EP1141181B1 - Verfahren zur wiederaufarbeitung von altölen - Google Patents

Verfahren zur wiederaufarbeitung von altölen Download PDF

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Publication number
EP1141181B1
EP1141181B1 EP99971836A EP99971836A EP1141181B1 EP 1141181 B1 EP1141181 B1 EP 1141181B1 EP 99971836 A EP99971836 A EP 99971836A EP 99971836 A EP99971836 A EP 99971836A EP 1141181 B1 EP1141181 B1 EP 1141181B1
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EP
European Patent Office
Prior art keywords
oil
oils
extraction
process according
waste
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP99971836A
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German (de)
English (en)
French (fr)
Other versions
EP1141181A1 (de
Inventor
Joachim Pöhler
Michael Mödler
Detlev Bruhnke
Holger Hindenberg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mineralol-Raffinerie Dollbergen GmbH
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Mineralol-Raffinerie Dollbergen GmbH
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Classifications

    • 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
    • C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
    • C10M175/0033—Working-up used lubricants to recover useful products ; Cleaning by thermal processes using distillation processes; devices therefor
    • 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
    • C10M175/005—Working-up used lubricants to recover useful products ; Cleaning using extraction processes; apparatus therefor

Definitions

  • the present invention relates to a process for the reprocessing of waste oils by distillation and extraction methods obtainable by the method Base oils and their use.
  • waste products plays an increasingly important role today, in particular the elimination of environmental pollutants, such as halogen-containing hydrocarbons, Aromatics and the like. These represent acute and latent threats to human health and other environmental goods, such as water, soil, air, Plants and animals dar.
  • environmental pollutants such as halogen-containing hydrocarbons, Aromatics and the like.
  • a recovery is generally possible in two ways: the product can be recycled, i.e. reprocessed, or it can be energetically used as a fuel become. In doing so, certain criteria must be met, those of the product and the respective pollutant load.
  • waste oils are subject to the so-called waste oil ordinance (AltölV) of 27.10.1987, which includes the processing, collection, labeling, collection and disposal of used oil regulates.
  • Waste oils to be reprocessed may usually have a maximum Value of 20 ppm polychlorinated biphenyls (PCB) and total halogen content of 0.2%. Exceptions are, however, depending on the selected Work-up procedure quite possible.
  • organic extractants are mentioned in particular: ethanol, diacetone alcohol, Ethylene glycol mono (lower alkyl) ether, diethylene glycol, diethylene glycol mono (lower alkyl) ether, o-chlorophenol, furfural, acetone, formic acid, 4-butyrolactone, lower alkyl ester of lower mono- and dicarboxylic acids, dimethylformamide, 2-pyrrolidone and N- (lower alkyl) -2-pyrrolidones, epichlorohydrin, dioxane, morpholine, lower alkyl and Amino (lower alkyl) morpholines, benzonitrile and di (lower alkyl) sulphoxides and - phosphonates.
  • Preferred extractants are ethylene glycol monomethyl ether, dimethylformamide or N-methyl-2-pyrrolidone.
  • the distillation should in this case carried out without a fractionating column or similar device become.
  • disturbing components can occur in an upstream step be removed by a diluent in the form of an organic solvent, in addition, heating the waste oil with an aqueous, strongly alkaline solution can precede.
  • this method does not always give satisfactory results in terms of quality of reclaimed oils, which after working up after show excessive exposure to pollutants.
  • the present invention is therefore based on the object described at the outset Further develop the process so that the base oils obtained as low as possible Exposure to pollutants, such as aromatics and especially polycyclic, aromatic Hydrocarbons possess. Furthermore, the procedure and the possible Starting materials can be flexibly designed. At the same time, in the reprocessing process achieved good yields despite high quality of the base oils to be obtained become.
  • waste oil in the present invention, any used semi-liquid or liquid substance which is wholly or partly made from mineral oil or synthetic oils, as well as any oily residue, as well as water-oil mixtures or similar.
  • waste oils suitable for lubricating oils, in particular used combustion engine oils and gear oils, mineral engine, turbine and hydraulic oils, including their synthetic and semi-synthetic components based on mineral hydrocarbons.
  • a first step A water fractions and fractions of low-boiling components, such as gasoline or solvent fractions, are distilled off. This is preferably done at atmospheric pressure or under a slight vacuum (up to about 600 mbar) at a temperature of about 140 to 150 ° C.
  • a concentrated, aqueous potassium hydroxide solution used.
  • the potassium hydroxide solution is highly concentrated, in particular about 5 to 50% pure.
  • the concentration of potassium hydroxide is obtained as a very homogeneously distributed, very concentrated and thus very effective reagent for binding acidic constituents in the waste oil used, including extensive demetallization of the used oils.
  • the use of potassium hydroxide solution by the specific "soaps" that form results in a particularly free-flowing and homogeneous distillation residue in the thin-film evaporation described below in step C ).
