CN106947529B - A method of the conversion production gasoline of cut fraction hydrogenation containing aromatics diesel - Google Patents
A method of the conversion production gasoline of cut fraction hydrogenation containing aromatics diesel Download PDFInfo
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- CN106947529B CN106947529B CN201610009274.6A CN201610009274A CN106947529B CN 106947529 B CN106947529 B CN 106947529B CN 201610009274 A CN201610009274 A CN 201610009274A CN 106947529 B CN106947529 B CN 106947529B
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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
- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
-
- 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
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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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 discloses a kind of hydrogenating conversion process containing aromatics diesel.Fraction containing aromatics diesel first carries out hydrofining reaction in weighted BMO spaces section, then carries out hydroconversion reactions in hydro-conversion section；Hydro-conversion section includes at least two hydroconversion zones, includes Hydrobon catalyst and hydrocracking catalyst in the first hydroconversion zone, the second hydroconversion zone is built-in to fill out hydrocracking catalyst；The method also includes the following contents: a step, wherein the second hydroconversion zone is used only, the first hydroconversion zone carries out short circuit, and the time is less than the deactivation time of hydrofinishing section；One step, during the step, all hydroconversion zones are used together, by the first hydroconversion zone series connection of short circuit before the second hydroconversion zone used in step a), and after hydrofinishing section.The method of the present invention shortens the time that the initial stage device of going into operation enters stable operation, and effectively extends the operation cycle of device.
Description
Technical field
The present invention relates to a kind of hydrogenating conversion process containing aromatics diesel, specifically a kind of hydro-conversion containing aromatics diesel
The method for producing high octane gasoline component.
Technical background
Catalytic cracking (FCC) technology is one of main technique means of heavy oil lighting, in the oil refining enterprise of countries in the world
In all occupy important status.In recent years, as the raw material heaviness and in poor quality increasingly that catalytic cracking unit is processed is led
The product of catalytic cracking is caused, the quality of especially catalytic cracking light cycle oil (LCO) more deteriorates.Catalytic cracking light cycle oil sulphur
Content and arene content are high, and engine ignition performance is poor, are mainly used for reconciliation fuel oil, non-derv fuel and heating oil in foreign countries
Deng.
Currently, foreign countries have using hydrocracking process technology by catalytic cracking light cycle oil be converted into ultra-low-sulphur diesel and
The relevant report of high-knock rating gasoline blend component.Such as: the meeting of nineteen ninety-five NPRA, VI d A.Pappal of Da et al. describe by
The MAK-LCO technology of Mobil, Akzo Nobel and the exploitation of M.W.Kellogg company；NPRA meeting in 2005, Vasant
P.Thakkar et al. describes the LCO Unicracking of Uop Inc.'s exploitationTMTechnology and HC-190 special-purpose catalyst.According to report
Road, both the above technology can convert high octane gasoline component and fine-quality diesel oil tune for the catalytic cycle oil ingredient of low value
And component.In addition, UOP describes the LCO-X new technology of its exploitation in NPRA meeting in 2007, the technology is by adding hydrogen to turn
Change-alkylation selectivity transferring route realizes the new way using fuels from FCC LCO volume increase aromatic hydrocarbons.It can thus be seen that external
Utilization for the fuels from FCC LCO of low value is also directly to be modified by initial to it in continuous exploration and progress
The level of oiling combination is promoted.Catalytic diesel oil hydro-conversion technology is furtherd investigate, by optimizing Catalyst packing scheme, greatly
Amplitude shortens the stable adjustment time that goes into operation, and extends catalyst service life, maximizes to optimization value of the product very significant.
US5114562 discloses a kind of two-stage method diesel oil hydrogenation treatment process, and one section is urged using traditional hydrofinishing
Agent deviates from the impurity such as sulphur, nitrogen in raw material, and second segment carries out the de- virtue of depth using the catalyst for having higher plus hydrogen saturated activity,
Technique hydrogen consumption is big, and investment is high, economical difference.
