CN1258666A - Saturated hydrocarbon recovering and utilizing technology - Google Patents
Saturated hydrocarbon recovering and utilizing technology Download PDFInfo
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- CN1258666A CN1258666A CN 99104229 CN99104229A CN1258666A CN 1258666 A CN1258666 A CN 1258666A CN 99104229 CN99104229 CN 99104229 CN 99104229 A CN99104229 A CN 99104229A CN 1258666 A CN1258666 A CN 1258666A
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Abstract
The present invention belongs to petrochemical technology and relates to one technological process of recovering saturated hydrocarbon from the extraction liquid during refining lubricating oil solvent from straight run oil. The first-section light hydrocarbon with a content of arene with 90-280 deg.c boiling spread lower than 10 mol% is used as the second solvent in the counter-extraction of the extraction liquid. The present invention makes it possible to recover 90 mol% of the saturated hydrocarbon in the extraction liquid and thus to raise the lubricating oil solvent by 1-10 percentage. The present invention may be also used to counter-extract 45-65 mol% of the first extraction oil during refining lubricating solvent as catalytic cracking material.
Description
The invention belongs to oil refining and petrochemical industry, relate to a kind of novel process of from the Extract of straight run oil lubrication Oil solvent treating process, recycling stable hydrocarbon.
In the lubricating oil solvent production process, producer all adopts single solvent treatment technology, and its solvent comprises furfural, N-Methyl pyrrolidone, phenol etc.It is extracted out, and saturated hydrocarbon content is 20m% to 35m% in the oil, and this part stable hydrocarbon can be used as lubricant base or catalytically cracked material after reclaiming.U.S. Pat 4381234 is revealed: in the lube oil furfural refining process, add R-COONH-CH in furfural
2CH
2-SO
3Na makes solubility promoter, can improve 4 percentage points of the yields (volume ratio) of raffinating oil, but R-COONH-CH
2CH
2-SO
3Na is difficult for reclaiming.USSR (Union of Soviet Socialist Republics) patent SU1004447 reveals: adds 20% to 30% ortho-cresol in the furfural and makes solubility promoter, can improve 2 to 4 percentage points of the yields of raffinating oil, but ortho-cresol and furfural ratio mutability in the solvent recuperation process.The solubility promoter that is used for furfural, phenol treating process in foreign patent and the bibliographical information also has a lot, mainly is some tensio-active agents, polar solvent, oxidation inhibitor etc.Domestic manufacturer also proposes the technology of oneself to the deep processing and utilization of extracting oil out.As Maoming petro-chemical corporation refinery at " oil refining design " [1997 Vol.27 (2), P10] on " furfural extract oil rationally utilizes " literary composition of delivering mention, carry out settlement separate with cooling-sedimentation-separation processes to lubricating oil furfural Extract, obtain more gently the separating out oil and heavily separate out oil of stable hydrocarbon, but gently separate out oil (raffinating oil) yield and heavily separate out oil (extracting oil out) aromatic hydrocarbons purity lower, in addition, this technology use range is limited by the column bottom temperature of lubricating oil solvent tower.
The purpose of this invention is to provide a kind of technology of from the Extract of straight run oil lubrication Oil solvent treating process, recycling stable hydrocarbon, can improve the stable hydrocarbon recovery utilization rate, and solvent for use is cheap and easy to get, reclaim easily, recycle to form in the process and stablize.
A kind of technology of from the Extract of straight run oil lubrication Oil solvent treating process, recycling stable hydrocarbon of the present invention, be characterised in that: in Process of Lube Solvent Refining, use a kind of boiling range aromaticity content between 90 ℃ to 280 ℃ to be lower than one section light hydrocarbon of 10m% as second solvent.Introduce the difference of position according to second solvent, technical solution of the present invention has two kinds, is specially:
First kind of technology of recycling stable hydrocarbon from the Extract of straight run oil lubrication Oil solvent treating process of the present invention comprises the steps:
(I) raw material and main solvent reverse contact in the lubricating oil solvent tower, finish liquid-liquid extractive process, generate a raffinate and an Extract, a raffinate removes once to be raffinated oil behind the solvent and goes out device as lubricant base, and an Extract goes out the solvent treatment tower and enters step (II);
(II) from the Extract and second solvent of step (I), blending ratio is, Extract: second solvent=1.0: 0.05～0.5 (mass ratio), described second solvent is one section light hydrocarbon that boiling range aromaticity content between 90 ℃ to 280 ℃ is lower than 10m%, mixed solution is through cooling and the constant temperature layering, and the upper strata obtains the secondary raffinate, and lower floor obtains the secondary Extract, the secondary Extract removes and obtains secondary behind the solvent and extract oil out and go out device, and the secondary raffinate enters step (III);
(III) remove from the secondary raffinate of step (II) and obtain secondary behind the solvent and raffinate oil, secondary is raffinated oil and is returned step (I) and mix with raw material or directly go out device;
Recycle after the main solvent and second solvent recuperation in the above-mentioned steps.
