CN104560184B - A kind of catalysis conversion method of voluminous gasoline - Google Patents

A kind of catalysis conversion method of voluminous gasoline Download PDF

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Publication number
CN104560184B
CN104560184B CN201310516479.XA CN201310516479A CN104560184B CN 104560184 B CN104560184 B CN 104560184B CN 201310516479 A CN201310516479 A CN 201310516479A CN 104560184 B CN104560184 B CN 104560184B
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catalytic cracking
reaction
hydrogenation
heavy
oil
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CN104560184A (en
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龚剑洪
毛安国
崔守业
唐津莲
张毓莹
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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Sinopec Research Institute of Petroleum Processing
China Petroleum and Chemical Corp
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4012—Pressure
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/70—Catalyst aspects

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

A kind of catalysis conversion method of voluminous gasoline, catalytic cracking light cycle oil obtains light fraction and heavy distillat through cutting, wherein heavy distillat obtains hydrogenation heavy distillat through hydrotreatment, light fraction, hydrogenation heavy distillat enter respectively separately different FCC riser, under catalytic cracking catalyst exists, carry out cracking reaction, reaction product isolated obtains comprising the product of gasoline, light cycle oil. The method adopts the two single cover catalytic cracking units that overlap catalytic cracking unit independently or have a duo-lift tube reactor to process respectively the heavy distillat after light fraction and the hydrogenation of light cycle oil, can be by adopting different operating parameters, optimize and meet the required harsh conditions of light cycle oil different fractions catalytic cracking reaction to greatest extent, thereby farthest produce catalytic gasoline.

