CN106398764A - Post-processing method of diesel oil - Google Patents
Post-processing method of diesel oil Download PDFInfo
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- CN106398764A CN106398764A CN201611114460.2A CN201611114460A CN106398764A CN 106398764 A CN106398764 A CN 106398764A CN 201611114460 A CN201611114460 A CN 201611114460A CN 106398764 A CN106398764 A CN 106398764A
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- Prior art keywords
- diesel oil
- oil
- processing method
- polar solvent
- extraction
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Classifications
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0409—Extraction of unsaturated hydrocarbons
- C10G67/0445—The hydrotreatment being a hydrocracking
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
-
- 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
- C10G2400/04—Diesel oil
Abstract
The invention relates to the field of petroleum refining processing, in particular to a post-processing method of diesel oil. The post-processing method of the diesel oil comprises the steps that polycyclic aromatic hydrocarbon in the diesel oil is extracted with a polar solvent, the polar solvent in obtained extractive oil is removed through separation, then hydrocracking treatment is conducted, and a product mainly containing kerosene and naphtha is obtained; after an organic solvent in raffinate oil is removed, hydrorefining treatment is conducted, and then refined diesel oil and a small part of gasoline are obtained, wherein the diesel oil comprises one or more of catalytically-cracked diesel oil, coking diesel oil and straight-run diesel oil. According to the method, polycyclic aromatic hydrocarbon in the diesel oil is extracted out, the extractive oil and the raffinate oil are treated separately, therefore, the quality of the obtained product is optimized, the yield is increased, and the cost is reduced.
Description
Technical field
The present invention relates to petroleum refining manufacture field, in particular to processing method after a kind of diesel oil.
Background technology
Catalytic cracking (fluid catalytic cracking, FCC) technology is the main technique means of heavy oil lighting
One of, it is to make mink cell focus that cracking reaction occurs in the presence of heat and catalyst, be changed into the mistake of cracked gas, gasoline and diesel oil etc.
Journey.Catalytic cracking all occupies critical role in the oil refining enterprise of countries in the world.Being mainly characterized by of catalytic cracking process technology
Alkane in charging and cycloalkane are carried out cracking, contract and, be generally enriched a large amount of condensed ring therefore in catalytic cracking diesel oil
Aromatic hydrocarbons.The sulfur content of catalytic cracking diesel oil and arene content are high, and engine ignition poor performance belongs to diesel oil blending group inferior
Point.Some urge bavin density more than 0.95g/cm3, more than 80%, Cetane number is less than 20 to arene content, even if these fraction of diesel oil
Process through hydro-upgrading, Cetane number is still less than 35 it is impossible to become the preferable blend component of light diesel fuel.
At present, the rear manufacturing process of catalytic cracking diesel oil, coker gas oil and straight-run diesel oil is mainly hydrofinishing and hydrogenation
Cracking.Because its condensed-nuclei aromatics content is high, its Cetane number to be improved it is necessary to by condensed ring under harsher hydroconversion condition
The aromatic ring saturation of aromatic hydrocarbons or open loop cracking.Because the hydrogenation open loop of mononuclear aromatics is not the ideal process of hydrogenation reaction, and
The component Cetane number such as alkylbenzene, cycloalkyl benzene are still relatively low, so the fraction of diesel oil through hydro-upgrading is not still light bavin
The preferable blend component of oil.A part of alkane (including the side chain on mononuclear aromatics) and ring can be led in hydro-upgrading simultaneously
Alkane ruptures, and is changed into gasoline fraction or gas, for various reasons, hydro-upgrading or be hydrocracked the gasoline of production and evaporate
Part still needs to process further could be as suitable gasoline blend component, so this processing mode to catalytic cracking diesel oil is still
It is not so a kind of preferable method.
Need a kind of technology being capable of sweetly disposition catalytic cracking light cycle oil at present, this technology can be according to market
Needs flexibly produce fine-quality diesel oil/kerosene component or gasoline/kerosene component.
In view of this, the special proposition present invention.
Content of the invention
It is an object of the invention to provide processing method after a kind of diesel oil, the condensed-nuclei aromatics in diesel oil is extracted by the method
Coming, and the part extracting and excess oil be respectively processed, thus optimizing the quality of prepared product, also improving yield,
Reduce cost.