  • other alkalis such as the sodium compounds described in US Pat. No. 4,021,333, tend to precipitate and agglomerate, severely disrupting the further course of the process.
  • step B After the removal of water and solvents contained fuel oil and diesel fractions are removed with a boiling cut of about 170 to 385 ° C in step B ) by distillation in vacuo from the waste oil.
  • the residue obtained in this case is subjected to a gentle thin-layer evaporation in a high vacuum after step C ), in which the actual lubricating oil fraction is obtained. To achieve desired viscosity layers, these can then be fractionated again.
  • step D The residue from the thin-film evaporation (bottoms) still contains highly viscous and very valuable lubricating oil components, which in step D ) by gentle distillation, such as a downstream 2nd thin film evaporation - at correspondingly higher distillation temperatures or lower pressure - win and also optionally fractionated.
  • step D is not always necessary, but improves the yield of base oils and thus the economy of the process when used.
  • the lubricating oil fractions (steps C ) and D )) produced from the previously described thin-layer evaporation and optionally fractionation steps are then extracted with N-methyl-2-pyrrolidone (hereinafter referred to as NMP) to give very high quality base oils for lubricant production.
  • NMP N-methyl-2-pyrrolidone
  • NMF N-formylmorpholine
  • the lubricating oils or fractions from step C ) and D ) can be further processed individually or partially combined and then processed further.
  • the extraction can preferably be carried out in a column (sieve bottom, packing) become.
  • the countercurrent process is used.
  • the use of Packings in this case has a higher robustness in terms of process management and Advantages regarding the possible throughputs (volume flows) and the extractant distribution from NMP or NMF in the oil.
  • the NMP / oil or NMF / oil ratio Depending on the requirements of the qualities of the base oils to be produced 0.5 and 2.0 (v / v).
  • the extraction can be in the temperature range of about 20 to 90 ° C. carry out.
  • the procedure is possible with application of a temperature gradient in the column.
  • the temperatures are about 50 to 90 ° C at the top of the column (raffinate) and about 10 to 50 ° C at the bottom of the column (Extract outlet).
  • the advantage here is the higher selectivity of the extractant (For example, NMP) at lower temperatures, so that it is to return in the extractant dissolved base oil components comes while the unwanted to be removed Components remain solved. As a result, finally, a significant increase in yield be achieved on refined base oil.
  • the NMP and / or NMF present in the raffinate phase and the extract is recovered in the usual way by subsequent distillation processes and recycled to the process. Due to the concentration of the potassium hydroxide solution carried out in step A ), an alkalinity reserve is created in the oil feed for extraction, which prevents the otherwise sometimes irreversible formation of acidic reaction products of the extractant.
  • the invention also provides the base oils obtainable by the process described above. Depending on the viscosity of the distillate fractions produced after step C ) and step D ), base oil grades with color values according to ASTM between 0.5 and 3.0 are obtained.
  • the neutralization number (abbreviated as NZ) as a measure of residual acid constituents in the base oil is between 0.01 and 0.03 mg KOH / g.
  • the aromatic portion (abbreviated as CA) in Base oil lowered significantly.
  • polycyclic aromatic hydrocarbons (PAK) almost quantitatively removed (sum of PAK to Grimmer - sum of fixed number of individual substances ⁇ 1 mg / kg, benzo (a) pyrene ⁇ 0.1 mg / kg).
  • PAK polycyclic aromatic hydrocarbons
  • benzo (a) pyrene ⁇ 0.1 mg / kg.
  • lubricating oils especially in the Combustion processes in car / truck engines, formed and play because of their health-endangering Properties, i. the carcinogenic effect, a big role.
  • benzo (a) pyrene the lead compound of PAHs applies and was included in the Hazardous Substances Ordinance (GefStoffV).
  • waste oils with a content of vegetable oils so-called readily biodegradable oils, to be reprocessed. It can be up to about 5% of such oils may be contained in the waste oil, without causing an impairment of the Base oil quality comes.
  • the base oils obtained are versatile, for example as Starting products for lubricants or for products in the petrochemical sector, there due to the excellent quality within the scope of the invention, no restrictions available.
  • the advantages associated with the invention are complex.
  • the process according to the invention is far superior to the conventional processes of bleaching earth treatment, chemical treatment or hydrogenation as well as to the known prior art distillation processes.
  • the inventive method can be carried out without waste, since the extractant NMP or NMF can be recovered and reused, and the extract is used as fuel oil or as Edelöläquivalent.
  • oil-contaminated bleaching earth remains behind in the bleaching earth process, and the exhausted catalysts have to be disposed of during the hydrogenation and the reaction gases (H 2 S, HCl) must be rendered harmless.
  • the energy balance according to the method of the invention is very favorable. It can almost be worked without pressure. Only to overcome the internal fluid friction and the pipe resistances during transport are pressures in the range of max. 5 bar necessary. The maximum temperature range is 230 ° C, around the recovery of the extractant for its reuse. In other procedures Refining effects occur only at temperatures between 290 and 300 ° C (bleaching earth process), or additionally high pressures must be used (hydrogenation: Temperatures up to 350 ° C and operating pressures between 30 and 200 bar).
