CN106467758A - A kind of method of group technology processing heavy oil - Google Patents
A kind of method of group technology processing heavy oil Download PDFInfo
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- CN106467758A CN106467758A CN201510518892.9A CN201510518892A CN106467758A CN 106467758 A CN106467758 A CN 106467758A CN 201510518892 A CN201510518892 A CN 201510518892A CN 106467758 A CN106467758 A CN 106467758A
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Abstract
The invention discloses a kind of method of group technology processing heavy oil, the method includes：A, heavy oil is carried out separating treatment, obtain SA1 component and A2A3 component；Wherein, on the basis of the gross mass of SA1 component, in described SA1 component, the total mass fraction of saturated hydrocarbons and mononuclear aromatics is more than 80 mass %；On the basis of the gross mass of A2A3 component, in described A2A3 component, the total mass fraction of monocyclic above aromatic hydrocarbons and colloid is more than 75 mass %, and the mass fraction of monocyclic above aromatic hydrocarbons is more than 35 mass %；B, the SA1 component of gained in step a is carried out the first catalytic cracking reaction, obtain dry gas, liquefied gas, gasoline, diesel oil, coke and cracked fuel oil.The method carries out catalytic cracking reaction respectively by the SA1 component obtained by heavy oil is carried out separating treatment and A2A3 component, has higher gasoline and liquefied gas yield and lower gasoline sulfur nitrogen content.
Description
Technical field
The present invention relates to a kind of method of group technology processing heavy oil.
Background technology
Catalytic cracking process is the secondary operations means of most important light materialization of heavy oil, is liquefied petroleum
The important production process of the light-end products such as gas, gasoline, diesel oil, is to improve constantly heavy oil conversion performance to add
Work process, is also constantly to pursue a goal the process of product selectivity.
It is derived from atmospheric and vacuum distillation unit at present and enter the raw material of heavy oil catalytically cracking equipment processing not from fraction
Make a distinction on composition and its reactivity worth, be all in the form of mixing refining, various raw materials to be mixed
Enter catalytic cracking unit, and and converted under the conditions of same process, not in same reactor
The reactivity worth difference of the different hydro carbons of with good grounds structure takes Optimized Measures respectively.Substantial amounts of easy in raw material
Hydro carbons in conversion together feeds reaction with non-hydrocarbons, condensed-nuclei aromatics, certainly will be in same reaction zone
Interior generation harmful competition absorption, the reaction of the raw material strong to cracking performance produces retardation, thus affecting
The reaction conversion of whole raw material.The reaction rate of the preferable convertible hydrocarbons of reactivity worth is higher, warmer
Just high conversion ratio can be realized under the process conditions of sum, and substantial amounts of condensed ring non-hydrocarbons, condensed ring
Aromatic hydrocarbons and glial response speed are low, need harsher process conditions and longer response time can be only achieved
Preferably conversion level.The distinct hydro carbons of multiple crackings is in same reactor and same process condition
Under reacted, the reactivity worth difference of different hydrocarbons and reaction step inconsistent, reaction can be caused deep
Degree does not optimize and interferes, and has had a strong impact on the catalytic cracking transformation efficiency of whole raw material.
On the developing way of conventional catalytic cracking process and catalyst, continue to along increase heavy oil
Conversion per pass ability is development goal.These technology are mostly by technological operation optimization parameter and catalyst
To strengthen heavy oil catalytic cracking reaction process although these methods can only improve light oil to a certain extent
Yield, improves the distribution of catalytic cracking production.But for processing inferior raw material, only urged by adjustment
Agent composition and technological parameter are often attended to one thing and lose sight of another, and increasing would generally be along with while heavy oil conversion performance
Being significantly increased of dry gas and coke yield, so undoubtedly will lead to heavy oil conversion selectivity to be deteriorated, that is, turn
Obvious contradiction is there is it is difficult to realize the hydrocarbon distribution of hydro carbons between rate and dry gas and coke selectivity
Optimization and oil product maximize.
In heavy oil catalytic cracking process, raw material oil nature, catalyst performance, process conditions (temperature,
Agent oil quality ratio, air speed etc.) etc. factor all product slates are had a major impact, wherein raw material hydro carbons composition
Remain the basis of product slates.Heavy oil feedstock is carried out separate and can carry to a certain extent according to boiling point
The conversion capability of high heavy oil, and improve its products distribution.According to boiling point, raw oil is cut into and relatively easily splits
Change fraction and relatively difficult cracked distillate can weaken the harmful effect of difficult cracked distillate to a certain extent, be
Easily cracked distillate provides a preferable reaction environment, improves product yield and product slates.CN
It is classification point that 102102029 A disclose with 500-540 DEG C, carbon residue gravimetric value for 2～4%, by heavy oil
Raw material is divided into quality raw materials and inferior raw material, its result compared with traditional handicraft, heavy oil classification after, product
Distribution is obviously improved, and yield of light oil improves, and coke and dry gas yield reduce.Button root woods etc. (button root woods,
Chen Jie. the research of Catalytic Cracking of Shengli Vacuun Residue. oil refining design, 1995,25 (2):6-10) profit
With supercritical fluid extraction precision segregation apparatuss, catalytically cracked material is cut into comparative good-quality according to boiling point
With raw material inferior, Shengli VR is divided into 15 components and has investigated the catalytic cracking of front 13 fractions
Performance, experiment shows to become weight with fraction, and yield of light oil reduces successively, and coke yield gradually rises.
Heavy oil is cut into different narrow of boiling spread by the method such as true boiling point distillation or supercritical fluid extraction
Fraction, although boiling spread can be cut very narrow, each narrow fraction remains the mixture of various hydro carbons.
For different fcc raw materials, the larger difference of boiling range scope and chemical constitution and composition determines it
Reactivity worth there is larger difference.It is big that various hydro carbons absorbability on a catalyst presses its strong and weak order
Cause can arrange as follows：Condensed-nuclei aromatics>Condensed ring cycloalkane>Alkene>The mononuclear aromatics of monoalkyl side chain>Cycloalkanes
Hydrocarbon>Alkane.According to the sequence arrangement of chemical reaction rate, then substantially situation is as follows：Alkene>Big point
The mononuclear aromatics of sub- monoalkyl side chain>Isoparaffin and cycloalkane>The monocyclic virtue of small molecule monoalkyl side chain
Hydrocarbon>N-alkane>Condensed-nuclei aromatics.As can be seen that various hydro carbons, non-hydrocarbons are in catalysis in raw material
There is very big difference in the absorption on agent surface and cracking capability, the non-hydrocarbons of condensed ring, condensed-nuclei aromatics and
Condensed ring cycloalkane high adsorption capacity and reaction rate is low, and carry mononuclear aromatics and the macromole of longer side chain
Isoparaffin, cycloalkane absorbability is weak and reaction rate is high, and this has resulted in competing between different hydrocarbons
Strive absorption and the retardation to reaction.High adsorption capacity and the low condensed ring non-hydrocarbons chemical combination of reaction rate
, once occupying catalyst surface first, their reaction rates are slow for thing, condensed-nuclei aromatics, are difficult to be desorbed, or even
Condensation becomes coke and covers in catalyst surface, causes catalyst to inactivate, has had a strong impact on other and be easy to split
Change the reaction rate of hydro carbons.
