CN108018067A - The double solvents and method of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate - Google Patents
The double solvents and method of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate Download PDFInfo
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
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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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/28—Recovery of used solvent
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1081—Alkanes
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1096—Aromatics or polyaromatics
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/30—Aromatics
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to diesel oil distillate extracting aromatics separation field, discloses the double solvents and method of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate.The double solvents includes the cosolvent B of the main solvent A and 1~40 weight % of 60~99 weight %；Main solvent A is selected from the ionic liquid that cation is alkyl-substituted imidazoles or pyridylium, anion is hexafluoro-phosphate radical, tetrafluoroborate or bis trifluoromethyl sulfimide root, the total carbon number for substituting alkyl in cation is 6~12, and the carbon number of monosubstituted alkyl is 1~10；Cosolvent B is selected from the ionic liquid that cation is alkyl-substituted imidazoles or pyridylium, anion is hexafluoro-phosphate radical, tetrafluoroborate or bis trifluoromethyl sulfimide root, the total carbon number for substituting alkyl in cation is 2~5, and the carbon number of monosubstituted alkyl is 1~4；Main solvent A is identical with the anion of cosolvent B.The double solvents can more effectively separate the aromatic component in diesel oil distillate, improve the property of diesel product.
Description
Technical field
The present invention relates to diesel oil distillate extracting aromatics separation field, and in particular, in one kind extracting separation diesel oil distillate
The double solvents and method of aromatic hydrocarbons and alkane.
Background technology
In the case where developing low-carbon economy, realize the big situation of sustainable development, oil quality upgrading paces are substantially accelerated, new
Control in environmental regulation on motor vehicle exhaust emission is higher and higher for diesel quality requirement, and particularly aromatic hydrocarbons in diesel oil is contained
The requirement of amount and Cetane number is more and more stringenter.
The catalytic diesel oil (LCO) of China's secondary operation, coker gas oil, to be hydrocracked the quantity such as diesel oil relatively more, secondary
It is 50% or so to process diesel oil accounting in diesel pool, and wherein LCO accounts for 30% of diesel pool or so.Arene content exists in LCO
Arene content is more up to more than 60% in the LCO that feedstock oil beyond more than 40%, particularly paraffinic base is produced through catalytic cracking,
Cetane number is very low.This part diesel oil is difficult to meet increasingly stringent diesel oil standard, it is necessary to can just be used as finished product bavin by modification
The blend component of oil.
Traditional method for modifying is to carry out hydrotreating to secondary processing diesel oil, makes the aromatic hydrocarbons saturation in diesel oil, improves one
Diesel oil blending component is used as after fixed Cetane number.Limited by environmental requirement and the market demand promotes, China Diesel adds
Hydrogen modification technology is rapidly developed, but the operating cost of hydrogenation modifying process is high, operating condition is harsh, causes diesel production
Cost it is unprecedented soaring.Therefore, it is imperative to develop the non-hydrogenated diesel oil modification technology that new cost is low, investment is small.
Solvent extraction (aromatics production field commonly referred to as " extracts ") technology can efficiently separate saturated hydrocarbons and aromatic hydrocarbons,
BTX is produced and gasoline fraction aromatics separation aspect, has had many industrialized extraction process, such as the extracting of liquid liquid, extractive distillation
Deng.Aromatic hydrocarbons is isolated from diesel oil distillate using liquid liquid extraction technique, can not only improve diesel quality, while obtained aromatic hydrocarbons
The BTX or high-knock rating gasoline of high value can be obtained by carrying out processing, can receive obvious economic benefit, moreover it is possible to be greatly reduced
Environmental pollution, produces good social benefit.
CN102021024A discloses a kind of system and method for preparing high-quality diesel.The system includes extracting and fills
Put, a part of aromatic hydrocarbons in diesel oil is removed by solvent extraction, raffinates oil and obtains high-quality diesel through hydrogenated processing, containing aromatic hydrocarbons
Tapped oil is through separation, light aromatic hydrocarbons and heavy aromatics discharge system, most light component as return lotion return tapped oil back scrubber bottom and
Extraction tower bottom.The diversification of feedstock of this method processing, can be various diesel oil, aromatic hydrocarbons is separated from diesel oil, is carried significantly
The high Cetane number of diesel oil, reduces condensation point of diesel oil, extraction solvent used is selected from sulfolane, 1-methyl-2-pyrrolidinone or two
Methyl sulfoxide.
