CN104560184A - Catalytic conversion method of maximizing gasoline - Google Patents

Catalytic conversion method of maximizing gasoline Download PDF

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Publication number
CN104560184A
CN104560184A CN201310516479.XA CN201310516479A CN104560184A CN 104560184 A CN104560184 A CN 104560184A CN 201310516479 A CN201310516479 A CN 201310516479A CN 104560184 A CN104560184 A CN 104560184A
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China
Prior art keywords
catalytic cracking
reaction
oil
hydrogenation
light cycle
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CN201310516479.XA
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CN104560184B (en
Inventor
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

The invention relates to a catalytic conversion method of maximizing gasoline. Light catalytic cracking cycle oil is cut to obtain light fractions and heavy fractions, wherein the heavy fractions are hydrotreated to obtain hydrogenated heavy fractions; the light fractions and the hydrogenated heavy fractions independently and respectively enter into different riser reactors of catalytic cracking devices and cracking reaction is carried out in the presence of a catalytic cracking catalyst. The reaction products are separated to obtain products including gasoline and light cycle oil. By adopting two sets of independent catalytic cracking devices or a single set of catalytic cracking device provided with double riser reactors to respectively process light fractions of light cycle oil and hydrogenated heavy fractions, the severe condition required by catalytic cracking reaction of different fractions of the light cycle oil is optimized and satisfied to the maximum extent by adopting different operating parameters, so that catalytic gasoline is produced to the maximum extent.

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 absence of hydrogen, more particularly, is a kind of catalysis conversion method being maximized the gasoline produced by catalytic cracking light cycle oil.
Background technology
Along with the development of crude oil heaviness and market are to the quick growth of light-end products demand, in China, the catalytic cracking technology as heavy oil lighting is rapidly developed.But, must faced by a fact be that the quality of catalytic cracking diesel oil (or claim " light cycle oil ") is but always relatively poor, density is large, and aromaticity content is high, cetane value is low, even if be also difficult to by diesel oil hydrogenation modification technology the diesel oil regulation reaching increasingly stringent.How solving catalytic cracking light cycle oil is an increasingly serious problem.Simultaneous another one problem is domestic gasoline product chronic shortage, and catalytically cracked gasoline accounts for 80% of gasoline product.Therefore, how to realize heavy feed stock maximization production stop bracket gasoline and not produce light cycle oil may being the new way solved the problem by catalytic cracking process.
US4585545 discloses one and complete for catalytic cracking light cycle oil cut is first carried out hydrotreatment, and the hydrogenated diesel oil obtained goes catalytic cracking to produce the catalysis conversion method being rich in mononuclear aromatics gasoline again.
CN1422327A discloses a kind of method of catalytic cracking light cycle oil upgrading, is the light cycle oil that the first catalytic cracking unit taking mink cell focus as raw material is produced is carried out deep hydrogenation, and the hydrogenation turning oil obtained enters the second catalytic cracking unit again.On the basis of the method, CN1423689A emphasizes that catalyst requirement in the second catalytic cracking unit is more than or equal to the large pore zeolite of about 0.7nm, optionally to improve light olefins yields containing the aperture of selecting shape zeolite and about 5-50% of 50-95%.
CN1466619A discloses a kind of method for transformation of catalytic cracking light cycle oil, that catalytic cracking riser reactor is divided into upstream and downstream two reaction zones, wherein mink cell focus injects catchment, and the hydrogenation turning oil that its catalytic cracking production light cycle oil obtains after hydrotreatment injects upstream.On the basis of the method, the charging in CN1425054A method middle and lower reaches district, except hydrogenation turning oil, also add petroleum naphtha.In the method, not only hydrogen consumption is high, and hydrogenation turning oil can have a strong impact on the conversion of the mink cell focus in downstream in upstream reaction.
Can find from disclosed document above, catalytic cracking light cycle oil being carried out to one of important channel processed is that it is first carried out hydrotreatment, and then catalytic cracking.It must be noted that, light cycle oil no matter whether hydrogenation, compare, its molecule is little with mink cell focus macromole, bond energy is large, the operating parameters therefore how controlling catalytic cracking is one of key of light cycle oil processing.In addition, if light cycle oil carries out hydrogenation, 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 the catalysis conversion method that a kind of voluminous gasoline is provided on the basis of existing technology.
