CN101875855B - Method for hydrogenation and catalytic cracking of residual oil - Google Patents
Method for hydrogenation and catalytic cracking of residual oil Download PDFInfo
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- CN101875855B CN101875855B CN 200910207372 CN200910207372A CN101875855B CN 101875855 B CN101875855 B CN 101875855B CN 200910207372 CN200910207372 CN 200910207372 CN 200910207372 A CN200910207372 A CN 200910207372A CN 101875855 B CN101875855 B CN 101875855B
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Abstract
The invention discloses a method for the hydrogenation and catalytic cracking of residual oil. In the method, the hydrogenation of a residual oil raw material is performed in the presence of hydrogen and a hydrogenation catalyst; the effluent of the hydrogenation is subjected to gas-liquid separation; a gas phase is circularly used for hydrogenation; a liquid phase directly enters a catalytic cracking device without fractionation; and dry gases, liquefied gases and the catalytic cracking heavy fraction obtained after the catalytic cracking of gasoline are separated from the effluent of the catalytic cracking reaction and mixed with a hydrogenating raw material to undergo hydrogenation. Compared with the prior art, the method can produce gasoline with a maximum yield and can save equipment investment, make full use of reaction heat energy and reduce production energy consumption at the same time.
Description
Technical field
The present invention relates to a kind of residual oil weight-lightening method, specifically with residual hydrocracking and catalytic cracking organic assembling, mainly produce the processing method of gasoline products take residual oil as raw material.
Background technology
Along with crude oil day by day becomes heavy, becomes bad, increasing residual oil needs processing treatment.Processing treatment heavy, residual oil will be not lower boiling product with its cracking still, such as petroleum naphtha, intermediate oil and pressure reduction gas wet goods, but also will improve their hydrogen-carbon ratio, and this just need to realize by the method for decarburization or hydrogenation.Wherein decarbonization process comprises coking, solvent deasphalting, heavy oil fluid catalytic cracking etc.; Hydrogenation comprises hydrocracking, hydrofining etc.Hydrogenation method can hydrocracking residual oil, improves the productive rate of liquid product, and can also remove heteroatoms wherein, and quality product is not bad.But hydrogenation method is the catalysis complete processing, has hydrogenation catalyst inactivation problem, and when especially processing poor quality, heavier hydrocarbon feeds, Catalysts Deactivation Problems is more serious.At present, in order to reduce the cost of heavy, poor residuum processing, increase the oil refining enterprise profit, the technique of processing heavy, poor residuum is still take decarbonization process as main, but its poor product quality need to be carried out aftertreatment and could be utilized, wherein deasphalted oil and wax tailings cut especially need to carry out hydrotreatment, could continue to use the lighting devices such as catalytic cracking or hydrocracking 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 the devices such as catalytic cracking or coking.By 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 catalytic cracking unit, therefore at present in heavy, the residual hydrogenation modifying process technology take residue fixed-bed hydrotreatment and catalytic cracking combination technique as mainstream 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, hydrogenation tail oil is as the heavy oil fluid catalytic cracking charging, carry out catalytic cracking reaction, product is dry gas, liquefied gas, gasoline, diesel oil and coke, recycle stock carry out the catalysis freshening or with loop back residual hydrogenation equipment and mix with the residual hydrocracking raw material and carry out hydrotreatment, catalytic slurry gets rid of outward or partially catalyzed 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 large, the unfavorable factors such as facility investment height.
US4,713,221 disclose on the residual hydrogenation of routine and catalytic cracking combined basis, and the heavy cycle oil of catalytic cracking is circulated to residual hydrogenation equipment, and carry out hydrogenation after residual oil mixes, and enter catalytic cracking unit again.But catalytically cracked oil is not utilized effectively, and the method is limited to reduction coke yield, raising product yield.
CN1119397C discloses a kind of hydrogenation and catalystic cracking combined process for residual oil, in the method, residual oil and clarified oil enter residual hydrogenation equipment together, react in the presence of hydrogen and hydrogenation catalyst, and heavy cycle oil circulates in catalytic cracking unit inside; The slurry oil of reaction gained obtains clarified oil through the separator separation, is back to hydrogenation unit.But slurry oil enters the residual hydrocracking device, and the easy green coke thing in the slurry oil will increase the carbon deposit of hydrogenation catalyst, has reduced hydrogenation activity and the operational cycle of hydrogenation catalyst, and heavy cycle oil is inner in catalytic cracking unit.Therefore, this method is limited to reducing coke yield, improving the quality of products.