US4971680 disclose it is a kind of using hydrocracking catalyst by the aromatic hydrocarbons in diesel oil, especially double ring arene selects
Selecting property is cracked into gasoline component, but gasoline products octane number is low, still needs to be further processed.
Summary of the invention
In view of the deficiencies of the prior art, the present invention provides a kind of hydrogenating conversion process containing aromatics diesel, can significantly contract
Short go into operation adjusts the period, so that gasoline fraction product octane number is faster reached higher level, and extend the device cycle of operation.
Hydrogenating conversion process containing aromatics diesel of the invention, including the following contents:
A method of the conversion production gasoline of cut fraction hydrogenation containing aromatics diesel, wherein in weighted BMO spaces section, bavin containing aromatic hydrocarbons
Oil distillate and hydrogen pass through Hydrobon catalyst bed under Hydrofinishing conditions, and then hydrofinishing effluent is adding hydrogen to turn
By the hydrogenation conversion catalyst in hydro-conversion section under the conditions of change, hydro-conversion effluent carries out gas-liquid separation, and liquid is through dividing
It evaporates to obtain gas, gasoline component and diesel component；Wherein hydro-conversion section includes at least two hydroconversion zones, and first plus hydrogen turn
Change in area according to including Hydrobon catalyst and hydrocracking catalyst with material engagement sequence, the second hydroconversion zone is built-in
Fill out hydrocracking catalyst；Therefore, the method also includes the following contents:
A) step, wherein the second hydroconversion zone is used only, the first hydroconversion zone carries out short circuit, and the time is less than
The deactivation time of hydrofinishing section；
B) step, during the step, all hydroconversion zones are used together, and the first of short circuit plus hydrogen are turned
Change area's series connection before the second hydroconversion zone used in step a), and after weighted BMO spaces section.
In method of the invention, wherein the arene content of the fraction containing aromatics diesel is in 50wt% or more, preferably
70wt% or more；Initial boiling point is 50 DEG C~280 DEG C, and 95wt% recovered (distilled) temperature is 330 DEG C~450 DEG C.Containing polycyclic in aromatics diesel
Aromatic hydrocarbons (referring to the above aromatic hydrocarbons of two rings) content is in 30wt% or more, preferably 40wt% or more.
The fraction containing aromatics diesel is generally selected from catalytic cracking diesel oil, aromatic extraction unit is raffinated oil, coal liquefaction bavin
One or more of oil, coal tar diesel oil, shale oil diesel oil distillate.
In method of the invention, the weighted BMO spaces section is filled with Hydrobon catalyst.First hydro-conversion is anti-
It answers in area, successively loads Hydrobon catalyst and hydrocracking catalyst according to the engagement sequence with material.
In method of the invention, the Hydrofinishing conditions of the weighted BMO spaces section are as follows: 2.0~16.0MPa of hydrogen partial pressure, hydrogen
For oil volume than 300: 1~1500: 1, volume space velocity is 0.1~5.0h-1, 200 DEG C~450 DEG C of reaction temperature；Optimum condition are as follows: excellent
The operating condition of choosing is 4.0~12.0MPa of reaction pressure, hydrogen to oil volume ratio 300: 1~1500: 1,2.0~3.0h of volume space velocity-1, 250 DEG C~430 DEG C of reaction temperature section.