Second kind of technology of recycling stable hydrocarbon from the Extract of straight run oil lubrication Oil solvent treating process of the present invention comprises the steps:
(I) raw material enters at lubricating oil solvent tower middle part, main solvent enters on lubricating oil solvent tower top, second solvent enters in lubricating oil solvent tower bottom, after liquid-liquid extracting, raffinate is extracted out from the solvent treatment top of tower, Extract is extracted out from the solvent treatment tower bottom, described second solvent is one section light hydrocarbon that boiling range aromaticity content between 90 ℃ to 280 ℃ is lower than 10m%, and solvent ratio is: main solvent: raw material: second solvent=1.0～3.5: 1.0: 0.1～1.0 (mass ratioes);
(II) Extract removes and obtains extracting out oil behind the solvent and go out device; Raffinate is raffinated oil after removing solvent, and raffinating oil goes out device as lubricant base;
Recycle after the main solvent and second solvent recuperation in the above-mentioned steps.
In two technical schemes of the invention described above:
Raw material comprises after the dewaxing of the various crude oil that are suitable for producing lubricant base and/or straight run oil and light, the heavy deasphalted oil of not dewaxing.Main solvent comprises furfural, phenol, N-Methyl pyrrolidone etc.The tower top temperature of lubricating oil solvent tower can be 90～150 ℃, and tower middle part temperature can be 50～140 ℃, and column bottom temperature can be 45～90 ℃.
Second solvent used in the present invention has back suction effect and the change effect of balancing each other in treating process, can reclaim the stable hydrocarbon in the Extract, because of itself and main solvent density difference are big, so recycle convenient, and it is can not cause that the main solvent composition after the recovery changes, and cheap and easy to get.Use the present invention, can reclaim the above stable hydrocarbon of 90m% in the lubex, thereby improve 1 to 10 percentage point of lubricant base yield, the viscosity index of the lubricant base of the viscosity index of this lubricant base and former lubricating oil solvent explained hereafter is suitable, and other character (as: sulphur, nitrogen etc.) increases the back in base oil yield and changes little.If adopt first kind of technology of the present invention, the secondary after reclaiming is raffinated oil (being stable hydrocarbon) as fcc raw material, but back suction go out lubricating oil solvent once extract 45m% to 65m% in the oil out as catalytically cracked material.Compare with former lubricating oil solvent technology, adopt the extraction oil aromatic hydrocarbons purity of producing behind the present invention, can improve more than 10 percentage points, reach between the 75m% to 95m%, be convenient to chemical utilization.
Describe the present invention in detail below in conjunction with accompanying drawing, but accompanying drawing does not limit the present invention.
Fig. 1: the typical flowchart of first kind of scheme of the present invention;
Fig. 2: the typical flowchart of second kind of scheme of the present invention.