CN1382776A discloses the method for a kind of residual hydrocracking and catalytically cracking heavy oil, and the method is carried out hydrogenation reaction with residual oil at hydrotreater, and reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenated residue.The hydrogenated residue of gained enters catalytic cracking unit with optional vacuum gas oil and carries out cracking reaction, and the heavy cycle oil of catalytic cracking returns hydrotreater, and the thing that steams that the distillation slurry oil obtains returns hydrotreater.The method is organically joined together two devices, residual oil, heavy cycle oil and slurry oil can be converted into light-end products.But the method all arranges fractionating system in hydrotreatment and catalytic cracking process, increased investment cost; Because the process heat exchange, heat-energy losses is more; Simultaneously, hydrotreater and catalytic cracking unit have diesel product, and comparatively speaking, the total recovery of gasoline and gas products will reduce.In addition, the slag oil cracking rate of residual hydrocracking device is lower, and it is limited that hydrogenated oil carries out petroleum naphtha, diesel yield that fractionation obtains, and the diesel oil distillate that the residual hydrocracking process obtains still can not satisfy the requirement of high-quality diesel product.The foreign matter contents such as catalytic cracking diesel oil sulphur are higher, and character is relatively poor, also needs further hydrotreatment just to can be used as qualified diesel product.
In residual hydrocracking and the catalytic cracking combined technique, the energy consumption of fractionation plant accounts for larger ratio, and the energy consumption that how to reduce fractionation plant also is the content that needs emphasis to consider.
Summary of the invention
For the deficiencies in the prior art, the invention provides a kind of residual hydrocracking and catalytic cracking combination method, can maximum produce gasoline products, technological process is simple simultaneously, whole Energy Intensity Reduction.
Residual hydrocracking of the present invention and catalytic cracking combination method comprise: residual oil raw material carries out hydrogenation reaction in the presence of hydrogen and hydrotreating catalyst, the hydrogenation reaction effluent gas-liquid separation, gas phase is cycled to used in hydrogenation reaction, liquid phase directly enters catalytic cracking unit without fractionation, and the catalytic cracking reaction effluent is isolated catalytic cracking last running behind dry gas, liquefied gas and the catalytically cracked gasoline and mixed with residual oil raw material and carry out hydrogenation reaction.
In the inventive method, residual oil raw material comprises long residuum or vacuum residuum, can be the residual oil raw material in other source also, also can contain simultaneously in the residual oil raw material among a kind of or several in part wax tailings, deasphalted oil, the heavy distillate.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, through being cycled to used in hydrogenation reaction after the selectable depriving hydrogen sulphide processing, hydrogenation process needs to replenish new hydrogen simultaneously with the consumption of postreaction process.The liquid phase that obtains after the hydrogenation reaction effluent gas-liquid separation enters light pressure separator, then directly enters catalytic cracking unit, and light pressure separator can flash off the hydrogen sulfide of a small amount of light hydrocarbons and dissolving and hydrogen etc.
The residual hydrogenation technology can be any technology of the present invention that is applicable to, such as fixed bed residual hydrocracking technology, suspension bed residual oil hydrogenation treatment technology, boiling bed residual oil hydrotreatment technology, moving-bed residual hydrocracking technology etc.Take present industrial ripe fixed bed residual hydrocracking technology as example, single catalyst or the combination catalyst of the functions such as the catalyst for hydrotreatment of residual oil of employing refers to have residuum hydrogenating and metal-eliminating, hydrogenating desulfurization, hydrodenitrification and hydrocracking.These catalyzer generally all are as carrier take porous refractory inorganic oxides such as aluminum oxide, the oxide compound of group vib and/or VIII family metal such as W, Mo, Co, Ni etc. is active ingredient, the catalyzer that optionally adds other various auxiliary agents such as P, Si, the elements such as F, B, CEN, the FZC that is for example produced by catalyzer branch office of Sinopec Group, ZTN, ZTS series residual oil hydrocatalyst, ZTN, the ZTS catalyst series produced by Qilu Petrochemical Company the first fertilizer plant just belong to this class catalyzer.At present in fixed bed residual hydrogenation technology; often be that multiple catalysts supports the use; protective material, Hydrodemetalation catalyst, Hydrobon catalyst, hydrodenitrogenation catalyst are wherein arranged, and the filling order generally is that stock oil is contacted with protective material, hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrogenation catalyst successively.Technology with these several catalyst mix fillings is also arranged certainly.The a plurality of reactors of hydrotreatment operated by rotary motion are to improve amount of finish.Be 5MPa-35MPa in absolute pressure normally, preferably 10MPa-20MPa, temperature are 300 ℃-500 ℃, preferably 350 ℃-450 ℃ lower operations.Volume space velocity and hydrogen dividing potential drop are to select according to the characteristic for the treatment of material and transformation efficiency and the refining depth of requirement during liquid.Volume space velocity is generally at 0.1h during fresh residual oil raw material liquid
-1-5.0h
-1, 0.15h preferably
-1-2.0h
-1Scope in, total hydrogen to oil volume ratio is 100-5000, is preferably 300-3000.The present invention is applicable to normal pressure and vacuum residuum hydrotreatment, is particularly useful for the hydrocracking of heavy hydrocarbon oil.The actual conditions of residual hydrocracking process can specifically be determined according to the requirement of raw material properties and catalytic cracking unit charging.