Catalysis conversion method provided by the invention comprises:
(1) catalytic cracking light cycle oil obtains lighting end and last running through cutting;
(2) step (1) described last running carries out hydrotreatment reaction under hydrogen and hydrotreating catalyst exist, and reaction product isolated obtains hydrogenation last running;
(3) step (1) described lighting end, the last running of step (2) described hydrogenation enter different FCC riser separately respectively, catalytic cracking reaction is carried out under catalytic cracking catalyst exists, be separated catalytic cracking catalyst to be generated and reaction oil gas, wherein reaction oil gas is isolated to the product comprising gasoline, light cycle oil.
Preferred the method also comprises: the described catalytic cracking catalyst to be generated of step (3) gained regeneration catalyzing cracking catalyst after stripping, regeneration returns riser reactor and recycles.
The described catalytic cracking light cycle oil of step (1) be selected from allocatalysis cracking unit produce light cycle oil or/and present method catalytic cracking unit step (3) produce light cycle oil, preferred allocatalysis light cycle oil that cracking unit produces and present method catalytic cracking unit step (3) produce light cycle oil.
Method provided by the invention is specific as follows:
Catalytic cracking light cycle oil enters independent separation column and cuts, cutting temperature controls at 250 ~ 260 DEG C, preferred cutting temperature is 260 DEG C, obtains respectively not higher than the lighting end of this cutting temperature and the last running higher than this cutting temperature from the top of separation column and bottom.
Hydrotreater is removed in described last running, and under hydrogen and hydrogenation catalyst exist, carry out hydrotreatment reaction, hydroprocessing condition is: hydrogen dividing potential drop 10.0 ~ 25.0MPa, preferably 10.0 ~ 22.0MPa; Temperature of reaction 330 ~ 450 DEG C, preferably 340 ~ 380 DEG C; Volume space velocity 0.1 ~ 2.0 hour -1, hydrogen to oil volume ratio 1000 ~ 2000Nm 3/ m 3.Reaction product isolated obtains the cut of the preferred > of initial boiling point > 250 DEG C 260 DEG C, or claims hydrogenated diesel oil, hydrogenation last running.In described hydrogenation last running, two ring aromatic content wants≤10 heavy %, the heavy % in preferably≤8.
Described activity of hydrocatalyst metal component is selected from group vib metal and/or group VIII base metal, in support selected from alumina, silicon-dioxide, amorphous aluminum silicide any one or several.Described group vib metal be molybdenum or/and tungsten, group VIII base metal is that nickel is or/and cobalt.The combination of the preferred nickel-tungsten of active metal component, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum.
Lighting end and the hydrogenation last running obtained individually enter different FCC riser, under catalytic cracking catalyst exists, carry out cracking reaction, reaction product isolated obtains dry gas, liquefied gas, gasoline, light cycle oil, slurry oil, coke.The new light cycle oil that catalytic cracking unit produces goes independent separation column cutting, cyclical operation.
Described lighting end and hydrogenation last running individually enter different FCC riser, can refer to two overlap independently catalytic cracking unit, also singly can overlap catalytic cracking unit there is parallel independently duo-lift tube reactor.Described riser reactor is isometrical riser reactor or reducing riser reactor.
The concrete operations condition of catalytic cracking unit is as follows:
For the riser reactor of light cycle oil lighting end charging, temperature of reaction is 540 ~ 660 DEG C, preferably 560 ~ 620 DEG C; Agent oil quality than 10 ~ 100, preferably 15 ~ 50; Oil gas residence time 1-10 second, preferably 2 ~ 8 seconds; Pressure (absolute pressure) 0.15 ~ 0.4MPa; The weight ratio of water vapor and raw material is 0.01 ~ 0.5 preferably 0.02 ~ 0.2.