Based on this, various heavy oil feedstocks do not fed as one " overall ", to take into full account wide boiling range
The larger difference that in heavy oil feedstock, different component cracking performance exists, can will be poor for cracking performance in raw oil
Different larger component carries out catalytic cracking after carrying out separating respectively.
Traditional catalytically cracked material is mainly the vacuum distillate that in refinery, atmospheric and vacuum distillation unit provides.Decompression
Wax oil fraction can be divided into different hydrocarbon system's component such as non-aromatic components and virtue according to the difference of hydrocarbon structure
Hydrocarbon component, saturated hydrocarbon component and aromatic component (without colloid), but the mononuclear aromatics in aromatic component,
The reflex action in catalytic cracking process of double ring arene and polycyclic aromatic hydrocarbon still has larger difference, and current grinds
Study carefully to rarely have in report and carry out catalytic cracking reaction by after aromatic hydrocarbons separation and concentration from raw material of different number of rings
Research.
At present, market to oil product continuous lighting, high quality and the requirement cleaning and oil supply
The aggravation of contradictions of increasingly heaviness, in poor quality, and light, the middle matter oil to high value for China's economic development
The demand of product is continuously increased.Therefore, as how more economical rational cost realizes heavy oil lighting, institute
Obtain product and can meet the oil Refining Technologies of the constantly petrol and diesel oil product specification of harshness again having become domestic and international oil refining
One of technology of technological development business's focus development.
The arene content of catalytic cracking diesel oil is high, and Cetane number is low, and engine ignition poor performance belongs to bad
The diesel oil blending component of matter, has a strong impact on diesel product quality, Shi Ge enterprise diesel product quality upgrading
One of biggest obstacle.Weighted BMO spaces are carried out to faulty wax oil raw material, aromatic hydrocarbons obtains different degrees of saturation,
Except desulfuration, nitrogen, metal impurities, it is re-used as the raw material of catalytic cracking, can be raw according to producing needs
Produce quality product and the intermediate products such as diesel oil, gasoline, such that it is able to improve its Catalytic Cracking Performance, significantly
Improve the structure of product.CN 1896192 A discloses a kind of wax oil hydrogenation process and catalytic cracking is two-way
Method, wax oil enters hydrotreater together with heavy catalytic cycle oil and catalytic cracking diesel oil and reacts
After obtain the products such as gas, hydrotreated naphtha, hydrogenated diesel oil and hydrogenation tail oil, wherein hydrogenation tail oil enters
Catalytic cracking unit reacts, and the method increases light oil yield, reduces coke yield, reduce simultaneously
The arene content of diesel oil and sulfur content simultaneously improve its Cetane number.
Similarly, CN101434865A is also disclosed a kind of heavy distillate hydrotreating and is split with catalysis
Change united method.But these methods are all directly by second-rate catalytic cracking heavy oil and catalytic cracking diesel oil
Mixed with the wax oil raw material containing a large amount of saturated hydrocarbons, the saturated hydrocarbons in wax oil are in hydroprocessing processes
Due on catalyst the effect of acid centre and be easy to be cracked into lighter hydrocarbons, cause gas yield increase, simultaneously
Generate hydrogenation heavy oil proportion less, as catalytic cracking unit charging when lightweight oily yield decline.
Therefore, there is space to be modified in current processing of heavy oil technique.
Content of the invention
It is an object of the invention to provide a kind of method of group technology processing heavy oil, the method is passed through heavy oil
Carry out the SA1 component obtained by separating treatment and A2A3 component carries out catalytic cracking reaction respectively, have
Higher gasoline and liquefied gas yield and lower gasoline sulfur nitrogen content.
To achieve these goals, the present invention provides a kind of method of group technology processing heavy oil, the method
Including：A, heavy oil is carried out separating treatment, obtain SA1 component and A2A3 component；Wherein, with SA1
On the basis of the gross mass of component, in described SA1 component, the total mass fraction of saturated hydrocarbons and mononuclear aromatics is more than
80 mass %；On the basis of the gross mass of A2A3 component, monocyclic above aromatic hydrocarbons in described A2A3 component
It is more than 75 mass % with the total mass fraction of colloid, the mass fraction of monocyclic above aromatic hydrocarbons is more than 35 matter
Amount %；B, the SA1 component of gained in step a is carried out the first catalytic cracking reaction, obtain dry gas,
Liquefied gas, gasoline, diesel oil, coke and cracked fuel oil.
Preferably, wherein, on the basis of the gross mass of SA1 component, saturated hydrocarbons in described SA1 component
It is more than 85 mass % with the total mass fraction of mononuclear aromatics；On the basis of the gross mass of A2A3 component, institute
State monocyclic above aromatic hydrocarbons and colloid in A2A3 component total mass fraction be more than 80 mass %, monocyclic more than
The mass fraction of aromatic hydrocarbons is more than 40 mass %.
Preferably, the method also includes step c：Gained A2A3 component in step a is carried out second urge
Change cracking reaction.
Preferably, the method also includes step d：By gained A2A3 component in step a in hydrotreating
Carry out hydrotreating reaction in the presence of catalyst, obtain hydrogenated oil.
Preferably, the method also includes step e：Gained hydrogenated oil in step d is carried out the 3rd urge
Change cracking reaction, obtain dry gas, liquefied gas, gasoline, diesel oil, coke and cracked fuel oil.
Preferably, the method also includes：The diesel oil that obtains described first catalytic cracking reaction and/or split
Change at least a portion of heavy oil and diesel oil that described 3rd catalytic cracking reaction obtains and/or cracked fuel oil
At least a portion carry out described hydrotreating reaction together with described A2A3 component.
Preferably, the method also includes step f：By in gained hydrogenated oil in step d and step a
Gained SA1 component carries out described first catalytic cracking reaction together, obtain dry gas, liquefied gas, gasoline,
Diesel oil, coke and cracked fuel oil.
Preferably, the method also includes：The diesel oil that obtains described first catalytic cracking reaction and/or split
At least a portion changing heavy oil carries out described hydrotreating reaction together with described A2A3 component.
Preferably, the method also includes：Hydrocracking tail oil is carried out institute together with described SA1 component
State the first catalytic cracking reaction.
Preferably, wherein, described heavy oil be straight run vacuum distillate more than 350 DEG C for the initial boiling point and/
Or secondary processing process gained initial boiling point is more than 350 DEG C of fraction.
