US3919075A - Process for regenerating used lubricating oils - Google Patents
Process for regenerating used lubricating oils Download PDFInfo
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- US3919075A US3919075A US459413A US45941374A US3919075A US 3919075 A US3919075 A US 3919075A US 459413 A US459413 A US 459413A US 45941374 A US45941374 A US 45941374A US 3919075 A US3919075 A US 3919075A
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- 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
- C10M175/06—Working-up used lubricants to recover useful products ; Cleaning by ultrafiltration or osmosis
Definitions
- PROCESS FOR REGENERATING USED LUBRICATING OILS The invention concerns a new process for regenerating used oils recovered, for example, from internal combustion engines, gear-boxes and differentials.
- These impurities consist of suspended solid materials, such as:
- coal-like materials metals resulting from wear iron, copper, tin, aluminum
- lead derivatives for example lead oxides, chlorides, oxychlorides or bromides.
- dispersant-detergent additives for example calcium, barium, magnesium, zinc or aluminum salicylates, sulfonates, phenates and thio-phosphonates.
- Ashless additives such as acrylic copolymers, polyamides and alkyl derivatives of succinimide;
- antioxidant antiwear additives, such as metal dithiophosphates, for example zinc dithiophosphate, sulfur organic compounds, chlorine compounds, phosphates, phosphites, phosphonates or phosphinates (the latter being chiefly recovered from gear-box or differential oils, particularly those whose metal is calcium, barium, magnesium, zinc or aluminum;
- metal dithiophosphates for example zinc dithiophosphate, sulfur organic compounds, chlorine compounds, phosphates, phosphites, phosphonates or phosphinates (the latter being chiefly recovered from gear-box or differential oils, particularly those whose metal is calcium, barium, magnesium, zinc or aluminum;
- anti-foam additives for example silicone oils
- polyolefins polyisobutene, ethylene-propylene copolymers
- ester polymers polyacrylates, polymethacrylates or polyfumarates.
- the oil may also contain lead compounds, for example lead soaps.
- the metal content of the used oils, particularly in the form of the hereinbefore described soluble metal compounds, is from 0.1 to by weight as metal.
- the invention concerns a process for regenerating used lubricating oil containing soluble metal compounds, which comprises circulating such an oil along a first side of a membrane permeable to hydrocarbons and recovering a purified oil on the other side of the membrane.
- the preferred membranes to be used according to the invention are ultrafiltration membranes.
- membranes having ultra-filtration properties we mean membranes which can be traversed by elements of small size, for example molecules of solvent, and which can retain elements, for example molecules, of larger size.
- ultrafiltration membranes for purifying organic liquids such as oils is not new, it could not be expected that good results would be obtained with modern lubricating oils which contain not only mineral oil but also additives of various types, for example oil-soluble metal salts or complexes. It could not be expected that the ultrafiltration membranes would selectively retain these soluble metal additives or the products derived therefrom.
- an ultrafiltration membrane having a cut zone of from 5,000 to 300,000, preferably 10,000 to 100,000.
- cut zone of an ultrafiltration membrane we mean the approximate molecular weight constituting the limit between the molecular weights of the proteins retained by the membrane and the molecular weights of the proteins not-retained by the membrane, provided the aqueous solution of these proteins is ultra-filtrated under a pressure of about 2 bars.
- ultrafiltration membranes we preferably use those formed of the following materials: cellulose, cellulose esters, polytetrafluoroethylene, polypentaerythritol, sulfonated polystyrene, quaternary ammonium salts obtained from dialkylamino polystyrene; ionically cross-linked complex polyelectrolytes manufactured from a polymer having sulfonic group and a polymer having quaternary ammonium groups, these polymers being preferably individually insoluble in water and hydrocarbons; sulfonated polyarylethersulfones; polyethylene, polypropylene, polymers of 2-chlorobutadiene; butadiene-styrene copolymers; vulcanized natural rubber; isoprene-isobutene copolymers; copolymers of acrylonitrile and ionic monomers, specially those subjected to thermal water treatment.
- membranes contain the following materials: polyisoprene, polybutadiene, copolymers of butadiene with acrylonitrile having a low content of nitrile groups; butyl rubber, ethylene-propylene copolymers having short molecular chains, such as EPR-EPDM- EPT.
- the ultrafiltration of the oil may be carried out without solvent, we prefer to operate with a solution of the oil in a solvent, so as to reduce its viscosity.
