CN109652112B - Method for reducing viscosity of high-viscosity oil - Google Patents
Method for reducing viscosity of high-viscosity oil Download PDFInfo
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- CN109652112B CN109652112B CN201710941023.6A CN201710941023A CN109652112B CN 109652112 B CN109652112 B CN 109652112B CN 201710941023 A CN201710941023 A CN 201710941023A CN 109652112 B CN109652112 B CN 109652112B
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- 238000000034 method Methods 0.000 title claims abstract description 33
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 150
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 75
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 75
- 239000012530 fluid Substances 0.000 claims abstract description 33
- 238000010791 quenching Methods 0.000 claims description 29
- 238000000926 separation method Methods 0.000 claims description 22
- 238000002156 mixing Methods 0.000 claims description 9
- 230000003247 decreasing effect Effects 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims 1
- 230000000694 effects Effects 0.000 abstract description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 84
- 238000000605 extraction Methods 0.000 description 38
- 239000002904 solvent Substances 0.000 description 20
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 11
- 239000001273 butane Substances 0.000 description 10
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 10
- 230000000171 quenching effect Effects 0.000 description 9
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical group C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 7
- 239000005977 Ethylene Substances 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- 239000007788 liquid Substances 0.000 description 7
- 239000000203 mixture Substances 0.000 description 6
- 230000001105 regulatory effect Effects 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 230000000704 physical effect Effects 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 239000010779 crude oil Substances 0.000 description 3
- 239000005431 greenhouse gas Substances 0.000 description 3
- 239000010426 asphalt Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000009792 diffusion process Methods 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 239000001282 iso-butane Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000000194 supercritical-fluid extraction Methods 0.000 description 1
- 238000005406 washing 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
-
- 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
-
- 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
-
- 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
-
- 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
Abstract
The invention relates to the field of petrochemical production, and discloses a viscosity reduction method for high-viscosity oil. The method comprises the following steps: (1) Contacting and separating the high viscosity oil with supercritical carbon dioxide to obtain a light fluid phase containing low viscosity components and carbon dioxide and a heavy fluid phase containing high viscosity components; (2) Separating the components of the light fluid phase containing the low-viscosity component and the carbon dioxide to obtain the low-viscosity component and the carbon dioxide; the viscosity of the high viscosity oil is greater than 50mm when at 50 DEG C 2 And/s is 10000mm 2 At a temperature of 50 ℃ or below, the viscosity of the low-viscosity component is 20mm 2 And/s or less. The viscosity reduction of the high-viscosity oil is realized by utilizing the supercritical carbon dioxide, and the greenhouse effect caused by carbon dioxide emission into the atmosphere is avoided.
Description
Technical Field
The invention relates to the field of petrochemical production, in particular to a method for reducing viscosity of high-viscosity oil.
Background
The viscosity of an oil affects its mass and heat transfer capabilities. High viscosity oil consumes more energy during pipe transportation due to its higher viscosity, low diffusion coefficient, greater mass and heat transfer resistance, requires more heat exchange area during heat exchange, and requires longer residence time during reaction. In summary, high viscosity oils cause more energy and material losses in petroleum and chemical operations.
Taking quench oil as an example, the viscosity at 50 ℃ is in the range of 50mm 2 /s～10000mm 2 And/s is a typical high viscosity oil, and as an important heat transfer medium for ethylene units, the viscosity rise of the oil can directly influence the normal operation of a cracking furnace, an oil washing tower and a dilution steam generation system, and even the accidents of blockage of pipelines and equipment of a quenching oil circulation system occur.
CN103305259a discloses that viscosity reduction is performed on ethylene unit quench oil by using supercritical propane, butane, etc., asphaltenes in the quench oil are removed, and the viscosity of the quench oil is reduced. However, the method also extracts part of colloid in the quenching oil into the light oil, and the viscosity of the obtained viscosity-reduced light oil is 20mm 2 /s～40mm 2 In the range of/s. There is a need to find a more efficient way to reduce the viscosity of high viscosity oils.
Disclosure of Invention
The invention aims to solve the problem that the viscosity of high-viscosity oil cannot be effectively reduced in the prior art, and provides a method for reducing the viscosity of the high-viscosity oil.
