CN101928602A - Method for separating paraffin from readymade oil - Google Patents
Method for separating paraffin from readymade oil Download PDFInfo
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- CN101928602A CN101928602A CN2010102669464A CN201010266946A CN101928602A CN 101928602 A CN101928602 A CN 101928602A CN 2010102669464 A CN2010102669464 A CN 2010102669464A CN 201010266946 A CN201010266946 A CN 201010266946A CN 101928602 A CN101928602 A CN 101928602A
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- readymade
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Abstract
The invention discloses a method for separating paraffin from cut oil. The method comprises the following steps of: directly adding the cut oil into a buffer tank to deaerate and dehydrate; pumping the processed cut oil into a first-stage centrifugal molecular distiller, and separating out base oil at the temperature of 150 to 250 DEG C and under the pressure of 20 to 1Pa; and feeding the material after the base oil is separated out into a second-stage centrifugal molecular distiller, and separating out the paraffin by controlling the temperature to be between 200 and 350 DEG C and the pressure to be between 25 and 0.1Pa. In the invention, the centrifugal molecular distillers are adopted to separate and distil the base oil and the paraffin, and in a cut oil process, the processes such as extracting with a solvent, washing with an acid, washing with an alkali, decolouring and the like, are eliminated; therefore, the flow is simple, no sodium salt after neutralization and no discolouring agent are discharged and no pollution is caused. The obtained base oil can reach the quality index of the national standard base oil.
Description
Technical field
The present invention relates to petrochemical complex and petrochemical industry grease field of refinement, particularly relate to a kind of method of utilizing centrifugal type technique of molecular distillation to separate paraffin in the readymade oil.
Background technology
Chinese invention patent CN1673319A discloses a kind of method of using dewaxing agent to be lubricated the Oil solvent dewaxing.This method joins 0.01～0.1% poly-a alkene dewaxing agent in the waxy feeds oil, mixes with dewaxing solvent, successively through overcooling, filtration, solvent recuperation, obtains pressed distillate and gatch then.Use this poly-a alkene dewaxing agent can improve the filtration velocity and the wax oil yield of solvent dewaxing, reduce the wax oil-containing simultaneously, thereby improve the device amount of finish, reduce the wax deoiling load.The poly-a olefin polymer that uses, its side chain carbon number is C
10～24, number-average molecular weight is 8000～150000, weight-average molecular weight is 400000～900000 o'clock, is suitable for the solvent treatment second line of distillation, subtracts third fractional oil and hydrotreatment.Poly-a alkene dewaxing agent has been used in this invention is improved the efficient of solvent dewaxing, but still dewaxes with a large amount of solvents.
Readymade oil is meant the oil of crude oil vacuum still output.Difference according to boiling point mainly is divided into a line to four line readymade oils, progressively raises to subtracting four lines oil boiling point from first vacuum side stream.Readymade oil is a basic material of producing lubricating oil, and wherein, the vacuum 1st side cut quality is better, also can be as transferring diesel oil to use.Compare with general base oil, readymade oil belongs to nonstandard oil, by solvent deasphalting, solvent dewaxing, solvent treatment, hydrofining or 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 of qualified lubricating oil.Its leading indicator has density, condensation point, colourity, viscosity, flash-point etc.First vacuum side stream is exactly a line oil of crude oil vacuum still output.The rest may be inferred.
As shown in Figure 1, the technology of taking usually from the technology of readymade oil separation and Extraction base oil at present is: the solvent treatment technology by solvent dewaxing obtains the base oil that qualified lubricating oil is used.But there is following problem in this technology: 1, consume a large amount of solvents, 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 from readymade oil the method for separating paraffin, treating processes is pollution-free, readymade oil directly entered in the centrifugal molecular distillating device need not pre-treatment, need not the long-time heating sedimentation, do not need pressure filtration, can isolate base oil and wax.
Readymade oil of the present invention dewaters, outgases in surge tank 1 earlier before entering centrifugal molecular distillator and enters centrifugal molecular still then, in this device, what readymade oil sepn process first step centrifugal molecular distillating came out is base oil, what second stage centrifugal molecular distillating came out is paraffin, secondary centrifugal molecular distillating device can be adjusted according to the readymade oil of different sources, and base oil in the readymade oil of different ratios content and wax are separated.
For achieving the above object, technical scheme of the present invention is:
A kind of from readymade oil the method for separating paraffin, comprise the steps and processing condition:
(1) readymade oil is entered directly the surge tank place outgases, processed;
(2) in the readymade oil suction first step centrifugal molecular distillator after step (1) is handled, 150～250 ℃ of temperature, pressure is to isolate base oil under the processing condition of 20Pa～1Pa;
(3) material behind step (2) the separation base oil is imported in the centrifugal molecular distillator of the second stage again, be controlled at 200～350 ℃ in temperature, pressure is 25Pa～0.1Pa, isolates paraffin
Be further to realize the object of the invention, described step (1) with readymade oil enter directly that the surge tank place outgases, processed is to be 50～90 ℃ in temperature, pressure be-0.6Mpa～-the 0.95Mpa condition under, the degassing, dehydration are up to the boiling termination.
