CN108707475A - A kind of method of catalytic cracking diesel oil and the method for processing poor ignition quality fuel - Google Patents
A kind of method of catalytic cracking diesel oil and the method for processing poor ignition quality fuel Download PDFInfo
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- CN108707475A CN108707475A CN201810524730.XA CN201810524730A CN108707475A CN 108707475 A CN108707475 A CN 108707475A CN 201810524730 A CN201810524730 A CN 201810524730A CN 108707475 A CN108707475 A CN 108707475A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1048—Middle distillates
-
- 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
- C10G2300/1048—Middle distillates
- C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
-
- 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
- C10G2300/1048—Middle distillates
- C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/30—Physical properties of feedstocks or products
- C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
-
- 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 method of catalytic cracking diesel oil and the methods for processing poor ignition quality fuel, are related to technical field of petrochemical industry.The method of the catalytic cracking diesel oil includes obtaining adding hydrogen light cycle oil after the light cycle oil that the first fractionating column and after-fractionating tower generate is carried out hydrofinishing；Hydrogen light cycle oil will be added to carry out component analysis, to determine cut point；Hydrogen light cycle oil will be added to be separated into light fraction and heavy distillat by fractionating column；The heavy-cycle oil that heavy distillat and the first fractionating column generate is subjected to solvent pairs liquid-liquid extraction, obtains the extraction oil rich in aromatic hydrocarbons and the raffinate oil rich in saturated hydrocarbons；Raffinate oil and light fraction are passed through the second riser reactor and carry out catalytic cracking.The method of the processing poor ignition quality fuel includes the method for above-mentioned catalytic cracking diesel oil, and the two can promote the yield of gasoline in product, reduce diesel yield and coke output.
Description
Technical field
The present invention relates to technical field of petrochemical industry, and the method for more particularly to a kind of catalytic cracking diesel oil and processing are inferior
The method of diesel oil.
Background technology
Country's refinery FCC apparatus LCO (light cycle oil) Cetane number is generally relatively low at present, and derv fuel Cetane number is wanted
It asks and is being continuously improved, the V automobile-used 0# diesel oil standards of state on January 1st, 2017, implementation then require Cetane number to be not less than 51, therefore
It is difficult to meet refinery's reconciliation production derv fuel so that certain catalytic cracking light cycle oils are after hydrogenated refined or modification
Demand, and hydro-upgrading needs to consume a large amount of hydrogen and extremely low reaction velocity, and plant construction and operating cost are very high,
It has not been economically feasible route.
Domestic refinery is generally by HCO (heavy-cycle oil) freshening, in order to which by useful component " eating dry squeeze only ", freshening compares
Height reduces the treating capacity of catalytic unit；And a large amount of polycyclic aromatic hydrocarbon is condensed green coke in riser reactor in HCO, it will not
The yield for increasing purpose product gasoline instead results in dry gas and is increased with coke yield.
Invention content
The purpose of the present invention is to provide a kind of methods of catalytic cracking diesel oil, it is intended to promote the yield of gasoline in product.
Another object of the present invention is to provide a kind of methods of processing poor ignition quality fuel, can be obviously improved in product high
Octane rating gasoline content.
The present invention solves its technical problem using following technical scheme to realize.
The present invention proposes a kind of method of catalytic cracking diesel oil, and fcc raw material is carried out by the first riser reactor
The catalytic cracking production of first riser reactor is passed through the first fractionating column by catalytic cracking, by the second riser reactor
Catalytic cracking production is passed through after-fractionating tower, includes the following steps：
It is obtained after the light cycle oil that first fractionating column is generated with after-fractionating tower is carried out hydrofinishing plus hydrogen gently recycles
Oil；
Hydrogen light cycle oil will be added to carry out component analysis, to determine cut point；
Will plus hydrogen light cycle oil be separated into light fraction and heavy distillat by fractionating column, and the operating condition of fractionating column is according to cutting
Cutpoint is determined；
The heavy-cycle oil that heavy distillat and the first fractionating column generate is subjected to solvent pairs liquid-liquid extraction, obtains the extraction rich in aromatic hydrocarbons
Take oil and the raffinate oil rich in saturated hydrocarbons；
Raffinate oil and light fraction are passed through the second riser reactor and carry out catalytic cracking；
Wherein, the extractant in solvent pairs liquid-liquid extraction include the first extractant and the second extractant, first
Extractant is furfural or dimethyl sulfoxide (DMSO), and the second extractant is petroleum ether or 6# solvent naphthas.
The present invention also proposes a kind of method of processing poor ignition quality fuel comprising the method for above-mentioned catalytic cracking diesel oil.
The embodiment of the present invention provides a kind of advantageous effect of the method for catalytic cracking diesel oil：It uses double lifting leg to react
Device carries out catalytic cracking, and the first riser reactor is main riser, is mainly used for processing catalytically cracked material, the second riser
Reactor processes light fraction and enriched saturated hydrocarbon oil；The reaction product of first riser reactor is detached by the first fractionating column
Gasoline, light cycle oil, heavy-cycle oil and slurry oil are obtained, the reaction product of the second riser reactor is carried out by after-fractionating tower
Isolated gasoline and light cycle oil；After the light cycle oil that first fractionating column and after-fractionating tower generate is carried out hydrofinishing
It obtains adding hydrogen light cycle oil, then light fraction and heavy distillat is obtained after being fractionated, the weight that heavy distillat and the first fractionating column are generated
Recycle oil carries out solvent pairs liquid-liquid extraction, obtains the extraction oil rich in aromatic hydrocarbons and the raffinate oil rich in saturated hydrocarbons；Finally by raffinate
Oil is passed through the second riser reactor with light fraction and carries out catalytic cracking.It can be obtained using catalyst cracking method provided by the invention
Higher yield of gasoline is obtained, and reduces the green coke of catalysis, improves the selectivity of product distribution.The present invention also provides a kind of processing
The method of poor ignition quality fuel comprising the method for above-mentioned catalytic cracking diesel oil, yield of gasoline is high in the product being likewise supplied with
Advantage meets the policy requirements of country.
