CN105419859A - Reverse back extraction refining method for petroleum reduced pressure distillation distillate and application thereof - Google Patents
Reverse back extraction refining method for petroleum reduced pressure distillation distillate and application thereof Download PDFInfo
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- CN105419859A CN105419859A CN201510764525.7A CN201510764525A CN105419859A CN 105419859 A CN105419859 A CN 105419859A CN 201510764525 A CN201510764525 A CN 201510764525A CN 105419859 A CN105419859 A CN 105419859A
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- oil
- nmp
- distillate
- base oil
- solvent
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- 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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/02—Working-up used lubricants to recover useful products ; Cleaning mineral-oil based
-
- 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
- C10G2300/1003—Waste materials
- C10G2300/1007—Used oils
-
- 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
- C10G2300/1062—Lubricating oils
-
- 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
- C10G2300/1074—Vacuum distillates
-
- 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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a reverse back extraction refining method for petroleum reduced pressure distillation distillate. Impurity compositions in the distillate are extracted through NMP to refine the distillate, based on the principle that the solubility of base oil in NMP changes along with the content of water in NMP, the base oil dissolved by NMP is reversely back-extracted, and then the base oil in the distillate is purified and efficiently recycled. Compared with the prior art, the method has the following advantages that the technology is simple, the use amount of a solvent can be greatly reduced, the recycling efficiency of the base oil is improved, and the quality of oil products can be flexibly adjusted according to the requirements of use fields and cost; cost control is good, and the profit rate is high; only one chemical solvent is used in the whole technological process, the chemical solvent can be recycled, cost can be effectively controlled, and the waste emission problem can be well solved.
Description
Technical field
The present invention relates to oil refining technical field of refinement, in particular a kind of reverse reextraction process for purification of oil underpressure distillation distillate.
Background technology
In the Atmospheric vacuum workshop section of refinery, with regard to vacuum distillation tower, its overhead product becomes and subtracts top oil, and side line, according to the difference of technological design, has vacuum 1st side cut, second line of distillation, subtracts three lines, subtract four lines and lower residual oil.Wherein subtract top comparatively light with vacuum 1st side cut, experienced raw material can be returned as normal pressure, subtract two subtract three lines can as the raw material of paraffin according to design, subtract four lines with subtract end residual oil can as the charging of catalytic cracking, also can as the raw material of pitch.Tower top and side line are be separated according to the difference of boiling range with bottom product.Usual Light lube oil can be used as the base oil of lubricating oil, but can as except the composition of lubricant base except containing in Light lube oil, also contain the impurity of 5 ~ 10%, main component normally heavy aromatic oil, the resin and asphalt of impurity.In order to improve oil product so that the field of high grade requirements can be applied to, need to refine this part distillate.The process for purification that existing technology adopts uses carclazyte to filter after pickling, but such technique not only can produce a large amount of acid sludge and discarded carclazyte, and treatment scheme is complicated.Waste time and energy, seriously polluted and cost cannot reduce.Same problem is also present in the treating process of the distillate of waste lubricating oil underpressure distillation.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, provide a kind of reverse reextraction process for purification and application thereof of oil underpressure distillation distillate.
The present invention is achieved by the following technical solutions: a kind of reverse reextraction process for purification of oil underpressure distillation distillate: it is characterized in that step is as follows:
Step one, use nmp solvent carry out extracting to distillate, obtain Extract and raffinate;
Step 2, raffinate carried out to the nmp solvent that Distillation recovery wherein dissolves, obtain refining base oil;
Step 3, in Extract, add water, the base oil wherein dissolved is separated out, obtains after oily water separation and separate out base oil;
Step 4, isolated for step 3 aqueous phase is removed moisture through distillation procedure, obtain impurity oil after reclaiming nmp solvent, impurity oil is for the preparation of high-grade pitch.
As further improvement of these options, the temperature of distilling raffinate is 240 ~ 280 DEG C, and pressure is normal pressure.
As further improvement of these options, the volume ratio of described step one intermediate distillates and NMP is 1:0.5 ~ 1:2.
As further improvement of these options, the volume of the water added in described step 3 is 0.2 ~ 0.8 times of step one intermediate distillates volume.
The present invention also provides a kind of renovation process of waste lubricating oil, it is characterized in that step is as follows:
Step one, obtain waste lubricating oil distillate and vacuum residuum by underpressure distillation;
Step 2, the refining Reclaimed Base Oil of reverse reextraction process for purification process waste lubricating oil distillate acquisition using any one oil underpressure distillation distillate above-mentioned and precipitation Reclaimed Base Oil;
The mixed-solvent extraction vacuum residuum of step 3, use NMP and octane, the volume ratio of mixed solvent and vacuum residuum is 1:2, wherein in mixed solvent, the volume ratio of NMP and octane is 1:3, Extract obtains residual oil Reclaimed Base Oil after distillating recovering solvent, residuum is for the preparation of high-grade asphaltic products. after distillating recovering solvent for raffinate, and the octane of recovery and NMP drop in the extraction procedure of vacuum residuum again.