- oil-solvent mixtures having an oil content of, for example, l0 to 50 by volume (v/v), preferably l5 to 35 by volume (v/v).
- the solvent is preferably selected from the light hydrocarbons, so that it may be easily separated from the oil.
- the light hydrocarbons propane, butane, pentane, hexane, hep- 3 tane, petroleum ether or a light gasoline cut.
- the solvents we can mention lower cyclanic and aromatic hydrocarbons and chlorinated hydrocarbons. The conditions of temperature and pressure must be such as to maintain the oil-solvent mixture in the liquid state.
- An efficient means for increasing the oil passage rate consists of increasing the difference between the respective pressures on both sides of the membrane. Although, beyond a given pressure difference, the polarization phenomena tend to reduce the so-obtained gain, so that pressure differences in excess of IO to atmospheres are not advantageous in practice. Pressure differences of from 0.2 to 10 atmospheres are thus preferred.
- the oil flow rate is preferably higher than 0.5 m/sec, so as to reduce the polarization effect, and preferably lower than 3 m/sec, so as to avoid too high flow rates.
- the oil is preferably circulated in the form of a liquid layer whose thickness ranges from 0.5 to 5 millimeters.
- the membranes which can be used for ultrafiltration may often be also used for dialysis.
- An advantage of the dialysis technique results from the possibility of fractionating the regenerated oils.
- FIGS. 1-5 illustrate different systems of apparatus for carrying out the process of the invention.
- the apparatus preferably comprises one or more, preferably serially disposed, cells and evaporators for concentrating the collected oil.
- a cell consists, for example, of membranes arranged in a parallel direction between plates, so as to constitute enclosures through which the feed charge is circulated.
- the used oil is fed through line 3 of FIG. No. l to the enclosures l and the solvent through line 4 to the enclosures 2.
- a solution of purified oil in the solvent is discharged through line 5 and the residue through line 6.
- FIG. 2 illustrates the dialysis embodiment.
- the feed charge consisting of a mineral oil containing dissolved or suspended impurities is supplied, as such or diluted in the extraction solvent, to the cell 1 (FIG. 2) through line 11 and is thus contacted with the dialysis membranes. It is discharged through line 12 with a lower content of mineral oil and a higher content of solvent, which solvent has been passed through the membrane in a direction opposite to that of the extracted oil.
- the residue is supplied from line 12 to the evaporator 13 (the valves 28 and 29 are closed and the valve 27 open) where it is made free of its solvent; it is dis- 4 charged through lines 14 and 15 (the valve 30 is closed).
- the solvent is supplied to cell I through line 16 (the valves 17 and 18 are closed and the valve 19 is open and is discharged through line 20 with a higher mineral oil content; the oily solution is supplied to evaporator 21 wherefrom the solvent is discharged through line 22 (the valve 23 is closed).
- the dry dialyzed oil is recovered in line 24.
- the solvent vapors are circulated through line 22 and supplied to condenser 25, while the recovered liquid solvent accumulates in tank 26 and is recycled to cell I.
- the extraction efficiency may be increased by providing two or more serially arranged cells.
- the solventcontaining residue which is discharged from cell I through line 12 may be fed to cell II where it is reextracted (valve 27 closed and valves 28 and 29 open); it is then supplied through line 12 to evaporator 13.
- the collected residue is discharged through purge pipe 15 or partly recycled through line 31 to the main feed pipe (valve 30 is open) when it has a too high content of mineral oil
- the solvent is supplied through line 16 (valve 19 is open and valves 17 and 18 are closed) to cell II where it extracts a portion of the mineral oil; the resulting oily solution is fed through line 32 to cell 1, where its content of mineral oil increases again.
- the dialyzate is then fed to evaporator 21 wherefrom mineral oil is discharged through line 24.
- Dialyzed oils of various viscosities may be also manufactured from the same charge of used oil.
- the feed charge is circulated as above from one cell to another cell while pure solvent is supplied to each cell (the valves 17, 19, 23 and 33 are open while the valve 18 is closed); the resulting dialyzates are fed to the evaporators 21 and 35, one through line 20 and the other through line 34, we obtain in line 36 an oil of greater viscosity than the oil of line 24.
- EXAMPLE I The experiment is carried out with used oil consisting mainly of used motor oil; this oil is subjected to steamstripping at C for removal of the lightest constituents thereof.
- FIG. 3 A mixture of oil and hexane is supplied through pipe 51; the solvent to oil ratio is 2:1 by volume.