Preferably, wherein, described secondary processing process be selected from hydroprocessing processes, hydrocracking process,
At least one in catalytic cracking process and solvent deasphalting process.
Preferably, wherein, separating treatment described in step a is selected from solvent extraction process, Solid-Phase Extraction
Process and at least one in membrane separation method.
Preferably, wherein, described solvent extraction is processed as selected from solvent refining extraction, supercritical fluid extraction
Take and at least one in ion liquid abstraction.
Preferably, wherein, described Solid-Phase Extraction processes and comprises the following steps：First described heavy oil is adopted dilute
Send in fixing phase after releasing dilution agent, obtain the first fixing phase；Then aromatic hydrocarbons and C5-C6Alkane volume
Than for 1：(15-25) the first fixing phase described in solvent washing, obtains described SA1 component and second admittedly
Determine phase；Then aromatic hydrocarbons and monohydric alcohol volume ratio is used to be 1：(0.8-1.5) solvent washing second fixing phase,
Obtain described A2A3 component；Wherein, described fixing phase contains the aluminium oxide of load silver, with described load
On the basis of the gross mass of aluminium oxide of silver, the mass fraction of the silver of load is 0.5-12 mass %.
Preferably, wherein, described fixing phase also contains the oxidation being located at described load silver according to fluid flow direction
The silica gel of aluminum upstream and the aluminium oxide being located at the silver-colored aluminium oxide downstream of described load；In mass, described
The aluminium oxide of silica gel, the aluminium oxide of described load silver and the described aluminium oxide downstream positioned at described load silver
Mass ratio be 1：(2.5-5.0)：(0-1.2)；Wherein, the specific surface area of described aluminium oxide is 50-300
Rice2/ gram, pore volume is 0.1-0.55 ml/g, and the specific surface of described silica gel is 250-850 rice2/ gram,
Pore volume is 0.25-0.99 ml/g.
Preferably, wherein, described diluent is C5-C6Alkane, by volume, described diluent with
The ratio of the volume of heavy oil is (1-10)：1；Described aromatic hydrocarbons is benzene and/or toluene, and described monohydric alcohol is methanol
And/or ethanol；In mass, described fixing phase and the mass ratio of described heavy oil are (8-30)：1.
Preferably, wherein, described in step b, the condition of the first catalytic cracking reaction is：Temperature is
420-520 DEG C, mass space velocity is 2-20 hour-1, oil ratio is (1-10)：1.
Preferably, wherein, described in step c, the condition of the second catalytic cracking reaction is：Temperature is
480-540 DEG C, mass space velocity is 2-20 hour-1, oil ratio is (2-30)：1.
Preferably, wherein, the condition of hydrotreating reaction described in step d is：Hydrogen dividing potential drop is 3-12
MPa, reaction temperature is 280-360 DEG C, and hydrotreating catalyst is the aromatic hydrogenation not containing acid site
Saturation catalyst；The initial boiling point of hydrogenated oil described in step d is 155-175 DEG C.
Preferably, wherein, described in step e, the condition of the 3rd catalytic cracking reaction is：Temperature is
450-540 DEG C, mass space velocity is 2-20 hour-1, oil ratio is (2-30)：1.
Compared with prior art, the present invention is advantageous in that：
1st, the separation of SA1 component and A2A3 component in heavy oil oil is achieved based on isolation technics, for
The SA1 component that dynamic behavior differs greatly and A2A3 component can be respectively in the catalytic cracking of coupling
Under the conditions of individually reacted, both eliminated influencing each other between different hydrocarbons, every kind of hydrocarbon can have been made again
Race reacts under the conditions of optimized, improves the utilization rate of hydrogen in heavy oil, thus saving petroleum resources.
2nd, the solution of the present invention can be connected at a hydrogenation before the catalytic cracking unit of A2A3 component
Reason unit, to realize two kinds of purposes：First, hydrogen addition technology is selective hydrogenation, and A2A3 component occurs
Hydrodesulfurization, hydrodenitrogeneration reaction, and selectivity saturation polycyclic aromatic hydrocarbon and colloid, appropriate saturated bicyclic virtue
Hydrocarbon, mononuclear aromatics saturation is few, and does not almost have acid site on catalyst, the fractional saturation of generation or complete
The macromolecule hydrocarbon of saturation is farthest retained, and producing low-sulphur oil for catalytic cracking unit provides
Quality raw materials, can control catalytic gasoline sulfur nitrogen to contain by controlling the reaction depth of hydrotreating unit simultaneously
Amount；Secondly, all return from the catalytic cracking diesel oil of different catalytic cracking unit outflows and catalytic cracking heavy oil
Return to hydrotreating unit, split as catalysis after the appropriateness hydrogenation saturated reaction of bicyclic above aromatic hydrocarbons therein
Change the charging of unit, producing high-knock rating gasoline for catalytic cracking unit provides high-quality charging.
Catalytic cracking diesel oil and catalytic cracking heavy oil can be returned by the 3, method being provided by the present invention
Hydrotreating unit carries out cracking again after being hydrogenated with, catalytic cracking conversion per pass first does not pursue high conversion
Rate, and pursue the total conversion of whole process, catalytic cracking unit do not produce arene content high, 16
The low catalytic diesel oil of alkane value, reduces the yield of dry gas and coke, improves liquefied gas and high-octane rating vapour
The yield of oil；Secondly the fractionating system of catalytic cracking reaction effluent only fractionates out the lightweights such as gasoline fraction and produces
Product, the theoretical cam curve needed for fractionating column substantially reduces；Finally to the raw material rich in polycyclic aromatic hydrocarbon and colloid
Play diluting effect, the two is more prone to make the conveying of mixed material oil after certain proportion mixing.
4th, increased catalytic cracking process material choice scope, improve the hydrogen utilization rate in raw material, change
It has been apt to products distribution, improved gasoline yield and productivity of propylene, make product restructuring more flexible.
5th, idetified separation process, hydrotreating and catalytic cracking technology are more reasonably integrated, for oil refining
Efficient and refined oil product the rationalization of production process provides a new approach.
6th, heavy oil is carried out separating treatment by the present invention, reduces the sulfur nitrogen content in SA1 component, goes forward side by side
One step reduces the sulfur nitrogen content of SA1 group lease making catalytic cracking products obtained therefrom, in addition, high-sulfur nitrogen content
A2A3 component, can carry out hydrotreating reaction and carry out removing sulfur nitrogen, thus reduce catalytic cracking producing
Sulfur nitrogen content in product.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description
Accompanying drawing is used to provide a further understanding of the present invention, and constitutes the part of description, with
Detailed description below is used for explaining the present invention together, but is not construed as limiting the invention.?