  • the process according to the invention also offers advantages in terms of occupational safety, since the extractants NMP and NMF are classified as non-toxic (classification as Xi: irritant according to GefStoffV, with hazard class A III, WGK 1).
  • Xi irritant according to GefStoffV, with hazard class A III, WGK 1).
  • hydrogen as a highly flammable gas requires high safety requirements.
  • H 2 S is formed as a highly toxic gas and hydrogen chloride as a very corrosive gas.
  • the base oils possess extraordinary good color values, a low neutralization number (NZ) and a high viscosity index (VI).
  • NZ low neutralization number
  • VI high viscosity index
  • PAK polycyclic aromatic hydrocarbons
  • PCB polychlorinated biphenyls
  • PCBs polychlorinated biphenyls
  • the PCB content in the base oils obtained according to the invention is below the limit of quantification of the analytical method in this case as well, the strict national and European regulations concerning the reconditioning of Used oils are respected.
  • levels of vegetable, biological easily degradable oils up to about 5% are present in the waste oil to be reprocessed, without any impairment of the base oil quality.
  • This excellent quality of the base oil according to the invention can be achieved by the methods can not be achieved from the prior art.
  • the bleaching earth process worse color values, with an unpleasant smell, a distinct higher NZ, a lower VI, a significantly worse aging behavior and a achieved insufficient removal of polycyclic aromatic hydrocarbons.
  • Hydrogenation processes provide better yields with lower viscosity index (VI) and otherwise comparable values, but a quantitative removal of polycyclic aromatic hydrocarbons is at best under extreme hydrogenation conditions and use of noble metal catalysts, as in the practice of Oil base oil production are not common, possible.
  • the currently known Process for the treatment of waste oils to base oils including the known distillation and extraction methods, none is yet capable of polycyclic to remove aromatic hydrocarbons to the extent as described with the here Procedure is possible.
  • the resulting dry oil is freed in a subsequent Mittelöldestillation at a vacuum of 60 mbar and a temperature in the bottom of the column of 260 ° C from the middle distillate section - boiling point 380 ° C.
  • the bottom product of the middle oil distillation column passes into a thin-layer evaporation, in which, at a vacuum of 3 mbar and a heat transfer oil temperature of 384 ° C, the gentle separation of feeds in a Schmieröldestillatgemisch and a bottom product.
  • the lubricating oil distillate mixture is separated in a subsequent fractionation into two boiling sections at the process conditions 80 mbar and 280 ° C distillation temperature.
  • the oil used (feed) is driven to the solvent used NMP in countercurrent.
  • the undesirable constituents, inter alia, the polycyclic aromatic hydrocarbons from the feed used with a simultaneous improvement in the quality of the used lubricating oil distillate solve.
  • the raffinate-NMP mixture exiting at the top of the column, according to the alternating procedures, is subsequently fed to NMP solvent recovery in order to reuse this solvent in the process.
  • the obtained lubricating oil distillate or lubricating oil raffinate of the respectively used viscosity stage V40 either 20 mm 2 / s or 36 mm 2 / s is then used for the formulation of new lubricating oils, such as engine oils, gear oils, hydraulic oils and other applications.
  • the resulting extract also passes through a solvent recovery plant, around the extract solvent NMP from the extract for a new use to win back.
  • the resulting extract can be used as fuel oil or as Bankölverrough used in heating oil mixtures.
  • the bottom product from the thin-film evaporation is subjected to a further distillation in a subsequent further thin-film evaporation step at a higher vacuum - 0.1 mbar and a temperature of 410 ° C.
  • a separation into a highly viscous lubricating oil fraction with a viscosity of 253 mm 2 / s and a remaining residue, which is used as heating oil Zumischkomponente eg as a reduction oil in fuel oil mixtures for steel production is used.
  • the highly viscous lubricating oil distillate obtained is likewise subjected to one of the subsequent selective refining with NMP (extraction), in which case the reaction conditions in the column are operated isothermally at 90 ° C.
  • the obtained properties of the recovered base oil are as follows: raffinate temperature [° C] 80 isothermal Recycling oil phase from extract Yes NMP / oil ratio [V / v] 1.5 yield [Wt .-%] 84 Color ASTM 0.5 Neutralization number [mg KOH / g] 0.01 Viscosity 40 ° C [mm 2 / s] 20.93 Viscosity 100 ° C [mm 2 / s] 4.23 viscosity Index 106 Aromatic portion CA (IR) [%] 3.5 PAK, total n.
  • Grimmer [Mg / kg] 0.257 Benzo (a) pyrene [Mg / kg] 0.0034
  • Example 2 The procedure was as in Example 1, wherein the selected extraction conditions and the resulting properties of the obtained base oils are shown in Table 2 below: raffinate temperature [° C] 80 isothermal Recycling oil phase from extract Yes NMP / oil ratio [V / v] 1.8 yield [Wt .-%] 85 Color ASTM L 1.5 Neutralization number [mg KOH / g] ⁇ 0.03 Viscosity 40 ° C [mm 2 / s] 36.05 Viscosity 100 ° C [mm 2 / s] 6.07 viscosity Index 114 Aromatic portion CA (IR) [%] 3.9 PAK, Sum n. Grimmer [Mg / kg] ⁇ 1 mg Benzo (a) pyrene [Mg / kg]