- Pump P feeds the ultrafiltration module M I, provided with a membrane having a surface of 500 cm, at a rate of 500 cc of mixture per hour.
- the membrane employed is made of a copolymer of acrylonitrile and sodium methallylsulfonate which has been subjected to a hot water treatment.
- the recirculation pump P arranged on line 53 maintains a flow rate of the mixture oil/hexane along the membrane of 1 meter per second.
- the ultrafiltration temperature is 25C. Two fractions are discharged from the module.
- the fraction discharged from line 52 consists of an impurity concentrate and a hexane fraction.
- Valve V I is so regulated as to maintain a pressure difference of 2 atmospheres between the two compartments of the cell.
- the ultrafiltrate discharged through pipe 54 consists of the treated oil and the solvent fraction which is simultaneously discharged.
- the oil yield is defined as the ratio by weight) of the oil discharged through 54 to the oil charged in 51: it is 80 We have observed that the solvent filters at a higher speed than the oil, so that the ratio by volume of the solvent to the oil is only l.l7 in the mixture discharged through pipe 52.
- EXAMPLE 2 The oil to be treated is the same as in Example 1. 170cc per hour of this oil (pump P and 170 cc per hour of hexane (pump P are supplied and the mixture is fed through pipe 62 to the ultrafiltration module M I which is provided with a membrane of a surface of 430 cm. The membrane is the same as in Example l and there is applied a difference of pressure of 2 atmospheres between the two compartments separated by the membrane.
- the ultrafiltration temperature is 25C.
- a circulation velocity of 1 meter per second is applied by means of a recirculation pump not shown on the drawing.
- 258 cc per hour of mixture is recovered'from pipe 59; after separation of the solvent, 118 cc per hour of treated oil is obtained.
- the mixture with an increased impurity content is recovered from pipe 64 and passed through pump P it is admixed with 170 cc per hour of solvent supplied from pump P and pipe 58 and fed through pipe 63 to a second filtering module M II, which is provided with a membrane having a surface of 70 cm.
- the difference of pressure between the two compartments separated by the membrane is 2 atmospheres, the ultrafiltration temperature 25C and the circulation velocity 1 meter per second.
- 120 cc per hour of mixture is collected in pipe 60; after separation of the solvent, the flow rate of treated oil is 30 cc per hour.
- the oil of higher impurity content is discharged through line 61.
- the number of serially arranged stages is not necessarily limited to 2 and the arrangement of FIG. 4 may be used with any number of stages.
- EXAMPLE 3 We have treated the same oil as in Example 2.
- the pump P feeds the pipe with 140 cc of this oil which is admixed with 200 cc per hour of the recycled material supplied through pipe 66.
- This mixture is supplied through pipe 73 to the ultrafiltration unit M I, which has the same membrane and the same membrane surface as in Example 2..
- the difference between the respective pressures applied on each side of the membrane is 2 atmospheres, the ultrafiltration temperature 25C and the circulation flow rate 1 meter per second.
- 270 cc per hour of mixture is discharged through pipe and, after solvent separation, 125 cc per hour of treated oil.
- the mixture of increased impurity content is discharged through pipe 71 and passed through pump P admixed with 200 cc per hour of solvent supplied from pump P and pipe 67 and passed through pipe 72 to the ultrafiltration unit M II, whose membrane surface is cm; the difference between the respective pressures on each side of the membrane is 2 atmospheres, the ultrafiltration temperature is 25 C and the circulation flow rate l meter per second.
- each stage may consist of several filtration zones serially arranged, each zone being provided with its recirculation device. In this manner, the ultrafiltration rate is higher than that obtained in units arranged in parallel or provided with only one recirculation device since the concentration of impurities increases only stepwise from one unit to another.
- EXAMPLE 4 5 cc of used oil are diluted with 45 cc of n-hexane (the specific viscosity of the mixture is 0.3 at 25C).
- EXAMPLE 5 We have repeated example 4, except that we have used a mixture obtained by diluting cc of used oil with 40 cc of n-hexane (specific viscosity of the mixture: 0.8).
- EXAMPLE 6 We have repeated Example 4, except that we have used a mixture obtained by diluting cc of the used oil with 30 cc of n-hexane (specific viscosity of the mixture: 2.8).
- EXAMPLE 7 We have subjected to ultrafiltration a mixture obtained by diluting 300 cc of used oil with 1700 cc of nhexane.
- the used oil was the same as in Examples 4-6.
