CN116606669A - Solvent for deasphalting cycloalkyl vacuum residuum and solvent deasphalting method - Google Patents
Solvent for deasphalting cycloalkyl vacuum residuum and solvent deasphalting method Download PDFInfo
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- CN116606669A CN116606669A CN202310633700.3A CN202310633700A CN116606669A CN 116606669 A CN116606669 A CN 116606669A CN 202310633700 A CN202310633700 A CN 202310633700A CN 116606669 A CN116606669 A CN 116606669A
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- Prior art keywords
- solvent
- deasphalting
- vacuum residuum
- cycloalkyl vacuum
- cycloalkyl
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- 239000002904 solvent Substances 0.000 title claims abstract description 88
- 125000000753 cycloalkyl group Chemical group 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 23
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 claims abstract description 39
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical compound CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000010426 asphalt Substances 0.000 claims abstract description 8
- 238000011084 recovery Methods 0.000 claims description 39
- 238000000605 extraction Methods 0.000 claims description 36
- VZWGRQBCURJOMT-UHFFFAOYSA-N Dodecyl acetate Chemical compound CCCCCCCCCCCCOC(C)=O VZWGRQBCURJOMT-UHFFFAOYSA-N 0.000 claims description 10
- QUKGYYKBILRGFE-UHFFFAOYSA-N benzyl acetate Chemical compound CC(=O)OCC1=CC=CC=C1 QUKGYYKBILRGFE-UHFFFAOYSA-N 0.000 claims description 10
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 6
- 229940007550 benzyl acetate Drugs 0.000 claims description 6
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 claims description 3
- 125000003438 dodecyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 claims description 3
- 229920002503 polyoxyethylene-polyoxypropylene Polymers 0.000 claims description 3
- 239000012046 mixed solvent Substances 0.000 abstract description 5
- 239000002994 raw material Substances 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 49
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical group CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 239000000084 colloidal system Substances 0.000 description 5
- 239000010779 crude oil Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000000052 comparative effect Effects 0.000 description 3
- 239000001294 propane Substances 0.000 description 3
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- QUKGYYKBILRGFE-VJJZLTLGSA-N benzyl acetate Chemical group C[13C](=O)OCC1=CC=CC=C1 QUKGYYKBILRGFE-VJJZLTLGSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000008094 contradictory effect Effects 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
-
- 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
- C10G21/12—Organic compounds only
- C10G21/14—Hydrocarbons
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a solvent for deasphalting cycloalkyl vacuum residuum and a solvent deasphalting method, and relates to the technical field of solvent deasphalting. The invention provides a solvent for deasphalting cycloalkyl vacuum residuum, which comprises pentane and hexane, wherein the mass ratio of the pentane to the hexane is 1:1-10:1. The invention provides a solvent deasphalting method of cycloalkyl vacuum residuum, which comprises the following steps: mixing and extracting a solvent, an entrainer and cycloalkyl vacuum residuum in a molten state to obtain a light deoiling solution and an asphalt oil solution; the solvent is the solvent in the technical scheme; and (3) recovering the solvent of the light deoiling solution to obtain deasphalted oil. According to the invention, the pentane and hexane mixed solvent with the mass ratio of 1:1-10:1 is used as the solvent, and the entrainer is used as the auxiliary material, so that the yield and the property of the deasphalted oil can be remarkably improved, the deasphalted oil is more suitable as the bright stock, and the supply of the bright stock production raw material is improved.
Description
Technical Field
The invention relates to the technical field of solvent deasphalting, in particular to a solvent for deasphalting cycloalkyl vacuum residuum and a solvent deasphalting method.
Background
Cycloalkyl crude oil belongs to a scarce resource, the reserves only account for 2.2% of the world's ascertained petroleum reserves, and is recognized as a high-quality resource for producing bright stock. Because the naphthenic base crude oil has unique and rare performance, the processing purpose is mainly used for producing high-quality lubricating oil base stock, and the production of fuel is not used as the main material, so that higher added value can be created. At present, the global demand for naphthenic crude oil is rapidly increased, and products such as bright stock, transformer oil, refrigerator oil and the like produced by taking the naphthenic crude oil as raw materials are favored in domestic and foreign markets.
Solvent deasphalting is one of the important ways to produce bright oil, and has strong advantages and attractive force in the deep processing of heavy oil. The solvent deasphalting device has lower construction cost and mainly comprises an extraction tower, a sedimentation tower, a solvent recovery tower and other matched equipment. The contradictory relationship of good quality of deasphalted oil, low yield, high yield and poor quality exists in the operation of the solvent deasphalting process. The bright stock has special requirements on the composition of the raw materials, and the processing technology has great difficulty and is limited by the light deoiling yield and quality of the raw materials.