The operating condition of hydro-conversion section described in step a) are as follows: hydrogen partial pressure is 2.0~16.0MPa, hydrogen to oil volume ratio 300
: 1~1500: 1, volume space velocity is 0.5~5.0h-1, 200 DEG C~450 DEG C of reaction temperature；Preferred operating condition is reaction pressure
4.0~12.0MPa, hydrogen to oil volume ratio 300: 1~1500: 1,1.0~2.0h of volume space velocity-1, 300 DEG C of reaction temperature section~
430℃。
The operating condition of hydro-conversion section described in step b) are as follows: 2.0~16.0MPa of hydrogen partial pressure, hydrogen to oil volume ratio 300: 1
~1500: 1, volume space velocity is 0.5~5.0h-1, 200 DEG C~450 DEG C of reaction temperature；Preferred operating condition is reaction pressure
4.0~12.0MPa, hydrogen to oil volume ratio 300: 1~1500: 1,0.5~1.5h of volume space velocity-1, 300 DEG C of reaction temperature section~
430℃。
Weighted BMO spaces section is filled with Hydrobon catalyst.Common diesel hydrofinishing can be used in Hydrobon catalyst
Catalyst, generally using VI B race and/or group VIII metal as active component, using aluminium oxide or silicon-containing alumina as carrier, the VIth B
Race's metal is generally Mo and/or W, and group VIII metal is generally Co and/or Ni.On the basis of the weight of catalyst, group VIB gold
Belong to content and 8wt%~28wt% is calculated as with oxide, group VIII metal content is calculated as 2wt%~15wt% with oxide, property
Matter is as follows: specific surface is 100~650m2/g, and 0.15~0.8mL/g of Kong Rongwei, alternative commercial catalysts are many kinds of,
Such as Fushun Petrochemical Research Institute (FRIPP) develop 3936,3996, FF-16, FF-26, FF-36, FF-46,
The Hydrobon catalysts such as FF56, FH-98, FH-UDS；Also can according to need by the common sense preparation of this field it is conventional plus hydrogen
Handle oxidized catalyst.
Hydrocracking catalyst is filled in hydro-conversion section.The hydrocracking catalyst includes Cracking Component and adds
Hydrogen component.Cracking Component generally includes amorphous silica-alumina and/or molecular sieve, such as Y type or USY molecular sieve, with the weight of catalyst
On the basis of, the content of Y type molecular sieve is 10~70%, and preferred molecular sieve content is 30~60%；Adhesive is usually aluminium oxide
Or silica.Hydrogenation component be selected from VI race, the metal of VII race or VIII race, metal oxide or metal sulfide, more preferably iron,
Chromium, molybdenum, tungsten, cobalt, nickel or one or more of its sulfide or oxide.On the basis of the weight of catalyst, hydrogenation component
Content be 5~40wt%.Conventional hydrocracking catalyst can choose existing various commercial catalysts, such as FRIPP is ground
Make the catalyst such as develop 3824, FC-24, FC-24B, FC-46.Also can according to need prepared by the common sense of this field it is specific
Hydrocracking catalyst.
Y molecular sieve used in hydrocracking catalyst preferably have the property that as lattice constant be 2.425~
2.450nm, the SiO of Y molecular sieve2/Al2O3Molar ratio is 5.0~50.0, and relative crystallinity is 80%~130%.
The hydrofinishing in Hydrobon catalyst and weighted BMO spaces section loaded in first hydroconversion zone
Catalyst can be identical or different, and hydrocracking catalyst can be identical with the hydrocracking catalyst in the second hydroconversion zone
Or it is different.In first hydroconversion zone, the admission space ratio of Hydrobon catalyst and hydrocracking catalyst is 1:1
~1:2.
The weighted BMO spaces section generally comprises the reactor of at least one or two above serial or parallel connections.
In method of the invention, the initial stage that goes into operation carries out according to step a), in oepration at full load, when can not be by adjusting work
When the means of skill parameter make hydroconversion reaction zone obtain the requirement of product<210 DEG C gasoline products yield satisfaction>40%, that is, switch to
Step b).
Compared with prior art, method of the invention has the advantages that
1, the method for the present invention can overcome catalytic diesel oil hydro-conversion common process in the initial stage catalyst hydrogenation activity that goes into operation
The problem that superfluous, aromatic hydrocarbons supersaturation causes gasoline products octane number low.By reasonably adjusting catalyst grading distribution scheme, containing virtue
The initial stage that diesel oil hydrogenation reforming unit goes into operation makes the Hydrobon catalyst usage amount for participating in reacting be less than common process dosage,
To reduce the supersaturation of aromatic component.By weak plus hydrogen, the matching of strong cracking, the optimum response area of aromatic hydrogenation saturation is avoided
Domain, so as to which such as catalytic diesel oil inferior containing aromatics diesel is partially converted into high octane gasoline component.