Description of the drawings
In order to illustrate the technical solution of the embodiments of the present invention more clearly, below will be to needed in the embodiment attached
Figure is briefly described, it should be understood that the following drawings illustrates only certain embodiments of the present invention, therefore is not construed as pair
The restriction of range for those of ordinary skill in the art without creative efforts, can also be according to this
A little attached drawings obtain other relevant attached drawings.
Fig. 1 is the corresponding production equipment flow chart of method of catalytic cracking diesel oil provided in an embodiment of the present invention.
Icon：1- hydrofining reactors；2- reaction effluents；3- high-pressure separators；4- circulating hydrogens；5- liquid phases are produced
Object；6- strippers；7- gasoline；8- refined diesel oils；9- refined diesel oils；10- fractionating columns；11- light fractions；12- heavy distillat；13- liquid
Liquid extraction tower；14- raffinate oil；15- extraction oils；16- strippers；17- extractants；18- richness aromatic naphtha；19- steam；20- vapour
Stripper；21- extractants；22- enriched saturated hydrocarbon oil；23- steam；24- solvent tanks；The first extractants of 25-；26- contains extraction
The water of solvent；27- dehydrating towers；28- solvents；29- sewage；30- steam；The second riser reactors of 31-；The second settlers of 32-；
33- reaction products；The first settlers of 34-；35- external warmers；36- fcc raw materials；The main riser reactors of 37-；38- reaction productions
Object；39- main fractionating towers；40- gases；41- gasoline；42-LCO；43-HCO；44- slurry oils；45- pair fractionating columns；46- gases；47-
Gasoline；48-LCO；49- slurry oils；The second extractants of 50-；The parts 51- are outer to get rid of.
Specific implementation mode
It in order to make the object, technical scheme and advantages of the embodiment of the invention clearer, below will be in the embodiment of the present invention
Technical solution be clearly and completely described.The person that is not specified actual conditions in embodiment, builds according to normal condition or manufacturer
The condition of view carries out.Reagents or instruments used without specified manufacturer is the conventional production that can be obtained by commercially available purchase
Product.
The method to catalytic cracking diesel oil provided in an embodiment of the present invention and the method for processing poor ignition quality fuel have below
Body explanation.
A kind of method of catalytic cracking diesel oil provided in an embodiment of the present invention, uses duo-lift tube reactor to be catalyzed
Cracking, the first riser reactor are main riser, are mainly used for processing catalytically cracked material, the processing of the second riser reactor
Light fraction and enriched saturated hydrocarbon oil；The reaction product of first riser reactor by the first fractionating column carry out isolated gasoline,
The reaction product of light cycle oil, heavy-cycle oil and slurry oil, the second riser reactor is isolated by the progress of after-fractionating tower
Gasoline and light cycle oil.Include the following steps：
S1, hydrofinishing
Specifically, it obtains adding hydrogen after the light cycle oil that the first fractionating column and after-fractionating tower generate being carried out hydrofinishing
Light cycle oil.
A large amount of aromatic hydrocarbons is mainly based on mononuclear aromatics, double ring arene in LCO, also the aromatic hydrocarbons of part tricyclic, in addition
There is also a certain proportion of alkane, cycloalkane or alkene in LCO.LCO is unstable after hydrofinishing desulfurization, denitrogenation
Alkadienes is saturated, and the bicyclic aromatic ring with thrcylic aromatic hydrocarbon in part is saturated, and saturated hydrocarbons and mononuclear aromatics contain in hydrogenation products
Amount will greatly improve, and especially the mononuclear aromatics content with side chain can reach 50 weight % or more.Mononuclear aromatics with side chain is
The precursor of antiknock component, these mononuclear aromatics side chains with side chain are easily broken, and chain can enter gasoline on rear side of cracking
Component, and the mononuclear aromatics of remaining shorter side chain also just enters gasoline fraction, this part is high octane gasoline component.
Specifically, it is controlled in LCO and the parameter in hydrogen contact process, to reach better refining effect.
In subtractive process, reaction temperature is 250-450 DEG C, hydrogen partial pressure 1-12MPa, liquid hourly space velocity (LHSV) 0.3-10h-1, hydrogen to oil volume ratio
For 100-1500Nm3/m3；Preferably, reaction temperature is 260-400 DEG C, hydrogen partial pressure 2-10MPa, liquid hourly space velocity (LHSV) 0.5-
8.0h-1, hydrogen to oil volume ratio 150-1000Nm3/m3。
Further, hydrodesulfurization reaction, hydrodenitrogeneration reaction, hydrodemetallization are carried out under the action of hydrogenation catalyst
Reaction, olefin saturation and aromatic hydrocarbons saturated reaction；Hydrobon catalyst includes hydrogenation activity ingredient and carrier, hydrogenation activity
Ingredient is group vi and/or group VIII metal, and carrier is heat-resistant inorganic oxide carrier；Preferably, hydrogenation activity is at sorting
One or more in autoxidation nickel, molybdenum oxide, tungsten oxide and phosphorous oxide, carrier is selected from aluminium oxide, silica, titanium oxide, oxygen
Change one or more in zirconium and molecular sieve；It is highly preferred that carrier is silica and aluminium oxide.
It should be pointed out that generally using the form of hydrochlorate for raw material such as ammonium molybdate, phosphoric acid, nitric acid in preparation process
Corresponding active constituent is obtained after the roastings such as nickel, ammonium metatungstate, phosphoric acid.
Hydrobon catalyst further includes organic additive, and organic additive is oxygen-containing organic compound and/or itrogenous organic substance；
Preferably, oxygen-containing organic compound is one or more in Organic Alcohol and organic acid, and organic compounds containing nitrogen is selected from organic
One or more of amine and organic amine salt.
S2, cutting fractionation
Hydrogen light cycle oil will be added to carry out component analysis, to determine cut point；Hydrogen light cycle oil will be added to be detached by fractionating column
Operating condition for light fraction and heavy distillat, and fractionating column is determined according to cut point.Specifically flow includes：Adding hydrogen smart
After system, hydrotreated product is cooled down, then carries out gas-liquid separation, component then is carried out to the liquid phase that gas-liquid separation obtains
Analysis, to determine that cut point is fractionated.Using conventional analysis method, such as element composition, boiling range, detailed hydrocarbon system composition
Deng.Cut point is determined according to analysis data, to the greatest extent to separate mononuclear aromatics and di pah to be subject to profit respectively
With.