In accompanying drawing：
Fig. 1 is the schematic flow sheet of the first specific embodiment of the inventive method；
Fig. 2 is the schematic flow sheet of the inventive method second specific embodiment；
Fig. 3 is the schematic flow sheet of the third specific embodiment of the inventive method.
Specific embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in detail.It should be appreciated that
Specific embodiment described herein is merely to illustrate and explains the present invention, is not limited to this
Bright.
The present invention provides a kind of method of group technology processing heavy oil, and the method includes：A, heavy oil is entered
Row separating treatment, obtains SA1 component and A2A3 component；Wherein, with the gross mass of SA1 component it is
Benchmark, in described SA1 component, the total mass fraction of saturated hydrocarbons and mononuclear aromatics is more than 80 mass %, excellent
Choosing is more than 85 mass %；On the basis of the gross mass of A2A3 component, in described A2A3 component monocyclic with
The total mass fraction of upper aromatic hydrocarbons and colloid be more than 75 mass %, preferably greater than 80 mass %, monocyclic more than
The mass fraction of aromatic hydrocarbons is more than 35 mass %, preferably greater than 40 mass %；B, by gained in step a
SA1 component carries out the first catalytic cracking reaction, obtain dry gas, liquefied gas, gasoline, diesel oil, coke and
Cracked fuel oil.
According to the present invention, in described SA1 component, mainly contain the saturated hydrocarbons including alkane and cycloalkane
And mononuclear aromatics, remaining can be monocyclic above aromatic hydrocarbons, and wherein said aromatic hydrocarbons is people in the art
Known to member, the present invention repeats no more；Colloid contained by described A2A3 component by residual oil just refers to
The component that heptane solvent obtains after aluminium oxide liquid chromatograph isolates saturated hydrocarbons and aromatic hydrocarbons, specifically may be used
Referring to《Catalytic cracking chemistry and technique》, perhaps friendly work, 2013, Science Press, for example, it is possible to
Separation determination is carried out using RIPP10-90 method of testing, because heavy oil composition can be using full with residual oil
It is bound with hydrocarbon, aromatic hydrocarbons, resin and asphalt, therefore the colloid in heavy oil can also be so defined.
Currently preferred is that, under conditions of meeting the definition of each component, separating treatment should make chain as far as possible
Alkane, cycloalkane and mononuclear aromatics are enriched in SA1 component, and monocyclic above aromatic hydrocarbons and colloid are at utmost
Be enriched in A2A3 component, reduce intersection therebetween.
Present invention aims to different hydrocarbons competitive Adsorption in Conventional catalytic cracking reactor at present,
The hydro carbons of difficult cracking such as polycyclic aromatic hydrocarbon and colloid produce strong adsorption in catalyst surface and are but difficult to cracking, right
The cracking reaction of saturated hydrocarbons produces retardation, leads to quite a few easy cracking hydrocarbons not sufficiently reactive just
It is stripped and enters into the problem gone in product, gained A2A3 component in step a can be carried out by the present invention
Second catalytic cracking reaction.
According to the present invention, because the degree of unsaturation of A2A3 component is higher, therefore the method can also include
Step d：Gained A2A3 component in step a is carried out at hydrogenation in the presence of hydrotreating catalyst
Reason reaction, obtains hydrogenated oil.In the present invention hydrotreating be in order to by hydrogenation make double ring arene,
There is different degrees of saturation in polycyclic aromatic hydrocarbon and colloid, and as few as possible being saturated of mononuclear aromatics, simultaneously
Retain the aromatic hydrocarbons after hydrogenation as much as possible, the therefore hydrotreating of employing is preferably at selective hydrogenation
Reason, the product obtaining is mainly hydrogenated oil, and its yield is preferably not less than 70-99 weight %.Institute
State the distillate that hydrogenated oil refers to that boiling point is 150 DEG C -600 DEG C about, with HT-A2A3 labelling, excellent
The initial boiling point selecting hydrogenated oil is 150 DEG C -250 DEG C, more preferably 155 DEG C -175 DEG C.The present invention is permissible
Control the degree of hydro-upgrading by the yield of hydrogenated oil when controlling hydrotreating, so that it is guaranteed that plus
Both be not result in that gas yield was too high during hydrogen modification, lead to lose too many light oil it is also possible to guarantee after
Continuous catalytic cracking is easily carried out.
According to the present invention, described hydrogenated oil is a kind of good catalyst cracking raw material, the therefore party
Method also includes step e：Gained hydrogenated oil in step d is carried out the 3rd catalytic cracking reaction, obtains
Dry gas, liquefied gas, gasoline, diesel oil, coke and cracked fuel oil；And may further include step f：
Gained hydrogenated oil in step d is carried out together with gained SA1 component in step a described first catalysis
Cracking reaction, obtains dry gas, liquefied gas, gasoline, diesel oil, coke and cracked fuel oil.
According to the present invention, in order to further with the diesel oil of catalytic cracking reaction gained and cracked fuel oil, real
Existing diesel oil and the full conversion of cracked fuel oil, therefore the method can also include after step e：Will be described
The diesel oil that first catalytic cracking reaction obtains and/or at least a portion of cracked fuel oil and the described 3rd are urged
At least a portion changing the diesel oil that obtains of cracking reaction and/or cracked fuel oil is together with described A2A3 component
Carry out described hydrotreating reaction.The method can also include after step f：Described first catalysis is split
The diesel oil that change reaction obtains and/or at least a portion of cracked fuel oil are carried out together with described A2A3 component
Described hydrotreating reaction.The diesel oil of catalytic cracking gained is primarily referred to as in catalytic cracking full distillate product
221 DEG C -343 DEG C about fraction, the cracked fuel oil of gained refers mainly in catalytic cracking full distillate product
More than 350 DEG C fractions.Wherein, in the diesel oil of catalytic cracking gained, bicyclic above arene content can account for 40
More than quality %, further up to 50 mass % more than, this part fraction return hydrotreating unit carries out
Appropriate saturation, proceeds cracking reaction subsequently into catalytic cracking unit, for generating high-knock rating gasoline
High-quality charging is provided；Mass fraction scope in hydrotreating unit mixed feeding for the diesel oil of the present invention is permissible
It is more than 0 to 50 weight %, more preferably higher than 0 to 30 weight %.In described cracked fuel oil bicyclic and
Above arene content can reach more than 40 mass %, further up to 50 mass % more than, this part evaporates
Divide return hydrotreating unit to carry out appropriate saturation, increase hydrogen content, continue subsequently into catalytic cracking unit
Continue and carry out cracking reaction, provide high-quality charging for generating high-knock rating gasoline.The cracked fuel oil of the present invention exists
Mass fraction in hydrotreating unit mixed feeding ranges preferably from the heavy % more than 0 to 50, more preferably
More than 0 to 30 weight %.
According to the present invention it is possible to hydrocracking tail oil is carried out described first together with described SA1 component
Catalytic cracking reaction.Described hydrocracking tail oil refers to uncracked saturation produced by hydrocracking reaction
Hydrocarbon.