CN1769392A discloses a kind of method for modifying of poor ignition quality fuel.This method is by hydrogenation modifying process and solvent extraction
Process combination forms, and the liquid product after the hydrogenated modification of poor ignition quality fuel isolates most of aromatic hydrocarbons therein through solvent extraction,
Cleaning diesel oil is obtained, the aromatic component extracted is recycled back to hydro-upgrading unit and handles again.This method is sent out by group technology
The characteristics of waving two kinds of techniques each, can be greatly lowered the arene content of diesel oil distillate, improve diesel cetane-number, and keep
Higher diesel yield.
In the method for existing biodiesel solvent extracting modification, use the solvent of gasoline fraction Aromatics Extractive Project mostly, as sulfolane,
NMP etc., though these solvents can isolate the aromatic hydrocarbons in diesel oil, there is also selective poor, Determination of Alkane Content in extraction aromatic hydrocarbons
The defects of higher, and if when arene content is high in diesel oil distillate, it may appear that solvent and original miscible phenomenon, it is difficult to point
From.Have again using above-mentioned solvent heat endurance and poor chemical stability, the side reaction such as easily decompose, aoxidize, to operation bar
Part is more demanding.In addition the certain residual of meeting in the product of acquisition, influences the indexs such as the sulphur nitrogen content of oil product.
CN1524006A discloses a kind of homogeneous and multiphase vapor of mixture for utilizing ionic liquid (IL) separation of close-boiling
The method of thing.This method using ionic liquid as rectifying in additive, to separate alkane and olefine, ketone and alcohol and acyl
The mixture such as amine and acid.The selectivity of ionic liquid is substantially better than common additives.In addition the vapour pressure of ionic liquid is very low, its
Shared partial pressure is approximately equal to 0 in overhead mixture, so may dispense with overhead product and alloying agent separative element, with regard to cost and
For energy, better than conventional extraction rectifying.
CN101265152A discloses a kind of application of ionic liquid as extracting rectifying and separating benzene and the solvent of hexamethylene, makes
Ionic liquid with glyoxaline cation, hexafluorophosphoric acid anion or halide anion is solvent, and benzene and hexamethylene are passed through extraction
Separated.
CN104945327A discloses the extraction solvent of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate, uses ion
Liquid is extraction solvent, and the cation of the ionic liquid is alkyl-substituted imidazoles or pyridylium, anion BF4 -
Or PF6 -。
The content of the invention
, should the object of the present invention is to provide the double solvents and method of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate
Method can effectively extract aromatic hydrocarbons and alkane component in separation diesel oil using double solvents, and improve the quality of diesel oil distillate.
The present invention provides the double solvents of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate, including 60~99 weight %
Main solvent A and 1~40 weight % cosolvent B；The main solvent A is selected from cation as alkyl-substituted imidazoles or pyridine sun
Ion, anion be hexafluoro-phosphate radical, tetrafluoroborate or bis trifluoromethyl sulfimide root ionic liquid, wherein, sun from
The total carbon number for substituting alkyl in son is 6~12, and the carbon number of monosubstituted alkyl is 1~10；The cosolvent B is alkane selected from cation
The imidazoles or pyridylium, anion of base substitution are hexafluoro-phosphate radical, tetrafluoroborate or bis trifluoromethyl sulfimide root
Ionic liquid, wherein, total carbon number that alkyl is substituted in cation is 2~5, and the carbon number of monosubstituted alkyl is 1~4；The master
Solvent orange 2 A is identical with the anion of cosolvent B.
Present invention also offers a kind of method of aromatic hydrocarbons and alkane in extracting separation diesel oil distillate, including：By diesel oil distillate
Fed from below into extraction tower, extraction solvent is sent into the extraction tower from top and carries out liquid phase extracting, the obtained pumping rich in alkane
Excess oil is discharged from the top of extraction tower, and the obtained rich solvent rich in aromatic hydrocarbons and extraction solvent is discharged from the bottom of extraction tower；Institute
The top that rich solvent is sent into back extraction tower is stated, back washing agent is sent into back extraction tower from the lower part of back extraction tower and is stripped, and what is obtained is poor molten
Agent is recycled back into extraction tower, obtained back extraction is mutually from the top discharge of back extraction tower from the bottom discharge of back extraction tower；The back extraction phase
It is sent into vacuum distillation tower to be evaporated under reduced pressure, obtained back washing agent discharges from the top of vacuum distillation tower and is recycled back into back extraction tower
Lower part, the obtained tapped oil rich in aromatic hydrocarbons discharges from the bottom of vacuum distillation tower；Wherein, the extraction solvent is the present invention
Double solvents.