The present invention has the following advantages compared to existing technology: technique is simple, greatly can save the usage quantity of solvent, improve the organic efficiency of base oil, can adjust oil quality flexibly according to the requirement of use field and cost; Cost control is good, and rate of profit is high; Only use a kind of chemical solvents in whole technological process, and chemical solvents can also recycle and reuse, cost can be effectively controlled, and waste discharge problem obtains good solution.
Embodiment
Elaborate to embodiments of the invention below, the present embodiment is implemented under premised on technical solution of the present invention, give detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following embodiment.
Embodiment 1
A kind of reverse reextraction process for purification of oil underpressure distillation distillate: it is characterized in that step is as follows:
Step one, use nmp solvent carry out extracting to distillate, obtain Extract and raffinate.The volume ratio of its intermediate distillates and NMP is 1:0.5.The used in amounts of extraction solvent will strictly control, can not because of the recyclable and excessive use of solvent; Although the consumption of NMP is larger, in refining base oil, foreign matter content is lower, and the amount of Extract also increases thereupon, and base oil also can be partly dissolved with extract, causes the usage quantity of water in step 3 to increase, and aftertreatment cost improves.Comprehensively every, use the ratio that the volume ratio of distillate and NMP is 1:0.5 ~ 1:2, oil quality and cost can be taken into account.
Step 2, raffinate carried out to the nmp solvent that Distillation recovery wherein dissolves, obtain refining base oil; The temperature of distilling raffinate is 240 ~ 280 DEG C, and pressure is normal pressure.
Step 3, in Extract, add water, the volume of the water wherein added is 0.2 times of step one intermediate distillates volume, the base oil wherein dissolved is separated out, obtains and separate out base oil after oily water separation.By the usage quantity of strict the controls NMP of step one, under the prerequisite ensureing oil product, the usage quantity of NMP controls as far as possible, only needs to add a small amount of water and can either realize the base oil be dissolved in NMP and separate out, realize separation in this operation steps.The usage quantity reducing water reduces on the one hand the quantity discharged of waste water, also saves a large amount of energy distilling in the process dewatered on the other hand, makes the cost of whole technique be able to strict control.
Step 4, isolated for step 3 aqueous phase is removed moisture through distillation procedure, obtain impurity oil after reclaiming nmp solvent, impurity oil is for the preparation of high-grade pitch.
The available base oil composition contained in distillate accounts for 90 ~ 95%, all the other compositions are the impurity such as heavy arene, resin and asphalt, NMP is to the solvability be better than the solvability of these impurity components base oil, this makes it possible to the content realizing being reduced magazine in distillate by extracting operation, improve oil quality.But nmp solvent still has certain solvability for base oil, if do not reclaim the base oil in Extract, huge waste will be caused, raw materials cost can be made simultaneously significantly to increase, the problem of the discharge of waste can be caused in addition.
Although NMP is far short of what is expected compared with the solvability of the impurity such as heavy arene, resin and asphalt for the solvability of base oil, after extraction procedure, in Extract, still can be dissolved with the base oil composition of a part.Water and NMP can dissolve each other, and are that the base oil dissolved in the Extract of solvent becomes branch because solubleness reduces further and separates out after adding water with NMP; And impurity component has extraordinary solubleness in NMP, the add-on of water controlled well can make impurity still be dissolved in system.By this cover treatment process, additionally chemical solvents need not be added, namely can optimized integration oil and being effectively separated of impurity, reach refining effect.
By such technique, greatly can save the usage quantity of solvent, substantially increase the organic efficiency of base oil, and technique be simple.The oil quality of refining base oil improves along with the rising of the consumption of NMP, can adjust oil quality flexibly according to the requirement of use field and cost.The base oil of separating out can again be re-refined by NMP extracting more as required or directly apply, though the comparatively refining base oil of its oil quality is poor, not do under further disposition its colourity and oil product grade also higher than common distillate, and separate out by reclaiming the yield that base oil can improve entirety greatly, profit is improved significantly.Only use a kind of chemical solvents in whole technological process, and chemical solvents can also recycle and reuse, cost can be effectively controlled, and waste discharge problem obtains good solution.
Embodiment 2
A reverse reextraction process for purification for oil underpressure distillation distillate, wherein the volume ratio of step one intermediate distillates and NMP is 1:2, and the volume of the water added in step 3 is 0.8 times of step one intermediate distillates volume.All the other are with embodiment 1.
Embodiment 3
A renovation process for waste lubricating oil, is characterized in that step is as follows:
Step one, obtain waste lubricating oil distillate and vacuum residuum by underpressure distillation;
Step 2, the refining Reclaimed Base Oil of reverse reextraction process for purification process waste lubricating oil distillate acquisition using the oil underpressure distillation distillate in embodiment 1 or 2 and precipitation Reclaimed Base Oil;
The mixed-solvent extraction vacuum residuum of step 3, use NMP and octane, the volume ratio of mixed solvent and vacuum residuum is 1:2, wherein in mixed solvent, the volume ratio of NMP and octane is 1:3, Extract obtains residual oil Reclaimed Base Oil after distillating recovering solvent, residuum is for the preparation of high-grade asphaltic products. after distillating recovering solvent for raffinate, and the octane of recovery and NMP drop in the extraction procedure of vacuum residuum again.