In the solvent deasphalting process using alkane as solvent, the solvent composition is the most important factor, and the solvent composition has great influence on the yield and properties of deasphalted oil. The higher the molecular weight of the solvent used, the stronger the solvent dissolution capacity, and the higher the yield of deasphalted oil, but the poorer the separation effect, and the poorer the deasphalted oil properties. Various low molecular alkanes have a certain deasphalting capacity but different effects. The current commonly used deasphalting solvent for naphthenic vacuum residuum is propane, but the deasphalted oil has lower yield and poor properties.
Disclosure of Invention
In view of the above, an object of the present invention is to provide a solvent for deasphalting cycloalkyl vacuum residuum and a solvent deasphalting method. The solvent provided by the invention is used for deasphalting cycloalkyl vacuum residuum, so that the yield and the property of deasphalted oil can be greatly improved.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a solvent for deasphalting cycloalkyl vacuum residuum, which comprises pentane and hexane, wherein the mass ratio of the pentane to the hexane is 1:1-10:1.
The invention provides a solvent deasphalting method of cycloalkyl vacuum residuum, which comprises the following steps:
mixing and extracting a solvent, an entrainer and cycloalkyl vacuum residuum in a molten state to obtain a light deoiling solution and an asphalt oil solution; the solvent is the solvent in the technical scheme;
and (3) recovering the solvent of the light deoiling solution to obtain deasphalted oil.
Preferably, the mass content of colloid in the cycloalkyl vacuum residue is 45-55%, and the viscosity of the cycloalkyl vacuum residue at 100 ℃ is more than 1000 mPa.s.
Preferably, the mass ratio of the solvent to the cycloalkyl vacuum residuum is 1:1-3:1.
Preferably, the entrainer comprises one or more of dodecyl polyoxyethylene polyoxypropylene ether, lauryl acetate and benzyl acetate.
Preferably, the entrainer is 0.1-5% by mass of the cycloalkyl vacuum residuum.
Preferably, the extraction is performed in an extraction column, with a light deoiling solution being obtained at the top of the extraction column and an asphaltic oil solution being obtained at the bottom of the extraction column.
Preferably, the pressure of the extraction tower is 3-6 MPa, and the tower top temperature is 50-80 ℃.
Preferably, the solvent recovery is performed in a supercritical recovery column, and the deasphalted oil is obtained at the bottom of the supercritical recovery column.
Preferably, the pressure of the supercritical recovery tower is 4-8 MPa, and the tower top temperature is 90-120 ℃.
The invention provides a solvent for deasphalting cycloalkyl vacuum residuum, which comprises pentane and hexane, wherein the mass ratio of the pentane to the hexane is 1:1-10:1. The solvent provided by the invention is used for deasphalting cycloalkyl vacuum residuum, so that the yield and the property of deasphalted oil can be greatly improved.
The invention provides a solvent deasphalting method of cycloalkyl vacuum residuum, which comprises the following steps: mixing and extracting a solvent, an entrainer and cycloalkyl vacuum residuum in a molten state to obtain a light deoiling solution and an asphalt oil solution; the solvent is the solvent in the technical scheme; and (3) recovering the solvent of the light deoiling solution to obtain deasphalted oil. According to the invention, the pentane and hexane mixed solvent with the mass ratio of 1:1-10:1 is used as the solvent, and the entrainer is used as the auxiliary material, so that the yield and the property of the deasphalted oil can be remarkably improved, the deasphalted oil is more suitable as the bright stock, and the supply of the bright stock production raw material is improved. The results of the examples show that the solvent deasphalting method of cycloalkyl vacuum residuum provided by the invention has the deasphalted oil yield of 42.8-45.9% and the deasphalted oil viscosity of 53.58-56.92 mm at 100 DEG C 2 Per second, the carbon residue is 0.62-1.13%, the higher the viscosity of the deasphalted oil isThe lower the char, the better its properties.
Detailed Description
The invention provides a solvent for deasphalting cycloalkyl vacuum residuum, which comprises pentane and hexane, wherein the mass ratio of the pentane to the hexane is 1:1-10:1, preferably 1:1-9:1. The solvent provided by the invention is used for deasphalting cycloalkyl vacuum residuum, so that the yield and the property of deasphalted oil can be greatly improved.
The invention provides a solvent deasphalting method of cycloalkyl vacuum residuum, which comprises the following steps:
mixing and extracting a solvent, an entrainer and cycloalkyl vacuum residuum in a molten state to obtain a light deoiling solution and an asphalt oil solution; the solvent is the solvent in the technical scheme;
and (3) recovering the solvent of the light deoiling solution to obtain deasphalted oil.