The present invention forms double solvents using two kinds of ionic liquids, limits the ionic liquid that main solvent and cosolvent select
Species, and compound dosage, so as to improve the effect of aromatic hydrocarbons and alkane in extracting separation diesel oil distillate, and improve gained bavin
The quality of oil distillate, such as Cetane number.
Other features and advantages of the present invention will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Attached drawing is for providing a further understanding of the present invention, and a part for constitution instruction, with following tool
Body embodiment is used to explain the present invention together, but is not construed as limiting the invention.In the accompanying drawings：
Fig. 1 is the flow diagram of aromatic hydrocarbons and alkane in present invention separation diesel oil distillate.
Embodiment
The embodiment of the present invention is described in detail below.It is it should be appreciated that described herein specific
Embodiment is merely to illustrate and explain the present invention, and is not intended to limit the invention.
The endpoint of disclosed scope and any value are not limited to the accurate scope or value herein, these scopes or
Value should be understood to comprising the value close to these scopes or value.For number range, between the endpoint value of each scope, respectively
It can be combined with each other between the endpoint value of a scope and single point value, and individually between point value and obtain one or more
New number range, these number ranges should be considered as specific open herein.
The first object of the present invention, there is provided the double solvents of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate, including
The cosolvent B of the main solvent A of 60~99 weight % and 1~40 weight %；It is alkyl-substituted that the main solvent A, which is selected from cation,
Imidazoles or pyridylium, the ionic liquid that anion is hexafluoro-phosphate radical, tetrafluoroborate or bis trifluoromethyl sulfimide root
Body, wherein, total carbon number that alkyl is substituted in cation is 6~12, and the carbon number of monosubstituted alkyl is 1~10；The cosolvent B choosings
From cation be alkyl-substituted imidazoles or pyridylium, anion be hexafluoro-phosphate radical, tetrafluoroborate or double fluoroforms
The ionic liquid of base sulfimide root, wherein, total carbon number that alkyl is substituted in cation is 2~5, and the carbon number of monosubstituted alkyl is
1~4；The main solvent A is identical with the anion of cosolvent B.
Ionic liquid refers to what is be in a liquid state in room temperature or close to room temperature when, completely by organic cation and inorganic or organic the moon
From molecular salt.Ionic liquid heat endurance and chemical stability are good, nonflammable, not easy to explode, not oxidizable, nothing
Poison；Ionic liquid is not volatile, and rather low steam pressure can be also kept at higher temperature and vacuum.
In double solvents of the present invention, main solvent A and cosolvent B each select specific ionic liquid, overcome using single
The limitation of one ionic liquid, the aromatic hydrocarbons in diesel oil distillate is separated to extracting has the dissolubility of higher, and diesel oil is separated for extracting
Aromatic hydrocarbons and alkane have more preferable separating effect in cut.The diesel product obtained at the same time has higher Cetane number, Ke Yiman
The quality standard of sufficient diesel oil.
In the case of, according to the invention it is preferred to, the alkyl-substituted glyoxaline cation has the structure of formula (I), the alkane
The pyridylium of base substitution has the structure of formula (II)：
Wherein, in the main solvent A, R1、R2、R3、R4Respectively C1~C8Alkyl, R in formula (I)1+R2Total carbon number be 6
~12, R in formula (II)3+R4Total carbon number be 6~12；
In the cosolvent B, R1、R2、R3、R4Respectively C1~C4Alkyl, R in formula (I)1+R2Total carbon number be 2~5,
R in formula (II)3+R4Total carbon number be 2~5.
In the present invention, the anion of the ionic liquid is hexafluoro-phosphate radical ([PF6]-), tetrafluoroborate ([BF4]-) or
Bis trifluoromethyl sulfimide root ([NTF2]-)。
In the case of, according to the invention it is preferred to, total carbon number of cationic substituent is 8~12 in the main solvent A, cosolvent
Total carbon number of cationic substituent is 2~5 in B；Anion in main solvent A and cosolvent B is selected from tetrafluoroborate, hexafluoro phosphorus
Acid group or bis trifluoromethyl sulfimide root anion, and main solvent A is identical with the anion in cosolvent B.
In the case of, according to the invention it is preferred to, the double solvents includes the main solvent A and 2~30 weights of 70~98 weight %
Measure the cosolvent B of %.