As Fig. 1, raw material 1 enters from lubricating oil solvent tower 16 middle parts, main solvent 2 enters from lubricating oil solvent tower 16 tops, second solvent 3 and an Extract 5 mix with static mixer 26 after interchanger 27 is cooled to a certain temperature (40～50 ℃) back constant temperature layering in minute flow container 28 with certain proportion, upper solution 8 obtains secondary to secondary raffinate stripping tower 18 and raffinates oil 10 and moisture after steam 13 stripping desolventizings, the logistics 6c that contains second solvent 3 and main solvent 2, secondary raffinates oil 10 or be circulated to lubricating oil solvent tower 16 middle parts and increase the lubricant base yield, or goes out this device and make catalytically cracked material; Logistics 6c moisture, that contain second solvent 3 and main solvent 2 enters demixing of solvents water knockout 23.After lower floor's solution 9 to low pressure evaporator tower 21 and high pressure evaporation tower 20 takes off the mixture flow 6a that contains the main solvent 2 and second solvent 3, behind extract stripper 19 usefulness steam 13 strippings, obtain extracting out oil 11 and logistics 6c moisture, that contain second solvent 3 and main solvent 2 again; After the mixture flow 6a that contains the main solvent 2 and second solvent 3 enters the 22 sedimentation layerings of demixing of solvents jar, main solvent 2 is extracted out from demixing of solvents jar 22 bottoms and is circulated to lubricating oil solvent tower 16 tops, and second solvent 3 is extracted out from demixing of solvents jar 22 tops and is circulated to static mixer 26; Extract oil 11 out and go out device; Logistics 6c moisture, that contain second solvent 3 and main solvent 2 enters demixing of solvents water knockout 23.Raffinate 4 is extracted out from lubricating oil solvent tower 16 tops and is entered raffinate stripping tower 17 one time, is once raffinated oil 7 and moisture main solvent 6 behind steam 13 strippings, once raffinates oil 7 to go out device as lubricant base; Moisture main solvent 6 enters demixing of solvents water knockout 23.The moisture main solvent 6 that comes from raffinate stripping tower 17 top and be divided into three-phase after the logistics 6c moisture, that contain second solvent 3 and main solvent 2 that secondary raffinate stripping tower 18 and extract stripper 19 tops are come enters demixing of solvents water knockout 23: the upper strata is second solvent 3, is circulated to static mixer 26; The middle level is solvent-laden water 14; Lower floor is moisture main solvent 15.Moisture main solvent 15 enters 24 dehydrations of solvent dehydration tower, gets main solvent 2 after the dehydration and is circulated to lubricating oil solvent tower 16 tops, and water-containing solvent 6b is circulated to demixing of solvents water knockout 23.Solvent-laden water 14 enters solvent evaporator 25 and reclaims water-containing solvent 6b and be circulated to demixing of solvents water knockout 23, and water 12 is emitted from solvent evaporator 25 bottoms.
As Fig. 2, raw material 1 enters from lubricating oil solvent tower 16 middle parts, and main solvent 2 enters from lubricating oil solvent tower 16 tops, and second solvent 3 directly enters from lubricating oil solvent tower 16 bottoms.Raffinate 4d extracts out from lubricating oil solvent tower 16 tops and enters raffinate stripping tower 17d, behind steam 13 strippings, obtain raffinating oil 7d and logistics 6c moisture, that contain second solvent 3 and main solvent 2, and the 7d that raffinates oil goes out device as lubricant base; Logistics 6c moisture, that contain second solvent 3 and main solvent 2 enters demixing of solvents water knockout 23.Extract 5d from lubricating oil solvent tower 16 bottoms extract out enter low pressure evaporator tower 21 and high pressure evaporation tower 20 and take off the mixture flow 6a that contains the main solvent 2 and second solvent 3 after, behind extract stripper 19 usefulness steam 13 strippings, obtain extracting out oily 11d and logistics 6c moisture, that contain second solvent 3 and main solvent 2 again; After the mixture flow 6a that contains the main solvent 2 and second solvent 3 enters the 22 sedimentation layerings of demixing of solvents jar, main solvent 2 is extracted out from demixing of solvents jar 22 bottoms and is circulated to lubricating oil solvent tower 16 tops, and second solvent 3 is extracted out from demixing of solvents jar 22 tops and is circulated to lubricating oil solvent tower 16 bottoms.Be divided into three-phase after the logistics 6c moisture, that contain second solvent 3 and main solvent 2 that comes from raffinate stripping tower 17d top and extract stripper 19 tops enters demixing of solvents water knockout 23: the upper strata is second solvent 3, is circulated to lubricating oil solvent tower 16 bottoms; The middle level is solvent-laden water 14; Lower floor is moisture main solvent 15.Moisture main solvent 15 enters 24 dehydrations of solvent dehydration tower, gets main solvent 2 after the dehydration and is circulated to lubricating oil solvent tower 16 tops, and water-containing solvent 6b is circulated to demixing of solvents water knockout 23.Solvent-laden water 14 enters solvent evaporator 25 and reclaims water-containing solvent 6b and be circulated to demixing of solvents water knockout 23, and water 12 is emitted from solvent evaporator 25 bottoms.Compared to Figure 1, flow process shown in Figure 2 reduced secondary raffinate oil stripping tower 18, static mixer 26, interchanger 27, divide flow container 28 and intermediates secondary to raffinate oil 10, process simplification but the stable hydrocarbon rate of recovery is lower slightly.
Below the invention will be further described with embodiment, but do not limit the scope of the invention.