In order to achieve the above object, the present invention provides a method for viscosity reduction of high viscosity oil, wherein the method comprises the steps of:
(1) Contacting and separating the high viscosity oil with supercritical carbon dioxide to obtain a light fluid phase containing low viscosity components and carbon dioxide and a heavy fluid phase containing high viscosity components;
(2) Separating the components of the light fluid phase containing the low-viscosity component and the carbon dioxide to obtain the low-viscosity component and the carbon dioxide;
wherein the high viscosity oil has a viscosity of 10mm at 50 DEG C 2 /s-50mm 2 At/s, the low viscosity component has a viscosity of 3mm at 50 DEG C 2 And/s or less;
when saidThe viscosity of the high viscosity oil at 50 ℃ is greater than 50mm 2 /s and 5000mm 2 At a temperature of 50 ℃ or below, the viscosity of the low-viscosity component is 10mm 2 And/s or less;
the viscosity of the high viscosity oil is greater than 5000mm when at 50 DEG C 2 And/s is 10000mm 2 At a temperature of 50 ℃ or below, the viscosity of the low-viscosity component is 20mm 2 And/s or less.
Preferably, the supercritical carbon dioxide has a pressure of 7MPa to 69MPa, preferably 7MPa to 30MPa; the temperature of the supercritical carbon dioxide may be 30-70 ℃.
Preferably, the method further comprises pressurizing the high viscosity oil to 7MPa-69MPa, preferably 7MPa-30MPa, and heating the high viscosity oil to 30-70 ℃ prior to step (1).
Preferably, the viscosity of the high viscosity oil is greater than 50mm when at 50 DEG C 2 /s and 5000mm 2 At a temperature below/s, the low viscosity component has a viscosity of 3-10mm at 50 DEG C 2 /s。
Preferably, the viscosity of the high viscosity oil is greater than 5000mm when at 50 DEG C 2 And/s is 10000mm 2 At a temperature of 50 ℃ or below, the low-viscosity component has a viscosity of 10-20mm 2 /s。
Preferably, the high viscosity oil is one or more of quench oil, atmospheric residuum, vacuum residuum, slurry oil, and crude oil.
Preferably, in step (1), the mixing weight ratio of the high viscosity oil to the supercritical carbon dioxide is 1 (0.5-20), preferably 1: (2-8).
Preferably, in step (2), the component separation method is a temperature increasing method and/or a pressure decreasing method.
The invention achieves the effect of viscosity reduction of high-viscosity oil by using supercritical carbon dioxide. Firstly, because the solvent has little dissolution capacity drop relative to liquid under supercritical conditions, and the viscosity and the diffusion coefficient are closer to those of gas, namely the mass transfer performance is better, the supercritical extraction is much faster than the liquid extraction, and the device production capacity is high. Secondly, as the physical properties of the solvent are very sensitive to the change of temperature and pressure in a critical area, the dissolution capacity of the solvent can be adjusted by adjusting the temperature and the pressure of the solvent, and the process control is flexible. Moreover, carbon dioxide is the most common atmospheric emissions and greenhouse gas, and carbon dioxide is used to replace low-carbon hydrocarbons for viscosity reduction of high-viscosity oils, thereby saving precious petrochemical raw materials and reducing greenhouse gas emissions. Compared with the viscosity reduction of supercritical propane and butane, the supercritical carbon dioxide has low operating temperature and does not cause further increase of the viscosity of high-viscosity oil. The supercritical carbon dioxide does not extract excessive colloid from the high-viscosity oil, and the obtained low-viscosity component has lower viscosity and better viscosity reduction effect. Therefore, the invention utilizes supercritical carbon dioxide to extract low-viscosity components from high-viscosity oil, and the carbon dioxide is separated from the low-viscosity components by increasing the temperature or reducing the pressure, so that the viscosity of the obtained low-viscosity components can be greatly reduced relative to the high-viscosity oil.
Detailed Description
The endpoints and any values of the ranges disclosed herein are not limited to the precise range or value, and are understood to encompass values approaching those ranges or values. For numerical ranges, one or more new numerical ranges may be found between the endpoints of each range, between the endpoint of each range and the individual point value, and between the individual point value, in combination with each other, and are to be considered as specifically disclosed herein.