In order to realize the above-mentioned purpose of the present invention, spy employs the following technical solutions：
Processing method after a kind of diesel oil, is extracted to the condensed-nuclei aromatics in described diesel oil using polar solvent, will obtain
Tapped oil in polar solvent be separated off after carry out hydrocracked, treated and obtain the product based on kerosene and naphtha；
After organic solvent in raffinating oil removes, hydrogenated refinement treatment obtains refined diesel oil and small part gasoline；
Described diesel oil includes one or more of catalytic cracking diesel oil, coker gas oil and straight-run diesel oil.
In diesel oil, how more than 60%, wherein two rings, thrcylic aromatic hydrocarbon account for 75% (volume integral of arene content to arene content
Number) about, condensed-nuclei aromatics content is higher to be the low main cause of catalytic cracking diesel oil Cetane number, and in catalytic cracking diesel oil
Sulphur mainly presented in polycyclic aromatic hydrocarbon, sulfide as this kind of in dibenzothiophenes, due to the inhibition of phenyl ring, sulphur atom is very
The difficult hydrodesulfurization activity central contact with catalyst, therefore desulfurization are difficult, and catalyst by one of aromatic ring be hydrogenated with saturation,
After open loop, sulphur atom is easily contacted with catalyst active center, and desulfurization is also easy.
With respect to alkane and cycloalkane, the polarity of aromatic hydrocarbons especially condensed-nuclei aromatics is stronger, therefore can use polar solvent
By it, from diesel oil, extract and separate is out.Then, by the method for distillation, extractant is separated with diesel oil, extract is rich in
The product (tapped oil) of polycyclic aromatic hydrocarbon is hydrocracked, and obtains high-quality burning oil；Will be enriched in alkane, cycloalkane, mononuclear aromatics
Part (raffinating oil) and catalytic cracking feeds mix (including directly mixing, pre- charging, individually charging etc.) through different modes,
Processed under catalytic cracking condition, so not only obtain premium blend component, but also improve olefin yields.
The Hydrofinishing conditions that the present invention raffinates oil are different with raw material difference, due to eliminating the condensed ring virtue of the overwhelming majority
, compared with the raw material not being stripped accordingly, condition is relatively mild for hydrocarbon, therefore its Hydrofinishing conditions, and the gasoline of preparation is in harmonious proportion
Component quality is also more preferable.
The hydrocracking condition of tapped oil of the present invention is different with raw material difference, because purpose product is kerosene, its hydrogenation
, compared with corresponding fecund gasoline scheme, condition is relatively mild for cracking conditions.
Preferably, processing method after diesel oil as above, described polar solvent is (0.3 with the volume ratio of described diesel oil
～10)：1.
It is further preferred that processing method after diesel oil as above, the volume ratio of described polar solvent and described diesel oil
For (2～7)：1；More preferably (3～6)：1.
Preferably, processing method after diesel oil as above, the polarity of described polar solvent is more than 3.5, more preferably greater than
4.0.
It is furthermore preferred that processing method after diesel oil as above, described polar solvent include acetonitrile, methyl alcohol, ethanol, positive third
One or more of alcohol, isopropanol, furfural and dimethylformamide.
Preferably, processing method after diesel oil as above, the temperature carrying out described extraction is 5 DEG C～90 DEG C.
It is furthermore preferred that when described organic solvent is acetonitrile or ethanol, extraction temperature is 10 DEG C～70 DEG C；When described organic
When solvent is methyl alcohol, extraction temperature is 10 DEG C～60 DEG C.
In general, temperature raises, and condensed-nuclei aromatics solubility in organic solvent can increase, and this is favourable to extracting, separately
Outer temperature raises, and liquid viscosity reduces, and is also beneficial to organic solvent and separates with diesel oil.When excess temperature does not raise, also result in
Diesel oil volatilization increases it is often more important that temperature is too high also dangerous, and this is unfavorable to extraction, therefore will be according to used organic molten
The property of agent and diesel oil is passed through test and is determined temperature during extraction.
Preferably, processing method after diesel oil as above, described separate the polar solvent in the tapped oil obtaining is removed
The method gone is distillation.