- the ultrafiltration apparatus was provided with a device for recirculating liquid to the membrane inlet, this device permitting the circulation of the mixture to be ultra-filtrated at the membrane surface.
- the membrane was the same as in Example 1, and its useful surface was 1 10 cm.
- the velocity of the mixture to be ultra-filtrated at the membrane surface was 1.1 m/sec.
- the differential pressure between the two sides of the membrane was 2 bars.
- Example 7 was repeated, except that the treated mixture consisted of 500 cc of used oil and 1500 cc of nhexane (specific viscosity of the mixture: 1).
- Example 7 is repeated, except that the treated mixture consists of 700 cc of used oil and 1300 cc of n-hexane.
- Example 8 is repeated, except that the liquid to be treated is circulated along the membrane surface at a velocity of 2.3 m/s.
- Example 8 is repeated by providing the ultrafiltration apparatus with a polypropylene grid arranged on the membrane.
- This grid constitutes a turbulence promoter; it consists of two layers of straight wires all arranged in parallel in both layers (diameter of the wire: 1mm; mesh size: 5mm; angle of the wires:
- EXAMPLE 12 The experiment is carried out with used oil mainly consisting of used motor oil made free of its lightest constituents by steam-treatment at C.
- used oil mainly consisting of used motor oil made free of its lightest constituents by steam-treatment at C.
- Used oil feedstock 1,000 Kg Flow rate of the used oil: 192 liters/hour Flow rate of the solvent (hexane): 500 liters/hour Dialysis temperature: 30C
- Viscosity of the dialyzed oil at 37.8Cz30 centistokes Viscosity of the dialyzed oil: at 98.9C:5.25 centistokes ASTM color: 5
- Membrane efficiency (weight of oil/hour/m of the membrane): 9.2 kg/hour/m.
- EXAMPLE 13 The used oil of example 12 is employed again, but two cells are used and their dialyzates are separately concentrated.
- the feed rates are the same as above, the surface of the polyisoprene membrane being 40 m.
- Viscosity at 37.8C 50.7 cst
- Viscosity at 98.9C 6.8 cst
- EXAMPLE 14 25 The same used oil as in Examples No. 12 and 13 is treated with an ultra-filtration membrane of cellulose ester whose pores have a diameter of about 100 Angstroms; the temperature and feed rates are unchanged.
- a process for regenerating a used lubricating oil containing at least one soluble metal compound of lead, calcium, barium, magnesium, zinc or aluminum which comprises circulating said oil along a first face of a membrane permeable to hydrocarbons and collecting a purified oil on the second face of the membrane, said membrane having a cut zone in the range of from 5,000 to 300,000.
- the soluble metal compounds comprise at least one of calcium, barium, magnesium, zinc or aluminum salicylates, sulfonates, phenates, phosphonates or thiophosphonates or the decomposition products thereof.
- the ultrafiltration membrane comprises a material selected from the group consisting of cellulose, cellulosic esters, polytetrafluorethylene, polychlorotrifluorethylene, crosslinked or vulcanized organopolysiloxanes, polypentaerythritol, sulfonated polystyrene, quaternary ammonium salts of dialkylamino polystyrene, the ionically cross-linked complex polyelectrolytes obtained from a polymer containing sulfonic groups and a polymer containing quaternary ammonium groups, sulfonated polyarylether sulfones, polyethylene, polypropyl- 1 l ene, polymers of 2-chloro butadiene, butadienestyrene copolymers, vulcanized natural rubber, isopreneisobutene copolymers and copolymers of acrylonitrile with ionic monomers
- hydrocarbon is propane, butane, pentane or hexane.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Lubricants (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR7313360A FR2225509B1 (pt) | 1973-04-12 | 1973-04-12 | |
FR7328417A FR2239519B2 (pt) | 1973-04-12 | 1973-08-02 | |
FR7339811A FR2250819B2 (pt) | 1973-04-12 | 1973-11-08 |
Publications (1)
