CN104762103A - Method for removing asphalt from oil residues under reduced pressure - Google Patents
Method for removing asphalt from oil residues under reduced pressure Download PDFInfo
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- CN104762103A CN104762103A CN201510132520.2A CN201510132520A CN104762103A CN 104762103 A CN104762103 A CN 104762103A CN 201510132520 A CN201510132520 A CN 201510132520A CN 104762103 A CN104762103 A CN 104762103A
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- extraction
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- fat
- deasphalted oil
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Abstract
The invention relates to a method for removing asphalt from oil residues under reduced pressure, belonging to the field of petrochemical industry. A pre-extraction section, a fine removal section and a fine extraction section are adopted in one extraction tower to remove asphalt from oil residues under reduced pressure, thereby avoiding high equipment investment and high energy consumption caused by designing multiple extraction towers, and enhancing the quality and recovery rate of the deasphalted oil. Vacuum fractionating is adopted to recover the extraction solvent in the asphalt. The method has the advantages of low energy consumption and high efficiency.
Description
Technical field
The present invention relates to a kind of method that dregs of fat that reduce pressure remove pitch, belong to petrochemical industry.
Background technology
Under the condition of underpressure distillation, the thick oil component of some preciousnesses in paraffinic base or intermediate base crude oil, remain in vacuum residuum due to very high can not the gasification of boiling point, industrial is utilize they and other materials (colloid and pitch) difference in solubility in a solvent and carry out being separated.Conventional solvent is the mixture of propane, butane, pentane, hexane or propane and butane.When producing the base oil of thick oil, conventional propane makes solvent.The Deasphalting Unit of China can produce two kinds of deasphalted oils usually, and the frivolous asphalt oil that namely carbon residue is lower and the higher heavy deasphalted oil of carbon residue, the latter can be used as lube stock or catalytically cracked material.Adopt butane or pentane as the deasphalting process of solvent, for the production of catalytically cracked material, the de-oiled asphalt softening temperature of gained.
And the method removing pitch of routine is extraction process, in extraction tower, utilize that lower molecular weight oil can be dissolved in extraction solvent and bituminous matter can not be dissolved thus realize removing the effect of pitch, if but due to routine extraction adopt one-level extraction, then there is larger impact to the quality of deasphalted oil and the rate of recovery, and adopt two-stage or multistage, then equipment investment and energy consumption higher, in pitch, removing of extraction solvent generally adopts vaporizing extract process simultaneously, need higher pressure and temperature, and the solvent temperature that goes out of stripping is higher needs again energy to cool, energy consumption is higher.
Summary of the invention
in order to solve the problems referred to above that prior art exists, the invention provides a kind of method that dregs of fat that reduce pressure remove pitch, namely reduce facility investment and energy consumption, the rate of recovery and the quality of deasphalted oil can be improved again, and can rapid low consumption the extraction solvent in pitch is removed.
The technical solution adopted in the present invention is:
The dregs of fat that reduce pressure remove a method for pitch, comprise following step:
(1) pre-treatment of the decompression dregs of fat: the decompression dregs of fat being tentatively heated to temperature is 80-120 DEG C;
(2) overcritical counter-current extraction: the counter current contact in the pre-extraction section in the middle part of extraction tower by extraction solvent and the pretreated decompression dregs of fat, the volume ratio of extraction solvent and the pretreated decompression dregs of fat is 5-10:1, extraction temperature is 50-120 DEG C, mixing time is 0.5-5 hour, extracting pressure is 2.5-5.5Mpa, obtain the thick deasphalted oil a on top and the thick de-oiled asphalt b of bottom, the thick deasphalted oil a on top enters the essence section of taking off on extraction tower top together with extraction solvent, in the essence section of taking off, the volume ratio of extraction solvent and thick deasphalted oil a is 1-2:1, extraction temperature is 60-130 DEG C, mixing time is 0.5-2 hour, extracting pressure is 2.5-5.5Mpa, obtain smart deasphalted oil c and de-oiled asphalt d, essence deasphalted oil c is heated to 80-150 DEG C and then enters the extraction deasphalted oil of extraction solvent supercritical recovery tower and reclaim extraction solvent at extraction tower top, de-oiled asphalt d returns the pre-extraction section in the middle part of extraction tower, the thick de-oiled asphalt b obtained enters the quintessence section of extraction tower bottom together with extraction solvent, in quintessence section, the volume ratio of extraction solvent and thick de-oiled asphalt b is 0.5-1:1, extraction temperature is 40-110 DEG C, mixing time is 0.5-2 hour, extracting pressure is 2.5-5.5Mpa, obtain deasphalted oil e and smart de-oiled asphalt f, deasphalted oil e returns the section of extraction in advance, essence de-oiled asphalt f enters in pitch vaporizer bottom extraction tower,
(3) smart de-oiled asphalt reclaims extraction solvent: sprayed by smart de-oiled asphalt f and enter vacuum decompression separation column, during spraying, the particle diameter of drop is 0.1-5mm, pressure in tower is-0.09--0.08Mpa, temperature is 30-60 DEG C, and the extraction solvent fractionated out reclaims and returns step (2) after multi-stage condensing.
