CN101892073A - Method for extracting base oil from cutting line oil - Google Patents
Method for extracting base oil from cutting line oil Download PDFInfo
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- CN101892073A CN101892073A CN 201010239182 CN201010239182A CN101892073A CN 101892073 A CN101892073 A CN 101892073A CN 201010239182 CN201010239182 CN 201010239182 CN 201010239182 A CN201010239182 A CN 201010239182A CN 101892073 A CN101892073 A CN 101892073A
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- base oil
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a method for extracting base oil from cutting line oil, comprising the steps of carrying out modular distillation on the cutting line oil and sequentially separating light hydrocarbon oil, base oil and paraffin in three grades. In the process of treating the cutting line oil, chemical processes of acid pickling, alkali washing, decolorizing, precipitating, drying and the like and the pretreatment are avoided, so that the flow is simple; the discharge of acid-base neutralized sodium salts and decolorizing agent and the pollution can be avoided; and in addition, the base oil distilled and separated by the molecular distillation process can reach the quality index of national standard.
Description
Technical field
The present invention relates on the petrochemical complex separation field, particularly a kind of molecular distillation technique that utilizes separates the base oil in the purification readymade oil.
Background technology
As shown in Figure 1, the technology of taking usually from the technology of readymade oil separation and Extraction base oil at present is: by solvent deasphalting, solvent dewaxing, solvent treatment, acid-alkali refining, technology such as clay-filtered, remove or reduce material, the material of low-viscosity index, material, the paraffin of oxidation stability difference and the components such as chemical substance that influence the processed oil color of formation uncombined carbon, obtain the base oil that qualified lubricating oil is used.
There is following problem in this technical matters: 1, consume a large amount of solvents, the cost height.2, treating processes is leaked easily and is caused danger and pollution.3, consuming time, the power consumption of solvent recovery process long flow path.4, occupied ground is big, and production plant is that Infrastructure has high input by explosion-proof design.
Summary of the invention
For addressing the above problem, the purpose of this invention is to provide a kind of method of from readymade oil, extracting base oil, its treating processes is simple, pollution-free, can isolate the product of base oil, paraffin etc.
For achieving the above object, technical scheme of the present invention is: a kind of method of extracting base oil from readymade oil is characterized in that: readymade oil is carried out molecular distillation, divide three grades and isolate light hydrocarbon oil, base oil, paraffin successively.
Readymade oil before the fractional distillation at first outgases by thin-film evaporator and dewaters.
The present invention is in the process of handling readymade oil, not through chemical processes such as overpickling, alkali cleaning, decolouring, precipitation, dryings, need not pre-treatment, so flow process is simple, there are not the sodium salt behind the acid-base neutralisation and the discharging of discoloring agent, do not pollute, and adopted molecular distillation to separate the quality index that the base oil that distills can reach GB.
Description of drawings
Fig. 1 is the FB(flow block) of prior art;
Fig. 2 is a FB(flow block) of the present invention;
Fig. 3 is device line figure of the present invention.
Embodiment
Shown in Fig. 2,3, the present invention is a kind of method of extracting base oil from readymade oil, and it carries out molecular distillation to readymade oil, divides three grades and distills out light hydrocarbon oil, base oil, paraffin successively.