Specifically, separation can carry out in fractionating column, and the operating condition of fractionating column may include：Feeding temperature is 240-
320 DEG C, column bottom temperature be 280-350 DEG C, tower top temperature be 120-280 DEG C, tower top pressure be 0.05-1.05MPa (gauge pressure).From
The diesel oil (light fraction) rich in mononuclear aromatics is separated at the top of fractionating column, the diesel oil (heavy distillat) containing polycyclic aromatic hydrocarbon is separated from bottom of tower.
The study found that hydrogen light cycle oil (HLCO) is added to steam the catalytic diesel oil after hydrofinishing at a certain temperature
Evaporate cutting, the content of mononuclear aromatics reaches 65 mass % or more in cut point fraction below, two in fraction more than cut point
The content of ring and thrcylic aromatic hydrocarbon reaches 80 mass % or more.For this purpose, carrying out composition and property analysis to HLCO, suitable cutting is determined
Point is cut into light fraction and heavy distillat by fractionating column.Light fraction is rich in the mononuclear aromatics with side chain, send to catalytic cracking reaction
Device, cracking obtain the high-knock rating gasoline rich in aromatic hydrocarbons；Heavy distillat should not enter catalyst cracker, preferably carry out aromatic hydrocarbons profit
With.
S3, solvent pairs liquid-liquid extraction
Specifically, the heavy-cycle oil that heavy distillat and the first fractionating column generate is subjected to liquid-liquid extraction, obtained rich in aromatic hydrocarbons
Extraction oil and rich in saturated hydrocarbons raffinate oil.By liquid-liquid extraction, heavy distillat is separated into the oil of the raffinate rich in saturated hydrocarbons and richness
Extraction oil containing aromatic hydrocarbons.Raffinate oil rich in saturated hydrocarbons is sent to catalyst cracker, and cracking obtains high-knock rating gasoline；It is rich in
Feedstock viscosity can be greatly lowered in charging of the extraction oil of aromatic hydrocarbons as residual hydrocracking device, extend the operation cycle, carry
High product yield.
Wherein, the extractant in solvent pairs liquid-liquid extraction include the first extractant and the second extractant, first
Extractant is furfural or dimethyl sulfoxide (DMSO), and the second extractant is petroleum ether or 6# solvent naphthas.In extractant, double distilled
Point, the weight ratio of the first extractant and the second extractant be 1:0.4-1.3:0.2-0.8, the ability within the scope of aforementioned proportion
It is enough to ensure to extract whole alkanes, cycloalkane from single extract in aromatic hydrocarbons, reach good effect of extracting.
The characteristics of using solvent pairs liquid-liquid extraction compared to single solvent liquid-liquid extraction techniques：(1) by whole alkanes, cycloalkanes
Hydrocarbon is extracted from single extract in aromatic hydrocarbons, back in raffinate oil.(2) single most of one extracted in aromatic hydrocarbons, di pah are extracted
Out, it returns in raffinate oil.For the HCO fractions that molecular weight is 270, boiling range is 350~450 DEG C, one, di pah
A considerable amount of alkanes and cycloalkane will be carried.(3) quantity of raffinate oil obtained by double solvent extraction is used to be higher than Dan Cui,
Therefore gasoline production ratio Dan Cuigao.(4) for this part of aromatic hydrocarbons in HCO, in addition to it come green coke to provide catalysis
React it is not absolutely required to superfluous heat other than, they are split back to going to be re-used as in catalytic cracking without any reason
The charging of change, they are that qualified liquid is burnt.
It needs strictly to control the parameter of extraction process during liquid-liquid extraction.Specifically, it is filled in liquid-liquid extraction
In setting, operating pressure 0.5-1MPa, temperature is 35-110 DEG C, reflux ratio 1.0-1.5；Extractant is furfural or dimethyl
Sulfoxide.
In a preferred embodiment, the raffinate oil rich in saturated hydrocarbons is obtained at the top of liquid liquid extraction plant, is extracted in liquid liquid
The bottom of device is taken to obtain the extraction oil rich in aromatic hydrocarbons；The extraction oil that will be enriched in aromatic hydrocarbons obtains Fu Fang after stripper in bottom of tower
The extractant that stripper overhead obtains is returned as in the solvent tank that liquid liquid extraction plant provides solvent by hydrocarbon ils；It will be enriched in satisfying
Enriched saturated hydrocarbon oil is obtained in bottom of tower after another stripper with the raffinate oil of hydrocarbon, enriched saturated hydrocarbon oil and light fraction are passed through the
Two riser reactors carry out catalytic cracking, and it is molten to be returned as liquid liquid extraction plant offer in the extractant that stripper overhead obtains
In the solvent tank of agent.
In some embodiments, it is returned again in solvent tank after the solvent in solvent tank being dehydrated.
S4, catalytic cracking
Specifically, raffinate oil and light fraction are passed through the second riser reactor and carry out catalytic cracking, the first riser is anti-
Catalytic cracking of the device for fcc raw material, the two is answered to correspond to the first fractionating column and after-fractionating tower respectively.First fractionating column and
The boiling range for the light cycle oil that two fractionating columns obtain is 180-450 DEG C, and the boiling range for the heavy-cycle oil that the first fractionating column obtains is
300-530℃。
It should be pointed out that passing through the study found that every after being catalyzed reaction in obtained product, whether gently
Recycle oil (LCO) or heavy-cycle oil (HCO), it is disconnected due to the cycloalkanes open loop that is combined in the feed with aromatic ring and alkyl side chain
Chain, aromatic hydrocarbons substantially exist in the form of the alkyl of short-side chain and aromatic core combine.They are carrying out catalytic cracking again
In the process, aromatic ring is difficult to cracking, and through repeatedly recycling cracking as a result, aromatic hydrocarbons is condensed coke, gas is generated after short-side chain chain rupture
The yield (i.e. gasoline and diesel oil) of body, purpose product can not possibly be high.After liquid-liquid extraction, the raffinate oil of gained compares HCO
The fresh feed answered is more suitable for the charging as catalytic cracking.So refinery generally by HCO freshenings in the case of, it is fresh
Raw material adds raffinate oil to add HCO than fresh feed, is relatively easy to cracking.Under identical catalytic cracking condition, should have higher
Conversion ratio.After taking out to the undesirable components of catalysis, the green coke of catalysis is reduced, the selectivity of product distribution is improved, carries
High catalysis fresh feed treating capacity.