2, compared with conventional hydro conversion process, method of the invention may be implemented that vapour can be made in a relatively short period of time
Oil product octane number reaches higher level.As in the prior art, conventional hydro conversion process needs about one month time
Can just access the satisfactory gasoline component of octane number, and the method for the present invention only need to time less than 3 days, can be obtained and meet
It is required that gasoline products or blend component.Moreover, the present invention uses latter stage in catalytic diesel oil hydroconversion unit, passes through tune
Whole catalyst grading distribution scheme improves catalyst usage amount to suitable with common process, it can also be ensured that catalytic diesel oil hydro-conversion
Device long-term operation.
Detailed description of the invention
Fig. 1 is the process flow diagram of the method for the present invention.
Wherein, the first reaction zone of 1-, the second reaction zone 2-, 3- third reaction zone, the gas-liquid separation zone 4-, the fractionation zone 5-, 6-
Circulating hydrogen compressor, 7,8,9,10,11,13,14,16,17,18,19,20,21,22- pipeline, 12,15,23- valve.
Specific embodiment
Method of the invention is described in further detail with reference to the accompanying drawing.
Some necessary equipment, such as heating furnace, pump, heat exchanger are omitted in Fig. 1.The equipment of omission is art technology
Known to personnel, therefore no longer repeated in Fig. 1.
As shown in Figure 1, catalytic diesel oil hydrogenating conversion process of the invention includes the first reaction zone 1, second reaction zone 2 and the
Three reaction zones 3 are filled in second reaction zone 2 wherein being filled with pretreating catalyst by hydrocracking in the first reaction zone 1 and add hydrogen
Cracking pretreatment catalyst and hydrocracking catalyst are filled with hydrocracking catalyst in third reaction zone 3.
In start of run, valve 23 is opened, other valves are closed；Feedstock oil is mixed with the hydrogen by pipeline 7 through pipeline 1
After conjunction, enters in the first reaction zone 1 by pipeline 10 and carry out hydrofining reaction；Reaction effluent passes through pipeline 11, valve 23
Enter in third reaction zone with pipeline 16, and carries out hydroconversion reactions in the presence of hydrogen and hydrocracking catalyst；Instead
It answers effluent to enter gas-liquid separation zone 4 by pipeline 17, is separated into hydrogen-rich gas and liquid product herein.Gas-liquid separation zone 4 is logical
It often include high-pressure separator and low pressure separator.Hydrogen-rich gas enters circulating hydrogen compressor 6 by pipeline 18, and process is compressed
After hydrogen-rich gas is mixed with the supplement hydrogen introduced through pipeline 9, circulating hydrogen is formed by pipeline 7.Gas-liquid separation zone 4 obtains liquid
Product enters fractionation zone 5 through pipeline 19, obtains gas, gasoline component and diesel component by pipeline 20,21 and 22 respectively.
Later period in operation, process change as follows: valve 12,15 is opened, other valves are closed；Feedstock oil through pipeline 1, with
After the mixing of the hydrogen of pipeline 7, enters in the first reaction zone 1 by pipeline 10 and carry out hydrofining reaction；Reaction effluent
Enter in second reaction zone 2 by pipeline 11, valve 12, pipeline 13；The effluent of second reaction zone 2 without isolation, by pipe
Line 14, valve 15 and pipeline 16 enter third reaction zone 3, and carry out that hydrogen is added to turn in the presence of hydrogen and hydrocracking catalyst
Change reaction；Process of the separation of third reaction zone effluent with start of run.
Illustrate the present invention program and effect below by specific example.