Further, in described step (1), type of heating can at least one in electrically heated, oil bath heating, steam heating, microwave heating.
Further, in described step (2), extraction solvent is at least one in propane, butane, pentane, hexane, heptane, purity >=80% of described extraction solvent.
Further, in described step (3), condensing temperature is 15-30 DEG C.
Beneficial effect of the present invention is: in an extraction tower, adopt the section of extraction, the de-section of essence, quintessence section in advance to realize the decompression dregs of fat and remove pitch, namely avoid designing the facility investment that multiple extraction tower causes large, energy consumption is many, and improve quality and the rate of recovery of deasphalted oil, adopt vacuum decompression fractionation to realize the recovery of extraction solvent in pitch simultaneously, energy consumption is low, and efficiency is high.
Accompanying drawing explanation
Accompanying drawing Fig. 1 is the process flow diagram of method described in the present patent application.
Embodiment
Below in conjunction with accompanying drawing and concrete example; the method that a kind of dregs of fat that reduce pressure described in the present patent application remove pitch is described and is illustrated; object is in order to the public better understands technology contents of the present invention; instead of the restriction to described technology contents; under identical or approximate principle, to the improvement that described processing step carries out, comprise reaction conditions, agents useful for same improvement and replace; reach identical object, then all within the present patent application technical scheme required for protection.
Embodiment one
The dregs of fat that reduce pressure remove a method for pitch, comprise following step:
(1) pre-treatment of the decompression dregs of fat: the decompression dregs of fat being tentatively heated to temperature is 100 DEG C;
(2) overcritical counter-current extraction: the counter current contact in the pre-extraction section in the middle part of extraction tower by extraction solvent and the pretreated decompression dregs of fat, the volume ratio of extraction solvent and the pretreated decompression dregs of fat is 8:1, extraction temperature is 70 DEG C, mixing time is 4 hours, extracting pressure is 4.2Mpa, obtain the thick deasphalted oil a on top and the thick de-oiled asphalt b of bottom, the thick deasphalted oil a on top enters the essence section of taking off on extraction tower top together with extraction solvent, in the essence section of taking off, the volume ratio of extraction solvent and thick deasphalted oil a is 1.5:1, extraction temperature is 80 DEG C, mixing time is 2 hours, extracting pressure is 4.2Mpa, obtain smart deasphalted oil c and de-oiled asphalt d, essence deasphalted oil c is heated to 90 DEG C and then enters the extraction deasphalted oil of extraction solvent supercritical recovery tower and reclaim extraction solvent at extraction tower top, de-oiled asphalt d returns the pre-extraction section in the middle part of extraction tower, the thick de-oiled asphalt b obtained enters the quintessence section of extraction tower bottom together with extraction solvent, in quintessence section, the volume ratio of extraction solvent and thick de-oiled asphalt b is 1:1, extraction temperature is 60 DEG C, mixing time is 1 hour, extracting pressure is 4.2Mpa, obtain deasphalted oil e and smart de-oiled asphalt f, deasphalted oil e returns the section of extraction in advance, essence de-oiled asphalt f enters in pitch vaporizer bottom extraction tower,
(3) smart de-oiled asphalt reclaims extraction solvent: sprayed by smart de-oiled asphalt f and enter vacuum decompression separation column, during spraying, the particle diameter of drop is 1mm, pressure in tower is-0.085Mpa, and temperature is 45 DEG C, and the extraction solvent fractionated out reclaims and returns step (2) after multi-stage condensing.