The second object of the present invention, there is provided a kind of method of aromatic hydrocarbons and alkane in extracting separation diesel oil distillate, including：By bavin
Oil distillate is sent into the extraction tower from top and carries out liquid phase extracting fed from below into extraction tower, extraction solvent, and what is obtained is rich in alkane
Hydrocarbon is raffinated oil from the discharge of the top of extraction tower, and the obtained rich solvent rich in aromatic hydrocarbons and extraction solvent is arranged from the bottom of extraction tower
Go out；The rich solvent is sent into the top of back extraction tower, and back washing agent is sent into back extraction tower from the lower part of back extraction tower and is stripped, obtained
Lean solvent is recycled back into extraction tower, obtained back extraction is mutually from the top discharge of back extraction tower from the bottom discharge of back extraction tower；It is described anti-
Extraction is mutually sent into vacuum distillation tower and is evaporated under reduced pressure, and obtained back washing agent is discharged from the top of vacuum distillation tower and is recycled back into anti-
Extract the lower part of tower, the obtained tapped oil rich in aromatic hydrocarbons is discharged from the bottom of vacuum distillation tower；Wherein, the extraction solvent is this
The double solvents of invention.
According to the present invention, there is provided the above method in, the diesel oil distillate be selected from straight-run diesel oil, catalytic cracking light cycle oil
(LCO), at least one of coker gas oil, DCL/Direct coal liquefaction gained diesel oil distillate and diesel oil distillate obtained by coal tar.This method
It can be adapted to the diesel oil distillate for handling high arene content.
According to the present invention, the extraction tower is contacted for the diesel oil distillate with the extraction solvent, carries out liquid phase
Extracting, the diesel oil distillate and the extraction solvent can extract isolated raffinate oil and rich solvent with counter current contacting.Raffinate oil
In be rich in alkane, be rich in aromatic hydrocarbons and extraction solvent in rich solvent.The preferred guarantee of operating condition for carrying out the extracting evaporates diesel oil
Aromatic hydrocarbons in point has better choice.Under preferable case, the mass ratio of the extraction solvent and diesel oil distillate is (0.5~50)
: 1, be preferably (1~10): 1.Wherein, the quality requirement that can meet as diesel oil of raffinating oil, the group for concocted diesel oil
Point.
In the case of, according to the invention it is preferred to, in the extraction tower, extraction temperature is 15~120 DEG C, extraction pressure 0.1
~0.5MPa.
According to the present invention, the back extraction tower is used to be stripped, and the rich solvent is carried out liquid phase separation, is stripped
Phase and lean solvent, make the aromatic hydrocarbons in the rich solvent be separated with ionic liquid.The rich solvent is with back washing agent in the back extraction tower
In contacted, be preferably counter current contacting.Obtained back extraction is mutually rich in aromatic hydrocarbons, and obtained lean solvent is mainly extraction solvent.It is excellent
In the case of choosing, the back washing agent is selected from C4~C10Alkane or cycloalkane.Preferably, the back washing agent can be selected from hexamethylene,
Normal heptane.
In the case of, according to the invention it is preferred to, the mass ratio of the back washing agent and rich solvent is (0.2~7): 1, be preferably
(0.5~4): 1.
In the present invention, it is possible to further which the lean solvent is returned the extraction tower, circulation is as extraction solvent profit
With the utilization ratio of extraction solvent can be improved.
In the case of, according to the invention it is preferred to, the operation temperature of the back extraction tower is 15~50 DEG C, is preferably 20~40 DEG C；
The operating pressure of the back extraction tower is 0.1~0.5MPa, is preferably 0.1~0.2MPa.
According to the present invention, the vacuum distillation tower is used for the back extraction phase separation, separates back washing agent and aromatic hydrocarbons therein.It is excellent
In the case of choosing, the operation temperature of the vacuum distillation tower is 15~130 DEG C, the operating pressure of the vacuum distillation tower for 10~
50kPa.Through separation, obtained back washing agent can return to back extraction of the back extraction tower circulation for the rich solvent；It is separated
Aromatic hydrocarbons is obtained with the extraction oil form rich in aromatic hydrocarbons.
The method that explanation separates aromatic hydrocarbons in diesel oil using double solvents provided by the invention below in conjunction with the accompanying drawings.