Suitable operating condition can be controlled respectively by different catalytic cracking reaction zones, and raw material obtains to greatest extent
Processing and utilization, the yield and selectivity of product greatly improve.The catalytic cracking condition of first riser reactor includes：Reaction temperature
Degree is 480-570 DEG C, oil ratio 2-14, and the reaction time is 1-5 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 3-9:
100, reaction pressure 100-300KPa；The catalytic cracking condition of second riser reactor includes：Reaction temperature is 450-600
DEG C, oil ratio 1-20, the reaction time is 0.2-8 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 0.1-20:100, instead
It is 100-400KPa to answer pressure；Preferably, the catalytic cracking condition of the first riser reactor includes：Reaction temperature is 490-
560 DEG C, oil ratio 3-12, the reaction time is 2-4 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 4-8:100, reaction
Pressure is 120-300KPa；The catalytic cracking condition of second riser reactor includes：Reaction temperature is 500-550 DEG C, agent oil
Than for 5-12, the reaction time is 2-4 second, the weight ratio of aatomized water vapor amount and inlet amount is 0.5-2.0:100, reaction pressure is
150-300KPa。
Catalytic cracking catalyst can be carried by the prior art in first riser reactor and the second riser reactor
Any one or the combination of several of them of confession.These catalytic cracking catalysts usually contain zeolite, inorganic oxide and optional viscous
The content of soil, each component is respectively：Zeolite 5-50 weight %, inorganic oxide 5-95 weight %, clay 0-70 weight %.
You need to add is that charging of the extraction oil rich in aromatic hydrocarbons as residual hydrocracking device in S3, can adopt
With conventional method for hydrogen cracking, hydrocracking condition may include：340-400 DEG C or so of one stage hydrofining reaction temperature,
380-450 DEG C or so of secondary hydrogenation cracking reaction temperature；Reaction pressure about 14-20MPa；Hydrogen-consuming volume is inlet amount 1%~4%,
It is preferred that 2%~3%.
In addition, hydrocracking catalyst includes carrier and the active component that is supported on carrier, wherein active component by
Three kinds of molybdenum, cobalt and nickel groups are grouped as, and are counted by oxide and on the basis of the total weight of hydrocracking catalyst, the content of molybdenum is 5-
The content of 23 weight %, cobalt are 0.8-6 weight %, and the content of nickel is 0.2-2 weight %；Carrier contains solid acid component and inorganic
Refractory oxides, solid acid component are at least two in amorphous silica-alumina, big-hole zeolite molecular sieve and mesopore zeolite molecular sieve.
Solid acid component main function is that cracking activity is played in being hydrocracked, including isomery, open loop and lytic activity, and inorganic heat-resisting
The main function of oxide is to provide cementation and provides the effective carrier of hydrogenation active component.In order to enable to plus hydrogen split
Preferable Catalytic Cracking Performance and stability can be had both by changing catalyst, it is preferable that on the basis of the total weight of carrier, solid
The content of acid constituents is 2-96 weight %, more preferably 3-85 weight %；The content of inorganic refractory oxides is 15-95 weights
Measure %, more preferably 25-90 weight %.Amorphous silica-alumina can be that existing various can be used as consolidating for hydrocracking catalyst
The surface of body acid constituents has acid silica-alumina, it is however preferred to have silica-oxidation of structure of similar to thin diaspore
Aluminium.
The embodiment of the present invention additionally provides a kind of method of processing poor ignition quality fuel, includes the side of above-mentioned catalytic cracking diesel oil
Method, the high advantage of yield of gasoline in the product being likewise supplied with, can respond the policy requirements of country.
The feature and performance of the present invention are described in further detail with reference to embodiments.
Embodiment 1
The present embodiment provides a kind of methods of catalytic cracking diesel oil, are illustrated down below according to the flow chart in Fig. 1 whole
A technological process.
It is the LCO48 of after-fractionating tower from the main fractionating tower 39 i.e. LCO42 of the first fractionating column and from secondary fractionating column 45
Into hydrofining reactor 1, with hydrogenation catalyst haptoreaction；Reaction effluent 2 enters high-pressure separator 3, circulating hydrogen 4
Hydrofining reactor 1 is returned to, liquid product 5 is separated into gasoline 7 and refined diesel oil 8,9 through stripper 6；Refined diesel oil 8 can be with
As diesel oil blending component；Refined diesel oil 9 enters fractionating column 10, and tower top obtains light fraction 11, bottom of tower under the cut point of optimization
Obtain heavy distillat 12；Light fraction 11 is into the second riser reactor of catalytic cracking unit 31；Heavy distillat 12 with come from main fractionating tower
39 HCO43 mixing enters liquid-liquid extraction tower 13 from middle part, and the first extractant 25 enters liquid-liquid extraction tower 13 from top, and second
Extractant 50 enters liquid-liquid extraction tower 13 from lower part, heavy distillat 12, HCO and the first counter current contacting in tower of extractant 25,
Solvent, which mutually absorbs, continues downward, and 50 counter current contacting of the second extractant after aromatic hydrocarbons, and the second extractant 50 is by solvent phase
In saturated hydrocarbons extract, into raffinate；Bottom of tower obtains the extraction oil 15 rich in aromatic hydrocarbons, and tower top obtains being rich in saturated hydrocarbons
Raffinate oil 14；Extraction oil 15 enters stripper 16, and steam 19 enters from bottom of tower；16 bottom of tower of stripper obtain aromatic hydrocarbons purity >=
95% rich aromatic naphtha 18, rich aromatic naphtha 18 are mixed into residual hydrocracking reactor with resid feed；16 tower top of stripper obtains
To the extractant 17 of recycling；Raffinate oil 14 enters stripper 20, and steam 23 enters from bottom of tower；20 bottom of tower of stripper obtains rich full
With hydrocarbon ils 22, enriched saturated hydrocarbon oil 22 is into the second riser reactor of catalytic cracking unit 31；20 tower top of stripper is recycled
Extractant 21；Extractant 17 and extractant 21 enter solvent tank 24；First extractant 25 and the second extractant 50
Rework solution liquid extraction tower 13；Water 26 containing extractant enters dehydrating tower 27；Steam 30 enters from bottom of tower；27 tower top of dehydrating tower
Solvent 28 is returned to solvent tank 24；Sewage 29 is discharged from 27 bottom of tower of dehydrating tower.