In described step (1), type of heating is steam heating.
In described step (2), extraction solvent is butane, and the purity of described extraction solvent is 85%.
In described step (3), condensing temperature is 25 DEG C.
The decreasing ratio of final smart deasphalted oil c medium pitch reaches 95%, and the rate of recovery of smart deasphalted oil c is 96.2%, processes decompression dregs of fat observable index general method per ton and reduces more than 15%.
Embodiment two
The dregs of fat that reduce pressure remove a method for pitch, comprise following step:
(1) pre-treatment of the decompression dregs of fat: the decompression dregs of fat being tentatively heated to temperature is 110 DEG C;
(2) overcritical counter-current extraction: the counter current contact in the pre-extraction section in the middle part of extraction tower by extraction solvent and the pretreated decompression dregs of fat, the volume ratio of extraction solvent and the pretreated decompression dregs of fat is 9:1, extraction temperature is 70 DEG C, mixing time is 4 hours, extracting pressure is 4.3Mpa, obtain the thick deasphalted oil a on top and the thick de-oiled asphalt b of bottom, the thick deasphalted oil a on top enters the essence section of taking off on extraction tower top together with extraction solvent, in the essence section of taking off, the volume ratio of extraction solvent and thick deasphalted oil a is 1.5:1, extraction temperature is 80 DEG C, mixing time is 3 hours, extracting pressure is 4.3Mpa, obtain smart deasphalted oil c and de-oiled asphalt d, essence deasphalted oil c is heated to 90 DEG C and then enters the extraction deasphalted oil of extraction solvent supercritical recovery tower and reclaim extraction solvent at extraction tower top, de-oiled asphalt d returns the pre-extraction section in the middle part of extraction tower, the thick de-oiled asphalt b obtained enters the quintessence section of extraction tower bottom together with extraction solvent, in quintessence section, the volume ratio of extraction solvent and thick de-oiled asphalt b is 0.7:1, extraction temperature is 60 DEG C, mixing time is 1 hour, extracting pressure is 4.3Mpa, obtain deasphalted oil e and smart de-oiled asphalt f, deasphalted oil e returns the section of extraction in advance, essence de-oiled asphalt f enters in pitch vaporizer bottom extraction tower,
(3) smart de-oiled asphalt reclaims extraction solvent: sprayed by smart de-oiled asphalt f and enter vacuum decompression separation column, during spraying, the particle diameter of drop is 1mm, pressure in tower is-0.09Mpa, and temperature is 40 DEG C, and the extraction solvent fractionated out reclaims and returns step (2) after multi-stage condensing.
In described step (1), type of heating is steam heating.
In described step (2), extraction solvent is butane, and the purity of described extraction solvent is 85%.
In described step (3), condensing temperature is 25 DEG C.
The decreasing ratio of final smart deasphalted oil c medium pitch reaches 94%, and the rate of recovery of smart deasphalted oil c is 96.5%, processes decompression dregs of fat observable index general method per ton and reduces more than 15%.