In Fig. 1, diesel oil distillate enters extraction tower 1 through pipeline 5 from lower part, and extraction solvent enters through pipeline 4 from top to be extracted
Tower 1；By liquid phase extractive process, raffinate oil and discharged through pipeline 6 from the top of extraction tower 1, diesel oil blending component can be used as；It is rich in
The rich solvent of aromatic hydrocarbons and extraction solvent is discharged by the bottom of extraction tower 1, the top of back extraction tower 2 is entered through pipeline 7, back washing agent is through pipe
Line 8 enters back extraction tower 2 from lower part；By stripping process, poor extraction solvent enters from the bottom discharge of back extraction tower 2 through pipeline 10
1 top of extraction tower recycles；Back extraction mutually from the top discharge of back extraction tower 2, enters vacuum distillation tower 3, by decompression through pipeline 9
Distillation process, back washing agent are discharged from the top of vacuum distillation tower 3, and the lower part that back extraction tower 2 is entered through pipeline 11 recycles, and is rich in
The tapped oil of aromatic hydrocarbons is discharged through pipeline 12 from the bottom of vacuum distillation tower 3, and the component of tapped oil is essentially aromatic hydrocarbons, can be through further
Process for producing high-knock rating gasoline, light aromatics --- benzene, toluene and dimethylbenzene.
In the present invention, the effect of the aromatic hydrocarbons and alkane in separation diesel oil distillate, Ke Yitong are extracted for the extraction solvent
Selectivity factor is crossed to evaluate.The selectivity factor can use simulation diesel oil to be stripped, and evaluate the extracting of extraction solvent
Separating effect.Selectivity factor can be calculated by following formula：
Selectivity factor β=(yA/yB)/(xA/xB),
Wherein yA、yBFor the mass fraction of aromatic hydrocarbons, alkane in tapped oil, xA、xBFor the quality of raffinate oil middle aromatic hydrocarbons and alkane
Fraction.
In the present invention, shown pressure is absolute pressure.
The present invention will be described in detail by way of examples below.
In following embodiments and comparative example, the raw material diesel oil composition and Cetane number used is as shown in table 1.
The selectivity factor for evaluating extraction solvent uses binary simulation diesel oil A (hexadecane and naphthane in mass ratio 1: 1
The mixture being made into), binary simulation diesel oil B (mixture that hexadecane is made into 1- methyl naphthalenes in mass ratio 1: 1).
Table 1
| Raw material diesel oil | C(LCO) | D (LCO+ coker gas oils) |
| Composition, wt% | ||
| Alkane | 16.7 | 18.7 |
| Cycloalkane | 6.5 | 10.4 |
| Total aromatic hydrocarbons | 76.8 | 70.9 |
| Mononuclear aromatics | 24.7 | 45.8 |
| Bicyclic and above aromatic hydrocarbons | 52.1 | 25.1 |
| Cetane number | 20.6 | 27.5 |
Embodiment 1-1
This example demonstrates that the selectivity factor of the extraction solvent of the evaluation and test present invention.
With 1- n-heptyl -3- methylimidazoles hexafluorophosphate (hereinafter abbreviated as IL1, [HMIM] PF6, similarly hereinafter) based on it is molten
Agent, 1,3- methylimidazole hexafluorophosphate (IL2, [MMIM] PF6) it is cosolvent, in mass ratio double solvents is prepared for 95: 5
(IL1+IL2)。
Double solvents is mixed with simulation diesel oil A according to 3: 1 agent/oil quality ratio, single extracting is carried out under agitation, takes out
Temperature raising degree is 50 DEG C, extraction pressure 0.1MPa, and extracting mixing time is 30min.
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
Embodiment 1-2
With 1- n-heptyl -3- methyl imidazolium tetrafluoroborates (IL3, [HMIM] BF4) it is main solvent, 1,3- methylimidazole
Tetrafluoroborate (IL4, [MMIM] BF4) it is cosolvent, in mass ratio double solvents (IL3+IL4) is prepared for 95: 5.
Double solvents is mixed with simulation diesel oil A according to 3: 1 agent/oil quality ratio, single extracting is carried out under agitation, takes out
Temperature raising degree is 90 DEG C, extraction pressure 0.1MPa, and extracting mixing time is 30min.
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
Embodiment 1-3
With 1- n-heptyl -3- methylimidazole bis trifluoromethyls sulfimide salts (IL5, [HMIM] NTF2) it is main solvent, 1,
3- methylimidazole bis trifluoromethyls sulfimide salt (IL6, [MMIM] NTF2) it is cosolvent, prepared in mass ratio for 95: 5 multiple
Bonding solvent (IL5+IL6).