In the inventive method, catalytic cracking can be adopted this area routine techniques.Catalytic cracking unit can be that every covering device should comprise a reactor, a revivifier at least more than a cover or overlapped.Catalytic cracking unit arranges separation column, can every cover catalytic cracking unit set respectively, also can share.Catalytic cracking fractionating tower is dry gas, liquefied gas, catalytically cracked gasoline and catalytic cracking last running with the fractionation of catalytic cracking reaction effluent.Catalytic cracking fractionating tower is compared with conventional catalytic cracking fractionating tower can simplified design, only fractionates out dry gas, liquefied gas and catalytically cracked gasoline, and catalytic cracking last running comprises catalytic cracking diesel oil, heavy catalytic cycle oil and slurry oil.Catalytic cracking last running filters out first the micro-catalytic cracking catalyst powder that contains before looping back hydrotreater.
Catalytic cracking unit operates 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 second duration of contact of catalyzer, best 0.5～5 second; Pressure 0.1～0.5MPa.The catalytic cracking catalyst that adopts comprises the catalyzer that is generally used for catalytic cracking, such as 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 the active height of molecular sieve cracking catalyst, green coke is few, gasoline yield is high, and transformation efficiency is high.The reactor of described catalytic cracking unit can be the catalyst cracker of various types, and preferably riser reactor or riser tube add the bed reactor.Technical process is generally: stock oil injects from the riser reactor bottom, contact with the 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, finish the catalytic cracking reaction of whole stock oil.
The concrete operations condition of residual hydrocracking and catalytic cracking can be obtained by simple experiment according to feedstock property and product quality indicator by the technician.
The invention has the advantages that:
1, in whole combination process, main products is high octane number catalytic cracking gasoline, liquefied petroleum gas (LPG) and a small amount of dry gas, thereby can guarantee that maximum ground produces gasoline.The aromatic hydrocarbon from catalytic cracking diesel oil content that existing scheme obtains is high, and cetane value is low, and the foreign matter contents such as sulphur are high, and character is poor, also needs further hydrotreatment just to can be used as qualified diesel product.The fractionating system of catalytic cracking reaction effluent is not carried out the separation of catalytic cracking diesel oil cut among the present invention, saves the repetition procedure of processing.Simultaneously, the catalytic cracking fractionating system can be simplified greatly, reduces facility investment and operation energy consumption.
2, the catalytic cracking reaction effluent is not isolated catalytically cracked oil, has solved slurry oil goes out catalyst solid powder because viscosity is very much not easily separated problem.Contain diesel oil distillate in the catalytic cracking heavy distillate, because the diluting effect of diesel oil distillate, the cycle oil slurry viscosity significantly reduces, and is more prone to so that catalyst solid powder wherein filters.When conventional catalytically cracked oil separated, although can part utilize by clarification, utilization ratio was lower, and the inventive method does not produce and effluxes part owing to do not isolate catalytically cracked oil, has improved the utilization ratio of raw material and the yield of purpose product.
3, from whole combination process, need not establish fractionating system in the hydrotreater, hydrotreatment generates oil and directly enters catalyst cracker, need not establish fresh feed pump, has reduced simultaneously a large amount of heat-exchange equipments.The fractionating system of catalytic cracking reaction effluent only fractionates out the light-end productss such as gasoline fraction, and the required theoretical separation tray number of separation column reduces greatly.More than several aspects facility investment is greatly reduced.