For the riser reactor of light cycle oil hydrogenation last running charging, temperature of reaction is 530 ~ 650 DEG C, preferably 550 ~ 600 DEG C; Agent oil quality than 5 ~ 80, preferably 8 ~ 40; Oil gas residence time 1-10 second, preferably 2 ~ 8 seconds; Pressure (absolute pressure) 0.15 ~ 0.4MPa; The weight ratio of water vapor and raw material is 0.01 ~ 0.5 preferably 0.02 ~ 0.2.
For the list cover catalytic cracking unit with parallel independently duo-lift tube reactor, device leveler activity (MAT) >=65, preferably >=68.
Two are entered respectively for lighting end and hydrogenation last running and overlaps independently catalytic cracking unit, for the device taking lighting end as raw material, leveler activity (MAT) >=62, preferably >=65; For the device being divided into raw material with hydrogenation double distilled, leveler activity (MAT) >=65, preferably >=68.
Duo-lift tube reactor can share a set of settling vessel, main fractionating tower, absorbing-stabilizing system, stripper, revivifier, also can use respective settling vessel, main fractionating tower, absorbing-stabilizing system, stripper, revivifier.
Catalytic cracking catalyst comprises zeolite, inorganic oxide and optional clay.The content of each component is respectively: the heavy % of the heavy % of zeolite 10 ~ 50, the heavy % of inorganic oxide 5 ~ 90, clay 0 ~ 70.Wherein active ingredient be selected from containing or not containing rare earth Y, HY, USY or Beta zeolite in one, two or more.
The invention has the advantages that:
1, catalytic cracking unit light cycle oil is first cut, and wherein last running will remove hydrogenation, hydrogen consumption can be reduced to greatest extent;
2, two are adopted to overlap independently catalytic cracking unit or the list cover catalytic cracking unit with duo-lift tube reactor processes the last running after the lighting end of light cycle oil and hydrogenation respectively, can by adopting different operating parameterss, optimize the severe condition met needed for light cycle oil different fractions catalytic cracking reaction to greatest extent, thus farthest produce catalytic gasoline.
Accompanying drawing explanation
Fig. 1 is the catalysis conversion method schematic flow sheet of voluminous gasoline provided by the invention.
Embodiment
Further illustrate method provided by the present invention below in conjunction with accompanying drawing, but the present invention is not therefore 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.Shape, the size of equipment and pipeline not by the restriction of accompanying drawing, but are determined as the case may be.In accompanying drawing, each numbering is described as follows:
1,3-5,7,10-15 all represents pipeline; 2 is fractionation plant; 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 fractionation plant 2 through pipeline 1 and cuts, and obtains≤lighting end of 260 DEG C and the last running of > 260 DEG C.The lighting end of wherein≤260 DEG C enters catalytic cracking reaction device 8 through pipeline 3, under cracking catalyst exists, carry out catalytic cracking reaction.And the last running of > 260 DEG C enters diesel hydrotreating unit 6 through pipeline 4, hydrogen introduces diesel hydrotreating unit 6 through pipeline 5 simultaneously.Product hydrogenated diesel oil after hydrogenation enters catalytic cracking reaction device 9 through pipeline 7, under catalytic cracking catalyst exists, catalytic cracking reaction occurs.The stop bracket gasoline obtained from catalytic cracking unit 8,9 reaction product isolated is drawn through pipeline 10,11 respectively.Another catalytic cracking reaction product light cycle oil is drawn through pipeline 12,15 respectively, enter fractionation plant 2 through pipeline 13,14,1 circulates.For simplicity, other products such as dry gas, liquefied gas, slurry oil etc. do not draw in the drawings.
The following examples will be further described the present invention, but not thereby limiting the invention.In embodiment, in hydrotreatment fixed-bed reactor, the hydrotreating catalyst commercial grades of filling is RN-32V; protective material commercial grades is RG-1; hydrotreating catalyst and protectant admission space ratio are 95:5, produce by Sinopec catalyzer branch office.
In embodiment, comparative example, the physico-chemical property of the catalyzer that catalytic cracking unit uses is in table 1, and its commercial grades is HAC, is produced by Sinopec catalyzer branch office.
