CN106947529A - A kind of method of the conversion of cut fraction hydrogenation containing aromatics diesel production gasoline - Google Patents
A kind of method of the conversion of cut fraction hydrogenation containing aromatics diesel production gasoline Download PDFInfo
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- CN106947529A CN106947529A CN201610009274.6A CN201610009274A CN106947529A CN 106947529 A CN106947529 A CN 106947529A CN 201610009274 A CN201610009274 A CN 201610009274A CN 106947529 A CN106947529 A CN 106947529A
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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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- 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.Cut 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 including Hydrobon catalyst and hydrocracking catalyst at least two hydroconversion zones, the first hydroconversion zone, and the second hydroconversion zone is built-in to fill out hydrocracking catalyst；Methods described also includes herein below：One step, wherein using only the second hydroconversion zone, the first hydroconversion zone carries out short circuit, its 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 in step a）Before middle the second hydroconversion zone used, and after hydrofinishing section.The inventive method shortens the device at initial stage that goes into operation and enters the time of stable operation, and effectively extends the service 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, the oil refining enterprise in countries in the world
In all occupy important status.In recent years, the raw material processed with catalytic cracking unit heaviness and in poor quality increasingly is led
The product of catalytic cracking is caused, the quality of particularly catalytic cracking light cycle oil (LCO) more deteriorates.Catalytic cracking light cycle oil sulphur
Content and arene content are high, engine ignition poor performance, are mainly used in mediation fuel oil, non-derv fuel and heating oil abroad
Deng.
At present, it is external 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, d A.Pappal of Da VI et al. describe by
The MAK-LCO technologies of Mobil, Akzo Nobel and M.W.Kellogg companies exploitation；NPRA meetings in 2005, Vasant
P.Thakkar et al. describes the LCO Unicracking of Uop Inc.'s exploitationTMTechnology and HC-190 special-purpose catalysts.According to report
Road, the catalytic cycle oil ingredient of low value can be converted into high octane gasoline component by both the above technology and fine-quality diesel oil is adjusted
And component.In addition, UOP describes the LCO-X new technologies of its exploitation in NPRA meetings in 2007, the technology is turned by hydrogenation
Change-alkylation selectivity transferring route realizes the new way for increasing production aromatic hydrocarbons using fuels from FCC LCO.It can thus be seen that external
Utilization for the fuels from FCC LCO of low value is also that in continuous exploration and progress, its is directly modified by initial
The aspect of oiling combination is lifted.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 usage cycles, optimization value of the product is maximized very meaningful.
US5114562 discloses a kind of two-stage method diesel oil hydrogenation handling 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 hydrogenation saturated activity,
Technique hydrogen consumption is big, and investment is high, economical difference.
US4971680 discloses a kind of utilization hydrocracking catalyst and selects the aromatic hydrocarbons in diesel oil, particularly double ring arene
Selecting property is cracked into gasoline component, but gasoline products octane number is low, still needs to further processing.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of hydrogenating conversion process containing aromatics diesel, can significantly contract
It is short to go into operation the adjustment cycle, gasoline fraction product octane number is faster reached higher level, and the extension fixture cycle of operation.
The hydrogenating conversion process containing aromatics diesel of the present invention, including herein below：
A kind of method of the conversion of cut fraction hydrogenation containing aromatics diesel production gasoline, wherein in weighted BMO spaces section, bavin containing aromatic hydrocarbons
Oil distillate and hydrogen are by Hydrobon catalyst bed under Hydrofinishing conditions, and then hydrofinishing effluent is in hydrogenation 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
Evaporate and obtain gas, gasoline component and diesel component；Wherein hydro-conversion section includes at least two hydroconversion zones, and the first hydrogenation turns
Change in area includes Hydrobon catalyst and hydrocracking catalyst according to material engagement sequence, and the second hydroconversion zone is built-in
Fill out hydrocracking catalyst；Therefore, methods described also includes herein below：
A) step, wherein using only the second hydroconversion zone, the first hydroconversion zone carries out short circuit, and its time is less than
The deactivation time of hydrofinishing section；
B) step, during the step, all hydroconversion zones are used together, and the first hydrogenation of short circuit is turned
Before the second hydroconversion zone that change area's series connection is used in step a), and after weighted BMO spaces section.
In the method for the present invention, wherein the arene content of the cut containing aromatics diesel is in more than 50wt%, preferably
More than 70wt%；Initial boiling point is 50 DEG C~280 DEG C, and 95wt% recovered (distilled) temperatures are 330 DEG C~450 DEG C.Containing polycyclic in aromatics diesel
Aromatic hydrocarbons (referring to two ring above aromatic hydrocarbons) content is in more than 30wt%, preferably more than 40wt%.