According to the present invention, described heavy oil is well-known to those skilled in the art, can exist for initial boiling point
More than 350 DEG C of straight run vacuum distillate and/or secondary processing process gained initial boiling point evaporating more than 350 DEG C
Point, described initial boiling point refers to the minima of oil distillation.Wherein, described secondary processing process can be
In hydroprocessing processes, hydrocracking process, catalytic cracking process and solvent deasphalting process extremely
Few one kind.
According to the present invention, separating treatment described in step a refer to by heavy oil be separated into SA1 component and
The process of A2A3 component, can be to process and membrane separation selected from solvent extraction process, Solid-Phase Extraction
At least one in method, different method for separating and processing can be used alone it is also possible to be used in series.
Described solvent extraction processes and is preferably selected from solvent refining extraction, supercritical fluid extraction and ionic liquid extraction
At least one in taking, can adopt single solvent extraction, it would however also be possible to employ multi-solvent extracts mode, preferably
Mode is extracted using multi-solvent.Described Solid-Phase Extraction process described in solid phase can include detached dowel, true
The equipment such as empty set system, preferably include following steps：First that described heavy oil is solid using sending into after dilution dilution agent
Determine in phase, obtain the first fixing phase；Then aromatic hydrocarbons and C5-C6Alkane volume ratio be 1：(15-25)
The first fixing phase described in solvent washing, obtain described SA1 component and the second fixing phase；Then use aromatic hydrocarbons
It is 1 with monohydric alcohol volume ratio：(0.8-1.5) solvent washing second fixing phase, obtains described A2A3 group
Point；Wherein, described fixing phase contains the aluminium oxide of load silver, with total matter of the aluminium oxide of described load silver
On the basis of amount, the mass fraction of the silver of load is 0.5-12 mass %.Described fixing phase can also contain presses
It is located at the silica gel of the aluminium oxide upstream of described load silver and the oxygen being located at described load silver according to fluid flow direction
Change the aluminium oxide in aluminum downstream；In mass, described silica gel, the aluminium oxide of described load silver and institute's rheme
In described load silver aluminium oxide downstream aluminium oxide mass ratio can be 1：(2.5-5.0)：(0-1.2)；
Wherein, the specific surface area of described aluminium oxide can be 50-300 rice2/ gram, pore volume can be 0.1-0.55
Ml/g, the specific surface of described silica gel can be 250-850 rice2/ gram, pore volume can be 0.25-0.99
Ml/g.Described diluent can be C5-C6Alkane, by volume, described diluent and heavy oil
The ratio of volume can be (1-10)：1；Described aromatic hydrocarbons can be benzene and/or toluene, and described monohydric alcohol is permissible
For methanol and/or ethanol；In mass, described fixing phase and the mass ratio of described heavy oil can be (8-30)：
1.
According to the present invention, described catalytic cracking reaction is well-known to those skilled in the art, and the present invention is not
Repeat again.According to the difference of reaction raw materials, the condition of catalytic cracking reaction can be different, for example, step
Described in b, the condition of the first catalytic cracking reaction can be：Temperature is 420-520 DEG C, preferably
480-520 DEG C, mass space velocity is 2-20 hour-1, preferably 15-20 hour-1, oil ratio is (1-10)：
1, preferably (2-6)：1.Described in step c, the condition of the second catalytic cracking reaction can be：Temperature
For 480-540 DEG C, preferably 480-520 DEG C, mass space velocity is 2-20 hour-1, preferably 15-20 is little
When-1, oil ratio is (2-30)：1, preferably (2-6)：1.3rd catalytic cracking described in step e
Reaction condition can be：Temperature is 450-540 DEG C, preferably 480-520 DEG C, and mass space velocity is 2-20
Hour-1, preferably 15-20 hour-1, oil ratio is (2-30)：1, preferably (2-6)：1.
According to the present invention, described hydrotreating reaction is well-known to those skilled in the art, and the present invention is not
Repeat again.The condition of hydrotreating reaction described in step d can be：Hydrogen dividing potential drop is 3-12 MPa,
Reaction temperature is 280-360 DEG C, and hydrotreating catalyst is that the aromatic hydrogenation saturation not containing acid site is urged
Agent；The initial boiling point of hydrogenated oil described in step d is 155-175 DEG C.
The three kind specific embodiments of the inventive method are provided below, but the present invention is not limited to this.
The first specific embodiment of the present invention is as shown in Figure 1：
Heavy oil is carried out having obtained SA1 component and A2A3 component after separating treatment, by the SA1 of gained
Component and A2A3 component carry out the first catalytic cracking reaction and the second catalytic cracking reaction respectively, are done
Air-liquid activating QI, gasoline, diesel oil, coke and cracked fuel oil.Meanwhile, can by hydrocracking tail oil with
Carry out the first catalytic cracking reaction together after the mixing of SA1 component.
The second specific embodiment of the present invention is as shown in Figure 2：
Heavy oil is carried out having obtained SA1 component and A2A3 component after separating treatment, by the SA1 of gained
Component carries out the first catalytic cracking reaction, obtains dry gas, liquefied gas, gasoline, diesel oil, coke and cracking
Heavy oil；Gained A2A3 component is carried out hydrotreating reaction, the hydrogenated oil obtaining carries out the 3rd and urges
Change cracking reaction, obtain dry gas, liquefied gas, gasoline, diesel oil, coke and cracked fuel oil；By gained
Diesel oil and cracked fuel oil carry out hydrotreating reaction, obtain hydrogenated oil.Meanwhile, hydrogenation can be split
Carry out the first catalytic cracking reaction together with changing after tail oil is mixed with SA1 component.
The third specific embodiment of the present invention is as shown in Figure 3：Heavy oil is carried out obtaining after separating treatment
SA1 component and A2A3 component, gained A2A3 component carried out hydrotreating reaction, obtaining plus
Hydrogen generate oil carries out the first catalytic cracking reaction together with SA1 component, obtain dry gas, liquefied gas, gasoline,
Diesel oil, coke and cracked fuel oil；The diesel oil of gained and cracked fuel oil are carried out hydrotreating reaction, obtains
Hydrogenated oil.Meanwhile, together with after hydrocracking tail oil being mixed with SA1 component be hydrogenated to
Oil carries out the first catalytic cracking reaction.
The present invention will be further illustrated by embodiment below, but the present invention will not therefore be taken office
What limits.Reagent and instrument that the embodiment of the present invention is adopted, if no special instructions, are this area normal
The instrument of rule and reagent.
The catalytic cracking reaction taken in the embodiment of the present invention and comparative example produces in KTI company of the U.S.