Description

A kind of catalysis conversion method of voluminous gasoline
Technical field
The invention belongs to the catalysis conversion method of petroleum hydrocarbon in the situation that not there is not hydrogen, more specificallySaying, is a kind of catalysis conversion method that is maximized the gasoline of producing by catalytic cracking light cycle oil.
Background technology
Along with the development of crude oil heaviness and the rapid growth of market to light-end products demand, in China, doFor the catalytic cracking technology of heavy oil lighting is rapidly developed. But, a fact must facingThe quality that is catalytic cracking diesel oil (or title " light cycle oil ") is but always relatively poor, and density is large, virtueHydrocarbon content is high, and Cetane number is low, even be also difficult to reach increasingly stringent by diesel oil hydrogenation modification technologyDiesel oil regulation. How solving catalytic cracking light cycle oil is an increasingly serious problem. Deposit simultaneouslyAnother one problem be domestic gasoline product chronic shortage, and catalytically cracked gasoline accounts for gasoline product80%. Therefore, how to realize heavy charge by catalytic cracking process and maximize production higher octaneValue gasoline and not produce light cycle oil may be the new way addressing the above problem.
US4585545 has disclosed one full catalytic cracking light cycle oil cut has first been carried out to hydrotreatment,The hydrogenated diesel oil obtaining goes catalytic cracking to produce the catalysis conversion method that is rich in mononuclear aromatics gasoline again.
CN1422327A discloses a kind of method of catalytic cracking light cycle oil upgrading, is by with heavyThe light cycle oil that the first catalytic cracking unit that oil is raw material is produced carries out deep hydrogenation, the hydrogenation obtainingRecycle oil enters the second catalytic cracking unit again. On the basis of the method, CN1423689A emphasizesCatalyst in two catalytic cracking units requires the aperture of selecting shape zeolite and about 5-50% containing 50-95%Be more than or equal to the large pore zeolite of about 0.7nm, optionally to improve light olefin productive rate.
CN1466619A discloses a kind of method for transformation of catalytic cracking light cycle oil, is that catalysis is splitChange riser reactor and be divided into two of upstream and downstream reaction zone, wherein mink cell focus injects catchment, itsThe hydrogenation recycle oil that catalytic cracking production light cycle oil obtains after hydrotreatment injects upstream. At thisOn the basis of method, the charging in CN1425054A method middle and lower reaches district is except hydrogenation recycle oil, alsoIncrease naphtha. In the method, not only hydrogen consumption is high, and hydrogenation recycle oil can be tight in upstream reactionGhost image rings the conversion of the mink cell focus in downstream.
Can find from disclosed document above, that processes for catalytic cracking light cycle oil is importantOne of approach is that it is first carried out to hydrotreatment, and then catalytic cracking. It must be noted that, gently followTherefore how no matter whether hydrogenation of ring oil, compares with the large molecule of mink cell focus, and its molecule is little, bond energy is large,The operating parameter of controlling catalytic cracking is one of key of light cycle oil processing. In addition, light cycle oil asFruit carries out hydrogenation, and the operation control of hydrogenation process is also one of key of light cycle oil processing.
Summary of the invention
The object of the invention is to provide on the basis of existing technology a kind of catalyzed conversion of voluminous gasolineMethod.
Catalysis conversion method provided by the invention comprises:
(1) catalytic cracking light cycle oil obtains light fraction and heavy distillat through cutting;
(2) the described heavy distillat of step (1) is carried out hydrogenation under hydrogen and hydrotreating catalyst existenceProcessing reaction, reaction product isolated obtains hydrogenation heavy distillat;