Light fraction 11 enters the second riser reactor of catalytic cracking unit 31 with enriched saturated hydrocarbon oil 22, is contacted with catalyst
Reaction；By 32 separating catalyst of the second settler and reaction product 33；Reaction product 33 enters secondary fractionating column 45 and is separated into gas
Body 46, gasoline 47, HCO48 and slurry oil 49；Conventional catalytic raw material 36 enters main riser reactor 37, is contacted with catalyst instead
It answers；By 34 separating catalyst of the first settler and reaction product 38；Reaction product 38 is separated into gas into main fractionating tower 39
40, gasoline 41, light cycle oil LCO42, heavy-cycle oil HCO43 and slurry oil 44；Light cycle oil LCO42 and LCO48 are back to plus hydrogen
Finishing reactor 1；Heavy-cycle oil HCO43 rework solution liquid extraction tower 13 can also get rid of 51 outside part；Slurry oil 49 returns to main fractionating tower
39；Take heat superfluous in catalytic cracked regenerated burning process away by external warmer 35.
The parameter in each step is illustrated below.
(1) LCO is with the catalytic reaction condition of hydrogen：Reaction temperature is 320 DEG C, hydrogen partial pressure 6MPa, liquid space-time
Speed is 5.0h-1, hydrogen to oil volume ratio 650Nm3/m3。
(2) hydrofining catalyst carrier used in is by aluminium oxide and Ludox with Al2O3/SiO2Butt ratio is 6:1 mixing is equal
It is even, it is extruded into three leaf bar shapeds, 1.4 millimeters of outer diameter roasts 3 hours under the conditions of wet bar is 4 hours, 600 DEG C dry in 120 DEG C, oxygen is made
SiClx content is the carrier of 18 weight %；200 grams of carrier is weighed, with containing 11.5 grams of ammonium paramolybdate, 20.6 grams of phosphoric acid, nickel nitrate 19
Gram, 183 milliliters of the aqueous solution of 36.8 grams of ammonium metatungstate, 2.5 grams of phosphatase 11 impregnate the carrier 3 hours, 120 DEG C of dryings 4 hours, 480
DEG C roasting 4 hours, obtain Hydrobon catalyst.
(3) the first solvent is furfural in the solvent used in liquid-liquid extraction, and the second solvent is petroleum ether (60-90 DEG C), and again
The weight ratio of fraction, the first extractant and the second extractant is 1:1:0.5.Operating pressure is in liquid-liquid extraction tower
0.8MPa, temperature are 80 DEG C, reflux ratio 1.2.
The catalytic cracking condition of (4) first riser reactors includes：Reaction temperature is 520 DEG C, oil ratio 8, reaction
Time is 3 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 5:100, reaction pressure 200KPa；Second promotes tube reaction
The catalytic cracking condition of device includes：Reaction temperature be 520 DEG C, oil ratio 8, the reaction time be 4 seconds, aatomized water vapor amount with into
The weight ratio of doses is 10:100, reaction pressure 250KPa.
The catalyst used in embodiment is commercial catalyst, and the trade mark is respectively DFC-1 catalytic cracking catalysts and RS-
1000 Hydrobon catalyst properties are shown in Table 1, table 2；Conventional catalytic cracking feedstock property used is shown in Table 3.
1 catalytic cracking catalyst property of table
| The catalyst trade mark | DFC-1 |
| Micro-activity, % | 65 |
| Determine carbon, % | 0.03 |
| Surface area, m2.g-1 | 104.55 |
| Kong Rong, ml.g-1 | 0.172 |
| Abrasion index | 2.43 |
| Primary chemical forms, % | |
| SiO2 | 46.56 |
| Al2O3 | 44.10 |
| Re2O3 | 3.68 |
| SO4 = | 0.15 |
| P2O5 | 0.78 |
| Screening composition, % | |
| <20μm | 25.18 |
| 20-40μm | 45.05 |
| 40-80μm | 19.60 |
| 80-110μm | 8.73 |
| >110μm | 1.44 |
| Tenor, μ g.g-1 | |
| Ni | 8160 |
| V | 2110 |
| Fe | 3330 |
| Na | 1750 |
2 Hydrobon catalyst property of table
3 Conventional catalytic feedstock property of table
Embodiment 2
Identical as the substantially flow of embodiment 1 the present embodiment provides a kind of method of catalytic cracking diesel oil, difference is only
It is that following parameters, the present embodiment do not refer to that place please refers to embodiment 1.
The parameter in each step is illustrated below.
(1) LCO is with the catalytic reaction condition of hydrogen：Reaction temperature is 250 DEG C, hydrogen partial pressure 1MPa, liquid space-time
Speed is 0.3h-1, hydrogen to oil volume ratio 100Nm3/m3。
(2) hydrofining catalyst carrier used in is by aluminium oxide and Ludox with Al2O3/SiO2Butt ratio is 6:1 mixing is equal
It is even, it is extruded into three leaf bar shapeds, 1.4 millimeters of outer diameter roasts 3 hours under the conditions of wet bar is 4 hours, 600 DEG C dry in 120 DEG C, oxygen is made
SiClx content is the carrier of 18 weight %；200 grams of carrier is weighed, with containing 11.5 grams of ammonium paramolybdate, 20.6 grams of phosphoric acid, nickel nitrate 19
Gram, 183 milliliters of the aqueous solution of 36.8 grams of ammonium metatungstate, 2.5 grams of phosphatase 11 impregnate the carrier 3 hours, 120 DEG C of dryings 4 hours, 480
DEG C roasting 4 hours, obtain Hydrobon catalyst.
(3) the first solvent is dimethyl sulfoxide (DMSO) in the solvent used in liquid-liquid extraction, and the second solvent is 6# solvent naphthas, and double distilled
Point, the weight ratio of the first extractant and the second extractant be 1:0.4:0.2.Operating pressure is in liquid-liquid extraction tower
0.5MPa, temperature are 35 DEG C, reflux ratio 1.0.