The invention mixes and extracts solvent, entrainer and naphthenic vacuum residue in molten state to obtain light deoiling solution and asphalt oil solution; the solvent is the solvent in the technical scheme. In the present invention, the mass content of gum in the cycloalkyl vacuum residue is preferably 45 to 55%, more preferably 48 to 50%, and the viscosity of the cycloalkyl vacuum residue at 100 ℃ is preferably more than 1000mpa·s, more preferably 1100 to 1150mpa·s. The source of the cycloalkyl vacuum resid is not particularly limited by the present invention, and those skilled in the art will appreciate that sources of cycloalkyl vacuum resid are suitable for use in the present invention. In the present invention, the mass ratio of the solvent to the cycloalkyl vacuum residuum is preferably 1:1 to 3:1, more preferably 2.5:1 to 3:1. In the invention, the entrainer preferably comprises one or more of dodecyl polyoxyethylene polyoxypropylene ether, lauryl acetate and benzyl acetate, and when the entrainer is a mixture of a plurality of entrainers, the invention has no requirement on the mixing proportion and can be mixed in any proportion; in an embodiment of the invention, the entrainer is lauryl acetate or benzyl acetate. In the present invention, the entrainer is preferably 0.1 to 5% by mass, more preferably 2.5 to 4.5% by mass, and still more preferably 3% by mass of the cycloalkyl vacuum residue. In the present invention, the entrainer is capable of improving and maintaining extraction selectivity and increasing the solubility of the less volatile solutes and polar solutes, thereby contributing to further increase solvent deasphalting performance.
In the present invention, the extraction is preferably performed in an extraction column, a light deoiling solution is obtained at the top of the extraction column, and an asphalt oil solution is obtained at the bottom of the extraction column. The present invention is not particularly limited to the extraction column, and extraction columns well known to those skilled in the art may be used. In the present invention, the pressure of the extraction column is preferably 3 to 6MPa, more preferably 4.5 to 5MPa, and the column top temperature is preferably 50 to 80℃and more preferably 65 to 70 ℃.
After the light deoiling solution is obtained, the light deoiling solution is subjected to solvent recovery to obtain deasphalted oil. In the present invention, the solvent recovery is preferably performed in a supercritical recovery column, and the supercritical recovery column is not particularly limited to the present invention, and a supercritical recovery column well known to those skilled in the art may be used. In the present invention, the extraction column and the supercritical recovery column constitute a solvent deasphalting apparatus. In the present invention, the pressure of the supercritical recovery column is preferably 4 to 8MPa, more preferably 4.2 to 5MPa, and the column top temperature is preferably 90 to 120℃and more preferably 100 to 105 ℃. And after solvent recovery is carried out through a supercritical recovery tower, deasphalted oil is obtained at the bottom of the supercritical recovery tower, and the recovered solvent and entrainer are recycled.
The invention selects specific solvent, entrainer and technological parameters aiming at cycloalkyl vacuum residuum, greatly improves the yield and property of deasphalted oil, and makes the deasphalted oil more suitable as bright stock.
In order to further illustrate the present invention, the solvent for deasphalting cycloalkyl vacuum residuum and the method for solvent deasphalting provided herein are described in detail below with reference to examples, but are not to be construed as limiting the scope of the present invention.
Example 1
Feeding cycloalkyl vacuum residue with colloid content of 48% and viscosity of 1100 mPa.s at 100 ℃ into a solvent deasphalting device in a molten state, wherein the temperature of the top of an extraction tower is 68 ℃, the pressure of the extraction tower is 4.5MPa, and the mass ratio of the introduction of the extraction tower is 1:1 and an entrainer, wherein the mass of the mixed solvent and residual oil is 3:1, the entrainer is lauryl acetate, and the introducing amount is 3% of the mass of the residual oil.
The light deoiling solution flowing out of the top of the extraction tower enters a supercritical recovery tower, the temperature of the top of the supercritical recovery tower is 105 ℃, the pressure of the supercritical recovery tower is 4.2MPa, the solvent is recovered by the supercritical recovery tower, and then deasphalted oil is obtained at the bottom of the supercritical recovery tower, the yield of the deasphalted oil is 42.8%, and the viscosity of the deasphalted oil is 54.66mm at 100 DEG C 2 And/s, the carbon residue is 0.83%.
Example 2
Feeding cycloalkyl vacuum residue with colloid content of 48% and viscosity of 1100 mPa.s at 100 ℃ into a solvent deasphalting device in a molten state, wherein the temperature of the top of an extraction tower is 70 ℃, the pressure of the extraction tower is 4.8MPa, and the mass ratio of the introduction of the extraction tower is 10:1 and an entrainer, wherein the mass of the mixed solvent and residual oil is 3:1, the entrainer is benzyl acetate, and the introducing amount is 2.5% of the mass of the residual oil.