Illustrate technical solutions and effects of the present invention below by specific embodiment.Raw materials used oil nature is listed in table 1.Institute
It is listed in table 2 with catalyst, catalyst A is pretreating catalyst by hydrocracking, and catalyst B is hydrocracking catalyst.
1 raw material oil nature of table
| Feedstock oil | Catalytic diesel oil | Coal liquefaction diesel oil |
| Density (20 DEG C)/gcm-3 | 0.9375 | 0.9660 |
| Process/DEG C | 196~348 | 283~366 |
| Sulfur content/μ gg-1 | 3400 | 12000 |
| Nitrogen content/μ gg-1 | 850 | 3400 |
| Arene content, wt% | 67.4 | 77.8 |
| Polycyclic aromatic hydrocarbon, wt% | 55.3 | 60.5 |
2 catalyst property of table
Embodiment 1
Using process shown in Fig. 1.If three reactors, R1 is weighted BMO spaces reactor, and R2 and R3 are that hydro-conversion is anti-
Answer device.Loading catalyst B in loading catalyst A and catalyst B, R3 in loading catalyst A in R1, R2.It goes into operation initial stage, R2 is short
Road, catalytic cracking diesel oil and hydrogen are mixed into R1, obtain effluent and enter R3, obtain product, obtain gas by separating, being fractionated
Body, gasoline products and diesel product.Operation changes process after 5500 hours, R2 cuts process flow: catalytic cracking diesel oil and hydrogen
Enter R1 after gas mixing, obtain effluent and enter R2, obtain effluent and enter R3, obtains product by separation and fractionation and obtain gas
Body, gasoline products and diesel product.Process conditions and product property are shown in Table 3.
Comparative example 1
Using flow chart shown in Fig. 1, if three reactors, R1 is weighted BMO spaces reactor, and R2 and R3 are hydro-conversion
Reactor.Loading catalyst A and catalyst B, R3 loading catalyst B in loading catalyst A in R1, R2.Process flow is to be catalyzed
After cracked diesel oil is mixed with hydrogen, R1, R2 and R3 are passed sequentially through, isocrackate arrives gas, gasoline by separation and fractionation
Product and diesel product.Process conditions and product property are shown in Table 4.
Embodiment 2
Using process shown in Fig. 1.If three reactors, R1 is weighted BMO spaces reactor, and R2 and R3 are that hydro-conversion is anti-
Answer device.Loading catalyst A and catalyst B, R3 loading catalyst B in loading catalyst A in R1, R2.It goes into operation initial stage, R2 short circuit,
Feedstock oil and hydrogen are mixed into R1, obtain effluent and enter R3, obtain product, obtain gas, gasoline production by separating, being fractionated
Product and diesel product.Operation changes process after 5500 hours, R2 cuts process flow: feedstock oil enters R1 after mixing with hydrogen,
It obtains effluent and enters R2, obtain effluent and enter R3, obtain product by separation and fractionation and obtain gas, gasoline products and bavin
Oil product.Process conditions and product property are shown in Table 5.
3 process conditions of table and product property
*: step b) is switched to after 5000 hours.
4 process conditions of table and product property
5 process conditions of table and product property
*: step b) is switched to after 5000 hours.
Hydroconversion process it can be seen from the data result of embodiment and comparative example through the invention can make vapour
Oil product octane number reaches higher level in a relatively short period of time, and extends catalyst service life, reaches long-term operation
Purpose.