The catalytic cracking condition of (4) first riser reactors includes：Reaction temperature is 480 DEG C, oil ratio 2, reaction
Time is 1 second, and the weight ratio of aatomized water vapor amount and inlet amount is 3:100, reaction pressure 100KPa；Second promotes tube reaction
The catalytic cracking condition of device includes：Reaction temperature be 450 DEG C, oil ratio 1, the reaction time be 0.2 second, aatomized water vapor amount with
The weight ratio of inlet amount is 0.1:100, reaction pressure 100KPa.
Embodiment 3
Identical as the substantially flow of embodiment 1 the present embodiment provides a kind of method of catalytic cracking diesel oil, difference is only
It is that following parameters, the present embodiment do not refer to that place please refers to embodiment 1.
The parameter in each step is illustrated below.
(1) LCO is with the catalytic reaction condition of hydrogen：Reaction temperature is 450 DEG C, hydrogen partial pressure 12MPa, liquid space-time
Speed is 10h-1, hydrogen to oil volume ratio 1500Nm3/m3。
(2) hydrofining catalyst carrier used in is by aluminium oxide and Ludox with Al2O3/SiO2Butt ratio is 6:1 mixing is equal
It is even, it is extruded into three leaf bar shapeds, 1.4 millimeters of outer diameter roasts 3 hours under the conditions of wet bar is 4 hours, 600 DEG C dry in 120 DEG C, oxygen is made
SiClx content is the carrier of 18 weight %；200 grams of carrier is weighed, with containing 11.5 grams of ammonium paramolybdate, 20.6 grams of phosphoric acid, nickel nitrate 19
Gram, 183 milliliters of the aqueous solution of 36.8 grams of ammonium metatungstate, 2.5 grams of phosphatase 11 impregnate the carrier 3 hours, 120 DEG C of dryings 4 hours, 480
DEG C roasting 4 hours, obtain Hydrobon catalyst.
(3) the first solvent is furfural in the solvent used in liquid-liquid extraction, and the second solvent is 6# solvent naphthas, and heavy distillat, the
The weight ratio of one extractant and the second extractant is 1:1.3:0.8.Operating pressure is 1MPa in liquid-liquid extraction tower, and temperature is
110 DEG C, reflux ratio 1.5.
The catalytic cracking condition of (4) first riser reactors includes：Reaction temperature is 570 DEG C, oil ratio 14, reaction
Time is 5 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 9:100, reaction pressure 300KPa；Second promotes tube reaction
The catalytic cracking condition of device includes：Reaction temperature be 600 DEG C, oil ratio 20, the reaction time be 8 seconds, aatomized water vapor amount with
The weight ratio of inlet amount is 20:100, reaction pressure 400KPa.
Embodiment 4
Identical as the substantially flow of embodiment 1 the present embodiment provides a kind of method of catalytic cracking diesel oil, difference is only
It is that following parameters, the present embodiment do not refer to that place please refers to embodiment 1.
The parameter in each step is illustrated below.
(1) LCO is with the catalytic reaction condition of hydrogen：Reaction temperature is 260 DEG C, hydrogen partial pressure 2MPa, liquid space-time
Speed is 0.5h-1, hydrogen to oil volume ratio 150Nm3/m3。
(2) hydrofining catalyst carrier used in is by aluminium oxide and Ludox with Al2O3/SiO2Butt ratio is 6:1 mixing is equal
It is even, it is extruded into three leaf bar shapeds, 1.4 millimeters of outer diameter roasts 3 hours under the conditions of wet bar is 4 hours, 600 DEG C dry in 120 DEG C, oxygen is made
SiClx content is the carrier of 18 weight %；200 grams of carrier is weighed, with containing 11.5 grams of ammonium paramolybdate, 20.6 grams of phosphoric acid, nickel nitrate 19
Gram, 183 milliliters of the aqueous solution of 36.8 grams of ammonium metatungstate, 2.5 grams of phosphatase 11 impregnate the carrier 3 hours, 120 DEG C of dryings 4 hours, 480
DEG C roasting 4 hours, obtain Hydrobon catalyst.
(3) the first solvent is furfural in the solvent used in liquid-liquid extraction, and the second solvent is petroleum ether (60-90 DEG C), and again
The weight ratio of fraction, the first extractant and the second extractant is 1:1:0.5.Operating pressure is in liquid-liquid extraction tower
0.8MPa, temperature are 80 DEG C, reflux ratio 1.2.
The catalytic cracking condition of (4) first riser reactors includes：Reaction temperature is 490 DEG C, oil ratio 3, reaction
Time is 2 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 4:100, reaction pressure 120KPa；Second promotes tube reaction
The catalytic cracking condition of device includes：Reaction temperature be 500 DEG C, oil ratio 5, the reaction time be 2 seconds, aatomized water vapor amount with into
The weight ratio of doses is 0.5:100, reaction pressure 150KPa.
Embodiment 5
Identical as the substantially flow of embodiment 1 the present embodiment provides a kind of method of catalytic cracking diesel oil, difference is only
It is that following parameters, the present embodiment do not refer to that place please refers to embodiment 1.
The parameter in each step is illustrated below.
(1) LCO is with the catalytic reaction condition of hydrogen：Reaction temperature is 400 DEG C, hydrogen partial pressure 10MPa, liquid space-time
Speed is 8.0h-1, hydrogen to oil volume ratio 1000Nm3/m3。
(2) hydrofining catalyst carrier used in is by aluminium oxide and Ludox with Al2O3/SiO2Butt ratio is 6:1 mixing is equal
It is even, it is extruded into three leaf bar shapeds, 1.4 millimeters of outer diameter roasts 3 hours under the conditions of wet bar is 4 hours, 600 DEG C dry in 120 DEG C, oxygen is made
SiClx content is the carrier of 18 weight %；200 grams of carrier is weighed, with containing 11.5 grams of ammonium paramolybdate, 20.6 grams of phosphoric acid, nickel nitrate 19
Gram, 183 milliliters of the aqueous solution of 36.8 grams of ammonium metatungstate, 2.5 grams of phosphatase 11 impregnate the carrier 3 hours, 120 DEG C of dryings 4 hours, 480
DEG C roasting 4 hours, obtain Hydrobon catalyst.