Preferably, processing method after diesel oil as above, when described use polar solvent extracts to described diesel oil
Extraction device is carried out；
Described extraction device includes extraction tube and/or knockout drum.
Preferably, processing method after diesel oil as above, described use polar solvent is extracted to described diesel oil
Method is：
Diesel oil and polar solvent are pumped into from extraction tube upper and lower respectively, and standing after being sufficiently mixed in extraction tube
Layering is so that condensed-nuclei aromatics enters organic solvent layer thus being separated.
Preferably, processing method after diesel oil as above, described use polar solvent is extracted to described diesel oil
Method is：
Using one or more knockout drums, described diesel oil and polar solvent are pumped into and in tank, are sufficiently mixed rear stratification,
Condensed-nuclei aromatics is made to enter organic solvent layer thus being separated.
The mixture of tapped oil and solvent is extracted out laggard knockout tower, in knockout tower, solvent is separated with tapped oil, molten
Agent recycles, and tapped oil is entered hydrocracking unit and is hydrocracked, and obtains the product based on kerosene and gasoline.
Raffinate oil after extraction, after mixing individually or with other diesel oil distillates, enter hydro-refining unit and carry out hydrofinishing,
Obtain the product based on diesel oil distillate.
Preferably, processing method after diesel oil as above, described extraction times are one or many.
Compared with prior art, beneficial effects of the present invention are：
1) after, extracting most of condensed-nuclei aromatics from diesel oil, rich in saturated hydrocarbons, cycloalkane and part mononuclear aromatics
The ideal charging raffinated oil as hydro-refining unit, condition is relatively mild, can make the gasoline yield of hydrofining reaction
Amount increases, and can improve the yield of diesel oil distillate simultaneously.The treating capacity of hydro-refining unit can be increased, and energy consumption is relatively
Low.
2), condensed-nuclei aromatics is a kind of precipitation yellow sheet or acicular crystal from light petroleum, has light green fluorescence.In work
No produce and use value in industry, be typically only used as the accessory substance formed in production process with waste gas discharge.The present invention extracts out
Aromatic hydrocarbons or condensed-nuclei aromatics enter hydrocracking unit, and because purpose product is kerosene, its hydrocracking condition is steamed with corresponding more
Oily scheme is compared, and condition is relatively mild, with reducing energy consumption, and can increase the treating capacity of hydrocracking unit.
Specific embodiment
Below in conjunction with embodiment, embodiment of the present invention is described in detail, but those skilled in the art will
Understand, the following example is merely to illustrate the present invention, and be not construed as limiting the scope of the present invention.Unreceipted concrete in embodiment
Condition person, the condition according to normal condition or manufacturer's suggestion is carried out.Agents useful for same or the unreceipted production firm person of instrument, are
Can be by the commercially available conventional products bought and obtain.
Embodiment 1
Raw material：Catalytic cracking diesel oil, mononuclear aromatics content 45.3 (m%), polycyclic aromatic hydrocarbon content 18 (m%), Cetane number：
27.6, density (20 DEG C) 901.5g/kg.
Extraction tube is always high 8.0 meters, tower diameter 480mm, and extracting section is high 5 meters.1.5 meters of top is upper settling section, and 1.5 meters of bottom is
Lower settling section.At 1.5 meters of ttom of pipe, diesel oil import is at 1.5 meters of pipe top for solvent inlet.Catalytic cracking diesel oil is heated to
40 DEG C, pump into from the diesel oil import on extraction tube top.Acetonitrile is heated to 50 DEG C, pumps into from the solvent inlet of extraction tube bottom,
Keep the volume ratio 3 of the two:1.What the top of extraction tube obtained is the mixture of tapped oil and acetonitrile, and what bottom obtained is raffinate
Oil.
The mixture of tapped oil and acetonitrile is extracted out laggard knockout tower from top of tower, by acetonitrile and tapped oil in knockout tower
Separate, acetonitrile recycles, and tapped oil is entered hydrocracking unit and is hydrocracked.Hydrocracking condition is that treater is averagely warm
377 DEG C of degree, inlet pressure 10.87Mpa；398 DEG C of cracker mean temperature, inlet pressure 10.92Mpa.Product mainly forms：Gently
Naphtha 9.49%, heavy naphtha 16.72%, navigate coal 30.67%, diesel oil 8.65%.