Double solvents is mixed with simulation diesel oil A according to 3: 1 agent/oil quality ratio, single extracting is carried out under agitation, takes out
Temperature raising degree is 70 DEG C, extraction pressure 0.1MPa, and extracting mixing time is 30min.
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
Comparative example 1-1
Method according to embodiment 1-1 is stripped, unlike, with IL1 ([HMIM] PF6) alternative composite solvent (IL1
+IL2)。
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
Comparative example 1-2
Method according to embodiment 1-1 is stripped, unlike, with IL3 ([HMIM] BF4) alternative composite solvent (IL1
+IL2)。
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
Comparative example 1-3
Method according to embodiment 1-1 is stripped, unlike, with IL5 ([HMIM] NTF2) alternative composite solvent
(IL1+IL2)。
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
Comparative example 1-4
Method according to embodiment 1-1 is stripped, unlike, with sulfolane alternative composite solvent (IL1+IL2).
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
Comparative example 1-5
Method according to embodiment 1-1 is stripped, unlike, with n,N-Dimethylformamide (DMF) alternative composite
Solvent (IL1+IL2).
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 2.
As can be seen from Table 2, the ionic liquid composite solvent of main solvent and cosolvent mixing provided by the invention is to tetrahydrochysene
The selectivity of naphthalene is far above conventional organic solvent sulfolane and DMF, and arene content is also above routine in the tapped oil extracted
Organic solvent.The selectivity of ionic liquid composite solvent provided by the invention is higher than the extracting effect that single ionic liquid makees solvent
Fruit, arene content makees solvent also above single ionic liquid in obtained tapped oil.
Embodiment 2-1
This example demonstrates that the selectivity factor of the extraction solvent of the evaluation and test present invention.
With N- n-heptyl -4- picolines hexafluorophosphate (IL7, [HMPy] PF6) it is main solvent, N- normal-butyl -3- first
Yl pyridines hexafluorophosphate (IL8, [BMPy] PF6) it is cosolvent, in mass ratio double solvents (IL7+IL8) is prepared for 90: 10.
Double solvents is mixed with simulation diesel oil B according to 2: 1 agent/oil quality ratio, single extracting is carried out under agitation, takes out
Temperature raising degree is 50 DEG C, extraction pressure 0.1MPa, extracting mixing time 30min.
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to 1- methyl naphthalenes.Extracting the results are shown in Table 3.
Embodiment 2-2
This example demonstrates that the selectivity factor of the extraction solvent of the evaluation and test present invention.
With N- n-heptyl -4- picolines tetrafluoroborate (IL9, [HMPy] BF4) it is main solvent, N- normal-butyl -3- first
Yl pyridines tetrafluoroborate (IL10, [BMPy] BF4) it is cosolvent, in mass ratio double solvents (IL9+ is prepared for 90: 10
IL10)。
Double solvents is mixed with simulation diesel oil B according to 2: 1 agent/oil quality ratio, single extracting is carried out under agitation, takes out
Temperature raising degree is 50 DEG C, extraction pressure 0.1MPa, extracting mixing time 30min.
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to 1- methyl naphthalenes.Extracting the results are shown in Table 3.
Embodiment 2-3
This example demonstrates that the selectivity factor of the extraction solvent of the evaluation and test present invention.
With N- n-heptyl -4- picoline bis trifluoromethyls sulfimide salts (IL11, [HMPy] NTF2) it is main solvent, N-
Normal-butyl -3- picoline bis trifluoromethyls sulfimide salt (IL12, [BMPy] NTF2) it is cosolvent, be in mass ratio 90:
10 prepare double solvents (IL11+IL12).
Double solvents is mixed with simulation diesel oil B according to 2: 1 agent/oil quality ratio, single extracting is carried out under agitation, takes out
Temperature raising degree is 70 DEG C, extraction pressure 0.1MPa, extracting mixing time 30min.
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to 1- methyl naphthalenes.Extracting the results are shown in Table 3.
Comparative example 2-1
Method according to embodiment 2-1 is stripped, unlike, with IL7 ([HMPy] PF6) alternative composite solvent (IL7
+IL8)。
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to 1- methyl naphthalenes.Extracting the results are shown in Table 3.
Comparative example 2-2
Method according to embodiment 2-1 is stripped, unlike, with IL9 ([HMPy] BF4) alternative composite solvent (IL7
+IL8)。
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 3.
Comparative example 2-3
Method according to embodiment 2-1 is stripped, unlike, with IL11 ([HMPy] NTF2) alternative composite solvent
(IL7+IL8)。
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to 1- methyl naphthalenes.Extracting the results are shown in Table 3.