The invention provides a method for reducing viscosity of high-viscosity oil, which comprises the following steps:
(1) Contacting and separating the high viscosity oil with supercritical carbon dioxide to obtain a light fluid phase containing low viscosity components and carbon dioxide and a heavy fluid phase containing high viscosity components;
(2) Separating the components of the light fluid phase containing the low-viscosity component and the carbon dioxide to obtain the low-viscosity component and the carbon dioxide;
wherein the high viscosity oil has a viscosity of 10mm at 50 DEG C 2 /s-50mm 2 At/s, the low viscosity component has a viscosity of 3mm at 50 DEG C 2 And/s or less;
the viscosity of the high viscosity oil is greater than 50mm when at 50 DEG C 2 /s and 5000mm 2 At a temperature of 50 ℃ or below, the viscosity of the low-viscosity component is 10mm 2 And/s or less;
the viscosity of the high viscosity oil is greater than 5000mm when at 50 DEG C 2 And/s is 10000mm 2 At a temperature of 50 ℃ or below, the viscosity of the low-viscosity component is 20mm 2 And/s or less.
In the present invention, a substance exhibits a state change such as a liquid, a gas, or a solid depending on a temperature and a pressure, and if the temperature and the pressure are increased to a certain point or more, a phenomenon in which the interface between the liquid and the gas disappears occurs, the point is referred to as a critical point, a supercritical fluid (SCF) is a fluid in a temperature and pressure region or more of the critical point, and a phase state at this time is referred to as a supercritical state, and is a non-condensed state that is not liquefied even if the pressure is increased. In the vicinity of the critical point, the physical properties of all fluids such as density, viscosity, solubility, heat capacity, and dielectric constant of the fluid change rapidly. The physical properties of the supercritical fluid have the dual properties of liquid and gas, the density is close to that of liquid, the diffusivity is close to that of gas, and the viscosity is between that of gas and liquid. In addition, since such physical properties change depending on the pressure and temperature, the solvent is increasingly used as a new solvent for replacing the original organic solvent in terms of extraction, purification, reaction, and the like. In short, under supercritical conditions, i.e., both temperature and pressure are above the critical temperature and critical pressure of the solvent.
In the present invention, the supercritical carbon dioxide may have a pressure of 7MPa to 69MPa, preferably 7MPa to 30MPa, and for example, may have any value in the range of 7MPa, 15MPa, 30MPa, 40MPa, 60MPa, or any two of these values. The supercritical carbon dioxide may have a temperature of 30-70deg.C, such as 30deg.C, 35deg.C, 40deg.C, 50deg.C, 70deg.C, etc.
In the present invention, the method further comprises pressurizing the high viscosity oil to 7MPa to 69MPa, preferably 7MPa to 30MPa, for example, may be 7MPa, 15MPa, 30MPa, 40MPa, 60MPa and any value in the range of any two of these values before step (1). The high viscosity oil is heated to 30-70deg.C, such as 30deg.C, 35deg.C, 40deg.C, 50deg.C, 70deg.C, etc. That is, the pressure range of mixing the high viscosity oil with the supercritical carbon dioxide is 7MPa to 69MPa, preferably 7MPa to 30MPa, and the temperature range is 30 to 70 ℃, that is, the carbon dioxide is maintained in the supercritical state.
In the present invention, the temperatures of the high viscosity oil and supercritical carbon dioxide may be different before contacting, but not too much, so that it is necessary to maintain the supercritical state of the carbon dioxide in the column, and if the difference is too large, the phase state and density of the carbon dioxide may be affected.
In the present invention, the high viscosity oil has a viscosity of more than 10mm at 50 DEG C 2 S, preferably 50mm 2 /s-10000mm 2 /s。
In the present invention, the viscosity of the high viscosity oil is greater than 50mm when at 50 DEG C 2 /s and 5000mm 2 At a temperature below/s, the low viscosity component has a viscosity of 3-10mm at 50 DEG C 2 And/s. For example, may be 3mm 2 /s、4mm 2 /s、5mm 2 /s、9.5mm 2 /s, etc.
In the present invention, the viscosity of the high viscosity oil is greater than 5000mm when at 50 DEG C 2 And/s is 10000mm 2 At a temperature of 50 ℃ or below, the low-viscosity component has a viscosity of 10-20mm 2 And/s. For example, may be 11mm 2 /s、16mm 2 /s、18.5mm 2 /s, etc.
In the present invention, the high viscosity oil may be, but is not limited to: one or more of quench oil, atmospheric residuum, vacuum residuum, slurry oil, and crude oil.
In the present invention, in the step (1), the mixing weight ratio of the high viscosity oil to the supercritical carbon dioxide is 1 (0.5-20), preferably 1: (2-8).
In the present invention, in the step (2), the separation of the components is carried out with a reduced density, and for example, a temperature increasing method and/or a pressure decreasing method may be used.