Readymade oil need not pre-treatment can directly carry out molecular distillation, and preferably, readymade oil dewaters, outgases through thin-film evaporator earlier before entering molecular distillation and enters molecular distillation equipment then.In this device, what the readymade oil sepn process first step distilled is light hydrocarbon oil, and what the second stage distilled is base oil, and what the third stage distilled is paraffin.Molecular distillation apparatus can be adjusted according to the readymade oil of different sources, and the light hydrocarbon oil in the readymade oil of different ratios content, base oil, paraffin etc. are separated one by one.Step is as follows:
First, readymade oil is directly entered surge tank 1 place, be input to thin-film evaporator 2 by volume pump and outgas and dewater, temperature is 50～120 ℃, pressure is-and 0.5Mpa～-0.9Mpa;
Material after the degassing and the dehydration is input to first step molecular distillation post 3 through pump again, and temperature is 100～150 ℃, and pressure is 200Pa～20Pa, isolates light hydrocarbon oil;
Material behind the separation light hydrocarbon oil is imported in the second stage molecular distillation post 4 again, and it is 120～200 ℃ that temperature is controlled at temperature, and pressure is 100Pa～5Pa, and base oil is separated;
The material that separates behind the aforementioned material is input in the third stage molecular distillation post 5 again, and temperature is 180～300 ℃, and pressure is 20Pa～0.1Pa, and paraffin is separated;
Remaining at last impurity heavy oil is discharged.
Embodiment 1
1., measure 30 liters of certain first vacuum side streams, directly enter surge tank 1 place, be input to thin-film evaporator 2 by volume pump and outgas and dewater 120 ℃ of temperature, pressure-0.6Mpa.
2., the material after the degassing is input in the first step molecular distillation post 3 through pump, light hydrocarbon oil is separated, 110 ℃ of temperature, pressure 100Pa, the light hydrocarbon oil of separating are 250 milliliters.
3., the material that separates behind the light hydrocarbon oil is input in the second stage molecular distillation post 4 through pump again, isolates base oil, 185 ℃ of temperature, pressure 5Pa, the base oil of separating are 28 liters.
4., the material that separates behind the base oil passes through in the third stage molecular distillation post 5 again, paraffin separated again, temperature is 230 ℃, pressure is 0.5Pa, 1 liter in the paraffin of separating.
5., the total recovery rate 93.3% of base oil.
Embodiment 2
1., measure 100 liters of certain second line of distillation oil, directly enter surge tank 1 place, be input to thin-film evaporator 2 by volume pump and outgas and dewater 60 ℃ of temperature, pressure-0.9Mpa.
2., the material after the degassing is input in the first step molecular distillation post 3 through pump, light hydrocarbon oil is separated, 110 ℃ of temperature, pressure 20Pa, the light hydrocarbon oil of separating are 0.6 liter.
3., the material that separates behind the light hydrocarbon oil is input in the second stage molecular distillation post 4 through pump again, isolates base oil, 150 ℃ of temperature, pressure 15Pa, the base oil of separating are 85 liters.
4., the material that separates behind the base oil passes through in the third stage molecular distillation post 5 again, paraffin separated again, temperature is 230 ℃, pressure is 0.5Pa, 10 liters in the paraffin of separating.
5., the total recovery rate 85% of base oil.
1., measure 150 liters of certain second line of distillation oil, the material after the degassing is input in the first step molecular distillation post 3 through pump, light hydrocarbon oil is separated, 70 ℃ of temperature, pressure-0.85Mpa, the light hydrocarbon oil of separating are 6 liters.
2., the material that separates behind the light hydrocarbon oil is input in the second stage molecular distillation post 4 through pump again, isolates base oil, 135 ℃ of temperature, pressure 25Pa, the base oil of separating are 132 liters.
3., the material that separates behind the base oil passes through in the third stage molecular distillation post 5 again, paraffin separated again, temperature is 210 ℃, pressure is 0.5Pa, 11 liters in the paraffin of separating.
4., the total recovery rate 88% of base oil.
Claims (5)
1. the method from readymade oil extraction base oil is characterized in that: readymade oil is carried out molecular distillation, divide three grades and distill out light hydrocarbon oil, base oil, paraffin successively.
2. the method for extracting base oil from readymade oil according to claim 1 is characterized in that: described three grades of molecules distillation comprises: first step molecular distillation temperature is 100～150 ℃, and pressure is 200Pa～20Pa, isolates light hydrocarbon oil; Enter second stage molecular distillation then, temperature is 120～200 ℃, and pressure is 100Pa～5Pa, isolates base oil; Enter third stage molecular distillation at last, temperature is 180～300 ℃, and pressure is 20Pa～0.1Pa, isolates paraffin.