Comparative example 2-4
Method according to embodiment 2-1 is stripped, unlike, with sulfolane alternative composite solvent (IL7+IL8).
Analysis is raffinated oil to be formed with tapped oil, calculates selectivity of the solvent to naphthane.Extracting the results are shown in Table 3.
Embodiment 3
This example demonstrates that the extraction solvent of the present invention is stripped diesel oil distillate separation.
With IL7 ([HMPy] PF6) it is main solvent, IL2 ([MMIM] PF6) it is cosolvent, prepared in mass ratio for 95: 5 compound
Solvent (IL7+IL2).
By Fig. 1 flows, raw material diesel oil C is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 4
With 1,3- dibutyl limidazolium hexafluorophosphate (IL13, [BBIM] PF6) it is main solvent, IL2 ([MMIM] PF6) it is to help
Solvent, prepares double solvents (IL13+IL2) for 70: 30 in mass ratio.
By Fig. 1 flows, raw material diesel oil D is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 5
With IL1 ([HMIM] PF6) it is main solvent, IL8 ([BMPy] PF6) it is cosolvent, prepared in mass ratio for 85: 15 multiple
Bonding solvent (IL1+IL8).
By Fig. 1 flows, raw material diesel oil D is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 6
With IL9 ([HMPy] BF4) it is main solvent, IL4 ([MMIM] BF4) it is cosolvent, prepared in mass ratio for 95: 5 compound
Solvent (IL9+IL4).
By Fig. 1 flows, raw material diesel oil C is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 7
With 1,3- dibutyl tetrafluoroborate (IL14, [BBIM] BF4) it is main solvent, IL4 ([MMIM] BF4) it is to help
Solvent, prepares double solvents (IL14+IL4) for 70: 30 in mass ratio.
By Fig. 1 flows, raw material diesel oil C is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 8
With IL3 ([HMIM] BF4) it is main solvent, IL10 ([BMPy] BF4) it is cosolvent, prepared in mass ratio for 85: 15 multiple
Bonding solvent (IL3+IL10).
By Fig. 1 flows, raw material diesel oil D is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 9
With IL11 ([HMPy] NTF2) it is main solvent, IL6 ([MMIM] NTF2) it is cosolvent, prepared in mass ratio for 95: 5
Double solvents (IL11+IL6).
By Fig. 1 flows, raw material diesel oil C is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 10
With 1,3- dibutyl imidazoles bis-trifluoromethylsulfoandimides salt (IL15, [BBIM] NTF2) it is main solvent, IL6
([MMIM]NTF2) it is cosolvent, in mass ratio double solvents (IL15+IL6) is prepared for 70: 30.
By Fig. 1 flows, raw material diesel oil C is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Embodiment 11
With IL5 ([HMIM] NTF2) it is main solvent, IL12 ([BMPy] NTF2) it is cosolvent, in mass ratio 85: 15 prepare again
Bonding solvent (IL5+IL12).
By Fig. 1 flows, raw material diesel oil D is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Comparative example 3
By Fig. 1 flows, raw material diesel oil D is stripped using sulfolane as extraction solvent, extraction tower, back extraction in extractive process
The operating condition of tower and vacuum distillation tower is shown in Table 4, and extracting the results are shown in Table 5.
Comparative example 4
With IL3 ([HMIM] BF4) it is main solvent, sulfolane is cosolvent, prepares double solvents in mass ratio for 85: 15
(IL3+ sulfolane).
By Fig. 1 flows, raw material diesel oil D is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
Comparative example 5
It is main solvent with 1- butyl -3- methylimidazoles tosilate (IL16, [BMIM] TSA), 1,3- dimethyl miaow
Azoles dodecyl benzene sulfonate (IL17, [MMIM] DBSA) is cosolvent, prepares double solvents (IL16+ in mass ratio for 90: 10
IL17)。
By Fig. 1 flows, raw material diesel oil D is stripped with double solvents, extraction tower, back extraction tower and decompression in extractive process
The operating condition of destilling tower is shown in Table 4, and extracting the results are shown in Table 5.
It can be seen that from above-described embodiment, comparative example and list data and evaporated provided by the present invention for extracting separation diesel oil
The ionic liquid composite solvent of aromatic hydrocarbons and alkane in point, can there is the selectivity factor for isolating aromatic hydrocarbons of higher, obtained pumping
Fuel-displaced middle arene content higher, the mass fraction of non-aromatic component are less than 2%.And raffinate oil with more preferable Cetane number.