Remaining impurity heavy oil was discharged from the outlet (d) of second stage centrifugal molecular distillator after described step (3) was isolated paraffin.
The time that described step (2) is isolated base oil is preferably 30-45 minute, need to prove, at the base oil of different amounts and the first step centrifugal molecular distillator of differing capacities, the treatment time of step (2) is different.
The time that described step (3) is isolated paraffin is preferably 30-50 minute.Need to prove that at the base oil of different amounts and the second stage centrifugal molecular distillator of differing capacities, the treatment time of step (3) is different.
With respect to prior art, the present invention has following advantage and beneficial effect;
The present invention is in the process of handling readymade oil, do not pass through chemical processes such as solvent extraction and pickling, alkali cleaning, washing, decolouring, so flow process is simple, there is not the discharging of the sodium salt behind the acid-base neutralisation, do not pollute, and the base oil that has adopted centrifugal molecular distillator to separate can reach the quality index of GB.
Description of drawings
Fig. 1 is the FB(flow block) of prior art;
Fig. 2 be the present invention a kind of from readymade oil the FB(flow block) of the method for separating paraffin;
Fig. 3 be the present invention a kind of from readymade oil the device line figure of the method for separating paraffin.
Embodiment
The present invention is further illustrated below in conjunction with drawings and Examples, but the scope of protection of present invention is not limited to the scope of embodiment statement.
Shown in Fig. 2,3, the present invention is a kind of method of separating wax from readymade oil, and it carries out centrifugal molecular distillating to readymade oil, divides secondary to distill out base oil and paraffin successively.At first, readymade oil is directly entered surge tank 1 place from the inlet a of surge tank 1 outgas, dewater, end up to boiling, readymade oil outgases and the temperature of dewatering is 50～90 ℃, and pressure is-0.6Mpa～-0.95Mpa; Be input in the first step centrifugal molecular distillator 2 by volume pump then, 150～250 ℃ of temperature, pressure is to isolate base oil under the processing condition of 20Pa～1Pa, and base oil flows out from the outlet b of first step centrifugal molecular distillator 2.Material behind the separation base oil is imported in the second stage centrifugal molecular distillator 3 again, is controlled at 200～350 ℃ in temperature, and pressure is 25Pa～0.1Pa, and paraffin is separated, and paraffin wax flows out from the outlet c of second stage centrifugal molecular distillator 3; Remaining at last impurity heavy oil is discharged from the outlet d of second stage centrifugal molecular distillator 3.
(1) second line of distillation oil directly enters surge tank 1 place for 500 milliliters, and outgas and dewater, 80 ℃ of temperature, pressure-0.85Mpa ends up to boiling, and the time is 45 minutes.In volume percent, the base oil content of this second line of distillation oil is 90%.
(2) material after step (1) degassing is input in the first step centrifugal molecular distillator 2 through pump, base oil is separated, and 170 ℃ of temperature, pressure 5Pa, the time is 30 minutes; The base oil weight of separating is 420 milliliters, and after testing, when temperature was 100 ℃, kinematic viscosity was 6.765mm
2/ s, flash-point (opening) is 220 ℃, and pour point is-12 ℃, and mechanical impurity is 0, and viscosity index is 66, carbon residue is 0.031% (weight); Copper corrosion (100 ℃, 3h) is the 1a level, reaches the national standard of base oil.
(3) material after step (2) is separated base oil is input in the second stage centrifugal molecular distillator 3 through pump again, isolates paraffin, 250 ℃ of temperature, and pressure 1Pa, the time is 30 minutes, 43 milliliters and 30 milliliters impurity heavy oil of the paraffin of separating.
(1) subtract 500 milliliters of third fractional oils and directly enter surge tank 1 place, outgas and dewater, 90 ℃ of temperature, pressure-0.95Mpa ends up to boiling, and the time is 30 minutes.In volume percent, this base oil content that subtracts third fractional oil is 80%.
(2) material after step (1) degassing is input in the first step centrifugal molecular distillator 2 through pump, base oil is separated, and 250 ℃ of temperature, pressure 0.5Pa, the time is 45 minutes, separates 390 milliliters of bases.Detected result is roughly with embodiment 1.
(3) material after step (2) is separated base oil is input in the second stage centrifugal molecular distillator 3 through pump again, 350 ℃ of temperature, and pressure 0.1Pa, the time is 50 minutes, 55 milliliters and 46 milliliters impurity heavy oil of the wax of separating.