4, catalytic cracking last running is played diluting effect to fresh residual oil raw material, and oil property improves, and has reduced hydrogenation reaction difficulty and the processing severity of residual hydrocracking parallel feeding; In addition, catalytic cracking last running can reduce the viscosity of raw material, improves flow distribution and the mass transfer of raw material in reactive system, reduces to be diffused in the impact in the residual hydrocracking process, improve the deposition distribution of poisonous metal in catalytic reaction system such as nickel, vanadium, the work-ing life of extending catalyst; Simultaneously, the reduction of viscosity is more prone to the conveying of mixing raw material oil and filtration.
5, catalytic cracking diesel oil cut and above last running can be in the Residue Hydrotreating Technology process imurity-removal, aromatic saturation becomes better catalytically cracked material and forms, and has further improved catalytic cracking high value added product yield.
6, because hydrotreater is not established fractionating system, hydrogenated oil directly enters catalyst cracker, catalytic cracking generates oil after isolating gas products and catalytic gasoline, the residue mixing oil loops back hydrogenation unit after filtering, above-mentioned two processes greatly reduce the loss of heat, greatly reduce simultaneously the required energy of fractionation process, thereby reduced the energy consumption of whole technological process.
Description of drawings
Fig. 1 is residual hydrocracking of the present invention and catalytic cracking combination method process flow diagram.
Embodiment
Below in conjunction with accompanying drawing method provided by the present invention is further detailed, but does not therefore limit the present invention.
Technical process is described in detail as follows:
Catalytic cracking last running 17 after residual oil raw material 1 and the filtration mixes, boost after and recycle hydrogen 2 be mixed into hydrotreating reactor 3, by contacting with the hydrotreating catalyst bed, remove the impurity such as metal in the stock oil, sulphur, nitrogen, the carbon residue that reduces simultaneously raw material satisfies the charging requirement of downstream catalytic cracking unit.Hydrotreating reactor 3 outlet reaction effluents 4 enter high-pressure separator 5 and carry out gas-liquid separation, the gaseous stream that sub-argument goes out carries out being recycled to the hydrotreating reactor entrance after the laggard recycle compressors 8 of processing such as depriving hydrogen sulphide boost, the new hydrogen that replenishes also can be introduced after recycle compressor 8, isolated liquid phase stream arrives light pressure separator 6 more further to be separated, isolated liquid phase stream is without heat exchange and fractionation, adjust the pressure of light pressure separator, make liquid phase stream in the situation of not using feedstock pump, enter the reactive system 9 of catalytic cracking unit by pipeline 7.
Enter the reactive system 9 of catalytic cracking unit from the hydrogenated oil of pipeline 7, contact with the high temperature regeneration catalytic cracking catalyst and react, reacted oil gas logistics 10 enters the separation column 13 of catalytic unit, isolate gas 11 and catalytically cracked gasoline 12, gas 11 and catalytically cracked gasoline 12 dischargers, the remaining catalytic cracking last running 14 of separation column enters separator 15, the catalyst fines that filters out, mechanical impurity and solid particulate 16, the catalytic cracking last running 17 after the filtration is recycled to hydrotreater.
The following examples will further specify method provided by the invention, but not thereby limiting the invention.Reaction is to carry out in small riser formula catalytic cracking unit and pilot scale residual hydrocracking device.Used stock oil is normal 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; all are CEN, FZC, ZTN, ZTS series residual oil hydrocatalysts that catalyzer branch office of Sinopec Group produces; specifically comprise protective material; catalyst for demetalation; desulfurization catalyst; denitrification catalyst etc.; the filling order generally is that stock oil is contacted with protective material, hydrodemetallation (HDM), hydrogenating desulfurization, hydrodenitrogenation catalyst successively, and the technology with these several catalyst mix fillings is also arranged certainly.The technology contents that above-mentioned catalyst loading technology is well known to those skilled in the art.Catalytic cracking catalyst used in embodiment and the Comparative Examples is identical, is the catalyzer that 3,500,000 ton/years of heavy oil catalytically cracking equipments of Dalian Company use, and is industrial equilibrium catalyst.Its fresh dose consists of: 95wt%LBO-16 olefine lowering catalyst+5wt%LBO-A improves octane enhancing additive.
Comparative Examples
This Comparative Examples adopts conventional residual hydrocracking-catalyst cracking method, and namely residual oil carries out hydrogenation reaction at hydrotreater, and reaction product isolated obtains gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenated residue.The hydrogenated residue of gained enters catalytic cracking unit and carries out cracking reaction, and heavy catalytic cycle oil is processed at the catalytic cracking unit internal recycle.Table 2, table 3, table 4 are respectively processing condition, product distributes and main products character.