Double solvents provided by the invention can more effectively separate the aromatic component in diesel oil distillate, improve the property of diesel product.
Claims (9)
1. the double solvents of aromatic hydrocarbons and alkane in a kind of extracting separation diesel oil distillate, includes the main solvent A and 1 of 60~99 weight %
The cosolvent B of~40 weight %；
The main solvent A selected from cation be alkyl-substituted imidazoles or pyridylium, anion be hexafluoro-phosphate radical, tetrafluoro
The ionic liquid of borate or bis trifluoromethyl sulfimide root, wherein, total carbon number that alkyl is substituted in cation is 6~12,
The carbon number of monosubstituted alkyl is 1~10；
The cosolvent B selected from cation be alkyl-substituted imidazoles or pyridylium, anion be hexafluoro-phosphate radical, tetrafluoro
The ionic liquid of borate or bis trifluoromethyl sulfimide root, wherein, total carbon number that alkyl is substituted in cation is 2~5, single
The carbon number for substituting alkyl is 1~4；
The main solvent A is identical with the anion of cosolvent B.
2. double solvents according to claim 1, wherein, the alkyl-substituted glyoxaline cation has the knot of formula (I)
Structure, the alkyl-substituted pyridylium have the structure of formula (II)：
Wherein, in the main solvent A, R1、R2、R3、R4Respectively C1~C8Alkyl, R in formula (I)1+R2Total carbon number for 6~
12, R in formula (II)3+R4Total carbon number be 6~12；
In the cosolvent B, R1、R2、R3、R4Respectively C1~C4Alkyl, R in formula (I)1+R2Total carbon number be 2~5, formula
(II) R in3+R4Total carbon number be 2~5.
3. double solvents according to claim 1 or 2, wherein, total carbon number of cationic substituent is in the main solvent A
Total carbon number of cationic substituent is 2~4 in 8~12, cosolvent B；Anion in main solvent A and cosolvent B is selected from tetrafluoro
Borate, hexafluoro-phosphate radical or bis trifluoromethyl sulfimide root anion, and the anion phase in main solvent A and cosolvent B
Together.
4. a kind of method of aromatic hydrocarbons and alkane in extracting separation diesel oil distillate, including：
Diesel oil distillate is sent into the extraction tower from top and carries out liquid phase extracting, obtained fed from below into extraction tower, extraction solvent
Raffinating oil from the discharge of the top of extraction tower rich in alkane, the obtained rich solvent rich in aromatic hydrocarbons and extraction solvent is from extraction tower
Bottom discharge；
The rich solvent is sent into the top of back extraction tower, and back washing agent is sent into back extraction tower from the lower part of back extraction tower and is stripped, obtained
Lean solvent from back extraction tower bottom discharge, be recycled back into extraction tower, obtain back extraction mutually from back extraction tower top discharge；
The back extraction is mutually sent into vacuum distillation tower and is evaporated under reduced pressure, and obtained back washing agent is discharged simultaneously from the top of vacuum distillation tower
The lower part of back extraction tower is recycled back into, the obtained tapped oil rich in aromatic hydrocarbons is discharged from the bottom of vacuum distillation tower；
Wherein, the extraction solvent is the double solvents described in any one in claim 1-3.
5. according to the method described in claim 4, wherein, the mass ratio of the extraction solvent and diesel oil distillate is (0.5~50):
1, be preferably (1~10):1.
6. according to the method described in claim 4, wherein, in the extraction tower, extraction temperature is 15~120 DEG C, extraction pressure
For 0.1~0.5MPa.
7. according to the method described in claim 4, wherein, the back washing agent is selected from C4~C10Alkane or cycloalkane；It is described anti-
The mass ratio for extracting agent and rich solvent is (0.2~7)：1；The operation temperature of the back extraction tower is 15~50 DEG C, the back extraction tower
Operating pressure is 0.1~0.5MPa.
8. according to the method described in claim 4, wherein, the operation temperature of the vacuum distillation tower is 15~130 DEG C, described to subtract
The operating pressure for pressing destilling tower is 10~50kPa.
9. according to the method described in claim 4, wherein, the diesel oil distillate be selected from straight-run diesel oil, catalytic cracking light cycle oil,
At least one of diesel oil distillate obtained by diesel oil distillate obtained by coker gas oil, DCL/Direct coal liquefaction and coal tar.
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