Publication Number | Publication Date |
---|---|
US3919075A true US3919075A (en) | 1975-11-11 |
Family
ID=27250094
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US459413A Expired - Lifetime US3919075A (en) | 1973-04-12 | 1974-04-09 | Process for regenerating used lubricating oils |
Country Status (12)
Country | Link |
---|---|
US (1) | US3919075A (pt) |
JP (1) | JPS514464A (pt) |
BE (1) | BE812872A (pt) |
BR (1) | BR7402832D0 (pt) |
CA (1) | CA1054068A (pt) |
CH (1) | CH590915A5 (pt) |
DE (1) | DE2417452A1 (pt) |
ES (1) | ES425285A1 (pt) |
FR (3) | FR2225509B1 (pt) |
GB (1) | GB1458314A (pt) |
IT (1) | IT1007836B (pt) |
NL (1) | NL7405037A (pt) |
Cited By (35)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4045330A (en) * | 1975-06-04 | 1977-08-30 | Institut Francais Du Petrole | Process for regenerating lubricating oils |
JPS5521443A (en) * | 1978-08-03 | 1980-02-15 | Kanagawaken | Purification of waste oil and waste grease |
US4201664A (en) * | 1975-09-29 | 1980-05-06 | The Continental Group, Inc. | Ultrafiltration or reverse osmosis treatment of emulsified oil metal working coolants |
US4251360A (en) * | 1976-09-18 | 1981-02-17 | Goldie David J | Method and apparatus for the detection of a specific binding protein |
JPS5670095A (en) * | 1979-11-12 | 1981-06-11 | Kanagawaken | Purifying apparatus for waste oil and grease |
US4510047A (en) * | 1983-12-14 | 1985-04-09 | Exxon Research And Engineering Co. | Selective extraction solvent recovery using regenerated cellulose membrane under reverse osmosis conditions |
US4532029A (en) * | 1984-04-27 | 1985-07-30 | Exxon Research And Engineering Co. | Aromatic solvent upgrading using membranes |
US4571444A (en) * | 1984-04-27 | 1986-02-18 | Exxon Research And Engineering Co. | Process for separating alkylaromatics from aromatic solvents and the separation of the alkylaromatic isomers using membranes |
US4606903A (en) * | 1984-04-27 | 1986-08-19 | Exxon Research And Engineering Co. | Membrane separation of uncoverted carbon fiber precursors from flux solvent and/or anti-solvent |
EP0220753A1 (en) * | 1985-08-30 | 1987-05-06 | Shell Internationale Researchmaatschappij B.V. | Process for the separation of solvents from hydrocarbons dissolved in said solvents |
US4750990A (en) * | 1984-10-15 | 1988-06-14 | Uop Inc. | Membrane separation of hydrocarbons using cycloparaffinic solvents |
US4759850A (en) * | 1987-01-12 | 1988-07-26 | Energy, Mines And Resources Canada | Membrane process for separating methanol from methanol/hydrocarbon solutions |
US4797200A (en) * | 1984-05-04 | 1989-01-10 | Exxon Research And Engineering Company | Upgrading heavy oils by solvent dissolution and ultrafiltration |
US5326385A (en) * | 1992-02-24 | 1994-07-05 | Shell Oil Company | Method of treating sour liquefied petroleum gas |
EP0773058A1 (en) * | 1995-11-10 | 1997-05-14 | Kabushiki Kaisha Toyota Chuo Kenkyusho | Filtration membrane for oleophilic organic liquids, method for producing it and method for filtering oleophilic organic liquids |
US5849179A (en) * | 1992-10-13 | 1998-12-15 | Baxter International Inc. | Automatic apparatus for obtaining equilibration samples of dialysate |
EP0951933A2 (en) * | 1998-04-24 | 1999-10-27 | Mitsui Chemicals, Inc. | Method and apparatus for membrane filtration of liquids |
US6013174A (en) * | 1996-02-21 | 2000-01-11 | U.S. Filter Recovery Services (Mid-Atlantic, Inc.) | Process to remove ash-forming contaminants from used oil |
US6024880A (en) * | 1996-02-26 | 2000-02-15 | Ciora, Jr.; Richard J. | Refining of used oils using membrane- and adsorption-based processes |
WO2000037590A1 (en) * | 1998-12-18 | 2000-06-29 | Ron Waters | Process for the production of improved diesel fuels using reclaimed hydraulic oil |
US6090273A (en) * | 1997-12-03 | 2000-07-18 | U.S. Filter Recovery Services (Mid-Altantic, Inc.) | Process to remove ash-forming contaminants from wet used oil |
