CN101892073B - 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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- CN101892073B CN101892073B CN 201010239182 CN201010239182A CN101892073B CN 101892073 B CN101892073 B CN 101892073B CN 201010239182 CN201010239182 CN 201010239182 CN 201010239182 A CN201010239182 A CN 201010239182A CN 101892073 B CN101892073 B CN 101892073B
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- base oil
- readymade
- molecular distillation
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (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 a kind of molecular distillation technique that utilizes particularly, the base oil in the separating-purifying readymade oil.
Background technology
As shown in Figure 1, the technique of usually taking from the technology of readymade oil separation and Extraction base oil at present is: by solvent deasphalting, solvent dewaxing, solvent treatment, acid-alkali refining, the technique such as clay-filtered, remove or reduce the material, the material of low-viscosity index, the oxidation stability that form uncombined carbon poor material, paraffin and the components such as chemical substance that affect the processed oil color, 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, and cost is high.2, treating processes is leaked cause danger and pollution easily.3, consuming time, the power consumption of solvent recovery process long flow path.4, occupied ground is large, and production plant is by Explosion-proof Design, and Infrastructure has high input.
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 successively light hydrocarbon oil, base oil, paraffin.
Readymade oil before the fractional distillation is at first undertaken degassed by thin-film evaporator and dehydration.
The present invention is in the process of processing 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 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 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 successively light hydrocarbon oil, base oil, paraffin.
Readymade oil need not pre-treatment can directly carry out molecular distillation, preferably, readymade oil before entering molecular distillation first through thin-film evaporator dewater, the degassed molecular distillation equipment that then enters.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 carry out degassed and dehydration, temperature is 50～120 ℃, pressure is-and 0.5Mpa～-0.9Mpa;
Degassed and the dehydration after material be input to first step molecular distillation post 3 through pump again, temperature is 100～150 ℃, pressure is 200Pa～20Pa, isolates light hydrocarbon oil;
Material behind the separation light hydrocarbon oil is inputted 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 impurity heavy oil is discharged at last.
Embodiment 1
1., measure 30 liters of certain first vacuum side streams, directly enter surge tank 1 place, by volume pump be input to thin-film evaporator 2 carry out degassed and the dehydration, 120 ℃ of temperature, pressure-0.6Mpa.
2., the material after degassed 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.
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 carry out degassed and dehydration, temperature 60 C, pressure-0.9Mpa.
2., the material after degassed 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.
Embodiment 3
1., measure 150 liters of certain second line of distillation oil, the material after degassed is input in the first step molecular distillation post 3 through pump, light hydrocarbon oil is separated, temperature 70 C, 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 (4)
1. method of extracting base oil from readymade oil, it is characterized in that: readymade oil is carried out molecular distillation, divide three grades and distill out successively light hydrocarbon oil, base oil, paraffin, described three grades of molecules distillation comprises: first step molecular distillation temperature is 100～150 ℃, pressure is 200Pa～20Pa, isolates light hydrocarbon oil; Then enter second stage molecular distillation, temperature is 120～200 ℃, and pressure is 100Pa～5Pa, isolates base oil; Enter at last third stage molecular distillation, temperature is 180～300 ℃, and pressure is 20Pa～0.1Pa, isolates paraffin.
2. 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.
3. the method for extracting base oil from readymade oil according to claim 1, it is characterized in that: the readymade oil before the described fractional distillation is undertaken degassed by thin-film evaporator first and dehydration.
4. the method for from readymade oil, extracting base oil according to claim 3, it is characterized in that: it is 50～120 ℃ that described readymade oil carries out temperature degassed and dehydration, 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 |
|---|---|
| CN101892073A CN101892073A (en) | 2010-11-24 |
| CN101892073B true CN101892073B (en) | 2013-03-27 |
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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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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| 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 |
| 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 |
| 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 |
| 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 |
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 |
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2010
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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 |
|---|
| 朱宝璋等.分子蒸馏技术在石油化工中的应用.《化工进展》.2008,41-44. * |
| 陈芬芬 等.分子蒸馏技术及其在渣油分离中的应用.《石化技术与应用》.2010,第28卷(第3期),253-256. * |
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| CN101892073A (en) | 2010-11-24 |
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Granted publication date: 20130327 Termination date: 20200728 |