Carry out on ACE Model AP device, in experiment, catalyst loading amount is 9g, reaction temperature is 500 DEG C,
Mass space velocity is 16 hours-1, agent/oil quality ratio (C/O) is 4.After experiment parameter is stable, enter anti-
Answer program, catalyst is in self gravitation and N2Effect is lower to enter reactor, and raw oil promotes in plunger displacement pump
Lower edge charging tubule enters in reactor catalyst fluidized-bed layer, contacts instead with the catalyst granules of fluidisation state
Should, adopt N simultaneously2Stripping 600-900s.Product is by N2Circulation of qi promoting is entered in the liquid receipts bottle bringing -10 DEG C into
Liquid separates, and gaseous product is collected and completed by Agilent 6890 GC (TCD detector) on-line analyses group
Become；Weighed off line after liquid product collection, is simulated distillation respectively and gasoline detailed hydrocarbon analysis (adopts
RIPP81-90 method of testing is tested), the fraction cut point of gasoline and diesel oil be respectively 221 DEG C and
343℃；Green coke catalyst carries out coke and sulfur content after drawing off on multi EA 2000 carbon and sulfur analytical instrument
Analysis (being tested using RIPP106-90 method of testing), all product qualities add and calculate material puts down
Weighing apparatus.
In embodiment and comparative example using the trade mark that Sinopec catalyst company limited produces it is
, as experiment catalyst, its micro-activity can be by existing skill for the catalytic cracking catalyst of MLC-500
RIPP92-90 measuring method measurement in art, basic physical properties are listed in table 3.
The 500mL essence that the hydroprocessing processes of embodiment produce in Yantai Ke Li Chemical Equipment Co., Ltd.
Carry out in close autoclave, this reactor heating power is 1.5K weight, and dischargeable capacity is 0.5L,
High rotating speed 1500rpm.A certain amount of A2A3 is added in reactor, the catalyst being adopted is oil
In the sulphided state catalyst of 40～60 mesh, the trade mark is RIB-429 to the granularity that work research institute produces.With
By after air displacement in kettle, unlatchings speed of agitator is 338rpm to hydrogen, starts simultaneously at temperature programming to anti-
Temperature is answered to be 340 DEG C, after reaching design temperature, hydrogen dividing potential drop is adjusted to 5MPa, and speed of agitator is 985rpm,
After response time terminates for 12h reaction, ON cycle condensed water cooling down, to room temperature, uses N2Displacement
Gas reactor is vented for several times afterwards, carries out fraction cutting to the product liquid of product liquid in kettle, is hydrogenated with
Generate oily HT-A2A3.
SA1 component, hydrocarbon system's composition of A2A3 component, HT-A2A3 component and HCW adopt
RIPP10-90 method of testing is tested.
The RIPP method of testing of the present invention be selected from《Petrochemical Engineering Analysis method (RIPP test method)》,
Yang Cui surely waits and compiles, Science Press, and 1990.
Embodiment 1
The present embodiment is used for illustrating that in the method for group technology processing heavy oil that the present invention provides, heavy oil separates
The implementation of unit.In detached dowel, (specific surface area is 152 meters to bottom filling 30g neutral alumina2/ gram, pore volume is 0.213 ml/g), the aluminium oxide of middle filling 110g load silver ion be (silver
Mass fraction is 7.05 mass %, using the preparation of silver nitrate dipping method), upper strata filling 30g silica gel (ratio
Surface area is 479 meters2/ gram, pore volume is 0.349 ml/g)；By detached dowel lower end and evacuation system
System is connected.The cumulative volume of fixing phase is 150mL.(VGO, during Tahe Crude Oil is taken to take decompressed wax oil
State's petrochemical industry northwest branch company system in Tahe Oilfield, obtains Tahe in Research Institute of Petro-Chemical Engineering through true boiling point distillation
Decompressed wax oil) sample 10.06g (11.07mL), it is dissolved in 30mL normal hexane, first use 100mL's
The fixing phase of filling in the above-mentioned detached dowel of normal hexane moistening, then the hexane solution of above-mentioned oil sample is added to
In detached dowel.Use 255mL toluene respectively：Normal hexane volume ratio is 1：19 solvent washing goes out SA1
Component, 255mL toluene：Ethanol volume ratio is 1：1 solvent washing goes out A2A3 component.Using rotation
Turn the solvent that vaporizer is evaporated in SA1 component and A2A3 component, obtain SA1 component 6.46g, A2A3
Component 3.49g, 0.11 gram of loss.Raw oil used in embodiment, comparative example and the Asia after separation
The basic physical properties data of component is listed in table 1, and hydrocarbon system's composition data of subfraction SA1, A2A3 is listed in table 2.
Embodiment 2
As shown in figure 1, the SA1 component of embodiment 1 gained and A2A3 component are split as catalysis
Change raw material, reaction temperature be 500 DEG C, agent oil quality ratio for 4, air speed is 16 hours-1Under conditions of
Carry out the first catalytic cracking reaction and the second catalytic cracking reaction, its conversion ratio, total liquid yield, light oil are received
Rate, also six kinds of primary product dry gas, liquefied gas, gasoline, yields of diesel oil, cracked fuel oil and coke,
Sulfur content in gasoline and nitrogen content, as shown in table 4.
From table 4, data can be seen that compared with the experimental result of the direct catalytic cracking of VGO, by S
With A2A3 component after the liquefied gas of catalytic cracking gained, gasoline collect respectively respectively, liquefied gas, gasoline
Yield summarized results 1 are respectively higher than liquefied gas, the gasoline yield that wax oil directly carries out catalytic cracking, simultaneously
Sulfur content in gasoline and nitrogen content are less than content of sulfur in gasoline and the nitrogen content of the direct catalytic cracking of wax oil, this
Illustrate first to carry out heavy oil carrying out catalytic cracking again after separating treatment using the method for the present invention, obtained
High-value product yield and property are superior to heavy oil directly carries out the product of catalytic cracking.
Embodiment 3
As shown in Fig. 2 by the SA1 component of embodiment 1 gained reaction temperature be 500 DEG C, agent oil
Amount ratio is 4, and air speed is 16 hours-1Under conditions of carry out the first catalytic cracking；A2A3 group by gained
Divide and carry out hydrotreating in accurate autoclave, the initial boiling point obtaining is 160 DEG C of hydrogenated oils
(HT-A2A3, hydrocarbon system composition as shown in table 2), reaction temperature be 500 DEG C, agent oil quality ratio for 4,
Air speed is 16 hours-1Under conditions of carry out the 3rd catalytic cracking；First catalytic cracking and the 3rd catalysis are split
Change the catalytic cracking diesel oil of gained and catalytic cracking heavy oil returns hydrotreating and uses；The conversion ratio of raw material,
Total liquid yield, yield of light oil, also six kinds of primary product dry gas, liquefied gas, gasoline, diesel oil, crackings
Heavy oil and the yield of coke, the sulfur content in gasoline and nitrogen content, as shown in table 5.