In one embodiment of the present invention, the supercritical carbon dioxide and the low viscosity component may be separated by a temperature increase process, such as maintaining a substantially constant pressure, wherein the supercritical carbon dioxide has a substantially reduced density and substantially loses its ability to dissolve the oil, and in particular, by a temperature of 30 ℃ to 100 ℃ based on the temperature at which the high viscosity oil is contacted with the supercritical carbon dioxide.
In another embodiment of the present invention, the supercritical carbon dioxide and the low viscosity component may be separated by a pressure reduction method, for example, a temperature is substantially unchanged, and the pressure is reduced to convert the carbon dioxide from the supercritical state to the gaseous state, and the solvent capacity is lost, so that the carbon dioxide and the low viscosity component are separated, and in particular, the pressure may be 0.01MPa to 7MPa.
In another embodiment of the invention, the supercritical carbon dioxide and the low-viscosity component separation method can adopt a depressurization method and a heating method at the same time, and the specific pressure range is 0.01MPa-7MPa; the temperature is raised by 10-100 ℃ based on the temperature at which the high viscosity oil is contacted with supercritical carbon dioxide, for example, 50 ℃ at which the temperature is raised to 60-150 ℃.
In the invention, the carbon dioxide can be obtained by collecting the exhaust gas of the industrial furnace, thereby achieving the purpose of reducing the emission of greenhouse gases.
The present invention will be described in detail by examples.
Examples 1-7 are provided to illustrate the process of the present invention.
Example 1
A stream of quench oil is drawn from the ethylene unit quench oil circulation system and has a viscosity of 1500mm at 50 DEG C 2 And/s, pressurizing to 30MPa and injecting the mixture into the extraction tower from the upper part at 50 ℃. The supercritical carbon dioxide pressurized to 30MPa and 50 ℃ enters an extraction tower from the lower part, the mixing weight ratio of the quenching oil entering the extraction tower to the supercritical carbon dioxide is 1:2, and the heavy fluid phase rich in high-viscosity components is obtained at the bottom of the extraction tower. The light fluid phase which is extracted from the top of the extraction tower and is rich in low-viscosity components and carbon dioxide is reduced in pressure to 1MPa and at 50 ℃, then enters a separation tower, and the low-viscosity components in the light fluid phase are separated from the carbon dioxide; the carbon dioxide obtained from the top of the separation tower is boosted to 30MPa and is recycled to the extraction tower for use after being regulated to 50 ℃, and the separation tower is usedThe base gives a low viscosity component having a viscosity of 5mm at 50 DEG C 2 /s。
Example 2
A stream of quench oil is drawn from the ethylene unit quench oil circulation system and has a viscosity of 48mm at 50 DEG C 2 And/s, pressurizing to 7MPa and injecting the mixture into an extraction tower from the upper part at 30 ℃. And (3) introducing supercritical carbon dioxide pressurized to 7MPa and 30 ℃ into an extraction tower from the lower part, wherein the mixing weight ratio of the quenching oil entering the extraction tower to the supercritical carbon dioxide is 1:6, and obtaining a heavy fluid phase rich in high-viscosity components at the bottom of the extraction tower. The light fluid phase which is rich in low-viscosity components and carbon dioxide and is extracted from the top of the extraction tower is heated to 100 ℃ and the pressure is 7MPa, and then enters a separation tower, and the low-viscosity components in the light fluid phase are separated from the carbon dioxide; the pressure of the carbon dioxide obtained from the top of the separation tower is regulated to 7MPa, the temperature is reduced to 30 ℃ and then the carbon dioxide is recycled to the extraction tower for use, the low-viscosity component is obtained from the bottom of the separation tower, and the viscosity of the low-viscosity component at 50 ℃ is 3mm 2 /s。
Example 3
Dehydrated desalted crude oil having a viscosity of 245mm at 50 DEG C 2 And/s, pressurizing to 20MPa and injecting the mixture into an extraction tower from the upper part at 40 ℃. And (3) introducing supercritical carbon dioxide pressurized to 20MPa and 40 ℃ into an extraction tower from the lower part, wherein the mixing weight ratio of the quenching oil entering the extraction tower to the supercritical carbon dioxide is 1:8, and obtaining a heavy fluid phase rich in high-viscosity components at the bottom of the extraction tower. The light fluid phase which is extracted from the top of the extraction tower and is rich in low-viscosity components and carbon dioxide is reduced in pressure to 0.1MPa and at the temperature of 40 ℃, then enters a separation tower, and the low-viscosity components in the light fluid phase are separated from the carbon dioxide; the carbon dioxide obtained from the top of the separation tower is boosted to 20MPa, and is recycled to the extraction tower for use after being regulated to 40 ℃, the low-viscosity component is obtained from the bottom of the separation tower, and the viscosity of the low-viscosity component at 50 ℃ is 4mm 2 /s。
Example 4