Described cut containing aromatics diesel be generally selected from catalytic cracking diesel oil, aromatic extraction unit raffinate oil, coal liquefaction bavin
One or more in oil, coal tar diesel oil, shale oil diesel oil distillate.
In the method for the present invention, described weighted BMO spaces section is filled with Hydrobon catalyst.First hydro-conversion is anti-
Answer in area, Hydrobon catalyst and hydrocracking catalyst are loaded successively according to the engagement sequence with material.
In the method for the present invention, the Hydrofinishing conditions of the weighted BMO spaces section are：2.0~16.0MPa of hydrogen dividing potential drop, hydrogen
Oil volume is than 300: 1~1500: 1, and volume space velocity is 0.1~5.0h-1, 200 DEG C~450 DEG C of reaction temperature；Optimum condition is：It is 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 interval.
Hydro-conversion described in step a) section operating condition be：Hydrogen dividing potential drop 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；It is preferred that operating condition be 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 interval~
430℃。
Hydro-conversion described in step b) section operating condition be：2.0~16.0MPa of hydrogen dividing potential drop, 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；It is preferred that operating condition be 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 interval~
430℃。
Weighted BMO spaces section is filled with Hydrobon catalyst.Hydrobon catalyst can use common diesel hydrofinishing
Catalyst, typically using VI B races and/or group VIII metal as active component, using aluminum 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
Category content is calculated as 8wt%~28wt% with oxide, and group VIII metal content is calculated as 2wt%~15wt% with oxide, its property
Matter is as follows：It is 100~650m2/g than surface, pore volume is 0.15~0.8mL/g, and alternative commercial catalysts species is various,
For example 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；Conventional hydrogenation can also be prepared by the general knowledge of this area as needed
Handle oxidized catalyst.
Hydrocracking catalyst is filled with hydro-conversion section.Described hydrocracking catalyst includes Cracking Component and added
Hydrogen component.Cracking Component generally includes amorphous silica-alumina and/or molecular sieve, such as Y types 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 aluminum 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,
One or more in chromium, molybdenum, tungsten, cobalt, nickel or its sulfide or oxide.On the basis of the weight of catalyst, hydrogenation component
Content be 5~40wt%.Conventional hydrocracking catalyst can select existing various commercial catalysts, and such as FRIPP is ground
Make the catalyst such as develop 3824, FC-24, FC-24B, FC-46.It can also be prepared as needed by the general knowledge of this area specific
Hydrocracking catalyst.
The Y molecular sieve used in hydrocracking catalyst preferably has the following properties that：As lattice constant be 2.425~
2.450nm, the SiO of Y molecular sieve2/Al2O3Mol ratio is 5.0~50.0, and its relative crystallinity is 80%~130%.
The Hydrobon catalyst loaded in the first described hydroconversion zone and the hydrofinishing in weighted BMO spaces section
Catalyst can be with identical or different, and hydrocracking catalyst can be with identical with the hydrocracking catalyst in the second hydroconversion zone
Or it is different.In the first described hydroconversion zone, the admission space ratio of Hydrobon catalyst and hydrocracking catalyst is 1:1
~1:2.
Described weighted BMO spaces section generally comprises the reactor of at least one or two above serial or parallel connections.
In the method for the present invention, the initial stage that goes into operation is carried out according to step a), in oepration at full load, when can not be by adjusting work
The means of skill parameter make hydroconversion reaction zone obtain product<210 DEG C of gasoline products yields are met>During 40% requirement, that is, switch to
Step b).
Compared with prior art, the method for the present invention has the advantages that：
1st, the inventive method can overcome catalytic diesel oil hydro-conversion common process in the catalyst hydrogenation activity at initial stage that goes into operation
Superfluous, aromatic hydrocarbons supersaturation causes the problem of gasoline products octane number is low.By Reasonable adjustment catalyst grading distribution scheme, containing virtue
At the initial stage that diesel oil hydrogenation reforming unit goes into operation, the Hydrobon catalyst usage amount that participation is reacted is set to be less than common process consumption,
To reduce the supersaturation of aromatic component.By weak hydrogenation, 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.
2nd, compared with conventional hydro conversion process, the method for the present invention can be realized can make vapour in the short period of time
Oil product octane number reaches higher level.As in the prior art, conventional hydro conversion process needs the time of about one month
It can just access the satisfactory gasoline component of octane number, and the time that the inventive method only need to be less than 3 days, you can met
It is required that gasoline products or blend component.Moreover, the present invention uses latter stage in catalytic diesel oil hydroconversion unit, by adjusting
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.
Brief description of the drawings
Fig. 1 is the process flow diagram of the inventive method.