(3) the described light fraction of step (1), the described hydrogenation heavy distillat of step (2) are entered respectively separatelyEnter different FCC riser, under catalytic cracking catalyst exists, carry out catalysisCracking reaction, separate catalytic cracking catalyst to be generated and reaction oil gas, and wherein reaction oil gas is through separatingTo the product that comprises gasoline, light cycle oil.
Preferably the method also comprises: the described catalytic cracking catalyst to be generated of step (3) through stripping, againRaw rear gained regeneration catalyzing Cracking catalyst is returned to riser reactor and is recycled.
The described catalytic cracking light cycle oil of step (1) is selected from allocatalysis cracking unit and produces light circulationOil is or/and this method catalytic cracking unit step (3) light cycle oil that produces, preferably allocatalysis crackingDevice the light cycle oil that produces and this method catalytic cracking unit step (3) light cycle oil that produces.
Method provided by the invention is specific as follows:
Catalytic cracking light cycle oil enters independent fractionating column and cuts, and cutting temperature is controlled at250～260 DEG C, preferably cutting temperature is 260 DEG C, obtains respectively not high from top and the bottom of fractionating columnIn the light fraction of this cutting temperature with higher than the heavy distillat of this cutting temperature.
Hydrotreater is removed in described heavy distillat, under hydrogen and hydrogenation catalyst existence, carries out hydrogenation placeReason reaction, hydroprocessing condition is: hydrogen dividing potential drop 10.0～25.0MPa, preferably 10.0～22.0MPa;330～450 DEG C of reaction temperatures, preferably 340～380 DEG C; Volume space velocity 0.1～2.0 hour-1, hydrogen oil bodyLong-pending than 1000～2000Nm3/m3. Reaction product isolated obtains 260 DEG C of 250 DEG C of preferred >'s of initial boiling point >Cut, or claim hydrogenated diesel oil, hydrogenation heavy distillat. In described hydrogenation heavy distillat double ring arene content want≤10 heavy %, the heavy % in preferably≤8.
Described activity of hydrocatalyst metal component be selected from group vib metal and/or group VIII non-Noble metal, carrier is selected from aluminium oxide, silica, amorphous aluminum silicide any one or several. DescribedGroup vib metal is molybdenum or/and tungsten, and group VIII base metal is that nickel is or/and cobalt. Active metal groupDivide the combination of preferred nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum.
Light fraction and the hydrogenation heavy distillat obtaining enter separately respectively different catalytic cracking units and promotePipe reactor carries out cracking reaction under catalytic cracking catalyst exists, and reaction product isolated is doneGas, liquefied gas, gasoline, light cycle oil, slurry oil, coke. What catalytic cracking unit produced is new lightRecycle oil goes independent fractionating column cutting, cycling.
Described light fraction and hydrogenation heavy distillat enter separately respectively different catalytic cracking unit risersReactor, can refer to two to overlap independently catalytic cracking unit, also can singly overlap catalytic cracking unit and haveParallel independently duo-lift tube reactor. Described riser reactor is isometrical riser reactor or changeFootpath riser reactor.
The concrete operations condition of catalytic cracking unit is as follows:
For the riser reactor of light cycle oil light fraction charging, reaction temperature is 540～660 DEG C,Preferably 560～620 DEG C; Agent oil quality is than 10～100, and preferably 15～50; Oil gas time of staying 1-10 second,Preferably 2～8 seconds; Pressure (absolute pressure) 0.15～0.4MPa; The weight ratio of water vapour and raw material is0.01～0.5 preferably 0.02～0.2.
For the riser reactor of light cycle oil hydrogenation heavy distillat charging, reaction temperature is530～650 DEG C, preferably 550～600 DEG C; Agent oil quality is than 5～80, and preferably 8～40; When oil gas stopsBetween 1-10 second, preferably 2～8 seconds; Pressure (absolute pressure) 0.15～0.4MPa; Water vapour and raw materialWeight ratio be 0.01～0.5 preferably 0.02～0.2.
For single cover catalytic cracking unit with parallel independently duo-lift tube reactor, device balanceAgent activity (MAT) >=65, preferably >=68.