Raffinate oil and carry out hydrofinishing from the bottom of the tube laggard hydro-refining unit of extraction.Hydrofinishing conditions are air speed
1.3h-1, hydrogen-oil ratio 450,295 DEG C of reactor inlet temperature, inlet pressure 7.62Mpa.Product mainly forms：Gas 1.87%,
Gasoline 0.34%, diesel oil 97.7%, the Cetane number of diesel oil is more than 45.
Embodiment 2
Raw material：Coker gas oil, mononuclear aromatics content 47.2 (m%), polycyclic aromatic hydrocarbon content 19 (m%), Cetane number：
24.1, density (20 DEG C) 920.3g/kg.
Extraction tube is always high 8.0 meters, tower diameter 480mm, and extracting section is high 5 meters.1.5 meters of top is upper settling section, and 1.5 meters of bottom is
Lower settling section.At 1.5 meters of ttom of pipe, diesel oil import is at 1.5 meters of pipe top for solvent inlet.Coker gas oil is heated to 30
DEG C, pump into from the import on extraction tube top.Methyl alcohol is heated to 40 DEG C, pumps into from the solvent inlet of extraction tube bottom, keep pole
Property solvent and coker gas oil volume ratio 7:1.What the top of extraction tube obtained is the mixture of tapped oil and methyl alcohol, and bottom obtains
Be to raffinate oil.
The mixture of tapped oil and methyl alcohol is extracted out laggard knockout tower from top of tower, by methyl alcohol and tapped oil in knockout tower
Separate, methanol loop utilizes, tapped oil is entered hydrocracking unit and is hydrocracked.Hydrocracking condition is that treater is averagely warm
380 DEG C of degree, inlet pressure 10.45Mpa；400 DEG C of cracker mean temperature, inlet pressure 10.98Mpa.Product mainly forms：Gently
Naphtha 10.16%, heavy naphtha 17.55%, navigate coal 27.34%, diesel oil 8.17%.
Raffinate oil and carry out hydrofinishing from the bottom of the tube laggard hydro-refining unit of extraction.Hydrofinishing conditions are air speed
1.3h-1, hydrogen-oil ratio 450,295 DEG C of reactor inlet temperature, inlet pressure 7.62Mpa.Product mainly forms：Gas 1.87%,
Gasoline 0.34%, diesel oil 97.7%, the Cetane number of diesel oil is more than 45.
Embodiment 3
Raw material：Straight-run diesel oil and the mixture of catalytic cracking diesel oil, mononuclear aromatics content 40.5 (m%), polycyclic aromatic hydrocarbon contains
Amount 19 (m%), Cetane number：24.1, density (20 DEG C) 879.7g/kg.
Extraction tube is always high 8.0 meters, tower diameter 480mm, and extracting section is high 5 meters.1.5 meters of top is upper settling section, and 1.5 meters of bottom is
Lower settling section.At 1.5 meters of ttom of pipe, diesel oil import is at 1.5 meters of pipe top for solvent inlet.By straight-run diesel oil and catalytic cracking
The mixture of diesel oil is heated to 60 DEG C, pumps into from the import on extraction tube top.Ethanol is heated to 60 DEG C, from extraction tube bottom
Solvent inlet pumps into, and keeps the volume ratio 5 of polar solvent and straight-run diesel oil and the mixture of catalytic cracking diesel oil:1.Extraction tube
What top obtained is the mixture of tapped oil and ethanol, and what bottom obtained is to raffinate oil.
The mixture of tapped oil and ethanol is extracted out laggard knockout tower from top of tower, by ethanol and tapped oil in knockout tower
Separate, ethanol recycles, and tapped oil is entered hydrocracking unit and is hydrocracked.Hydrocracking condition is that treater is averagely warm
385 DEG C of degree, inlet pressure 11.26Mpa；395 DEG C of cracker mean temperature, inlet pressure 10.10Mpa.Product mainly forms：Gently
Naphtha 7.32%, heavy naphtha 17.09%, navigate coal 33.24%, diesel oil 8.97%.