US6117327A (en) * | 1997-08-22 | 2000-09-12 | Media And Process Technology Inc. | Deashing and demetallization of used oil using a membrane process |
US20040029721A1 (en) * | 2000-10-08 | 2004-02-12 | Jintang Wang | Catalytic activity accelerant used in petroleum hydrogenation |
US20080227674A1 (en) * | 2007-03-15 | 2008-09-18 | Rohrbach Ronald P | Method for regenerating lube oil dispersant |
US20090062590A1 (en) * | 2007-08-28 | 2009-03-05 | Nadler Kirk C | Process for separating a heavy oil feedstream into improved products |
US20090057226A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Reduction of conradson carbon residue and average boiling points utilizing high pressure ultrafiltration |
US20090057192A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Deasphalter unit throughput increase via resid membrane feed preparation |
US20090057203A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Enhancement of saturates content in heavy hydrocarbons utilizing ultrafiltration |
US20090057196A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Production of an enhanced resid coker feed using ultrafiltration |
US20090057200A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Production of an upgraded stream from steam cracker tar by ultrafiltration |
CN101070507B (zh) * | 2007-06-05 | 2010-05-19 | 天津新膜科技有限责任公司 | 一种废润滑油的再生方法及设备 |
US7815790B2 (en) | 2007-08-28 | 2010-10-19 | Exxonmobil Research And Engineering Company | Upgrade of visbroken residua products by ultrafiltration |
US20130305592A1 (en) * | 2011-02-01 | 2013-11-21 | Ohana Investments Works LLC | Methods and apparatus for controlling moisture in plant oils and liquid biofuels |
CN111229773A (zh) * | 2019-05-05 | 2020-06-05 | 云南新昊环保科技有限公司 | 一种油沾污物处置系统及工艺 |
US20220401895A1 (en) * | 2019-09-25 | 2022-12-22 | Shell Oil Company | Process for reducing injector deposits |
Families Citing this family (8)
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CA1263845A (en) * | 1985-08-28 | 1989-12-12 | Oleh Kutowy | Method of removing substances from fossil derived, hydrocarbon liquids |
IT1191733B (it) * | 1986-04-15 | 1988-03-23 | Ausimont Spa | Pompa per vuoto provvista di filtro per l'olio lubrificante |
IL79985A0 (en) * | 1985-09-13 | 1986-12-31 | Ausimont Spa | Purification of oils containing solid matter in suspension |
JP2613855B2 (ja) * | 1987-03-30 | 1997-05-28 | 株式会社 化研 | 分離膜を用いた疎水性物質分離装置 |
US4850498A (en) * | 1988-03-18 | 1989-07-25 | Separation Dynamics, Inc. | Fluid decontamination system |
DE102007044524A1 (de) * | 2007-09-18 | 2009-03-19 | Man Diesel Se | Einrichtung und Verfahren zum Reinigen von Schmiermitteln sowie Schmiermittelkreislauf |
US20170121632A1 (en) * | 2014-06-11 | 2017-05-04 | Fluitec International, Llc | Systems and methods for varnish abatement and removal from in-service fluids and components |
US20230159852A1 (en) * | 2020-04-20 | 2023-05-25 | ExxonMobil Technology and Engineering Company | Membrane Separation of Used Oil and Compositions Generated |
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1973
- 1973-04-12 FR FR7313360A patent/FR2225509B1/fr not_active Expired
- 1973-08-02 FR FR7328417A patent/FR2239519B2/fr not_active Expired
- 1973-11-08 FR FR7339811A patent/FR2250819B2/fr not_active Expired
-
1974
- 1974-03-27 BE BE1005831A patent/BE812872A/xx unknown
- 1974-04-01 CH CH448374A patent/CH590915A5/xx not_active IP Right Cessation
- 1974-04-09 US US459413A patent/US3919075A/en not_active Expired - Lifetime
- 1974-04-09 BR BR2832/74A patent/BR7402832D0/pt unknown
- 1974-04-10 IT IT21204/74A patent/IT1007836B/it active
- 1974-04-10 JP JP49040882A patent/JPS514464A/ja active Pending
- 1974-04-10 CA CA198,161A patent/CA1054068A/fr not_active Expired
- 1974-04-10 DE DE2417452A patent/DE2417452A1/de not_active Withdrawn
- 1974-04-11 GB GB1628774A patent/GB1458314A/en not_active Expired
- 1974-04-11 ES ES425285A patent/ES425285A1/es not_active Expired
- 1974-04-11 NL NL7405037A patent/NL7405037A/xx not_active Application Discontinuation