Raw material (catalytic cracking light cycle oil) character used in embodiment, comparative example lists in table 2.
Embodiment
The present embodiment illustrates and adopts method provided by the invention, and raw material first obtains light cycle oil lighting end and light cycle oil last running through boiling range cutting, and cut point is 250 DEG C.
Light cycle oil last running enters medium-sized hydrogenation unit, and the test conditions of hydrogenation is: hydrogen dividing potential drop 12.0MPa; Average bed temperature of reaction 360 DEG C, volume space velocity 0.5 hour -1, hydrogen to oil volume ratio 1400Nm 3/ m 3.In hydrogenation last running, two ring aromatic content is 4.9 heavy %.
Light cycle oil last running after light cycle oil lighting end and hydrogenation enters two covers independently medium-sized catalytic cracking riser reaction unit respectively.The main operating parameters of two cover kitty crackers is in table 3.Unified metering after the product normalization method 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 catalyzer.The same embodiment of boiling range cut point of light cycle oil, enters after the last running mixing just after light cycle oil lighting end and hydrogenation and singly overlaps kitty cracker.The wherein same embodiment of the hydroconversion condition of the last running of light cycle oil.The operational condition of the kitty cracker of comparative example is in table 3.
Comparative example 2
Medium-sized tester is identical with embodiment with catalyzer.Light cycle oil cuts without boiling range, and full cut directly removes hydrogenation unit hydrogenation, and the full cut of the light cycle oil after hydrogenation directly enters kitty cracker.The wherein same embodiment of hydroconversion condition of the full cut of light cycle oil.The operational condition of the kitty cracker of comparative example is in table 3.
Catalytic cracking product distribution, hydrogen consumption and gasoline octane rating are in table 4.
Contrast comparative example 1 and comparative example 2 can find, adopt the method for boiling range cutting, obviously can reduce hydrogen consumption in hydrogenation process, and hydrogen consumption is reduced to 2.6% from 4.3%.Can find, although products distribution makes moderate progress, as gasoline yield increases to some extent, be not clearly simultaneously.And comparative example and comparative example 2, then can find, not only hydrogen consumption is reduced to 2.6% from 4.3%, and products distribution is obviously improved, and when showing single-pass conversion, gasoline yield is significantly increased to 66.7% from 58.9%; As can be found from Table 4, compare ratio, the gasoline octane rating of embodiment has more obviously to be increased simultaneously.Table 1HAC catalyst property
Table 2 stock oil character
Stock oil title Catalytic cracking light cycle oil
Density (20 DEG C), kg/m 3 948.8
Zero pour, DEG C -24
Aniline point, DEG C <30
10% carbon residue, heavy % 0.37
Molecular-weight average 187
Boiling range, DEG C
Initial boiling point 190
5% 213
10% 222
30% 247
50% 272
70% 303
90% 348
95% 363
Final boiling point 369
Mass spectroscopy quality forms, %
Paraffinic hydrocarbons 10.7
Total naphthenic hydrocarbon 4.6
Total aromatic hydrocarbons 84.7
Mononuclear aromatics 31.7
Double ring arene 45.0
Total mass 100.0
Table 3 operating parameters
Table 4
Embodiment 1 Comparative example 1 Comparative example 2
Hydrogen consumes, % 2.6 2.6 4.3
Product slates, heavy %
Dry gas 1.7 2.1 2.2
Liquefied gas 22.5 24.8 25.4
Gasoline 66.7 59.5 58.9
Solar oil 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
Gasoline octane rating
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 lighting end and last running through cutting;
(2) step (1) described last running carries out hydrotreatment reaction under hydrogen and hydrotreating catalyst exist, and reaction product isolated obtains hydrogenation last running;
(3) step (1) described lighting end, the last running of step (2) described hydrogenation enter different FCC riser separately respectively, catalytic cracking reaction is carried out under catalytic cracking catalyst exists, be separated catalytic cracking catalyst to be generated and reaction oil gas, wherein reaction oil gas is isolated to the product comprising gasoline, light cycle oil.
2., according to the method for claim 1, it is characterized in that step (3) described light cycle oil returns step (1).