Enter respectively two for light fraction and hydrogenation heavy distillat and overlap independently catalytic cracking unit, forLight fraction is the device of raw material, poising agent activity (MAT) >=62, preferably >=65; For with hydrogenationDouble distilled is divided into the device of raw material, poising agent activity (MAT) >=65, preferably >=68.
Duo-lift tube reactor can share a set of settler, main fractionating tower, absorbing-stabilizing system, vapourCarry device, regenerator, also can use settler, main fractionating tower, absorbing-stabilizing system, stripping separatelyDevice, regenerator.
Catalytic cracking catalyst comprises zeolite, inorganic oxide and optional clay. The content of each componentBe respectively: the heavy % of zeolite 10～50, the heavy % of inorganic oxide 5～90, the heavy % of clay 0～70. WhereinActive component is to be selected to contain or do not contain the one, two in Y, HY, USY or the Beta zeolite of rare earthKind or multiple.
The invention has the advantages that:
1, catalytic cracking unit light cycle oil is first cut, and wherein hydrogenation is removed in heavy distillat, canReduce to greatest extent hydrogen consumption;
2, adopting two list that overlap catalytic cracking unit independently or have a duo-lift tube reactor to overlap urgesChange cracking unit and process respectively the heavy distillat after light fraction and the hydrogenation of light cycle oil, can be by adoptingDifferent operating parameters, optimizes and meets light cycle oil different fractions catalytic cracking reaction institute to greatest extentThe harsh conditions that need, thus catalytic gasoline farthest produced.
Brief description of the drawings
Fig. 1 is the catalysis conversion method schematic flow sheet of voluminous gasoline provided by the invention.
Detailed description of the invention
Further illustrate method provided by the present invention below in conjunction with accompanying drawing, but the present invention not therefore andBe subject to any restriction.
Accompanying drawing is catalysis conversion method schematic flow sheet provided by the invention.
Fig. 1 is the schematic flow sheet of preferred forms of the present invention, but does not limit the present invention. EquipmentWith the shape of pipeline, the restriction that size is not subject to accompanying drawing, but determine as the case may be. Each in accompanying drawingNumbering is described as follows:
1,3-5,7,10-15 all represent pipeline; 2 is fractionating device; 6 is diesel hydrotreating unit; 8,9 is catalytic cracking unit.
Below in conjunction with accompanying drawing, preferred forms provided by the present invention is further described.
Catalytic cracking light cycle oil enters fractionating device 2 through pipeline 1 and cuts, and obtains≤260 DEG CLight fraction and the heavy distillat of 260 DEG C of >. The light fraction of wherein≤260 DEG C enters catalysis through pipeline 3 and splitsChange reaction unit 8, under Cracking catalyst exists, carry out catalytic cracking reaction. And the double distilled of 260 DEG C of >Lease making pipeline 4 enters diesel hydrotreating unit 6, and hydrogen is introduced diesel hydrotreating unit 6 through pipeline 5 simultaneously.Product hydrogenated diesel oil after hydrogenation enters catalytic cracking reaction device 9 through pipeline 7, urges in catalytic crackingThere is the lower catalytic cracking reaction that occurs in agent. Obtain from catalytic cracking unit 8,9 reaction product isolatedHigh-knock rating gasoline draw through pipeline 10,11 respectively. Another catalytic cracking reaction product gently circulatesOil content is not drawn, is entered fractionating device 2 circulate through pipeline 13,14,1 through pipeline 12,15. ForFor the purpose of simplification, other products does not draw in the drawings as dry gas, liquefied gas, slurry oil etc.
The following examples will be further described the present invention, but not thereby limiting the invention.In embodiment, in hydrotreatment fixed bed reactors, the hydrotreating catalyst business trade mark of filling isRN-32V, the protective agent business trade mark is RG-1, hydrotreating catalyst and protectant admission spaceRatio is 95:5, produces by Sinopec catalyst branch company.