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Lubricants (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Fats And Perfumes (AREA)
  • Detergent Compositions (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Treatments For Attaching Organic Compounds To Fibrous Goods (AREA)
EP99971836A 1998-11-11 1999-11-11 Verfahren zur wiederaufarbeitung von altölen Expired - Lifetime EP1141181B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19852007 1998-11-11
DE19852007A DE19852007C2 (de) 1998-11-11 1998-11-11 Verfahren zur Wiederaufarbeitung von Altölen
PCT/EP1999/008667 WO2000027957A1 (de) 1998-11-11 1999-11-11 Verfahren zur wiederaufarbeitung von altölen, die mit dem verfahren erhältlichen grundöle und deren verwendung

Publications (2)

Publication Number Publication Date
EP1141181A1 EP1141181A1 (de) 2001-10-10
EP1141181B1 true EP1141181B1 (de) 2004-02-11

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US (1) US6712954B1 (enExample)
EP (1) EP1141181B1 (enExample)
JP (1) JP4246397B2 (enExample)
CN (1) CN1185327C (enExample)
AT (1) ATE259405T1 (enExample)
AU (1) AU1161900A (enExample)
BR (1) BR9916606B1 (enExample)
CA (1) CA2351606C (enExample)
CZ (1) CZ298571B6 (enExample)
DE (2) DE19852007C2 (enExample)
DK (1) DK1141181T3 (enExample)
ES (1) ES2222051T3 (enExample)
HU (1) HU226925B1 (enExample)
PL (1) PL191398B1 (enExample)
PT (1) PT1141181E (enExample)
RU (1) RU2217484C2 (enExample)
SK (1) SK285213B6 (enExample)
UA (1) UA69426C2 (enExample)
WO (1) WO2000027957A1 (enExample)