(3) the first solvent is furfural in the solvent used in liquid-liquid extraction, and the second solvent is petroleum ether (60-90 DEG C), and again
The weight ratio of fraction, the first extractant and the second extractant is 1:1:0.5.Operating pressure is in liquid-liquid extraction tower
0.8MPa, temperature are 80 DEG C, reflux ratio 1.2.
The catalytic cracking condition of (4) first riser reactors includes：Reaction temperature is 560 DEG C, oil ratio 12, reaction
Time is 4 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 8:100, reaction pressure 300KPa；Second promotes tube reaction
The catalytic cracking condition of device includes：Reaction temperature be 550 DEG C, oil ratio 12, the reaction time be 4 seconds, aatomized water vapor amount with
The weight ratio of inlet amount is 2.0:100, reaction pressure 300KPa.
Comparative example 1
Main riser is detached into Conventional catalytic cracking feedstock oil, crackate through main fractionating tower, what main fractionating tower was isolated
Raw gasoline promotes tube reaction into second, and heavy-cycle oil HCO is into main riser freshening.Control two risers under optimal conditions
It reacts, the catalyst trade mark used in comparative example is DFC-1 catalytic cracking catalysts.Operating condition is as shown in table 4.
4 operating condition of table
Test example
The product distribution in embodiment 1-5 and comparative example is measured using conventional method, the results are shown in Table 5.
5 product distribution of table compares
| Product distribution, % | Embodiment 1 | Embodiment 2 | Embodiment 3 | Embodiment 4 | Embodiment 5 | Comparative example 1 |
| Dry gas | 3.7 | 3.6 | 3.8 | 3.8 | 3.7 | 4.1 |
| Liquefied gas | 18.0 | 19.9 | 19.1 | 18.8 | 19.2 | 16.7 |
| Gasoline | 61.5 | 59.9 | 60.5 | 60.7 | 60.3 | 41.2 |
| Diesel oil | 3.6 | 3.8 | 3.7 | 3.8 | 3.9 | 25.6 |
| Mink cell focus | 5.5 | 5.3 | 5.3 | 5.4 | 5.5 | 4.5 |
| Coke | 7.6 | 7.5 | 7.6 | 7.5 | 7.4 | 7.8 |
As can be seen from Table 5, when the second riser charging after raw gasoline becomes hydrofining diesel oil, yield of gasoline
It significantly improves, average yield 60.58, the yield of gasoline of comparative example is 41.2, improves 47.04%.In addition, the present invention is implemented
Catalyst cracking method in example can be such that diesel yield significantly reduces, and dry gas and coke yield are declined slightly.
In conclusion a kind of method of catalytic cracking diesel oil provided by the invention, uses duo-lift tube reactor to carry out
Catalytic cracking, the first riser reactor are main riser, are mainly used for processing catalytically cracked material, the second riser reactor
Process light fraction and enriched saturated hydrocarbon oil；The reaction product of first riser reactor carries out isolated vapour by the first fractionating column
The reaction product of oil, light cycle oil, heavy-cycle oil and slurry oil, the second riser reactor by after-fractionating tower detach
To gasoline and light cycle oil；Added after the light cycle oil that first fractionating column and after-fractionating tower generate is carried out hydrofinishing
Hydrogen light cycle oil, then light fraction and heavy distillat are obtained after being fractionated, the heavy-cycle oil that heavy distillat and the first fractionating column are generated
Solvent pairs liquid-liquid extraction is carried out, the extraction oil rich in aromatic hydrocarbons and the raffinate oil rich in saturated hydrocarbons are obtained；Finally by raffinate oil and gently
Fraction is passed through the second riser reactor and carries out catalytic cracking.Higher can be obtained using catalyst cracking method provided by the invention
Yield of gasoline, and reduce the green coke of catalysis, improve the selectivity of product distribution.
The present invention also provides a kind of methods of processing poor ignition quality fuel comprising the method for above-mentioned catalytic cracking diesel oil, together
The high advantage of yield of gasoline in the product that sample has meets the policy requirements of country.
Embodiments described above is a part of the embodiment of the present invention, instead of all the embodiments.The reality of the present invention
The detailed description for applying example is not intended to limit the range of claimed invention, but is merely representative of the selected implementation of the present invention
Example.Based on the embodiments of the present invention, those of ordinary skill in the art are obtained without creative efforts
Every other embodiment, shall fall within the protection scope of the present invention.
Claims (10)
1. a kind of method of catalytic cracking diesel oil, fcc raw material is subjected to catalytic cracking by the first riser reactor, by the
The catalytic cracking production of one riser reactor is passed through the first fractionating column, and the catalytic cracking production of the second riser reactor is led to
Enter after-fractionating tower, which is characterized in that include the following steps：
It obtains adding hydrogen light cycle oil after the light cycle oil that first fractionating column and after-fractionating tower generate is carried out hydrofinishing；
Described plus hydrogen light cycle oil is subjected to component analysis, to determine cut point；
Described plus hydrogen light cycle oil is separated into light fraction and heavy distillat, and the operating condition root of the fractionating column by fractionating column
It is determined according to cut point；
The heavy-cycle oil that the heavy distillat and first fractionating column generate is subjected to solvent pairs liquid-liquid extraction, obtains being rich in aromatic hydrocarbons
Extraction oil and rich in saturated hydrocarbons raffinate oil；
The raffinate oil and the light fraction are passed through the second riser reactor and carry out catalytic cracking；
Wherein, the extractant in the solvent pairs liquid-liquid extraction includes the first extractant and the second extractant, described
First extractant is furfural or dimethyl sulfoxide (DMSO), and second extractant is petroleum ether or 6# solvent naphthas.
2. the method for catalytic cracking diesel oil according to claim 1, which is characterized in that described in the extractant
The weight ratio of heavy distillat, first extractant and second extractant is 1:0.4-1.3:0.2-0.8.
3. the method for catalytic cracking diesel oil according to claim 2, which is characterized in that in liquid liquid extraction plant, operation
Pressure is 0.5-1MPa, and temperature is 35-110 DEG C, reflux ratio 1.0-1.5；
The extractant is furfural or dimethyl sulfoxide (DMSO).