Embodiment
This embodiment adopts residual hydrocracking provided by the invention and catalytic cracking combination method, all liquid products of hydrotreatment directly enter catalytic cracking unit without fractionation, catalytic cracking reaction effluent fractionating system simplified design, only fractionate out dry gas, liquefied gas and gasoline fraction, catalytic cracking diesel oil, catalytic cracking turning oil and catalytic slurry do not carry out fractionation directly as catalytic cracking last running, and catalytic cracking last running is circulated to further processing in the hydrotreater after leaching solid impurity.Table 2, table 3, table 5 are respectively processing condition, product distributes and main products character.
Comparing result shows that after catalytic cracking heavy distillate and the processing of fresh residual oil raw material mixed hydrogenation, the catalytically cracked gasoline yield increases by 22.49 percentage points, and liquefied gas yield has increased by 9.23 percentage points, and coke yield descends to some extent, and the dry gas yield slightly increases.The inventive method can satisfy the enterprise that wishes increasing gasoline yield well.
Table 1 stock oil character
| Project | Data |
| S, quality % | 2.33 |
| N，μg/g | 3044 |
| Carbon residue (CCR), quality % | 11.8 |
| Density (20 ℃), kg/m 3 | 982.0 |
| Viscosity (100 ℃), mm 2/s | 98.0 |
| Ni+V，μg/g | 75.62 |
Table 2 hydrotreatment and catalytic cracking process condition
| Title | Comparative Examples | Embodiment |
| The hydroprocessing technique condition | ||
| Raw material | Fresh feed | Fresh feed+catalytic cracking last running |
| The hydrogen dividing potential drop, MPa | 14.0 | 14.0 |
| Temperature of reaction, ℃ | 385 | 385 |
| Volume space velocity ●，h -1 | 0.20 | 0.27 |
| Hydrogen-oil ratio | 600 | 600 |
| The catalytic cracking process condition | ||
| Raw material | The normal slag of hydrogenation | The mixing oil hydrogenated oil |
| Temperature of reaction, ℃ | 505 | 505 |
| Agent-oil ratio | 7.5 | 7.5 |
● calculate with the device inlet amount.The inlet amount of fresh feed is identical with Comparative Examples among the embodiment.
Table 3 product distributes
| Title | Comparative Examples | Embodiment |
| The hydrotreatment product distributes ●: quality % | ||
| Chemical hydrogen consumption | 1.20 | 1.43 |
| Gas | 2.54 | 2.76 |
| Petroleum naphtha | 1.14 | 2.32 |
| Diesel oil | 5.25 | |
| Hydrogenation tail oil | 92.27 | 96.35 |
| The catalytic cracking product distributes ●: quality % | ||
| Dry gas | 1.91 | 2.12 |
| Liquefied gas | 15.54 | 24.52 |
| Gasoline | 46.94 | 67.25 |
| Diesel oil | 19.40 | |
| Slurry oil | 7.47 | |
| Coke | 8.74 | 6.11 |
| Two covering devices add up to ●●, quality % | ||
| Chemical hydrogen consumption | 1.20 | 1.43 |
| Dry gas | 4.14 | 4.71 |
| Liquefied gas | 14.44 | 23.67 |
| Gasoline (comprising hydrotreated naphtha) | 44.67 | 67.16 |
| Diesel oil | 22.90 | - |
| Slurry oil | 6.94 | - |
| Coke | 8.11 | 5.89 |
● take the device inlet amount as 100% calculating, ● ● take fresh feed as 100% calculating.
The conventional hydrogenation and catalystic cracking main products of table 4 character
●
● the normal slag of hydrogenation, heavy catalytic cycle oil are intermediates in the present invention
Table 5 main products character of the present invention
| Product | Catalytically cracked gasoline |
| Density (20 ℃), g/cm 3 | 0.7400 |
| S，μg/g | 29.5 |
| RON | 91.9 |
Claims (10)
1. a residual hydrocracking and catalytic cracking combination method, it is characterized in that: residual oil raw material carries out hydrogenation reaction in the presence of hydrogen and hydrotreating catalyst, the hydrogenation reaction effluent gas-liquid separation, gas phase is cycled to used in hydrogenation reaction, liquid phase directly enters catalytic cracking unit without fractionation, and the catalytic cracking reaction effluent is isolated catalytic cracking last running behind dry gas, liquefied gas and the catalytically cracked gasoline and mixed with residual oil raw material and carry out hydrogenation reaction.