From table 5, data can be seen that the experimental result with the direct catalytic cracking of VGO in comparative example 1
Compare, by SA1 component in embodiment 2 and HT-A2A3 component respectively the liquefied gas of catalytic cracking gained,
After gasoline collects respectively, liquefied gas, gasoline yield summarized results 2 are respectively higher than wax oil and are directly catalyzed
The liquefied gas of cracking, gasoline yield, the sulfur content in gasoline and nitrogen content are direct significantly lower than wax oil simultaneously
The content of sulfur in gasoline of catalytic cracking and nitrogen content, illustrate first to carry out heavy oil separating using the method for the present invention
Carry out catalytic cracking again, obtained high-value product yield and property are better than after process and hydrotreating
Directly heavy oil is carried out the product of catalytic cracking.
Embodiment 4
As shown in figure 3, the A2A3 component of embodiment 1 gained is carried out adding in accurate autoclave
Hydrogen is processed, and the initial boiling point obtaining is that (HT-A2A3, hydrocarbon system forms as table 2 institute 160 DEG C of hydrogenated oils
Show), HT-A2A3 together with the SA1 component of embodiment 1 gained reaction temperature be 500 DEG C, agent oil
Mass ratio is 4, and air speed is 16 hours-1Under conditions of carry out the first catalytic cracking；By the first catalytic cracking
The catalytic cracking diesel oil of gained and catalytic cracking heavy oil return hydrotreating and use；The conversion ratio of raw material, total
Liquid is received, yield of light oil, also six kinds of primary product dry gas, liquefied gas, gasoline, diesel oil, cracking weights
Oil and yield, the sulfur content in gasoline and the nitrogen content of coke, as shown in table 6.
From table 6, data can be seen that compared with the experimental result of the direct catalytic cracking of VGO, S and
The liquefied gas of catalytic cracking, gasoline yield are respectively higher than wax oil and are directly catalyzed HT-A2A3 component together
The liquefied gas of cracking, gasoline yield, the sulfur content in gasoline and nitrogen content are direct significantly lower than wax oil simultaneously
The content of sulfur in gasoline of catalytic cracking and nitrogen content, illustrate first to carry out heavy oil separating using the method for the present invention
Carry out catalytic cracking again, obtained high-value product yield and property are better than after process and hydrotreating
Directly heavy oil is carried out the product of catalytic cracking.
Embodiment 5
By the SA1 component of embodiment 1 gained and hydrocracking tail oil, (HCW, from petrochemical industry section
Learn academy and be hydrocracked middle- scale device, as shown in table 1, hydrocarbon system's composition is as shown in table 2 for fundamental property)
With 1：The mixture of 1 mass ratio mixing reaction temperature be 500 DEG C, agent oil quality ratio for 4, air speed
For 16 hours-1Under conditions of carry out catalytic cracking reaction, its conversion ratio, total liquid yield, yield of light oil,
Also has six kinds of primary product dry gas, liquefied gas, gasoline, yields of diesel oil, cracked fuel oil and coke, vapour
Sulfur content in oil and nitrogen content, as shown in table 7.
As can be seen from Table 7, carry out catalytic cracking by after SA1 component and hydrocracking tail oil mixing,
Gained liquefied gas and gasoline products yield are high and sulfur in gasoline nitrogen content is low.
Comparative example 1
By VGO directly as catalytically cracked material, enter catalytic cracking unit, in reaction temperature be
500 DEG C, agent oil quality ratio for 4, air speed is 16 hours-1Under conditions of carry out catalytic cracking reaction, its
Conversion ratio, total liquid yield, yield of light oil, also six kinds of primary product dry gas, liquefied gas, gasoline, bavins
Yield, the sulfur content in gasoline and the nitrogen content such as table 4 of oil, cracked fuel oil and coke, shown in 5,6.
Table 1 heavy oil feedstock and the fundamental property of each hydrocarbon system component.
Table 2 is hydrocarbon system's composition of SA1, A2A3, HT-A2A3 and HCW, and in table, data unit is
Mass percent is attached most importance to %.
| Hydrocarbon types | SA1 | A2A3 | HT-A2A3 | HCW |
| Total saturated hydrocarbons | 74.9 | 0 | 23.6 | 99.4 |
| Total aromatic hydrocarbons | 25.1 | 77.2 | 76.4 | 0.6 |
| Total mononuclear aromatics | 19.1 | 12.0 | 37.6 | 0.6 |
| Total double ring arene | 3.1 | 14.3 | 26.2 | 0 |
| Bicyclic above aromatic hydrocarbons | 2.9 | 50.9 | 12.6 | 0 |
| Colloid | 0 | 22.8 | 0 | 0 |
| Amount to | 100 | 100 | 100 | 100 |
Table 3 is the basic physical properties of MLC-500.
| Project | MLC-500 |
| Physical property | |
| Specific surface area/(m2·g-1) | 122 |
| Pore volume/(cm3·g-1) | 0.184 |
| Granularity, mesh | 70～270 |
| Chemical composition (w), % | |
| Na2O | 0.25 |
| Al2O3 | 56.4 |
| SiO2 | 36.9 |
| RE2O3 | 3.7 |
| Micro-activity (12 hours aging) | 69 |
Table 4 is the experimental data of embodiment 2 and comparative example 1.
Table 5 is the experimental data of embodiment 3 and comparative example 1.
Table 6 is the experimental data of embodiment 4 and comparative example 1.
| Project | Embodiment 4 | Comparative example 1 |
| Raw material | SA1+(HT-A2A3) | VGO |
| Reaction temperature/DEG C | 500 | 500 |
| Air speed/h-1 | 16 | 16 |
| Catalyst | MLC-500 | MLC-500 |
| Oil ratio (C/O) | 4 | 4 |
| Conversion ratio (weight), % | 77.16 | 61.11 |
| Yield of light oil (weight), % | 73.59 | 64.52 |
| Total liquid yield (weight), % | 91.67 | 76.71 |
| Product yield (weight), % | ||
| Dry gas | 0.97 | 1.26 |
| Liquefied gas | 18.09 | 12.19 |
| Gasoline | 56.47 | 44.44 |
| Diesel oil | 17.12 | 20.08 |
| Cracked fuel oil | 5.13 | 18.81 |
| Coke | 1.63 | 3.23 |
| Gasoline property | ||
| Sulfur content (weight), μ g/g | 9.66 | 209.5 |
| Nitrogen content (weight), μ g/g | 1.66 | 7.38 |
Table 7 is the experimental data of embodiment 5.