Claims (13)
1. a kind of method of the conversion of cut fraction hydrogenation containing aromatics diesel production gasoline, wherein containing aromatics diesel in weighted BMO spaces section
Fraction and hydrogen pass through Hydrobon catalyst bed under Hydrofinishing conditions, and then hydrofinishing effluent is in hydro-conversion
Under the conditions of by the hydrogenation conversion catalyst in hydro-conversion section, hydro-conversion effluent carries out gas-liquid separation, and liquid is fractionated
Obtain gas, gasoline component and diesel component；Wherein hydro-conversion section includes at least two hydroconversion zones, the first hydro-conversion
According to including Hydrobon catalyst and hydrocracking catalyst with material engagement sequence in area, loaded in the second hydroconversion zone
Hydrocracking catalyst；Therefore, the method also includes the following contents:
A) step, wherein the second hydroconversion zone is used only, the first hydroconversion zone carries out short circuit, and the time is less than plus hydrogen
The deactivation time of refining stage；
B) step, during the step, all hydroconversion zones are used together, by the first hydroconversion zone of short circuit
Series connection is before the second hydroconversion zone used in step a), and after weighted BMO spaces section.
2. according to the method for claim 1, which is characterized in that the arene content of the fraction containing aromatics diesel exists
50wt% or more, initial boiling point are 50 DEG C ~ 280 DEG C, and 95wt% recovered (distilled) temperature is 330 DEG C ~ 450 DEG C.
3. according to the method for claim 2, which is characterized in that the arene content of the fraction containing aromatics diesel is
60wt%~95wt%.
4. according to the method for claim 2, which is characterized in that the content of polycyclic aromatic hydrocarbon in the fraction containing aromatics diesel
In 30wt% or more.
5. according to any method of claim 1-4, which is characterized in that the fraction containing aromatics diesel is selected from catalysis and splits
Change one or more of diesel oil, coal liquefaction diesel oil, coal tar diesel oil distillate.
6. according to the method for claim 1, which is characterized in that in first hydroconversion zone, hydrofinishing catalysis
The admission space of agent and hydrocracking catalyst ratio is 1:1~1:2.
7. according to the method for claim 1, which is characterized in that the Hydrofinishing conditions are as follows: hydrogen partial pressure 2.0~16.0
MPa, hydrogen to oil volume ratio 300: 1~1500: 1, volume space velocity are 0.1~5.0 h-1, 200 DEG C~450 DEG C of reaction temperature.
8. according to the method for claim 1, which is characterized in that the hydro-conversion condition are as follows: hydrogen partial pressure 2.0 ~
16.0MPa, hydrogen to oil volume ratio 300: 1~1500: 1, volume space velocity are 0.5 ~ 5.0h-1, 200 DEG C~450 DEG C of reaction temperature.
9. according to the method for claim 1, which is characterized in that the Hydrobon catalyst is with VI B race and/or the VIIIth
Race's metal is active component, using aluminium oxide or silicon-containing alumina as carrier, on the basis of the weight of catalyst, and group VIB metal
Content is calculated as 8wt%~28wt% with oxide, and group VIII metal content is calculated as 2wt%~15wt% with oxide.
10. according to the method for claim 9, which is characterized in that the group VIB metal is Mo and/or W, the VIIIth race
Metal is Co and/or Ni.
11. according to the method for claim 1, which is characterized in that the hydrocracking catalyst include Cracking Component and
Hydrogenation component, Cracking Component includes Y molecular sieve, and on the basis of the weight of catalyst, the content of Y molecular sieve is 10~60%.
12. according to the method for claim 11, which is characterized in that the lattice constant of the Y molecular sieve be 2.425~
2.450nm, the SiO of Y molecular sieve2/Al2O3Molar ratio is 5.0~50.0, and relative crystallinity is 80%~130%.
13. according to the method for claim 11, which is characterized in that on the basis of the weight of catalyst, described adds hydrogen group
The content divided is 5~40 wt%, and hydrogenation component is selected from iron, chromium, molybdenum, tungsten, cobalt, nickel or their oxide or their vulcanization
One or more of object.
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| CN101724454A (en) * | 2008-10-28 | 2010-06-09 | 中国石油化工股份有限公司 | Hydrocracking method for producing high-octane petrol |
| CN101987971A (en) * | 2009-08-06 | 2011-03-23 | 中国石油化工股份有限公司石油化工科学研究院 | Method for producing high-octane petrol by inferior diesel |
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