2. it is characterized in that in accordance with the method for claim 1: residual oil raw material comprises long residuum or vacuum residuum.
3. it is characterized in that in accordance with the method for claim 1: the residual oil raw material hydrogenation adopts fixed bed residual hydrocracking technology, suspension bed residual oil hydrogenation treatment technology, boiling bed residual oil hydrotreatment technology or moving-bed residual hydrocracking technology.
4. according to claim 1 or 3 described methods, it is characterized in that: residual oil raw material hydrogenation process condition is: absolute pressure is 5MPa-35MPa, and temperature is 300 ℃-500 ℃, and volume space velocity is 0.1h during fresh liquid
-1-5.0h
-1, total hydrogen to oil volume ratio is 100-5000.
5. according to claim 1 or 3 described methods, it is characterized in that: residual oil raw material hydrogenation process condition is: absolute pressure is 10MPa-20MPa, and temperature is that volume space velocity is 0.15h during fresh liquid under 350 ℃-450 ℃
-1-2.0h
-1, total hydrogen to oil volume ratio is 300-3000.
6. in accordance with the method for claim 1, it is characterized in that: catalytic cracking unit is that every cover catalytic cracking unit should comprise a reactor and a revivifier at least more than a cover or overlapped.
7. in accordance with the method for claim 6, it is characterized in that: catalytic cracking unit arranges separation column, and catalytic cracking fractionating tower is dry gas, liquefied gas, catalytically cracked gasoline and catalytic cracking last running with the fractionation of catalytic cracking reaction effluent.
8. according to claim 1 or 7 described methods, it is characterized in that: catalytic cracking last running filters out first the micro-catalytic cracking catalyst powder that contains before looping back hydrotreater.
9. according to claim 1 or 6 described methods, it is characterized in that: the catalytic cracking unit operational condition is: temperature of reaction is 450～600 ℃, and regeneration temperature is 600-800 ℃, and the agent weight of oil is than 2～30, with 0.1～15 second duration of contact of catalyzer, pressure 0.1～0.5MPa.
10. in accordance with the method for claim 1, it is characterized in that: the catalytic cracking unit operational condition is: temperature of reaction is 480～550 ℃, and regeneration temperature is 650-750 ℃, and the agent weight of oil is than 4～10, with 0.5～5 second duration of contact of catalyzer.
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| CN102732314A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking combined method for residuum |
| CN102732312A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
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| CN102732315A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking deeply-combined method for residuum |
| CN102732311A (en) * | 2011-04-15 | 2012-10-17 | 中国石油化工股份有限公司 | Hydrotreatment and catalytic cracking combined method for residuum |
| WO2012142723A1 (en) * | 2011-04-19 | 2012-10-26 | 中国石油化工股份有限公司 | Combined method for hydrogenation and catalytic cracking of residual oil |
| CN102863987A (en) * | 2011-07-07 | 2013-01-09 | 中国石油化工股份有限公司 | Hydrocarbon oil pretreatment and catalytic cracking combined technology |
| CN103059915B (en) * | 2011-10-21 | 2015-04-29 | 中国石油化工股份有限公司 | Poor-quality heavy oil hydro-upgrading method |
| CN103059960B (en) * | 2011-10-21 | 2014-12-31 | 中国石油化工股份有限公司 | Flexible hydrocracking method |
| CN103102985B (en) * | 2011-11-10 | 2015-06-17 | 中国石油化工股份有限公司 | Combined process of hydrotreatment and catalytic cracking for residual oil |
| CN103102981B (en) * | 2011-11-10 | 2015-10-21 | 中国石油化工股份有限公司 | A kind of working method of heavy feed stock |
| CN103131469B (en) * | 2011-11-25 | 2015-05-13 | 中国石油天然气股份有限公司 | Fixed bed residue oil hydrotreating method |
| CN103381366A (en) * | 2012-05-04 | 2013-11-06 | 中国石油天然气股份有限公司 | Good-hydrothermal-stability hydrodeoxygenation catalyst, and preparation and application thereof |
| CN113046125B (en) * | 2019-12-26 | 2023-07-04 | 中国石油化工股份有限公司 | Method for producing gasoline and low-sulfur ship combustion |
| CN113046128B (en) * | 2019-12-26 | 2023-07-04 | 中国石油化工股份有限公司 | Production method of gasoline and low-sulfur marine fuel |
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