A stream of quench oil is led from the quench oil circulation system of the ethylene unit, and the viscosity of the quench oil at 50 ℃ is 5000mm 2 And/s, pressurizing to 60MPa and spraying the mixture into an extraction tower from the upper part at 35 ℃. Introducing supercritical carbon dioxide pressurized to 60MPa and 35deg.C into extraction tower from lower part, and extractingThe mixing weight ratio of the quenching oil of the tower to the supercritical carbon dioxide is 1:0.5, and the bottom of the extraction tower is provided with a heavy fluid phase rich in high-viscosity components. The light fluid phase which is extracted from the top of the extraction tower and is rich in low-viscosity components and carbon dioxide is reduced in pressure to 7MPa, the temperature is increased to 100 ℃, and then the light fluid phase enters a separation tower, and the low-viscosity components in the light fluid phase are separated from the carbon dioxide; the carbon dioxide obtained from the top of the separation tower is boosted to 60MPa and is recycled to the extraction tower for use after being regulated to 35 ℃, the low-viscosity component is obtained from the bottom of the separation tower, and the viscosity of the low-viscosity component at 50 ℃ is 9.5mm 2 /s。
Example 5
A stream of quench oil is drawn from the ethylene unit quench oil circulation system and has a viscosity of 3000mm at 50 DEG C 2 And/s, pressurizing to 15MPa and injecting the mixture into an extraction tower from the upper part at 70 ℃. The supercritical carbon dioxide pressurized to 15MPa and 70 ℃ enters an extraction tower from the lower part, the mixing weight ratio of the quenching oil entering the extraction tower to the supercritical carbon dioxide is 1:20, and the heavy fluid phase rich in high-viscosity components is obtained at the bottom of the extraction tower. The light fluid phase which is extracted from the top of the extraction tower and is rich in low-viscosity components and carbon dioxide is reduced in pressure to 3MPa, and is heated to 150 ℃ and then enters the separation tower, and the low-viscosity components in the light fluid phase are separated from the carbon dioxide; the carbon dioxide obtained from the top of the separation tower is boosted to 15MPa, and is recycled to the extraction tower for use after being regulated to 70 ℃, the low-viscosity component is obtained from the bottom of the separation tower, and the viscosity of the low-viscosity component at 50 ℃ is 8mm 2 /s。
Example 6
The procedure of example 1 is followed, except that a viscosity of 10000mm at 50℃is used 2 High viscosity oil/s, low viscosity component obtained at the bottom of the separation column, having a viscosity of 16mm at 50 DEG C 2 /s。
Example 7
The procedure of example 1 is followed, except that a viscosity of 10mm at 50℃is used 2 High viscosity oil/s, low viscosity component obtained at the bottom of the separation column, having a viscosity of 2mm at 50 DEG C 2 /s。
Comparative example 1
A quench oil stream from the ethylene unit quench oil recycle system of example 1 was usedIts viscosity at 50℃is 1500mm 2 And/s. A butane solvent (50% each of n-butane and isobutane) was used at a temperature of 150℃and a pressure of 4.1MPa (the critical temperature of the butane solvent was 143.30 ℃and the critical pressure was 3.71 MPa). The extraction tower is a sieve plate tower, the pressure of the extraction tower is 4.1MPa, the quenching oil is pressurized and mixed with butane solvent according to the weight ratio of 1:2, the mixture enters the middle part of the extraction tower, and butane solvent with the weight 2 times of the quenching oil enters the lower part of the extraction tower, the temperature of the top of the extraction tower is 155 ℃, and the temperature of the bottom of the extraction tower is 150 ℃; the lighter oil phase is separated from the top of the column, and the heavier bitumen phase is separated from the bottom of the column. The asphalt phase is depressurized to normal pressure to remove the solvent and then is extracted as fuel oil. The lighter phase flowing out of the top of the extraction tower is heated to 190 ℃ and then is sent into the middle part of the recovery tower. The solvent recovery tower is a sieve plate tower, the pressure of the tower is 4.1MPa, and the temperature distribution in the tower is 190 ℃. At this time, the butane solvent density is reduced, and the dissolving capacity is reduced, so that separation of solvent butane and visbreaking quench oil is realized. And separating butane solvent from the top of the solvent recovery tower, and cooling the butane solvent to 150 ℃ for recycling. Separating from the bottom of the solvent recovery column a visbreaking quench oil having a viscosity of 23mm at 50 DEG C 2 /s。
As can be seen from the results of examples and comparative examples, the viscosity of the high-viscosity oil, which was 10mm at 50℃was effectively reduced by the method of the present invention 2 At/s, the viscosity of the low-viscosity component at 50℃is 2mm 2 S; the viscosity of the high viscosity oil is greater than 50mm when at 50 DEG C 2 /s and 5000mm 2 At a temperature below/s, the low viscosity component has a viscosity of 3-9.5mm at 50 DEG C 2 S; the viscosity of the high viscosity oil at 50 ℃ is 10000mm 2 At/s, the viscosity of the low viscosity component at 50℃is 16mm 2 And/s. By adopting the method provided by the invention, the viscosity reduction of the high-viscosity oil is realized.