Embodiment 1
Technical process is Fig. 1 scheme, promptly establishes mixing tank and makes second solvent and Extract mixing sedimentation back suction at the bottom of the lubricating oil solvent Tata.
Raw material 1 subtracts four line pressed oils for certain refinery, density (20 ℃) 932.8kg/m
3, carbon residue 0.35, sulfur-bearing 3680 μ g/g, nitrogenous 2670 μ g/g,, stable hydrocarbon 58.2m%, aromatic hydrocarbons 37.8m%, colloid 3.9m%; Main solvent 2 is a furfural, second solvent 3 is lower than the light hydrocarbon of 10m% at 90 ℃ to 120 ℃, aromaticity content for boiling range, the solvent ratio of lubricating oil solvent tower 16 is a main solvent: raw material=3.0: 1.0 (mass ratio), tower top temperature is 105 ℃, column bottom temperature is 65 ℃, the solvent ratio of static mixer 26 is an Extract: second solvent=1.0: 0.1 (mass ratio), the effluent of static mixer 26 enters the 28 constant temperature layerings of separatory jar after interchanger 27 coolings, dividing flow container 28 service temperatures is 45 ℃.Mixer temperature can be 45～110 ℃.
Divide flow container 28, demixing of solvents jar 22, demixing of solvents water knockout 23 temperature to can be 40～50 ℃.Divide the upper solution 8 of flow container 28 to enter secondary raffinate stripping tower 18, raffinate oil 10 with obtaining secondary behind superheated vapour 13 strippings, secondary is raffinated oil and 10 can be circulated to lubricating oil solvent tower 16 middle parts and mix with raw material 1, also can directly go out this device as catalytically cracked material.The operational condition of raffinate stripping tower 17, extract stripper 19, high pressure evaporation tower 20, low pressure evaporator tower 21, demixing of solvents jar 22, solvent dehydration tower 24, solvent evaporator 25 and logistics capacity with do not adopt the present invention before compare and remain unchanged, owing to introduce second solvent 3 their logistics property is slightly changed, the operational condition of demixing of solvents water knockout 23 with do not adopt the present invention before compare and remain unchanged, but logistics becomes three-phase.Its test-results sees Table 1.For the ease of comparing, Extract to above-mentioned raw materials 1 adopts cooling-sedimentation-separation method to test, Extract is reduced to 45 ℃ from 65 ℃, and what can obtain 21.6m% (to pressed oil) gently separates out oil, and the character of gently separating out oil (raffinating oil) and heavily separating out oil (extracting oil out) is also listed in the table 1.After adopting the present invention, the secondary yield 27.7m% (to pressed oil) that raffinates oil extracts oily aromatic hydrocarbons purity out and reaches 75.6m%.
Secondary in the employing table 1 is raffinated oil, and does FCC tests on small fixed flowing bed FCC tests device, and test conditions is: cracking catalyst, and CC-15 industry poiser, nickel content is 4900 μ g/g; Service temperature, 500 ℃; Agent-oil ratio, 5.0; The catalyzer micro-activity, 65.2; FCC tests the results are shown in Table 2.
Embodiment 2
Technical process is Fig. 2 scheme, and second solvent directly enters from lubricating oil solvent tower 16 bottoms, can increase the lubricant base yield.
Raw material 1 is certain refinery second line of distillation pressed oil, density (20 ℃) 910.9kg/m
3, carbon residue 0.32, sulfur-bearing 3090 μ g/g, nitrogenous 1470 μ g/g,, stable hydrocarbon 63.0m%, aromatic hydrocarbons 35.0m%, colloid 1.9m%; Main solvent 2 is a furfural, and second solvent 3 is lower than the light hydrocarbon of 10m% for boiling range at 200 ℃ to 280 ℃ aromaticity contents, and second solvent 3 is directly from the bottom feeds of lubricating oil solvent tower 16.The solvent ratio of lubricating oil solvent tower 16 is: main solvent: raw material: second solvent=3.0: 1.0: 0.2 (mass ratio), tower top temperature are 90 ℃, and column bottom temperature is 45 ℃.The operational condition of raffinate stripping tower 17d, extract stripper 19, high pressure evaporation tower 20, low pressure evaporator tower 21, demixing of solvents jar 22, solvent dehydration tower 24, solvent evaporator 25 and logistics capacity with do not adopt the present invention before compare and remain unchanged, owing to introduce second solvent 3 their logistics property is slightly changed, the operational condition of demixing of solvents water knockout 23 with do not adopt the present invention before compare and remain unchanged, but logistics becomes three-phase.Former lubricating oil solvent processing condition are: main solvent: raw material=3.0: 1.0 (mass ratio), tower top temperature are 90 ℃, and column bottom temperature is 45 ℃.See Table 3 with the comparative test result of former lubricating oil solvent technology.Yield of lubricating oil improves after adopting the present invention, and its quality index is constant substantially; Extract oily aromatic hydrocarbons purity out and be increased to 80.2m% by 67.2m%.