Raffinate oil and carry out hydrofinishing from the bottom of the tube laggard hydro-refining unit of extraction.Hydrofinishing conditions are air speed
1.3h-1, hydrogen-oil ratio 450,295 DEG C of reactor inlet temperature, inlet pressure 7.62Mpa.Product mainly forms：Gas 1.87%,
Gasoline 0.34%, diesel oil 97.7%, the Cetane number of diesel oil is more than 45.
Embodiment 4
Raw material：Coker gas oil and the mixture of straight-run diesel oil, mononuclear aromatics content 42.9 (m%), polycyclic aromatic hydrocarbon content 18
(m%), Cetane number：25.1, density (20 DEG C) 876.1g/kg.
Using a knockout drum, the mixture of coker gas oil and straight-run diesel oil is heated to 50 DEG C, from extraction tube top
Import pumps into.Isopropanol is heated to 65 DEG C, pumps into from the solvent inlet of extraction tube bottom, keep the volume ratio 10 of the two:1.
The mixture of described coker gas oil and straight-run diesel oil and isopropanol are pumped into and is sufficiently mixed rear stratification in tank so that condensed ring is fragrant
Hydrocarbon enters organic solvent layer thus being separated.What top obtained is the mixture of tapped oil and isopropanol, and what bottom obtained is
Raffinate oil.
The mixture of tapped oil and isopropanol is extracted out laggard knockout tower from top of tower, by isopropanol and taking out in knockout tower
Fuel-displaced separation, isopropanol recycles, and tapped oil is entered hydrocracking unit and is hydrocracked.Hydrocracking condition is treater
380 DEG C of mean temperature, inlet pressure 11.21Mpa；399 DEG C of cracker mean temperature, inlet pressure 11.04Mpa.Product is main
Composition：Light naphthar 738%, heavy naphtha 14.69%, navigate coal 32.15%, diesel oil 9.03%.
Raffinate oil and carry out hydrofinishing from the bottom of the tube laggard hydro-refining unit of extraction.Hydrofinishing conditions are air speed
1.3h-1, hydrogen-oil ratio 450,295 DEG C of reactor inlet temperature, inlet pressure 7.62Mpa.Product mainly forms：Gas 1.87%,
Gasoline 0.34%, diesel oil 97.7%, the Cetane number of diesel oil is more than 45.
Embodiment 5
Raw material：Coker gas oil and the mixture of catalytic cracking diesel oil, mononuclear aromatics content 40.78 (m%), polycyclic aromatic hydrocarbon contains
Amount 19 (m%), Cetane number：22.1, density (20 DEG C) 851.0g/kg.
Using 3 knockout drums, the mixture of coker gas oil and catalytic cracking diesel oil is heated to 30 DEG C, from extraction tube top
Import pump into.Isopropanol is heated to 45 DEG C, pumps into from the solvent inlet of extraction tube bottom, keep the volume ratio 0.5 of the two:
1.Described diesel oil and isopropanol are pumped into be sufficiently mixed rear stratification in tank so that condensed-nuclei aromatics enter organic solvent layer thus
Separated.What top obtained is the mixture of tapped oil and isopropanol, and what bottom obtained is to raffinate oil.
The mixture of tapped oil and isopropanol is extracted out laggard knockout tower from top of tower, by isopropanol and taking out in knockout tower
Fuel-displaced separation, isopropanol recycles, and tapped oil is entered hydrocracking unit and is hydrocracked.Hydrocracking condition is treater
367 DEG C of mean temperature, inlet pressure 11.11Mpa；389 DEG C of cracker mean temperature, inlet pressure 10.68Mpa.Product is main
Composition：Light naphthar 735%, heavy naphtha 14.24%, navigate coal 33.13%, diesel oil 8.19%.
Raffinate oil and carry out hydrofinishing from the bottom of the tube laggard hydro-refining unit of extraction.Hydrofinishing conditions are air speed
1.3h-1, hydrogen-oil ratio 450,295 DEG C of reactor inlet temperature, inlet pressure 7.62Mpa.Product mainly forms：Gas 1.87%,
Gasoline 0.34%, diesel oil 97.7%, the Cetane number of diesel oil is more than 45.