In addition, the method can recycle the supercritical carbon dioxide, thereby achieving the effects of synergism and emission reduction.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, a number of simple variants of the technical solution of the invention are possible, including combinations of the individual technical features in any other suitable way, which simple variants and combinations should likewise be regarded as being disclosed by the invention, all falling within the scope of protection of the invention.
Claims (3)
1. A method for viscosity reduction of high viscosity oil, comprising the steps of:
(1) Contacting and separating the high viscosity oil with supercritical carbon dioxide to obtain a light fluid phase containing low viscosity components and carbon dioxide and a heavy fluid phase containing high viscosity components;
(2) Separating the components of the light fluid phase containing the low-viscosity component and the carbon dioxide to obtain the low-viscosity component and the carbon dioxide;
wherein the high viscosity oil has a viscosity of 10mm at 50 DEG C 2 /s-50mm 2 At/s, the low viscosity component has a viscosity of 3mm at 50 DEG C 2 And/s or less;
the viscosity of the high viscosity oil is greater than 50mm when at 50 DEG C 2 /s and 5000mm 2 At a temperature below/s, the low viscosity component has a viscosity of 3-5mm at 50 DEG C 2 /s；
The viscosity of the high viscosity oil is greater than 5000mm when at 50 DEG C 2 And/s is 10000mm 2 At a temperature of 50 ℃ or below, the viscosity of the low-viscosity component is 20mm 2 And/s or less;
wherein the pressure of the supercritical carbon dioxide is 7MPa-30MPa; the temperature of the supercritical carbon dioxide is 30-50 ℃;
wherein the method further comprises pressurizing the high viscosity oil to 7MPa to 30MPa prior to step (1); heating the high viscosity oil to 30-50 ℃;
wherein in the step (1), the mixing weight ratio of the high-viscosity oil to the supercritical carbon dioxide is 1 (2-8);
wherein the high viscosity oil is quench oil with a viscosity of 10mm at 50deg.C 2 /s-10000mm 2 /s。
2. The method of claim 1, wherein,the viscosity of the high viscosity oil is greater than 5000mm when at 50 DEG C 2 And/s is 10000mm 2 At a temperature of 50 ℃ or below, the low-viscosity component has a viscosity of 10-20mm 2 /s。
3. The method according to claim 1, wherein in step (2), the method of component separation is a temperature rising method and/or a pressure decreasing method.
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| CN101323793A (en) * | 2008-08-01 | 2008-12-17 | 中国科学技术大学 | Method for quality improving of biomass cracked oil by using supercritical carbon dioxide |
| CN104046375A (en) * | 2014-06-11 | 2014-09-17 | 西安交通大学 | Microwave-assisted supercritical CO2 extraction system and microwave-assisted supercritical CO2 extraction method for crude oil in oil sand |
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| CN101323793A (en) * | 2008-08-01 | 2008-12-17 | 中国科学技术大学 | Method for quality improving of biomass cracked oil by using supercritical carbon dioxide |
| CN104046375A (en) * | 2014-06-11 | 2014-09-17 | 西安交通大学 | Microwave-assisted supercritical CO2 extraction system and microwave-assisted supercritical CO2 extraction method for crude oil in oil sand |
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