The physico-chemical property of catalyst that in embodiment, comparative example, catalytic cracking unit uses is in table 1, itsThe business trade mark is HAC, and by Sinopec catalyst, branch company produces.
Raw material (catalytic cracking light cycle oil) character using in embodiment, comparative example is listed in table 2.
Embodiment
The present embodiment explanation adopts method provided by the invention, and raw material is first gently circulated through boiling range cuttingOil light fraction and light cycle oil heavy distillat, cut point is 250 DEG C.
Light cycle oil heavy distillat enters medium-sized hydrogenation plant, and the experimental condition of hydrogenation is: hydrogen dividing potential drop12.0MPa; 360 DEG C of average bed reaction temperatures, volume space velocity 0.5 hour-1, hydrogen to oil volume ratio1400Nm3/m3. In hydrogenation heavy distillat, double ring arene content is 4.9 heavy %.
Light cycle oil heavy distillat after light cycle oil light fraction and hydrogenation enter respectively two covers independently inType catalytic cracking riser reaction unit. The main operating parameters of two cover kitty crackers is in Table3. Unified metering after the product normalization that the medium-sized catalytic cracking riser reaction unit of two covers is produced.
Comparative example 1
Medium-sized tester is identical with embodiment with catalyst. The boiling range cut point of light cycle oil is sameEmbodiment, just the heavy distillat after light cycle oil light fraction and hydrogenation enters the medium-sized catalysis of single cover after mixingCracking unit. The wherein same embodiment of the hydroconversion condition of the heavy distillat of light cycle oil. The medium-sized of comparative example urgedChange the operating condition of cracking unit in table 3.
Comparative example 2
Medium-sized tester is identical with embodiment with catalyst. Light cycle oil cuts without boiling range,Full cut directly removes hydrogenation plant hydrogenation, and the full cut of light cycle oil after hydrogenation directly enters medium-sized catalysis and splitsGasifying device. The wherein same embodiment of the hydroconversion condition of the full cut of light cycle oil. The medium-sized catalysis of comparative exampleThe operating condition of cracking unit is in table 3.
The distribution of catalytic cracking product, hydrogen consumption and octane number are in table 4.
Contrast comparative example 1 and comparative example 2 can be found, adopt the method for boiling range cutting, in hydrogenation mistakeIn journey, can obviously reduce hydrogen consumption, hydrogen consumption is reduced to 2.6% from 4.3%. Can find simultaneously, althoughProduct distributes and makes moderate progress, and as gasoline yield increases to some extent, but is not clearly. And contrast is implementedExample and comparative example 2, can find, not only hydrogen consumes from 4.3% and is reduced to 2.6%, and product dividesCloth obviously improves, and while showing conversion per pass, gasoline yield is significantly increased to 66.7% from 58.9%;As can be found from Table 4, compare ratio, the octane number of embodiment has more obviously to be increased simultaneously.Table 1HAC catalyst property
Table 2 feedstock oil character
Feedstock oil title Catalytic cracking light cycle oil
Density (20 DEG C), kg/m3 948.8
Freezing point, DEG C -24
Aniline point, DEG C <30
10% carbon residue, heavy % 0.37
Mean molecule quantity 187
Boiling range, DEG C
Initial boiling point 190
5% 213
10% 222
30% 247
50% 272
70% 303
90% 348
95% 363
The end point of distillation 369
Mass spectrography quality composition, %
Alkane 10.7
Total cycloalkane 4.6
Total aromatic hydrocarbons 84.7
Mononuclear aromatics 31.7
Double ring arene 45.0
Gross mass 100.0
Table 3 operating parameter
Table 4
Embodiment 1 Comparative example 1 Comparative example 2
Hydrogen consumption, % 2.6 2.6 4.3
Product distributes, heavy %
Dry gas 1.7 2.1 2.2
Liquefied gas 22.5 24.8 25.4
Gasoline 66.7 59.5 58.9
Light diesel fuel 7.3 10.8 10.9
Heavy oil 0.3 0.7 0.6
Coke 1.5 2.1 2.0
Add up to 100.0 100.0 100.0
Octane number
RON 96.5 94.8 94.0
MON 84.4 82.8 82.1