| Project | Embodiment 5 |
| Raw material | SA1+HCW |
| Reaction temperature/DEG C | 500 |
| Air speed/h-1 | 16 |
| Catalyst | MLC-500 |
| Oil ratio (C/O) | 4 |
| Conversion ratio (weight), % | 89.89 |
| Yield of light oil (weight), % | 71.72 |
| Total liquid yield (weight), % | 95.91 |
| Product yield (weight), % | |
| Dry gas | 0.84 |
| Liquefied gas | 24.20 |
| Gasoline | 63.48 |
| Diesel oil | 8.23 |
| Cracked fuel oil | 1.87 |
| Coke | 1.37 |
| Total | 100 |
| Gasoline property | |
| Sulfur content (weight), μ g/g | 6.95 |
| Nitrogen content (weight), μ g/g | 0.04 |
Claims (20)
1. a kind of method of group technology processing heavy oil, the method includes：
A, heavy oil is carried out separating treatment, obtain SA1 component and A2A3 component；Wherein, with SA1
On the basis of the gross mass of component, in described SA1 component, the total mass fraction of saturated hydrocarbons and mononuclear aromatics is more than
80 mass %；On the basis of the gross mass of A2A3 component, monocyclic above aromatic hydrocarbons in described A2A3 component
It is more than 75 mass % with the total mass fraction of colloid, the mass fraction of monocyclic above aromatic hydrocarbons is more than 35 matter
Amount %；
B, the SA1 component of gained in step a is carried out the first catalytic cracking reaction, obtain dry air-liquid
Activating QI, gasoline, diesel oil, coke and cracked fuel oil.
2. method according to claim 1, wherein, on the basis of the gross mass of SA1 component, described
In SA1 component, the total mass fraction of saturated hydrocarbons and mononuclear aromatics is more than 85 mass %；With A2A3 component
Gross mass on the basis of, in described A2A3 component, the total mass fraction of monocyclic above aromatic hydrocarbons and colloid is more than
80 mass %, the mass fraction of monocyclic above aromatic hydrocarbons is more than 40 mass %.
3. method according to claim 1, the method also includes step c：By gained A2A3 in step a
Component carries out the second catalytic cracking reaction.
4. method according to claim 1, the method also includes step d：By gained A2A3 in step a
Component carries out hydrotreating reaction in the presence of hydrotreating catalyst, obtains hydrogenated oil.
5. method according to claim 4, the method also includes step e：Gained in step d is hydrogenated with
Generate oil and carry out the 3rd catalytic cracking reaction, obtain dry gas, liquefied gas, gasoline, diesel oil, coke and split
Change heavy oil.
6. method according to claim 5, the method also includes：By described first catalytic cracking reaction
The diesel oil obtaining and/or at least a portion of cracked fuel oil and described 3rd catalytic cracking reaction obtain
At least a portion of diesel oil and/or cracked fuel oil carries out described hydrotreating together with described A2A3 component
Reaction.
7. method according to claim 4, the method also includes step f：Gained in step d is hydrogenated with
Generate oil carries out described first catalytic cracking reaction together with gained SA1 component in step a, obtain dry gas,
Liquefied gas, gasoline, diesel oil, coke and cracked fuel oil.
8. method according to claim 7, the method also includes：By described first catalytic cracking reaction
The diesel oil obtaining and/or at least a portion of cracked fuel oil carry out described adding together with described A2A3 component
Hydrogen processes reaction.
9. the method according to any one in claim 1-8, the method also includes：To be hydrogenated with
Cracking tail oil carries out described first catalytic cracking reaction together with described SA1 component.
10. method according to claim 1, wherein, described heavy oil is initial boiling point more than 350 DEG C
The straight run vacuum distillate and/or secondary processing process gained initial boiling point fraction more than 350 DEG C.
11. methods according to claim 10, wherein, described secondary processing process is at hydrogenation
At least one in reason process, hydrocracking process, catalytic cracking process and solvent deasphalting process.
12. methods according to claim 1, wherein, separating treatment described in step a is selected from solvent
At least one in extraction processing, Solid-Phase Extraction process and membrane separation method.
13. methods according to claim 12, wherein, described solvent extraction is processed as selected from solvent essence
At least one in system extraction, supercritical fluid extraction and ion liquid abstraction.
14. methods according to claim 12, wherein, described Solid-Phase Extraction processes and comprises the following steps：
First described heavy oil is sent in fixing phase using after dilution dilution agent, obtain the first fixing phase；Then
Aromatic hydrocarbons and C5-C6Alkane volume ratio be 1：(15-25) described in solvent washing, the first fixing phase, obtains
To described SA1 component and the second fixing phase；Then aromatic hydrocarbons and monohydric alcohol volume ratio is used to be 1：(0.8-1.5)
Solvent washing second fixing phase, obtain described A2A3 component；Wherein, described fixing phase contains load
The aluminium oxide of silver, on the basis of the gross mass of the aluminium oxide of described load silver, the mass fraction of the silver of load
For 0.5-12 mass %.
15. methods according to claim 14, wherein, described fixing phase also contains according to fluid flow direction
Positioned at the silica gel of the aluminium oxide upstream of described load silver and positioned at the described aluminium oxide downstream loading silver
Aluminium oxide；In mass, described silica gel, described load silver aluminium oxide and described positioned at described load
The mass ratio of the aluminium oxide in aluminium oxide downstream of silver is 1：(2.5-5.0)：(0-1.2)；Wherein, described oxygen
The specific surface area changing aluminum is 50-300 rice2/ gram, pore volume is 0.1-0.55 ml/g, the ratio of described silica gel
Surface is 250-850 rice2/ gram, pore volume is 0.25-0.99 ml/g.
16. methods according to claim 14, wherein, described diluent is C5-C6Alkane, with body
Long-pending meter, described diluent is (1-10) with the ratio of the volume of heavy oil：1；Described aromatic hydrocarbons is benzene and/or toluene,
Described monohydric alcohol is methanol and/or ethanol；In mass, described fixing phase and the mass ratio of described heavy oil are
(8-30)：1.
17. methods according to claim 1, wherein, the first catalytic cracking reaction described in step b
Condition is：Temperature is 420-520 DEG C, and mass space velocity is 2-20 hour-1, oil ratio is (1-10)：1.
18. methods according to claim 3, wherein, the second catalytic cracking reaction described in step c
Condition is：Temperature is 480-540 DEG C, and mass space velocity is 2-20 hour-1, oil ratio is (2-30)：1.
19. methods according to claim 4, wherein, the condition of hydrotreating reaction described in step d
For：Hydrogen dividing potential drop is 3-12 MPa, and reaction temperature is 280-360 DEG C, and hydrotreating catalyst is not contain
The hydrocatalyst for saturating arylhydrocarbon in acid site；The initial boiling point of hydrogenated oil described in step d is
155-175℃.
20. methods according to claim 5, wherein, the 3rd catalytic cracking reaction described in step e
Condition is：Temperature is 450-540 DEG C, and mass space velocity is 2-20 hour-1, oil ratio is (2-30)：1.
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