Table 1
Do not adopt the present invention to adopt the employing of the present invention project of the present invention that do not adopt of the present invention
gently separate out the extraction oil yield that oily secondary is raffinated oil and heavily separated out oil, m% 21.6 27.7 24.0 17.9 density, 20 ℃, kg/m
3926.1 914.2 1027.8 1084.0 carbon residues, m% 0.18 0.12 2.20 1.05 condensation point, ℃/-13.0 // sulphur content, μ g/g 3,756 4,100 6,605 6200 nitrogen contents, μ g/g 1,202 1,950 7,906 9990 viscosity, mm
2/ s40 ℃/367.5 // 100 ℃ 8.9/89.0 207.0 group compositions; M% saturated hydrocarbons 57.4 58.5 15.5 12.5 aromatic hydrocarbons 39.8 37.8 71.2 75.6 colloids+former lubricating oil solvent of asphalitine 2.8 3.7 13.3 11.9 table 2 raw materials adopts refining extraction of the present invention oil secondary cracked product distribution m% dry gas 2.9 3.2 liquefied gas 8.3 12.0 gasoline 37.6 45.2 light diesel fuels 15.8 20.7 heavy oil 27.9 12.4 coke 6.9 5.8 losses 0.6 0.7 conversion ratios of raffinating oil; M% 56.3 66.9 light oil yields; M% 53.4 65.9 liquefied gas+light oil, m% 61.7 77.9 tables 3
The extraction oil of the lube base lubricating oil base oil system of the wonderful usefulness of the former lubricating oil solvent of the wonderful usefulness of former lubricating oil solvent profit of the present invention project system of the present invention is extracted oil out
The oil yield, m% 64.18 68.43 35.82 31.57 density, 20 ℃, kg/m
3877.8 877.1 992.5 1011.4 carbon residues, m% 0.02 0.02 1.00 1.10 acid number, mgKOH/g 0.08 0.10 // condensation point, ℃-5.8-8.0 // sulphur content, μ g/g 1,060 1,150 6,604 7240 nitrogen contents, μ g/g 73 87 3,820 4242 viscosity, mm
2/ s40 ℃ of 28.28 27.84 // 100 ℃ // 8.049 13.12 viscosity index (VI) 89 90 // group compositions; M% saturated hydrocarbons 82.0 84.3 29.2 15.9 aromatic hydrocarbons 17.1 14.7 67.2 80.2 colloids+asphalitine 0.9 1.0 3.6 3.9 flash-points, ℃ 210 206 //
Claims (6)
1, a kind of technology of recycling stable hydrocarbon from the Extract of straight run oil lubrication Oil solvent treating process comprises the steps:
(I) raw material (1) and main solvent (2) reverse contact in lubricating oil solvent tower (16), finish liquid-liquid extractive process, generate a raffinate (4) and an Extract (5), once raffinated oil after a raffinate (4) removes solvent (7) go out device as lubricant base, an Extract (5) goes out solvent treatment tower (16) and enters step (II);
(II) Extract (5) from step (I) mixes with second solvent (3), blending ratio is, an Extract (5): second solvent (3)=1.0: 0.05～0.5 (mass ratio), described second solvent (3) is lower than one section light hydrocarbon of 10m% for boiling range aromaticity content between 90 ℃ to 280 ℃, mixed solution is through cooling and the constant temperature layering, the upper strata obtains secondary raffinate (8), lower floor obtains secondary Extract (9), secondary Extract (9) removes and obtains secondary behind the solvent and extract oil (11) out and go out device, and secondary raffinate (8) enters step (III);
(III) remove from the secondary raffinate (8) of step (II) and obtain secondary behind the solvent and raffinate oil (10), secondary raffinate oil (10) return step (I) and mix with raw material (1) or directly go out device;
Main solvent in the above-mentioned steps (2) recycles after reclaiming with second solvent (3).
2, according to the described technology of claim 1, it is characterized in that: described raw material (1) is straight run oil and light, the heavy deasphalted oil of dewaxing back and/or not dewaxing.