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US3821108A (en) * | 1972-05-23 | 1974-06-28 | S Manjikian | Reverse osmosis or ultrafiltration module |
US3785968A (en) * | 1972-07-12 | 1974-01-15 | Mobil Oil Corp | Sorbent and process for heavy metal removal from motor fuel |
Cited By (47)
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US4045330A (en) * | 1975-06-04 | 1977-08-30 | Institut Francais Du Petrole | Process for regenerating lubricating oils |
US4201664A (en) * | 1975-09-29 | 1980-05-06 | The Continental Group, Inc. | Ultrafiltration or reverse osmosis treatment of emulsified oil metal working coolants |
US4251360A (en) * | 1976-09-18 | 1981-02-17 | Goldie David J | Method and apparatus for the detection of a specific binding protein |
JPS5521443A (en) * | 1978-08-03 | 1980-02-15 | Kanagawaken | Purification of waste oil and waste grease |
JPS5670095A (en) * | 1979-11-12 | 1981-06-11 | Kanagawaken | Purifying apparatus for waste oil and grease |
US4510047A (en) * | 1983-12-14 | 1985-04-09 | Exxon Research And Engineering Co. | Selective extraction solvent recovery using regenerated cellulose membrane under reverse osmosis conditions |
US4532029A (en) * | 1984-04-27 | 1985-07-30 | Exxon Research And Engineering Co. | Aromatic solvent upgrading using membranes |
US4571444A (en) * | 1984-04-27 | 1986-02-18 | Exxon Research And Engineering Co. | Process for separating alkylaromatics from aromatic solvents and the separation of the alkylaromatic isomers using membranes |
US4606903A (en) * | 1984-04-27 | 1986-08-19 | Exxon Research And Engineering Co. | Membrane separation of uncoverted carbon fiber precursors from flux solvent and/or anti-solvent |
US4797200A (en) * | 1984-05-04 | 1989-01-10 | Exxon Research And Engineering Company | Upgrading heavy oils by solvent dissolution and ultrafiltration |
US4750990A (en) * | 1984-10-15 | 1988-06-14 | Uop Inc. | Membrane separation of hydrocarbons using cycloparaffinic solvents |
US4748288A (en) * | 1985-08-30 | 1988-05-31 | Shell Oil Company | Process for the separation of solvents from hydrocarbons dissolved in the solvents |
EP0220753A1 (en) * | 1985-08-30 | 1987-05-06 | Shell Internationale Researchmaatschappij B.V. | Process for the separation of solvents from hydrocarbons dissolved in said solvents |
US4759850A (en) * | 1987-01-12 | 1988-07-26 | Energy, Mines And Resources Canada | Membrane process for separating methanol from methanol/hydrocarbon solutions |
US5326385A (en) * | 1992-02-24 | 1994-07-05 | Shell Oil Company | Method of treating sour liquefied petroleum gas |
US5849179A (en) * | 1992-10-13 | 1998-12-15 | Baxter International Inc. | Automatic apparatus for obtaining equilibration samples of dialysate |
EP0773058A1 (en) * | 1995-11-10 | 1997-05-14 | Kabushiki Kaisha Toyota Chuo Kenkyusho | Filtration membrane for oleophilic organic liquids, method for producing it and method for filtering oleophilic organic liquids |
US5932104A (en) * | 1995-11-10 | 1999-08-03 | Kabushiki Kaisha Toyota Chuo Kenkyusho | Filtration membrane for oleophilic organic liquids, method for producing it, and method for filtering oleophilic organic liquids |
US6013174A (en) * | 1996-02-21 | 2000-01-11 | U.S. Filter Recovery Services (Mid-Atlantic, Inc.) | Process to remove ash-forming contaminants from used oil |
US6024880A (en) * | 1996-02-26 | 2000-02-15 | Ciora, Jr.; Richard J. | Refining of used oils using membrane- and adsorption-based processes |
US6117327A (en) * | 1997-08-22 | 2000-09-12 | Media And Process Technology Inc. | Deashing and demetallization of used oil using a membrane process |
US6090273A (en) * | 1997-12-03 | 2000-07-18 | U.S. Filter Recovery Services (Mid-Altantic, Inc.) | Process to remove ash-forming contaminants from wet used oil |
EP0951933A3 (en) * | 1998-04-24 | 2000-08-02 | Mitsui Chemicals, Inc. | Method and apparatus for membrane filtration of liquids |
EP0951933A2 (en) * | 1998-04-24 | 1999-10-27 | Mitsui Chemicals, Inc. | Method and apparatus for membrane filtration of liquids |