4. the method for catalytic cracking diesel oil according to claim 3, which is characterized in that on the top of the liquid liquid extraction plant
Portion obtains the raffinate oil rich in saturated hydrocarbons, and the extraction oil rich in aromatic hydrocarbons is obtained in the bottom of the liquid liquid extraction plant；
The extraction oil rich in aromatic hydrocarbons is obtained into rich aromatic naphtha after stripper in bottom of tower, the extraction that stripper overhead is obtained
Solvent is taken to be returned as in the solvent tank that the liquid liquid extraction plant provides solvent；
The raffinate oil rich in saturated hydrocarbons is obtained into enriched saturated hydrocarbon oil after another stripper in bottom of tower, it will be described rich full
It is passed through the second riser reactor with hydrocarbon ils and the light fraction and carries out catalytic cracking, in the extractant that stripper overhead obtains
It is returned as in the solvent tank that the liquid liquid extraction plant provides solvent；
Preferably, it is returned again to after the solvent in the solvent tank being dehydrated in the solvent tank.
5. the method for catalytic cracking diesel oil according to claim 1, which is characterized in that in unifining process, reaction
Temperature is 250-450 DEG C, hydrogen partial pressure 1-12MPa, liquid hourly space velocity (LHSV) 0.3-10h-1, hydrogen to oil volume ratio 100-1500Nm3/
m3；
Preferably, reaction temperature is 260-400 DEG C, hydrogen partial pressure 2-10MPa, liquid hourly space velocity (LHSV) 0.5-8.0h-1, hydrogen to oil volume ratio
For 150-1000Nm3/m3。
6. the method for catalytic cracking diesel oil according to claim 5, which is characterized in that under the action of hydrogenation catalyst into
Row hydrodesulfurization reaction, hydrodenitrogeneration reaction, hydrodemetallization reaction, olefin saturation and aromatic hydrocarbons saturated reaction；
Hydrobon catalyst includes hydrogenation activity ingredient and carrier, and the hydrogenation activity ingredient is group vi and/or Section VIII
Race's metal, the carrier are heat-resistant inorganic oxide carrier；
Preferably, the hydrogenation activity ingredient is one or more in nickel oxide, molybdenum oxide, tungsten oxide and phosphorous oxide, institute
It is one or more in aluminium oxide, silica, titanium oxide, zirconium oxide and molecular sieve to state carrier；
It is highly preferred that the carrier is silica and aluminium oxide.
7. the method for catalytic cracking diesel oil according to claim 6, which is characterized in that the Hydrobon catalyst also wraps
Organic additive is included, the organic additive is oxygen-containing organic compound and/or itrogenous organic substance；
Preferably, the oxygen-containing organic compound is one or more in Organic Alcohol and organic acid, described nitrogenous to organise
It closes object and is selected from one or more of organic amine and organic amine salt.
8. the method for catalytic cracking diesel oil according to claim 1, which is characterized in that after hydrofinishing, pair plus hydrogen
Refined products are cooled down, then carry out gas-liquid separation, are then carried out component analysis to the liquid phase that gas-liquid separation obtains, are cut with determination
Cutpoint is fractionated；
The operating condition of fractionating device includes in fractional distillation process：Feeding temperature is 240-320 DEG C, column bottom temperature 280-350
DEG C, tower top temperature is 120-280 DEG C, tower top pressure 0.05-1.05MPa.
9. the method for catalytic cracking diesel oil according to claim 1, which is characterized in that first riser reactor
Catalytic cracking condition includes：Reaction temperature is 480-570 DEG C, oil ratio 2-14, and the reaction time is 1-5 seconds, aatomized water vapor
The weight ratio of amount and inlet amount is 3-9:100, reaction pressure 100-300KPa；The catalysis of second riser reactor is split
Change condition includes：Reaction temperature be 450-600 DEG C, oil ratio 1-20, the reaction time be 0.2-8 second, aatomized water vapor amount and
The weight ratio of inlet amount is 0.1-20:100, reaction pressure 100-400KPa；
Preferably, the catalytic cracking condition of first riser reactor includes：Reaction temperature is 490-560 DEG C, oil ratio
For 3-12, the reaction time is 2-4 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 4-8:100, reaction pressure 120-
300KPa；The catalytic cracking condition of second riser reactor includes：Reaction temperature is 500-550 DEG C, oil ratio 5-
12, the reaction time is 2-4 seconds, and the weight ratio of aatomized water vapor amount and inlet amount is 0.5-2.0:100, reaction pressure 150-
300KPa。
10. a kind of method of processing poor ignition quality fuel, which is characterized in that split including the catalysis described in any one of claim 1-9
Change the method for diesel oil.
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| CN115895722A (en) * | 2022-09-27 | 2023-04-04 | 中国石油化工股份有限公司 | System for preparing light aromatic hydrocarbon from heavy oil raw material |
| CN116515524A (en) * | 2022-07-25 | 2023-08-01 | 中国石油化工股份有限公司 | Method for producing light aromatic hydrocarbon by secondary hydrogenation of inferior diesel oil |
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| CN103540358A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Residual oil conversion-aromatic hydrocarbon extraction combined process |
| CN107903943A (en) * | 2017-11-02 | 2018-04-13 | 中石化炼化工程（集团）股份有限公司 | The method and high-knock rating gasoline or high-knock rating gasoline blend component that catalytic cracking diesel oil utilizes |
| CN207899021U (en) * | 2018-01-19 | 2018-09-25 | 南京师范大学 | A kind of outer circulation reaction liquid liquid extraction plant |
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| CN103540358A (en) * | 2012-07-12 | 2014-01-29 | 中国石油天然气股份有限公司 | Residual oil conversion-aromatic hydrocarbon extraction combined process |
| CN107903943A (en) * | 2017-11-02 | 2018-04-13 | 中石化炼化工程（集团）股份有限公司 | The method and high-knock rating gasoline or high-knock rating gasoline blend component that catalytic cracking diesel oil utilizes |
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| CN116515524A (en) * | 2022-07-25 | 2023-08-01 | 中国石油化工股份有限公司 | Method for producing light aromatic hydrocarbon by secondary hydrogenation of inferior diesel oil |
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