In sum, processing method after the diesel oil that the present invention provides, most of condensed-nuclei aromatics is extracted from diesel oil
Afterwards, the ideal raffinated oil as hydro-refining unit rich in saturated hydrocarbons, cycloalkane and part mononuclear aromatics is on the one hand made to enter
Material, condition is relatively mild, the gasoline yield amount of hydrofining reaction can be made to increase, can improve the product of diesel oil distillate simultaneously
Rate.The treating capacity of hydro-refining unit can be increased, and energy consumption is relatively low.Aromatic hydrocarbons or condensed ring that the another aspect present invention extracts out
Aromatic hydrocarbons enters hydrocracking unit, because purpose product is kerosene, its hydrocracking condition with corresponding fecund gasoline scheme compared with,
Condition is relatively mild, with reducing energy consumption, and can increase the treating capacity of hydrocracking unit.
Finally it should be noted that：Various embodiments above only in order to technical scheme to be described, is not intended to limit；To the greatest extent
Pipe has been described in detail to the present invention with reference to foregoing embodiments, but it will be understood by those within the art that：Its
Still the technical scheme described in foregoing embodiments can be modified, or to wherein some or all of technical characteristic
Carry out equivalent；And these modifications or replacement, do not make the essence of appropriate technical solution depart from various embodiments of the present invention skill
The scope of art scheme.
Claims (10)
1. after a kind of diesel oil processing method it is characterised in that being extracted to the condensed-nuclei aromatics in described diesel oil using polar solvent
Take, carry out hydrocracked, treated after the polar solvent in the tapped oil obtaining is separated off and obtain based on kerosene and naphtha
Product；
After organic solvent in raffinating oil removes, hydrogenated refinement treatment obtains refined diesel oil and small part gasoline；
Described diesel oil includes one or more of catalytic cracking diesel oil, coker gas oil and straight-run diesel oil.
2. after diesel oil according to claim 1 processing method it is characterised in that the body of described polar solvent and described diesel oil
Long-pending ratio is (0.3～10)：1.
3. after diesel oil according to claim 1 processing method it is characterised in that described polar solvent polarity be more than 3.5；
Preferably, described polar solvent includes acetonitrile, methyl alcohol, ethanol, normal propyl alcohol, isopropanol, furfural and dimethylformamide
One or more of.
4. after diesel oil according to claim 3 processing method it is characterised in that carry out described extraction temperature be 5 DEG C～
90℃.
5. after diesel oil according to claim 4 processing method it is characterised in that
When described organic solvent is acetonitrile or ethanol, extraction temperature is 10 DEG C～70 DEG C；
When described organic solvent is methyl alcohol, extraction temperature is 10 DEG C～60 DEG C.
6. after diesel oil according to claim 1 processing method it is characterised in that described by the polarity in the tapped oil obtaining
The method that solvent is separated off is distillation.
7. after diesel oil according to claim 1 processing method it is characterised in that described use polar solvent is to described diesel oil
Carry out in extraction device when being extracted；
Described extraction device includes extraction tube and/or knockout drum.
8. after diesel oil according to claim 7 processing method it is characterised in that described use polar solvent is to described diesel oil
The method being extracted is：
Diesel oil and polar solvent are pumped into from extraction tube upper and lower respectively, and standing point after being sufficiently mixed in extraction tube
Layer is so that condensed-nuclei aromatics enters organic solvent layer thus being separated.
9. after diesel oil according to claim 7 processing method it is characterised in that described use polar solvent is to described diesel oil
The method being extracted is：
Using one or more knockout drums, described diesel oil and polar solvent are pumped into be sufficiently mixed rear stratification in tank so that
Condensed-nuclei aromatics enters organic solvent layer thus being separated.
10. after the diesel oil according to any one of claim 1～9 processing method it is characterised in that described extraction times be one
Secondary or multiple.
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| CN108414340A (en) * | 2018-01-25 | 2018-08-17 | 潍坊学院 | Combined extraction fluorescence spectrum detection method applied to oil sources identification |
| CN110540875A (en) * | 2018-05-28 | 2019-12-06 | 中国石油化工股份有限公司 | Process for producing high density jet fuel and clean diesel |
| CN110540875B (en) * | 2018-05-28 | 2022-03-11 | 中国石油化工股份有限公司 | Process for producing high density jet fuel and clean diesel |
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