 |
| Coke | 9.2 | 6.5 | -2.7 |
| Add up to | 100.0 | 100.0 | |
| Liquefied gas+gasoline+diesel oil, wt% | 64.0 | 81.5 | 17.5 |
Annotate: with the device inlet amount is 100% calculating.
Table 4 catalytically cracked gasoline main products character
| Product | Comparative Examples | Embodiment |
| Density (20 ℃), g/cm 3 | 0.7402 | 0.7421 |
| S，μg/g | 38.6 | 30.2 |
| RON | 91.8 | 93.1 |
Claims (11)
1. residual hydrocracking and catalytic cracking combination process; Wherein riser reactor is adopted in catalytic cracking; Described riser reactor is provided with the two-stage opening for feed; Wherein first step opening for feed is arranged on the bottom of riser tube, and second stage opening for feed is above first step opening for feed, and the boiling bed residual oil hydroprocessing technique is adopted in residual hydrocracking; This method comprises: residual oil raw material gets into the boiling bed hydrogenation treatment reactor; In the presence of hydrogen and hydrotreating catalyst, carry out hydrogenation reaction; Hydrogenation reaction effluent gas-liquid separation, liquid phase fractionate out light constituent and heavy constituent, and wherein the cut point of light constituent and heavy constituent is 320～380 ℃; Light constituent gets into reactor drum as the charging of the catalytic cracking riser reactor first step by first step opening for feed; Heavy constituent get into separation column by the bottom of catalytic cracking fractionating tower; Heavy constituent get into the entry position of catalytic cracking fractionating tower above catalytic cracking reaction elute entering catalytic cracking fractionating tower entry position; Heavy constituent and catalytic cracking reaction elute are isolated dry gas, liquefied gas, gasoline fraction, diesel oil distillate, recycle stock and slurry oil through fractionation, and wherein recycle stock is as the charging of the catalytic cracking riser reactor second stage; Get into reactor drum by second stage opening for feed, carry out catalytic cracking reaction.
2. according to the described method of claim 1, it is characterized in that described slurry oil is as the delayed coking feed component.
3. according to the described method of claim 1, it is characterized in that riser tube second stage opening for feed is arranged on the top of first step opening for feed, account for 1/30～1/5 of whole riser tube height apart from the distance of first step opening for feed.
4. according to the described method of claim 1, it is characterized in that riser tube second stage opening for feed is arranged on the top of first step opening for feed, account for 1/10～1/6 of whole riser tube height apart from the distance of first step opening for feed.
5. according to the described method of claim 1, it is characterized in that described residual oil raw material is long residuum or vacuum residuum.
6. according to the described method of claim 5, it is characterized in that, also contain in wax tailings, deasphalted oil, the heavy distillate one or several in the residual oil raw material.
7. according to the described method of claim 5; It is characterized in that; The boiling bed hydrogenation catalyst that described boiling bed residual oil hydroprocessing technique adopts, carrier are that in aluminum oxide, silicon oxide, aluminium oxide-silicon oxide or the titanium oxide one or more are formed, and are benchmark with the weight of catalyzer; Nickel oxide or powder blue are 1%～20%, and molybdenum oxide or Tungsten oxide 99.999 are 1%～30%; Catalyst property is following: bulk density is 0.4～0.9g/cm
3, particle diameter is 0.08～1.2mm, specific surface area is 100～300m
2/ g.
8. according to claim 1 or 7 described methods, it is characterized in that the operational condition that boiling bed hydrogenation is handled is: reaction pressure 6～30MPa, 400～490 ℃ of temperature of reaction, volume space velocity 0.1～5.0h during liquid
-1, hydrogen to oil volume ratio 200～2000.
9. according to claim 1 or 7 described methods, it is characterized in that the operational condition that boiling bed hydrogenation is handled is: reaction pressure 15～20MPa, 420～470 ℃ of temperature of reaction, volume space velocity 0.5～2.0h during liquid
-1Hydrogen to oil volume ratio 400～1000.
10. according to the described method of claim 1, it is characterized in that the CCU operational condition is: temperature of reaction is 450～600 ℃; Regeneration temperature is 600～800 ℃; Agent weight of oil ratio is 2～30, with 0.1～15.0 second duration of contact of catalyzer, and pressure 0.1～0.5MPa.
11., it is characterized in that the CCU operational condition is according to the described method of claim 1: temperature of reaction is 480～550 ℃; Regeneration temperature is 650～750 ℃; Agent weight of oil ratio is 4～10, with catalyzer duration of contact be 0.5～5.0 second, pressure 0.1～0.5MPa.
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