(1) subtract four lines oil and directly enter surge tank 1 place for 500 milliliters, outgas and dewater, 50 ℃ of temperature, pressure-0.6Mpa ends time 60min up to boiling.In volume percent, this base oil content that subtracts four line oil is 75%.
(2) material after step (1) degassing is input in the first step centrifugal molecular distillator 2 through pump, base oil is separated, and 150 ℃ of temperature, pressure 20Pa, the time is 30 minutes, separates 375 milliliters of bases.Detected result is roughly with embodiment 1.
(3) material after step (2) is separated base oil is input in the second stage centrifugal molecular distillator 3 through pump again, 200 ℃ of temperature, and pressure 25Pa, the time is 30 minutes, 72 milliliters and 40 milliliters impurity heavy oil of the wax of separating.
The present invention does not pass through chemical processes such as solvent extraction and pickling, alkali cleaning, washing, decolouring in handling the process of readymade oil, flow process is simple, does not have the discharging of the sodium salt behind the acid-base neutralisation, does not pollute.Readymade oil of the present invention need not pre-treatment, directly enters the surge tank degassing and dehydration and then carries out the secondary centrifugal molecular distillating.The base oil that the present invention has adopted centrifugal molecular distillator to separate can reach the quality index of GB.
Claims (5)
1. the method for a separating paraffin from readymade oil is characterized in that comprising the steps and processing condition:
(1) readymade oil is entered directly the surge tank place outgases, processed;
(2) in the readymade oil suction first step centrifugal molecular distillator after step (1) is handled, 150～250 ℃ of temperature, pressure is to isolate base oil under the processing condition of 20Pa～1Pa;
(3) material behind step (2) the separation base oil is imported in the centrifugal molecular distillator of the second stage again, be controlled at 200～350 ℃ in temperature, pressure is 25Pa～0.1Pa, isolates paraffin.
2. according to claim 1 from readymade oil the method for separating paraffin, it is characterized in that: described step (1) with readymade oil enter directly that the surge tank place outgases, processed is to be 50～90 ℃ in temperature, pressure is-0.6Mpa～-the 0.95Mpa condition under, the degassing, dehydration stop up to boiling.
3. according to claim 1 from readymade oil the method for separating paraffin, it is characterized in that: remaining impurity heavy oil was discharged from the outlet (d) of second stage centrifugal molecular distillator after described step (3) was isolated paraffin.
4. according to claim 1 from readymade oil the method for separating paraffin, it is characterized in that: the time that described step (2) is isolated base oil is 30-45 minute.
5. according to claim 1 from readymade oil the method for separating paraffin, it is characterized in that: the time that described step (3) is isolated paraffin is 30-50 minute.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN 201010266946 CN101928602B (en) | 2010-08-30 | 2010-08-30 | Method for separating paraffin from readymade oil |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 201010266946 CN101928602B (en) | 2010-08-30 | 2010-08-30 | Method for separating paraffin from readymade oil |
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| CN101928602A true CN101928602A (en) | 2010-12-29 |
| CN101928602B CN101928602B (en) | 2013-03-20 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102719266A (en) * | 2012-07-03 | 2012-10-10 | 宁波博汇石油化工有限公司 | Heavy oil short-path distillation (molecular distillation) continuous production process |
| 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 |
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| CN101177646A (en) * | 2007-10-26 | 2008-05-14 | 华南理工大学 | Method for deacidizing and regenerating waste used oil by using molecular distillation technology |
| CN101624557A (en) * | 2009-07-31 | 2010-01-13 | 重庆市日用化学工业研究所 | Method for extracting neroli absolute by supercritical carbon dioxide |
| CN101717690A (en) * | 2009-10-30 | 2010-06-02 | 华南理工大学 | Method for refining camellia oil by adopting short-path distillation |
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2010
- 2010-08-30 CN CN 201010266946 patent/CN101928602B/en not_active Expired - Fee Related
Patent Citations (4)
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| US4988434A (en) * | 1989-12-13 | 1991-01-29 | Exxon Research And Engineering Company | Removal of metallic contaminants from a hydrocarbonaceous liquid |
| CN101177646A (en) * | 2007-10-26 | 2008-05-14 | 华南理工大学 | Method for deacidizing and regenerating waste used oil by using molecular distillation technology |
| CN101624557A (en) * | 2009-07-31 | 2010-01-13 | 重庆市日用化学工业研究所 | Method for extracting neroli absolute by supercritical carbon dioxide |
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Non-Patent Citations (4)
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| 刘庆文: "废发动机润滑油循环使用的工艺技术", 《天津化工》 * |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN102719266A (en) * | 2012-07-03 | 2012-10-10 | 宁波博汇石油化工有限公司 | Heavy oil short-path distillation (molecular distillation) continuous production process |
| CN102719266B (en) * | 2012-07-03 | 2014-03-12 | 宁波博汇石油化工有限公司 | Heavy oil short-path distillation (molecular distillation) continuous production process |
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