Wherein, the reaction zones of 1- first, 2- second reaction zone, the reaction zones of 3- the 3rd, 4- gas-liquid separation zones, 5- fractionation zones, 6-
Circulating hydrogen compressor, 7,8,9,10,11,13,14,16,17,18,19,20,21,22- pipelines, 12,15,23- valves.
Embodiment
The method of the present invention is described in further detail below in conjunction with the accompanying drawings.
Some necessary equipment, such as heating furnace, pump, heat exchanger are eliminated in Fig. 1.The equipment of omission is art technology
Known to personnel, therefore no longer repeat in Fig. 1.
As shown in figure 1, the catalytic diesel oil hydrogenating conversion process of the present invention includes the first reaction zone 1, second reaction zone 2 and the
Three reaction zones 3, hydrogenation is filled with wherein being filled with the first reaction zone 1 in pretreating catalyst by hydrocracking, second reaction zone 2
Hydrocracking catalyst is filled with cracking pretreatment catalyst and hydrocracking catalyst, the 3rd reaction zone 3.
In start of run, valve 23 is opened, and other valves are closed；Feedstock oil is through pipeline 1, with being mixed by the hydrogen of pipeline 7
After conjunction, enter by pipeline 10 in the first reaction zone 1 and carry out hydrofining reaction；Reaction effluent passes through pipeline 11, valve 23
Enter with pipeline 16 in the 3rd reaction zone, and carry out in the presence of hydrogen and hydrocracking catalyst hydroconversion reactions；Instead
Answer effluent to enter gas-liquid separation zone 4 by pipeline 17, hydrogen-rich gas and fluid product are separated into herein.Gas-liquid separation zone 4 leads to
Often include high-pressure separator and low pressure separator.Hydrogen-rich gas enters circulating hydrogen compressor 6 by pipeline 18, after overcompression
After hydrogen-rich gas is mixed with the supplement hydrogen introduced through pipeline 9, by the formation circulating hydrogen of pipeline 7.Gas-liquid separation zone 4 obtains liquid
Product enters fractionation zone 5 through pipeline 19, and gas, gasoline component and diesel component are obtained respectively through pipeline 20,21 and 22.
In operation the later stage, flow changes as follows：Valve 12,15 is opened, and other valves are closed；Feedstock oil through pipeline 1, with
After the hydrogen mixing of pipeline 7, enter by pipeline 10 in the first reaction zone 1 and carry out hydrofining reaction；Reaction effluent
Enter by pipeline 11, valve 12, pipeline 13 in second reaction zone 2；The effluent of second reaction zone 2 without isolation, by pipe
Line 14, valve 15 and pipeline 16 enter the 3rd reaction zone 3, and progress hydrogenation turns in the presence of hydrogen and hydrocracking catalyst
Change reaction；Flow of the separation of 3rd reaction zone effluent with start of run.
Illustrate the present invention program and effect below by instantiation.
Illustrate technical scheme and effect below by specific embodiment.Raw materials used oil nature is listed in table 1.Institute
Table 2 is listed in catalyst, catalyst A is pretreating catalyst by hydrocracking, and catalyst B is hydrocracking catalyst.
The raw material oil nature of table 1
| Feedstock oil | Catalytic diesel oil | Coal liquefaction diesel oil |
| Density (20 DEG C)/gcm-3 | 0.9375 | 0.9660 |
| Flow/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 |
The catalyst property of table 2
Embodiment 1
Using flow 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.Go into operation initial stage, R2 is short
Road, catalytic cracking diesel oil is mixed into R1 with hydrogen, obtains effluent and enters R3, obtains product, and gas is obtained by separation, fractionation
Body, gasoline products and diesel product.Operation changes flow, R2 incision technological processes after 5500 hours：Catalytic cracking diesel oil and hydrogen
Enter R1 after gas mixing, obtain effluent and enter R2, obtain effluent and enter R3, obtain product and obtain gas by separation and fractionation
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.Technological process is to be catalyzed
After cracked diesel oil is mixed with hydrogen, R1, R2 and R3 are passed sequentially through, isocrackate is by separation and is fractionated, to gas, gasoline
Product and diesel product.Process conditions and product property are shown in Table 4.
Embodiment 2
Using flow 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.Go into operation initial stage, R2 short circuits,
Feedstock oil is mixed into R1 with hydrogen, obtains effluent and enters R3, obtains product, and obtaining gas, gasoline by separation, fractionation produces
Product and diesel product.Operation changes flow, R2 incision technological processes after 5500 hours：Feedstock oil enters R1 after being mixed with hydrogen,
Obtain effluent and enter R2, obtain effluent and enter R3, obtain product and obtain gas, gasoline products and bavin by separation and fractionation
Oil product.Process conditions and product property are shown in Table 5.