3. according to the method for claim 1, it is characterized in that the method also comprises: the described catalytic cracking catalyst to be generated of step (3) gained regeneration catalyzing cracking catalyst after stripping, regeneration returns riser reactor and recycles.
4., according to the method for claim 1, it is characterized in that the cutting temperature of described light cycle oil is 250 ~ 260 DEG C.
5., according to the method for claim 1, it is characterized in that the condition of described step (2) described hydrotreatment is hydrogen dividing potential drop 10.0 ~ 25.0MPa, temperature of reaction 330 ~ 450 DEG C, volume space velocity 0.1 ~ 2.0 hour -1, hydrogen to oil volume ratio 1000 ~ 2000Nm 3/ m 3.
6. according to the method for claim 1, it is characterized in that the active metal component of described step (2) described hydrotreating catalyst is selected from group vib metal and/or group VIII base metal, in support selected from alumina, silicon-dioxide, 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 is selected from the combination of nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum.
9., according to the method for claim 1, it is characterized in that in hydrogenation last running, two ring aromatic content is not more than 10 heavy %.
10., according to the method for claim 9, it is characterized in that in hydrogenation last running, two ring aromatic content is not more than 8 heavy %.
11., according to the method for claim 1, is characterized in that described different FCC riser, can refer to two overlap independently catalytic cracking unit, also singly can overlap catalytic cracking unit there is parallel independently duo-lift tube reactor.
12., according to the method for claim 1 or 11, is characterized in that described riser reactor is isometrical riser reactor or reducing riser reactor.
13. according to the method in claim 11, it is characterized in that single cover catalytic cracking unit has Catalyst Balance Activity in parallel independently duo-lift tube reactor and is not less than 65.
14. according to the method in claim 11, it is characterized in that two overlap independently catalytic cracking unit time, lighting end is that the Catalyst Balance Activity of the device of raw material is not less than 62, and hydrogenation double distilled is divided into the Catalyst Balance Activity of the device of raw material to be not less than 65.
15. according to the method in claim 1, it is characterized in that the reaction conditions of lighting end is: temperature of reaction is 540 ~ 660 DEG C, agent oil quality than 10 ~ 100, oil gas residence time 1-10 second, pressure 0.15 ~ 0.4MPa, the weight ratio of water vapor and raw material is 0.01 ~ 0.5.
16. according to the method in claim 15, it is characterized in that the reaction conditions of lighting end is: temperature of reaction is 560 ~ 620 DEG C, and agent oil quality is than 15 ~ 50, and 2 ~ 8 seconds oil gas residence time, the weight ratio of water vapor and raw material is 0.02 ~ 0.2.
17. according to the method in claim 1, it is characterized in that the reaction conditions of hydrogenation last running is: temperature of reaction is 530 ~ 650 DEG C, agent oil quality than 5 ~ 80, oil gas residence time 1-10 second, pressure 0.15 ~ 0.4MPa, the weight ratio of water vapor and raw material is 0.01 ~ 0.5.
18. according to the method in claim 17, it is characterized in that the reaction conditions of hydrogenation last running is: temperature of reaction is 550 ~ 600 DEG C, and agent oil quality is than 5 ~ 80, and 2 ~ 8 seconds oil gas residence time, the weight ratio of water vapor and raw material is 0.02 ~ 0.2.
19. according to the method for claim 1, it is characterized in that step (3) described catalytic cracking catalyst comprises zeolite, inorganic oxide and optional clay, the content of each component is respectively: the heavy % of the heavy % of zeolite 10 ~ 50, the heavy % of inorganic oxide 5 ~ 90, clay 0 ~ 70, wherein active ingredient be selected from containing or not containing Y, HY, USY or Beta zeolite of rare earth one, two or more.
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110551526A (en) * 2018-05-30 2019-12-10 中国石油化工股份有限公司 Processing method of catalytic cracking light cycle oil

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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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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

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110551526A (en) * 2018-05-30 2019-12-10 中国石油化工股份有限公司 Processing method of catalytic cracking light cycle oil
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

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