3. the method for extracting base oil from readymade oil according to claim 1, it is characterized in that: described readymade oil need not pre-treatment and directly carries out molecular distillation.
4. the method for extracting base oil from readymade oil according to claim 1 is characterized in that: the readymade oil before the described fractional distillation outgases by thin-film evaporator earlier and dewaters.
5. the method for extracting base oil from readymade oil according to claim 4 is characterized in that: described readymade oil outgases and the temperature of dewatering is 50～120 ℃, and pressure is-0.5Mpa～-0.9Mpa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010239182 CN101892073B (en) | 2010-07-28 | 2010-07-28 | Method for extracting base oil from cutting line oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010239182 CN101892073B (en) | 2010-07-28 | 2010-07-28 | Method for extracting base oil from cutting line oil |
Publications (2)
| Publication Number | Publication Date |
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| CN101892073A true CN101892073A (en) | 2010-11-24 |
| CN101892073B CN101892073B (en) | 2013-03-27 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN 201010239182 Expired - Fee Related CN101892073B (en) | 2010-07-28 | 2010-07-28 | Method for extracting base oil from cutting line oil |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102120935A (en) * | 2011-01-10 | 2011-07-13 | 佛山汉维机电科技有限公司 | Method for recycling heptane and saxol from waste saxol containing heptane |
| CN102952583A (en) * | 2011-08-18 | 2013-03-06 | 江苏泰尔新材料科技有限公司 | Preparation method of temperature-sensing wax for automatic window opener |
| CN109486528A (en) * | 2018-12-29 | 2019-03-19 | 大连隆星新材料有限公司 | A kind of device producing Fischer-Tropsch wax crude product |
| CN109486524A (en) * | 2018-12-29 | 2019-03-19 | 大连隆星新材料有限公司 | A kind of device producing high-quality Fischer-Tropsch wax |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87105188A (en) * | 1986-07-23 | 1988-02-03 | 布斯公司 | Handle the method for short residuum oil in the crude oil refinement |
-
2010
- 2010-07-28 CN CN 201010239182 patent/CN101892073B/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN87105188A (en) * | 1986-07-23 | 1988-02-03 | 布斯公司 | Handle the method for short residuum oil in the crude oil refinement |
Non-Patent Citations (2)
| Title |
|---|
| 《化工进展》 20081231 朱宝璋等 分子蒸馏技术在石油化工中的应用 41-44 1-5 , * |
| 《石化技术与应用》 20100531 陈芬芬 等 分子蒸馏技术及其在渣油分离中的应用 253-256 1-5 第28卷, 第3期 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102120935A (en) * | 2011-01-10 | 2011-07-13 | 佛山汉维机电科技有限公司 | Method for recycling heptane and saxol from waste saxol containing heptane |
| CN102120935B (en) * | 2011-01-10 | 2014-06-04 | 佛山汉维机电科技有限公司 | Method for recycling heptane and saxol from waste saxol containing heptane |
| CN102952583A (en) * | 2011-08-18 | 2013-03-06 | 江苏泰尔新材料科技有限公司 | Preparation method of temperature-sensing wax for automatic window opener |
| CN102952583B (en) * | 2011-08-18 | 2016-03-09 | 江苏泰尔新材料股份有限公司 | The preparation method of automatic window opener temperature-sensing wax |
| CN109486528A (en) * | 2018-12-29 | 2019-03-19 | 大连隆星新材料有限公司 | A kind of device producing Fischer-Tropsch wax crude product |
| CN109486524A (en) * | 2018-12-29 | 2019-03-19 | 大连隆星新材料有限公司 | A kind of device producing high-quality Fischer-Tropsch wax |
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| CN101892073B (en) | 2013-03-27 |
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