3, according to the described technology of claim 1, it is characterized in that: described main solvent (2) is furfural, phenol, N-Methyl pyrrolidone.
4, a kind of technology of recycling stable hydrocarbon from the Extract of straight run oil lubrication Oil solvent treating process comprises the steps:
(I) raw material (1) enters at lubricating oil solvent tower (16) middle part, main solvent (2) enters on lubricating oil solvent tower (16) top, second solvent (3) enters in lubricating oil solvent tower (16) bottom, after liquid-liquid extracting, raffinate (4d) is extracted out from solvent treatment tower (16) top, Extract (5d) is extracted out from solvent treatment tower (16) bottom, described second solvent (3) is lower than one section light hydrocarbon of 10m% for boiling range aromaticity content between 90 ℃ to 280 ℃, solvent ratio is main solvent (2): raw material (1): second solvent (3)=1.0～3.5: 1.0: 0.1～1.0 (mass ratioes);
(II) Extract (5d) removes and obtains extracting out oil (11d) behind the solvent and go out device; Raffinated oil after raffinate (4d) removes solvent (7d), raffinate oil (7d) goes out device as lubricant base;
Main solvent in the above-mentioned steps (2) recycles after reclaiming with second solvent (3).
5, according to the described technology of claim 4, it is characterized in that: described raw material (1) is straight run oil and light, the heavy deasphalted oil of dewaxing back and/or not dewaxing.
6, technology according to claim 4 is characterized in that: described main solvent (2) is furfural, phenol, N-Methyl pyrrolidone.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN99104229A CN1077870C (en) | 1999-04-27 | 1999-04-27 | Saturated hydrocarbon recovering and utilizing technology |
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|---|---|---|---|
| CN99104229A CN1077870C (en) | 1999-04-27 | 1999-04-27 | Saturated hydrocarbon recovering and utilizing technology |
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| CN1258666A true CN1258666A (en) | 2000-07-05 |
| CN1077870C CN1077870C (en) | 2002-01-16 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103776961A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Lube oil solvent refining performance evaluation device |
| CN104593052A (en) * | 2015-01-19 | 2015-05-06 | 中国石油天然气股份有限公司 | Solvent refining equipment and method for inferior coker gas oil |
| CN105754707A (en) * | 2016-03-22 | 2016-07-13 | 中山大学 | Lubricating oil furfural refinement device provided with multi-stage extract recovery system and method |
| CN107460031A (en) * | 2017-09-14 | 2017-12-12 | 烟台神洲能源科技有限公司 | A kind of lube oil finishing solvent recovering system |
| CN114317093A (en) * | 2021-12-23 | 2022-04-12 | 安徽国孚凤凰科技有限公司 | Extraction device and method for distillation distillate oil of waste lubricating oil |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101684185B (en) * | 2008-09-27 | 2011-12-07 | 中国石油天然气股份有限公司 | Production method of high-aromatic-hydrocarbon environment-friendly rubber oil |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85100437A (en) * | 1985-04-01 | 1986-07-09 | 华东化工学院 | The mixed solvent of extractive refining of lube oils or aromatic hydrocarbons |
| CN1055303C (en) * | 1994-11-15 | 2000-08-09 | 荆门石油化工研究院 | Reusing method for extracted solution of lubricating oil solvent |
-
1999
- 1999-04-27 CN CN99104229A patent/CN1077870C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103776961A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Lube oil solvent refining performance evaluation device |
| CN103776961B (en) * | 2012-10-24 | 2015-06-17 | 中国石油化工股份有限公司 | Lube oil solvent refining performance evaluation device |
| CN104593052A (en) * | 2015-01-19 | 2015-05-06 | 中国石油天然气股份有限公司 | Solvent refining equipment and method for inferior coker gas oil |
| CN105754707A (en) * | 2016-03-22 | 2016-07-13 | 中山大学 | Lubricating oil furfural refinement device provided with multi-stage extract recovery system and method |
| CN105754707B (en) * | 2016-03-22 | 2018-08-21 | 中山大学 | A kind of lube oil furfural refining unit and method with multistage Extract recovery system |
| CN107460031A (en) * | 2017-09-14 | 2017-12-12 | 烟台神洲能源科技有限公司 | A kind of lube oil finishing solvent recovering system |
| CN114317093A (en) * | 2021-12-23 | 2022-04-12 | 安徽国孚凤凰科技有限公司 | Extraction device and method for distillation distillate oil of waste lubricating oil |
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| CN1077870C (en) | 2002-01-16 |
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