The light deoiling solution flowing out of the top of the extraction tower enters a supercritical recovery tower, the temperature of the top of the supercritical recovery tower is 105 ℃, the pressure of the supercritical recovery tower is 4.2MPa, the solvent is recovered by the supercritical recovery tower, and then deasphalted oil is obtained at the bottom of the supercritical recovery tower, the yield of the deasphalted oil is 45.9%, and the viscosity of the deasphalted oil is 56.92mm at 100 DEG C 2 And/s, the carbon residue is 0.62%.
Example 3
Feeding cycloalkyl vacuum residue with the colloid content of 50% and the viscosity of 1150 mPa.s at 100 ℃ into a solvent deasphalting device in a molten state, wherein the temperature of the top of an extraction tower is 69 ℃, the pressure of the extraction tower is 5.0MPa, and the mass ratio of the inlet of the extraction tower is 9:1 and hexane, and an entrainer, wherein the mass of the mixed solvent and residual oil is 2.5:1, the entrainer is benzyl acetate, and the introducing amount is 4.5% of the mass of residual oil.
The light deoiling solution flowing out of the top of the extraction tower enters a supercritical recovery tower, the temperature of the top of the supercritical recovery tower is 103 ℃, the pressure of the supercritical recovery tower is 4.8MPa, the solvent is recovered by the supercritical recovery tower, and deasphalted oil is obtained at the bottom of the supercritical recovery tower, and the deasphalted oil is recoveredThe rate is 44.5%, and the viscosity at 100 ℃ is 53.58mm 2 And/s, the carbon residue is 1.13%.
Comparative example 1
Feeding cycloalkyl vacuum residue with colloid content of 48% and viscosity of 1100 mPa.s at 100 ℃ into a solvent deasphalting device in a molten state, wherein the temperature of the top of an extraction tower is 68 ℃, the pressure of the extraction tower is 4.5MPa, propane is fed into the extraction tower, and the mass of the propane and the residue is 3.6:1.
the light deoiling solution flowing out of the top of the extraction tower enters a supercritical recovery tower, the temperature of the top of the supercritical recovery tower is 100 ℃, the pressure of the supercritical recovery tower is 4.2MPa, the solvent is recovered by the supercritical recovery tower, and deasphalted oil is obtained at the bottom of the supercritical recovery tower, the yield of the deasphalted oil is 31.6%, and the viscosity of the deasphalted oil is 52.05mm at 100 DEG C 2 And/s, the carbon residue is 1.45%.
The results show that the comparative example adopts the existing solvent deasphalting process to treat the naphthenic vacuum residuum, the solvent consumption is larger than that of the examples due to the fact that the solubility of the solvent is not matched with the properties of the naphthenic vacuum residuum, the deasphalted oil yield is about 10 percent lower than that of the examples, and the quality of the deasphalted oil of the comparative example is obviously lower than that of the examples.
The foregoing is merely a preferred embodiment of the present invention and is not intended to limit the present invention in any way. It should be noted that modifications and adaptations to the present invention may occur to one skilled in the art without departing from the principles of the present invention and are intended to be comprehended within the scope of the present invention.
Claims (10)
1. A solvent for deasphalting cycloalkyl vacuum residuum, which is characterized in that the solvent comprises pentane and hexane, and the mass ratio of the pentane to the hexane is 1:1-10:1.
2. A process for solvent deasphalting a cycloalkyl vacuum residuum, comprising the steps of:
mixing and extracting a solvent, an entrainer and cycloalkyl vacuum residuum in a molten state to obtain a light deoiling solution and an asphalt oil solution; the solvent is the solvent of claim 1;
and (3) recovering the solvent of the light deoiling solution to obtain deasphalted oil.
3. The method according to claim 2, wherein the mass content of gum in the cycloalkyl vacuum residue is 45-55%, and the viscosity of the cycloalkyl vacuum residue at 100 ℃ is greater than 1000 mPa-s.
4. A process according to claim 2 or 3, wherein the mass ratio of solvent to cycloalkyl vacuum residuum is from 1:1 to 3:1.
5. The method of claim 2, wherein the entrainer comprises one or more of dodecyl polyoxyethylene polyoxypropylene ether, lauryl acetate, and benzyl acetate.
6. The process according to claim 2 or 5, wherein the entrainer is present in an amount of 0.1 to 5% by mass of the cycloalkyl vacuum residuum.
7. The method according to claim 2, characterized in that the extraction is performed in an extraction column, a light deoiling solution is obtained at the top of the extraction column, and an asphalt oil solution is obtained at the bottom of the extraction column.
8. The process according to claim 7, wherein the pressure in the extraction column is 3 to 6MPa and the overhead temperature is 50 to 80 ℃.
9. The process according to claim 2, wherein the solvent recovery is carried out in a supercritical recovery column, and the deasphalted oil is obtained at the bottom of the supercritical recovery column.
10. The method according to claim 9, wherein the supercritical recovery column has a pressure of 4 to 8MPa and a column top temperature of 90 to 120 ℃.
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