Embodiment three
The dregs of fat that reduce pressure remove a method for pitch, comprise following step:
(1) pre-treatment of the decompression dregs of fat: the decompression dregs of fat being tentatively heated to temperature is 90 DEG C;
(2) overcritical counter-current extraction: the counter current contact in the pre-extraction section in the middle part of extraction tower by extraction solvent and the pretreated decompression dregs of fat, the volume ratio of extraction solvent and the pretreated decompression dregs of fat is 9:1, extraction temperature is 60 DEG C, mixing time is 5 hours, extracting pressure is 4.3Mpa, obtain the thick deasphalted oil a on top and the thick de-oiled asphalt b of bottom, the thick deasphalted oil a on top enters the essence section of taking off on extraction tower top together with extraction solvent, in the essence section of taking off, the volume ratio of extraction solvent and thick deasphalted oil a is 1.5:1, extraction temperature is 70 DEG C, mixing time is 3 hours, extracting pressure is 4.3Mpa, obtain smart deasphalted oil c and de-oiled asphalt d, essence deasphalted oil c is heated to 90 DEG C and then enters the extraction deasphalted oil of extraction solvent supercritical recovery tower and reclaim extraction solvent at extraction tower top, de-oiled asphalt d returns the pre-extraction section in the middle part of extraction tower, the thick de-oiled asphalt b obtained enters the quintessence section of extraction tower bottom together with extraction solvent, in quintessence section, the volume ratio of extraction solvent and thick de-oiled asphalt b is 0.7:1, extraction temperature is 50 DEG C, mixing time is 1 hour, extracting pressure is 4.3Mpa, obtain deasphalted oil e and smart de-oiled asphalt f, deasphalted oil e returns the section of extraction in advance, essence de-oiled asphalt f enters in pitch vaporizer bottom extraction tower,
(3) smart de-oiled asphalt reclaims extraction solvent: sprayed by smart de-oiled asphalt f and enter vacuum decompression separation column, during spraying, the particle diameter of drop is 1mm, pressure in tower is-0.09Mpa, and temperature is 40 DEG C, and the extraction solvent fractionated out reclaims and returns step (2) after multi-stage condensing.
In described step (1), type of heating is oil bath heating.
In described step (2), extraction solvent is propane, and the purity of described extraction solvent is 85%.
In described step (3), condensing temperature is 20 DEG C.
The decreasing ratio of final smart deasphalted oil c medium pitch reaches 94.5%, and the rate of recovery of smart deasphalted oil c is 95.8%, processes decompression dregs of fat observable index general method per ton and reduces more than 15%.
The present invention is not limited to above-mentioned preferred forms; anyone can draw other various forms of products under enlightenment of the present invention; no matter but any change is done in its shape or structure; every have identical with the application or akin technical scheme, all drops within protection scope of the present invention.
Claims (4)
1. the dregs of fat that reduce pressure remove a method for pitch, it is characterized in that, comprise following step:
(1) pre-treatment of the decompression dregs of fat: the decompression dregs of fat being tentatively heated to temperature is 80-120 DEG C;
(2) overcritical counter-current extraction: the counter current contact in the pre-extraction section in the middle part of extraction tower by extraction solvent and the pretreated decompression dregs of fat, the volume ratio of extraction solvent and the pretreated decompression dregs of fat is 5-10:1, extraction temperature is 50-120 DEG C, mixing time is 0.5-5 hour, extracting pressure is 2.5-5.5Mpa, obtain the thick deasphalted oil a on top and the thick de-oiled asphalt b of bottom, the thick deasphalted oil a on top enters the essence section of taking off on extraction tower top together with extraction solvent, in the essence section of taking off, the volume ratio of extraction solvent and thick deasphalted oil a is 1-2:1, extraction temperature is 60-130 DEG C, mixing time is 0.5-2 hour, extracting pressure is 2.5-5.5Mpa, obtain smart deasphalted oil c and de-oiled asphalt d, essence deasphalted oil c is heated to 80-150 DEG C and then enters the extraction deasphalted oil of extraction solvent supercritical recovery tower and reclaim extraction solvent at extraction tower top, de-oiled asphalt d returns the pre-extraction section in the middle part of extraction tower, the thick de-oiled asphalt b obtained enters the quintessence section of extraction tower bottom together with extraction solvent, in quintessence section, the volume ratio of extraction solvent and thick de-oiled asphalt b is 0.5-1:1, extraction temperature is 40-110 DEG C, mixing time is 0.5-2 hour, extracting pressure is 2.5-5.5Mpa, obtain deasphalted oil e and smart de-oiled asphalt f, deasphalted oil e returns the section of extraction in advance, essence de-oiled asphalt f enters in pitch vaporizer bottom extraction tower,
(3) smart de-oiled asphalt reclaims extraction solvent: sprayed by smart de-oiled asphalt f and enter vacuum decompression separation column, during spraying, the particle diameter of drop is 0.1-5mm, pressure in tower is-0.09--0.08Mpa, temperature is 30-60 DEG C, and the extraction solvent fractionated out reclaims and returns step (2) after multi-stage condensing.