The process conditions of table 3 and product property
*：Step b) was switched to after 5000 hours.
The process conditions of table 4 and product property
The process conditions of table 5 and product property
*：Step b) was switched to after 5000 hours.
By the hydroconversion process of the present invention it can be seen from the data result of embodiment and comparative example, vapour can be made
Oil product octane number reaches higher level in the 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 in weighted BMO spaces section, containing aromatics diesel
Cut and hydrogen are by Hydrobon catalyst bed under Hydrofinishing conditions, and then hydrofinishing effluent is in hydro-conversion
Under the conditions of gas-liquid separation is carried out by the hydrogenation conversion catalyst in hydro-conversion section, hydro-conversion effluent, liquid is fractionated into
Obtain gas, gasoline component and diesel component；Wherein hydro-conversion section includes at least two hydroconversion zones, the first hydro-conversion
Include filling in Hydrobon catalyst and hydrocracking catalyst, the second hydroconversion zone according to material engagement sequence in area
Hydrocracking catalyst；Therefore, methods described also includes herein below：
a）One step, wherein using only the second hydroconversion zone, the first hydroconversion zone carries out short circuit, its time is less than hydrogenation
The deactivation time of refining stage；
b）One step, during the step, all hydroconversion zones are used together, by the first hydroconversion zone of short circuit
Series connection is in step a）Before middle the second hydroconversion zone used, and after weighted BMO spaces section.
2. in accordance with the method for claim 1, it is characterised in that the arene content of the cut containing aromatics diesel exists
More than 50wt%, initial boiling point is 50 DEG C ~ 280 DEG C, and 95wt% recovered (distilled) temperatures are 330 DEG C ~ 450 DEG C.
3. in accordance with the method for claim 2, it is characterised in that the arene content of the cut containing aromatics diesel is
60wt%~95wt%.
4. in accordance with the method for claim 2, it is characterised in that the content of polycyclic aromatic hydrocarbon in the cut containing aromatics diesel
In more than 30wt%.
5. according to any described methods of claim 1-4, it is characterised in that described cut containing aromatics diesel splits selected from catalysis
Change the one or more in diesel oil, coal liquefaction diesel oil, coal tar diesel oil distillate.
6. in accordance with the method for claim 1, it is characterised in that in the first described hydroconversion zone, hydrofinishing is catalyzed
The admission space ratio of agent and hydrocracking catalyst is 1:1~1:2.
7. in accordance with the method for claim 1, it is characterised in that described Hydrofinishing conditions are：Hydrogen dividing potential drop 2.0~16.0
MPa, hydrogen to oil volume ratio 300: 1~1500: 1, volume space velocity is 0.1~5.0 h-1, 200 DEG C~450 DEG C of reaction temperature.
8. in accordance with the method for claim 1, it is characterised in that described hydro-conversion condition is：Hydrogen dividing potential drop 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.
9. in accordance with the method for claim 1, it is characterised in that described Hydrobon catalyst is with VI B races and/or the VIIIth
Race's metal is active component, using aluminum oxide or silicon-containing alumina as carrier, on the basis of the weight of catalyst, group VIB metal
Content is calculated as 8wt%~28wt% with oxide, and group VIII metal content is calculated as 2wt%~15wt% with oxide.
10. in accordance with the method for claim 9, it is characterised in that described group VIB metal is Mo and/or W, the VIIIth race
Metal is Co and/or Ni.
11. in accordance with the method for claim 1, it is characterised in that described hydrocracking catalyst include Cracking Component and
Hydrogenation component, Cracking Component includes Y molecular sieve, on the basis of the weight of catalyst, and the content of Y molecular sieve is 10~60%.
12. in accordance with the method for claim 11, it is characterised in that the lattice constant of described Y molecular sieve is 2.425~
2.450nm, the SiO of Y molecular sieve2/Al2O3Mol ratio is 5.0~50.0, and its relative crystallinity is 80%~130%.
13. in accordance with the method for claim 11, it is characterised in that on the basis of the weight of catalyst, described hydrogenation group
The content divided is 5~40 wt%, and hydrogenation component is selected from VI race, the metal of VII race or VIII race, metal oxide or metal sulfide.
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Cited By (1)
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| CN111978986A (en) * | 2019-05-23 | 2020-11-24 | 中国石油化工股份有限公司 | Method for producing gasoline by hydrogenation conversion of aromatic hydrocarbon-containing diesel oil fraction |
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| CN111978986B (en) * | 2019-05-23 | 2021-10-08 | 中国石油化工股份有限公司 | Method for producing gasoline by hydrogenation conversion of aromatic hydrocarbon-containing diesel oil fraction |
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