Claims (19)

1. a catalysis conversion method for voluminous gasoline, is characterized in that the method comprises:
(1) catalytic cracking light cycle oil obtains light fraction and heavy distillat through cutting;
(2) the described heavy distillat of step (1) is carried out hydrogenation under hydrogen and hydrotreating catalyst existenceProcessing reaction, hydrogen dividing potential drop 10.0～25.0MPa, reaction product isolated obtains hydrogenation heavy distillat;
(3) the described light fraction of step (1), the described hydrogenation heavy distillat of step (2) are entered respectively separatelyEnter different FCC riser, under catalytic cracking catalyst exists, carry out catalysisCracking reaction, separate catalytic cracking catalyst to be generated and reaction oil gas, and wherein reaction oil gas is through separatingTo the product that comprises gasoline, light cycle oil.
2. according to the method for claim 1, it is characterized in that the described light cycle oil of step (3) returnsStep (1).
3. according to the method for claim 1, it is characterized in that the method also comprises: step (3) instituteState catalytic cracking catalyst to be generated gained regeneration catalyzing Cracking catalyst after stripping, regeneration and return to liftingPipe reactor recycles.
4. according to the method for claim 1, it is characterized in that the cutting temperature of described light cycle oil is250～260℃。
5. according to the method for claim 1, it is characterized in that the described hydrotreatment of described step (2)Condition be 330～450 DEG C of reaction temperatures, volume space velocity 0.1～2.0 hour-1, hydrogen to oil volume ratio1000～2000Nm3/m3。
6. according to the method for claim 1, it is characterized in that the described hydrotreatment of described step (2)The active metal component of catalyst is selected from group vib metal and/or group VIII base metal, carrierBe selected from aluminium oxide, silica, amorphous aluminum silicide any one or several.
7. according to the method for claim 6, it is characterized in that described group vib metal be molybdenum or/And tungsten, group VIII base metal is that nickel is or/and cobalt.
8. according to the method for claim 6, it is characterized in that described active metal component be selected from nickel-tungsten,The combination of nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum.
9. according to the method for claim 1, it is characterized in that double ring arene content in hydrogenation heavy distillatBe not more than 10 heavy %.
10. according to the method for claim 9, it is characterized in that double ring arene content in hydrogenation heavy distillatBe not more than 8 heavy %.
11. according to the method for claim 1, it is characterized in that described different catalytic cracking unit carriesRiser reactors, can refer to two overlap independently catalytic cracking unit, also can singly overlap catalytic cracking unitThere is parallel independently duo-lift tube reactor.
12. according to the method for claim 1 or 11, it is characterized in that described riser reactor isIsometrical riser reactor or reducing riser reactor.
13. according to the method in claim 11, it is characterized in that single cover catalytic cracking unit hasIn parallel independently duo-lift tube reactor, Catalyst Balance Activity is not less than 65.
14. according to the method in claim 11, it is characterized in that two overlap independently catalytic cracking dressWhile putting, the Catalyst Balance Activity of the device that light fraction is raw material is not less than 62, and hydrogenation double distilled is divided into formerThe Catalyst Balance Activity of the device of material is not less than 65.
15. according to the method in claim 1, it is characterized in that the reaction condition of light fraction is: anti-Answering temperature is 540～660 DEG C, and agent oil quality is than 10～100, oil gas time of staying 1-10 second, pressure0.15～0.4MPa, the weight ratio of water vapour and raw material is 0.01～0.5.
16. according to the method in claim 15, it is characterized in that the reaction condition of light fraction is:Reaction temperature is 560～620 DEG C, and agent oil quality is than 15～50, and 2～8 seconds oil gas time of staying, water steamsThe weight ratio of vapour and raw material is 0.02～0.2.
17. according to the method in claim 1, it is characterized in that the reaction condition of hydrogenation heavy distillat is:Reaction temperature is 530～650 DEG C, and agent oil quality is than 5～80, oil gas time of staying 1-10 second, pressure0.15～0.4MPa, the weight ratio of water vapour and raw material is 0.01～0.5.
18. according to the method in claim 17, it is characterized in that the reaction condition of hydrogenation heavy distillatFor: reaction temperature is 550～600 DEG C, and agent oil quality is than 5～80,2～8 seconds oil gas time of staying, waterThe weight ratio of steam and raw material is 0.02～0.2.
19. according to the method for claim 1, it is characterized in that the described catalytic cracking of step (3) urgesAgent comprises zeolite, inorganic oxide and optional clay, and the content of each component is respectively: zeolite10～50 heavy %, the heavy % of inorganic oxide 5～90, the heavy % of clay 0～70, wherein active component is choosingSelf-contained or not containing the one of Y, HY, USY or the Beta zeolite of rare earth, two or more.
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CN110551526B (en) * 2018-05-30 2021-08-06 中国石油化工股份有限公司 Processing method of catalytic cracking light cycle oil

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0184669A2 (en) * 1984-12-07 1986-06-18 Ashland Oil, Inc. Process for the production of aromatic fuel
CN1422327A (en) * 2000-04-17 2003-06-04 埃克森美孚研究工程公司 Cycle oil conservation process
CN1466619A (en) * 2000-04-17 2004-01-07 ����ɭ�о����̹�˾ Cycle oil conversion process
CN101191081A (en) * 2006-11-30 2008-06-04 中国石油化工股份有限公司 Catalytic conversion method for hydrocarbon oil raw material

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0184669A2 (en) * 1984-12-07 1986-06-18 Ashland Oil, Inc. Process for the production of aromatic fuel
CN1422327A (en) * 2000-04-17 2003-06-04 埃克森美孚研究工程公司 Cycle oil conservation process
CN1466619A (en) * 2000-04-17 2004-01-07 ����ɭ�о����̹�˾ Cycle oil conversion process
CN101191081A (en) * 2006-11-30 2008-06-04 中国石油化工股份有限公司 Catalytic conversion method for hydrocarbon oil raw material

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