2. a kind of dregs of fat that reduce pressure according to claim 1 remove the method for pitch, it is characterized in that, in described step (1), type of heating can at least one in electrically heated, oil bath heating, steam heating, microwave heating.
3. a kind of dregs of fat that reduce pressure according to claim 1 remove the method for pitch, it is characterized in that, in described step (2), extraction solvent is at least one in propane, butane, pentane, hexane, heptane, purity >=80% of described extraction solvent.
4. a kind of dregs of fat that reduce pressure according to claim 1 remove the method for pitch, it is characterized in that, in described step (3), condensing temperature is 15-30 DEG C.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201510132520.2A CN104762103B (en) | 2015-03-25 | 2015-03-25 | A kind of method of the dregs of fat removing Colophonium that reduces pressure |
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| CN201510132520.2A CN104762103B (en) | 2015-03-25 | 2015-03-25 | A kind of method of the dregs of fat removing Colophonium that reduces pressure |
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| CN104762103A true CN104762103A (en) | 2015-07-08 |
| CN104762103B CN104762103B (en) | 2016-08-17 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105505430A (en) * | 2015-11-30 | 2016-04-20 | 青岛科技大学 | Waste rubber continuous cracking method and device |
| CN111655823A (en) * | 2018-01-31 | 2020-09-11 | 环球油品有限责任公司 | Process and apparatus for deasphalting and asphalt conversion |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1162973A (en) * | 1994-11-07 | 1997-10-22 | 康诺科有限公司 | Process for isolating mesophase pitch |
| US20060032789A1 (en) * | 1999-11-01 | 2006-02-16 | Ormat Industries Ltd. | Method of and apparatus for processing heavy hydrocarbon feeds |
| CN104053750A (en) * | 2011-10-19 | 2014-09-17 | Meg能源公司 | Enhanced Methods For Solvent Deasphalting Of Hydrocarbons |
-
2015
- 2015-03-25 CN CN201510132520.2A patent/CN104762103B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1162973A (en) * | 1994-11-07 | 1997-10-22 | 康诺科有限公司 | Process for isolating mesophase pitch |
| US20060032789A1 (en) * | 1999-11-01 | 2006-02-16 | Ormat Industries Ltd. | Method of and apparatus for processing heavy hydrocarbon feeds |
| CN104053750A (en) * | 2011-10-19 | 2014-09-17 | Meg能源公司 | Enhanced Methods For Solvent Deasphalting Of Hydrocarbons |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105505430A (en) * | 2015-11-30 | 2016-04-20 | 青岛科技大学 | Waste rubber continuous cracking method and device |
| CN111655823A (en) * | 2018-01-31 | 2020-09-11 | 环球油品有限责任公司 | Process and apparatus for deasphalting and asphalt conversion |
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| Publication number | Publication date |
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| CN104762103B (en) | 2016-08-17 |
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Inventor after: Xu Xiaoshan Inventor after: Wu Peng Inventor after: Zhang Rui Inventor after: Lou Xiaozhao Inventor after: Liu Wending Inventor after: Shen Bo Inventor after: Li Weifeng Inventor before: Dong Yalun |
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Effective date of registration: 20160719 Address after: Mount Huangshan Road, Yancheng District of Luohe City, Henan province 462300 Building No. 17, No. 302 Applicant after: Xu Xiaoshan Address before: 430070 Hubei Province, Wuhan city Hongshan District HUANGJIAHU Road No. 3 Applicant before: Dong Yalun |
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Effective date of registration: 20181219 Address after: 056200 North of West Laoyuyu Village, Fengfeng Mining Area, Handan City, Hebei Province, 850 meters Patentee after: Hebei Yading New Materials Technology Co., Ltd. Address before: 462300 Building 302, 17 Huangshan Road, Nuocheng District, Luohe City, Henan Province Patentee before: Xu Xiaoshan |