WO2000037590A1 (en) * | 1998-12-18 | 2000-06-29 | Ron Waters | Process for the production of improved diesel fuels using reclaimed hydraulic oil |
US20040029721A1 (en) * | 2000-10-08 | 2004-02-12 | Jintang Wang | Catalytic activity accelerant used in petroleum hydrogenation |
US7022639B2 (en) * | 2000-10-08 | 2006-04-04 | Nanjing University Of Technology | Catalytic activity accelerant used in petroleum hydrogenation |
US20080227674A1 (en) * | 2007-03-15 | 2008-09-18 | Rohrbach Ronald P | Method for regenerating lube oil dispersant |
CN101070507B (zh) * | 2007-06-05 | 2010-05-19 | 天津新膜科技有限责任公司 | 一种废润滑油的再生方法及设备 |
US20090062590A1 (en) * | 2007-08-28 | 2009-03-05 | Nadler Kirk C | Process for separating a heavy oil feedstream into improved products |
US7871510B2 (en) | 2007-08-28 | 2011-01-18 | Exxonmobil Research & Engineering Co. | Production of an enhanced resid coker feed using ultrafiltration |
US20090057203A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Enhancement of saturates content in heavy hydrocarbons utilizing ultrafiltration |
US20090057196A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Production of an enhanced resid coker feed using ultrafiltration |
US20090057200A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Production of an upgraded stream from steam cracker tar by ultrafiltration |
US20090057226A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Reduction of conradson carbon residue and average boiling points utilizing high pressure ultrafiltration |
US7736493B2 (en) | 2007-08-28 | 2010-06-15 | Exxonmobil Research And Engineering Company | Deasphalter unit throughput increase via resid membrane feed preparation |
US7815790B2 (en) | 2007-08-28 | 2010-10-19 | Exxonmobil Research And Engineering Company | Upgrade of visbroken residua products by ultrafiltration |
US7867379B2 (en) | 2007-08-28 | 2011-01-11 | Exxonmobil Research And Engineering Company | Production of an upgraded stream from steam cracker tar by ultrafiltration |
US20090057192A1 (en) * | 2007-08-28 | 2009-03-05 | Leta Daniel P | Deasphalter unit throughput increase via resid membrane feed preparation |
US7897828B2 (en) | 2007-08-28 | 2011-03-01 | Exxonmobile Research And Engineering Company | Process for separating a heavy oil feedstream into improved products |
US8177965B2 (en) | 2007-08-28 | 2012-05-15 | Exxonmobil Research And Engineering Company | Enhancement of saturates content in heavy hydrocarbons utilizing ultrafiltration |
US8864996B2 (en) | 2007-08-28 | 2014-10-21 | Exxonmobil Research And Engineering Company | Reduction of conradson carbon residue and average boiling points utilizing high pressure ultrafiltration |
US20130305592A1 (en) * | 2011-02-01 | 2013-11-21 | Ohana Investments Works LLC | Methods and apparatus for controlling moisture in plant oils and liquid biofuels |
US9028697B2 (en) * | 2011-02-01 | 2015-05-12 | Masatoshi Matsumura | Methods and apparatus for controlling moisture in plant oils and liquid biofuels |
CN111229773A (zh) * | 2019-05-05 | 2020-06-05 | 云南新昊环保科技有限公司 | 一种油沾污物处置系统及工艺 |
US20220401895A1 (en) * | 2019-09-25 | 2022-12-22 | Shell Oil Company | Process for reducing injector deposits |
US12023632B2 (en) * | 2019-09-25 | 2024-07-02 | Shell Usa, Inc. | Process for reducing injector deposits |
Also Published As
Publication number | Publication date |
---|---|
JPS514464A (en) | 1976-01-14 |
BE812872A (fr) | 1974-09-27 |
FR2225509A1 (pt) | 1974-11-08 |
FR2239519A2 (pt) | 1975-02-28 |
DE2417452A1 (de) | 1974-10-31 |
IT1007836B (it) | 1976-10-30 |
GB1458314A (en) | 1976-12-15 |
CA1054068A (fr) | 1979-05-08 |
FR2250819A2 (pt) | 1975-06-06 |
ES425285A1 (es) | 1976-11-01 |
CH590915A5 (pt) | 1977-08-31 |
BR7402832D0 (pt) | 1974-11-19 |
FR2239519B2 (pt) | 1978-07-07 |
FR2225509B1 (pt) | 1976-05-21 |
NL7405037A (pt) | 1974-10-15 |
FR2250819B2 (pt) | 1978-08-11 |
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