Families Citing this family (30)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2396206A1 (en) * 2002-07-30 2004-01-30 Nouredine Fakhri Process for the treatment of waste oils
JP2004210945A (ja) * 2002-12-27 2004-07-29 Toshiba Corp 芳香族ハロゲン化合物の分離方法
US8366912B1 (en) 2005-03-08 2013-02-05 Ari Technologies, Llc Method for producing base lubricating oil from waste oil
US7792815B2 (en) * 2006-03-06 2010-09-07 Veveo, Inc. Methods and systems for selecting and presenting content based on context sensitive user preferences
ES2346778T3 (es) * 2006-04-18 2010-10-20 Horst Fuhse Procedimiento para el tratamiento de aceites usados para dar aceites lubricantes con un alto indice de viscosidad.
ES2303447B1 (es) * 2006-07-27 2009-06-12 Juan Flores Velazquez Procedimiento de regeneracion de aceites minerales usados y residuos asfalticos por extraccion liquido / liquido y producto asi obtenido.
US20110139106A1 (en) * 2007-08-09 2011-06-16 21St Century R & D, Llc Modification of fats and oils for fuel and lubricating applications
US20090038692A1 (en) * 2007-08-09 2009-02-12 21St Century R & D, Llc Modification of vegetable oils for fuel applications
DE102007051373B4 (de) * 2007-10-26 2010-11-11 Hii-Gmbh - Industrianlagen - Bau Und Beratung Verfahren und Vorrichtung zur Gewinnung von Diesel oder Heizöl aus kohlenwasserstoffhaltigen Rückständen
WO2011074623A1 (ja) * 2009-12-18 2011-06-23 Kato Eisaku 再生油の製造方法
CN102373108B (zh) * 2010-08-18 2013-09-25 北京金隅红树林环保技术有限责任公司 一种废润滑油再生基础油的工艺方法
CN102604732A (zh) * 2012-02-14 2012-07-25 安徽国孚润滑油工业有限公司 再生基础油n-甲基吡咯烷酮静态混合旋流分离抽提工艺
WO2014135966A1 (en) 2013-03-07 2014-09-12 Verolube, Inc. Method and apparatus for recovering synthetic oils from composite oil streams
US9394495B1 (en) 2013-09-18 2016-07-19 Thomas George Murray Post hydrotreatment finishing of lubricant distillates
MX2016005893A (es) * 2013-11-08 2016-08-17 Sener Ing & Sist Proceso para aumentar el rendimiento de bases lubricantes en la regeneracion de aceites usados.
GB2521133A (en) * 2013-12-10 2015-06-17 Wei-Ming Chang Method for desulfurization and aromatic compound removal of re-refined base oil that is recovered from waste lubricating oil
CN104479736A (zh) * 2014-12-03 2015-04-01 烟台市牟平区留德润滑油销售有限公司 一种废润滑油馏分油精制方法
CN104893767B (zh) * 2015-05-19 2016-08-17 李菊明 一种废机油加工高品质燃料油的生产工艺
WO2017081552A1 (en) * 2015-11-10 2017-05-18 Hindustan Petroleum Corporation Limited A composition and a process for reducing aromatics from a hydrocarbon feedstock
ES2629851B1 (es) * 2016-02-15 2018-04-25 José Antonio GÓMEZ MIÑANA Procedimiento de triple destilación para la regeneración de aceites usados incluyendo tratamiento cáustico en línea en la segunda destilación
CN105797568B (zh) * 2016-05-18 2018-11-23 湖南省小尹无忌环境能源科技开发有限公司 一种利用废有机溶剂制复合脱硝剂的方法
US9920262B1 (en) * 2016-11-22 2018-03-20 Rj Lee Group, Inc. Methods of separation of pyrolysis oils
CN107699331B (zh) * 2017-09-18 2020-07-28 武汉工程大学 一种废润滑油分级除杂的净化方法
CN108085121A (zh) * 2017-12-22 2018-05-29 常州菲纳斯能源科技有限公司 废润滑油再生及回收芳烃的处理方法
CN109701509B (zh) * 2019-02-19 2023-08-08 安徽国孚凤凰科技有限公司 一种硅胶吸附抽提再生基础油后的再生装置及方法
KR102085351B1 (ko) * 2019-07-08 2020-03-05 이종호 폐유를 이용한 연료유의 제조방법
CN113061481A (zh) * 2021-03-27 2021-07-02 刘新华 一种废矿物油的回收净化再生利用工艺
CN114854484B (zh) * 2022-06-02 2023-04-25 河北车迪石油化工有限公司 废矿物油再生工艺及系统
CN115353928A (zh) * 2022-08-19 2022-11-18 唐亮 基于化学法处理的再生润滑油
WO2025177018A1 (en) * 2024-02-20 2025-08-28 Modalalian Mohammad Method for producing base oil from waste oil, and the generation of microspheres and organic or mineral salts from the produced waste