Because in waste lubricating oil vacuum residuum, impurity ratio is high, and viscosity is large, defines the structure of parcel mutually between impurity and base oil, uses single solvent to realize rapid solution.NMP is the good solvent of a kind of solubility property, can dissolve most organic substances, very high for colloid, bituminous matter and solubility of additive, but its solubleness for alkane is poor; And the dissolving properties of octane is exactly contrary with NMP, have extraordinary solubleness for alkane, and solubleness between NMP and octane is limited, and density difference is larger.Therefore by after these two kinds of solvent, can realize being mainly base oil composition and other magazins' layout of alkane.Again by distillation procedure by solvent recuperation, namely can realize waste lubricating oil vacuum residuum is effectively utilized.In addition, the boiling point of NMP and octane is all lower, very low by distillation procedure recycling design energy consumption.Can be reclaimed the most base oil compositions contained in waste lubricating oil vacuum residuum by this method, organic efficiency reaches more than 90%.
Waste lubricating oil vacuum residuum effectively can be utilized by this programme, reduce enterprise's raw materials cost and improve rate of profit; The Reclaimed Base Oil purity simultaneously obtained by present method is high, colourity good; In whole processing technological flow, the equal recycle and reuse of solvent, the product of acquisition also all obtains effective utilization, does not almost have the problem of waste discharge and process, environmentally friendly, economic environmental protection.
Claims (5)
1. a reverse reextraction process for purification for oil underpressure distillation distillate, is characterized in that step is as follows:
Step one, use nmp solvent carry out extracting to distillate, obtain Extract and raffinate;
Step 2, raffinate carried out to the nmp solvent that Distillation recovery wherein dissolves, obtain refining base oil;
Step 3, in Extract, add water, the base oil wherein dissolved is separated out, obtains after oily water separation and separate out base oil;
Step 4, isolated for step 3 aqueous phase is removed moisture through distillation procedure, obtain impurity oil after reclaiming nmp solvent, impurity oil is for the preparation of high-grade pitch.
2. the reverse reextraction process for purification of a kind of oil underpressure distillation distillate as claimed in claim 1, it is characterized in that described temperature of distilling raffinate is 240 ~ 280 DEG C, pressure is normal pressure.
3. the reverse reextraction process for purification of a kind of oil underpressure distillation distillate as claimed in claim 1, is characterized in that: the volume ratio of described step one intermediate distillates and NMP is 1:0.5 ~ 1:2.
4. the reverse reextraction process for purification of a kind of oil underpressure distillation distillate as claimed in claim 1, is characterized in that: the volume of the water added in described step 3 is 0.2 ~ 0.8 times of step one intermediate distillates volume.
5. a renovation process for waste lubricating oil, is characterized in that step is as follows:
Step one, obtain waste lubricating oil distillate and vacuum residuum by underpressure distillation;
Step 2, the refining Reclaimed Base Oil of reverse reextraction process for purification process waste lubricating oil distillate acquisition using any one oil underpressure distillation distillate in claim 1 to 3 and precipitation Reclaimed Base Oil;
The mixed-solvent extraction vacuum residuum of step 3, use NMP and octane, the volume ratio of mixed solvent and vacuum residuum is 1:2, wherein in mixed solvent, the volume ratio of NMP and octane is 1:3, Extract obtains residual oil Reclaimed Base Oil after distillating recovering solvent, residuum is for the preparation of high-grade asphaltic products. after distillating recovering solvent for raffinate, and the octane of recovery and NMP drop in the extraction procedure of vacuum residuum again.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN201510764525.7A CN105419859A (en) | 2015-11-10 | 2015-11-10 | Reverse back extraction refining method for petroleum reduced pressure distillation distillate and application thereof |
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| CN201510764525.7A CN105419859A (en) | 2015-11-10 | 2015-11-10 | Reverse back extraction refining method for petroleum reduced pressure distillation distillate and application thereof |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111849604A (en) * | 2020-07-20 | 2020-10-30 | 安徽国孚凤凰科技有限公司 | Waste lubricating oil distillate oil extraction regeneration process |
| CN114350433A (en) * | 2021-12-23 | 2022-04-15 | 安徽国孚凤凰科技有限公司 | Solvent extraction method for base oil |
| CN114854484A (en) * | 2022-06-02 | 2022-08-05 | 河北车迪石油化工有限公司 | Waste mineral oil regeneration process and system |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111849604A (en) * | 2020-07-20 | 2020-10-30 | 安徽国孚凤凰科技有限公司 | Waste lubricating oil distillate oil extraction regeneration process |
| CN114350433A (en) * | 2021-12-23 | 2022-04-15 | 安徽国孚凤凰科技有限公司 | Solvent extraction method for base oil |
| CN114854484A (en) * | 2022-06-02 | 2022-08-05 | 河北车迪石油化工有限公司 | Waste mineral oil regeneration process and system |
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Application publication date: 20160323 |