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4941967A (en) * 1983-11-23 1990-07-17 Kinetics Technology International B.V. Process for re-refining spent lubeoils
US5759385A (en) * 1994-10-17 1998-06-02 Institut Francais Du Petrole Process and plant for purifying spent oil

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US360420A (en) * 1887-04-05 Saw-swaging machine
US4021333A (en) * 1975-08-27 1977-05-03 The Lubrizol Corporation Method of rerefining oil by distillation and extraction
US4154670A (en) * 1975-11-24 1979-05-15 The Lubrizol Corporation Method of rerefining oil by dilution, clarification and extraction
US4328092A (en) 1980-03-07 1982-05-04 Texaco Inc. Solvent extraction of hydrocarbon oils
US4360420A (en) * 1980-10-28 1982-11-23 Delta Central Refining, Inc. Distillation and solvent extraction process for rerefining used lubricating oil
IT1154554B (it) * 1982-11-11 1987-01-21 D E L Co Di Coppo Mario Procedimento per il disinquinamento di oli minerali in genere e di fluidi siliconici dielettrici
CH657867A5 (de) * 1983-09-21 1986-09-30 Buss Ag Verfahren zur wiederaufbereitung von altoel und destillations-vorrichtung zur durchfuehrung des verfahrens.
DE3469301D1 (en) * 1983-12-07 1988-03-17 Electric Power Res Inst Removal of polychlorinated biphenyls by solvent extraction
DE3723607A1 (de) * 1987-07-17 1989-01-26 Ruhrkohle Ag Verfahren zum hydrierenden aufarbeiten von altoelen
RU2036960C1 (ru) * 1992-11-25 1995-06-09 Северо-Кавказский горно-металлургический институт Способ очистки отработанной масляной смазочно-охлаждающей жидкости
FR2703067B1 (fr) * 1993-03-22 1995-08-04 Sotulub Procédé et installation de régénération d'huiles lubrifiantes.
US6117309A (en) * 1997-09-08 2000-09-12 Probex Corporation Method of rerefining waste oil by distillation and extraction

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4941967A (en) * 1983-11-23 1990-07-17 Kinetics Technology International B.V. Process for re-refining spent lubeoils
US5759385A (en) * 1994-10-17 1998-06-02 Institut Francais Du Petrole Process and plant for purifying spent oil

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DK1141181T3 (da) 2004-06-14
CA2351606A1 (en) 2000-05-18
DE19852007A1 (de) 2000-05-18
PT1141181E (pt) 2004-06-30
JP4246397B2 (ja) 2009-04-02
SK285213B6 (sk) 2006-09-07
DE19852007C2 (de) 2002-06-13
AU1161900A (en) 2000-05-29
ES2222051T3 (es) 2005-01-16
EP1141181A1 (de) 2001-10-10
SK6362001A3 (en) 2001-11-06
HU226925B1 (en) 2010-03-01
PL348757A1 (en) 2002-06-03
CZ20011559A3 (cs) 2001-12-12
WO2000027957A1 (de) 2000-05-18
BR9916606A (pt) 2001-08-14
CZ298571B6 (cs) 2007-11-07
DE59908537D1 (de) 2004-03-18
HUP0104072A3 (en) 2004-08-30
HUP0104072A2 (hu) 2002-05-29
ATE259405T1 (de) 2004-02-15
US6712954B1 (en) 2004-03-30
CA2351606C (en) 2005-06-07
CN1326498A (zh) 2001-12-12
PL191398B1 (pl) 2006-05-31
RU2217484C2 (ru) 2003-11-27
JP2002529579A (ja) 2002-09-10
BR9916606B1 (pt) 2011-10-18
UA69426C2 (en) 2004-09-15
CN1185327C (zh) 2005-01-19

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