EP1141181B1 - Verfahren zur wiederaufarbeitung von altölen - Google Patents
Verfahren zur wiederaufarbeitung von altölen Download PDFInfo
- 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
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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]
Description
Raffinat | ||
Temperatur | [°C] | 80 isotherm |
Rückführung Ölphase aus Extrakt | ja | |
NMP/Öl-Verhältnis | [v/v] | 1,5 |
Ausbeute | [Gew.-%] | 84 |
Farbe ASTM | 0,5 | |
Neutralisationszahl | [mg KOH/g] | 0,01 |
Viskosität 40°C | [mm2/s] | 20,93 |
Viskosität 100°C | [mm2/s] | 4,23 |
Viskositätsindex | 106 | |
Aromatenanteil CA (IR) | [%] | 3,5 |
PAK, Summe n. Grimmer | [mg/kg] | 0,257 |
Benzo(a)pyren | [mg/kg] | 0,0034 |
Raffinat | ||
Temperatur | [°C] | 80 isotherm |
Rückführung Ölphase aus Extrakt | ja | |
NMP/Öl-Verhältnis | [v/v] | 1,8 |
Ausbeute | [Gew.-%] | 85 |
Farbe ASTM | L 1,5 | |
Neutralisationszahl | [mg KOH/g] | < 0,03 |
Viskosität 40°C | [mm2/s] | 36,05 |
Viskosität 100°C | [mm2/s] | 6,07 |
Viskositätsindex | 114 | |
Aromatenanteil CA (IR) | [%] | 3,9 |
PAK, Summe n. Grimmer | [mg/kg] | < 1 mg |
Benzo(a)pyren | [mg/kg] |
Raffinat | ||||
Temperatur | [°C] | 80 isotherm | 80 isotherm | 80/25 Gradient |
Rückführung Ölphase aus Extrakt | ja | ja | nein | |
NMP/Öl-Verhältnis | [v/v] | 2,0 | 1,1 | 1,1 |
Ausbeute | [Gew.-%] | 84 | 92 | 92 |
Farbe ASTM | 1,0 | L 2,0 | 2,0 | |
Neutralisationszahl | [mg KOH/g] | 0,01 | 0,03 | 0,04 |
Viskosität 40°C | [mm2/s] | 36,00 | 36,44 | 37,03 |
Viskosität 100°C | [mm2/s] | 6,08 | 6,07 | 6,10 |
Viskositätsindex | 116 | 112 | 110 | |
Aromatenanteil CA (IR) | [%] | 3,2 | 4,7 | 4,6 |
PAK, Summe n. Grimmer | [mg/kg] | 0,024 | 0,553 | 0,078 |
Benzo(a)pyren | [mg/kg] | 0,002 | 0,020 | 0,005 |
Claims (8)
- Verfahren zur Wiederaufarbeitung von Altölen und Erzeugung von Grundölen, umfassend die folgenden Schritte:A) Destillieren des Altöles zur Entfernung leichtsiedender organischer Fraktionen sowie Trocknen des Altöles durch Entfernen von Wasser, wobei das wieder aufzuarbeitende Altöl mit konzentrierter wässeriger Kalilauge als Reagenz behandelt wird und die Lauge bei der Destillation hinzugegeben wird;B) Destillieren des nach Schritt A) erhaltenen Altöles unter Vakuum zur Abtrennung von Heizöl- und Dieselfraktionen mit einem Siedeschnitt von etwa 170 bis 385°C;C) Schonendes Destillieren des Destillationsrückstandes aus Schritt B) mittels Dünnschichtverdampfung im Hochvakuum zur Erhaltung einer Schmierölfraktion mit einem üblichen Viskositätsbereich, die durch einen anschließenden destillativen Fraktionierungsschritt, gegebenenfalls unter Vakuum, in Siedeschnitte unterschiedlicher Viskositätslagen aufgetrennt werden kann;D) Gegebenenfalls schonendes Destillieren des Bodenproduktes aus Schritt C) zur Gewinnung einer Schmierölfraktion höherer Viskositätslage aus dem höhersiedenden Bereich, die durch einen anschließenden destillativen Fraktionierungsschritt, gegebenenfalls unter Vakuum, aufgetrennt werden kann; undE) Extrahieren der Fraktion oder Fraktionen in Form von Schmierölfraktionen oder Siedeschnitten unterschiedlicher Viskositätslagen aus Schritt C) und gegebenenfalls D) mit N-Methyl-2-pyrrolidon (NMP) und/oder N-Formylmorpholin (NMF) als Extraktionsmittel zur Erhaltung sehr hochwertiger Grundöle.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Kalilauge hochkonzentriert ist, insbesondere etwa 5 bis 50%ige Kalilauge darstellt.
- Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß dem Feed (Einsatz zur Extraktion) eine Alkalitätsreserve vermittelt wird, welche die sonst übliche, teilweise sogar irreversible Versauerung des zurückgewonnenen Extraktionsmittels verhindert.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Destillation in Schritt A) bei Normaldruck oder leichtem Unterdruck bis etwa 600 mbar und bei einer Temperatur von etwa 140 bis 150°C durchgerührt wird.
- Verfahren nach mindestens einem der vorangehenden Ansprüche, dadurch gekennzeichnet, daß die Extraktion im Gegenstromverfahren in einer Extraktionskolonne durchgeführt wird.
- Verfahren nach mindestens einem der vorangehenden Ansprüche, dadurch gekennzeichnet, daß die Extraktion isotherm bei einer Temperatur im Bereich von etwa 50 bis 90°C durchgeführt wird.
- Verfahren nach Anspruch 6, dadurch gekennzeichnet, daß die Extraktphase abgekühlt und die sich dabei absetzende Ölphase dem Zulauf (Feed) wieder zugegeben wird.
- Verfahren nach mindestens einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß die Extraktion mit einem Temperaturgradienten durchgeführt wird, wobei die Temperatur am Kolonnenkopf (Ablauf Raffinat) auf etwa 50 bis 90°C und am Kolonnenende (Extraktablauf) auf etwa 10 bis 50°C eingestellt wird.
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 |
Family
ID=7887428
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP99971836A Expired - Lifetime EP1141181B1 (de) | 1998-11-11 | 1999-11-11 | Verfahren zur wiederaufarbeitung von altölen |
Country Status (19)
Country | Link |
---|---|
US (1) | US6712954B1 (de) |
EP (1) | EP1141181B1 (de) |
JP (1) | JP4246397B2 (de) |
CN (1) | CN1185327C (de) |
AT (1) | ATE259405T1 (de) |
AU (1) | AU1161900A (de) |
BR (1) | BR9916606B1 (de) |
CA (1) | CA2351606C (de) |
CZ (1) | CZ298571B6 (de) |
DE (2) | DE19852007C2 (de) |
DK (1) | DK1141181T3 (de) |
ES (1) | ES2222051T3 (de) |
HU (1) | HU226925B1 (de) |
PL (1) | PL191398B1 (de) |
PT (1) | PT1141181E (de) |
RU (1) | RU2217484C2 (de) |
SK (1) | SK285213B6 (de) |
UA (1) | UA69426C2 (de) |
WO (1) | WO2000027957A1 (de) |
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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. |
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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 |
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US5759385A (en) * | 1994-10-17 | 1998-06-02 | Institut Francais Du Petrole | Process and plant for purifying spent oil |
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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. |
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- 1998-11-11 DE DE19852007A patent/DE19852007C2/de not_active Expired - Lifetime
-
1999
- 1999-11-11 DK DK99971836T patent/DK1141181T3/da active
- 1999-11-11 US US09/831,104 patent/US6712954B1/en not_active Expired - Lifetime
- 1999-11-11 PL PL348757A patent/PL191398B1/pl unknown
- 1999-11-11 RU RU2001116108/04A patent/RU2217484C2/ru active
- 1999-11-11 JP JP2000581124A patent/JP4246397B2/ja not_active Expired - Lifetime
- 1999-11-11 CZ CZ20011559A patent/CZ298571B6/cs not_active IP Right Cessation
- 1999-11-11 CN CNB998131733A patent/CN1185327C/zh not_active Expired - Lifetime
- 1999-11-11 EP EP99971836A patent/EP1141181B1/de not_active Expired - Lifetime
- 1999-11-11 AT AT99971836T patent/ATE259405T1/de active
- 1999-11-11 CA CA002351606A patent/CA2351606C/en not_active Expired - Lifetime
- 1999-11-11 WO PCT/EP1999/008667 patent/WO2000027957A1/de active IP Right Grant
- 1999-11-11 HU HU0104072A patent/HU226925B1/hu unknown
- 1999-11-11 AU AU11619/00A patent/AU1161900A/en not_active Abandoned
- 1999-11-11 SK SK636-2001A patent/SK285213B6/sk not_active IP Right Cessation
- 1999-11-11 DE DE59908537T patent/DE59908537D1/de not_active Expired - Lifetime
- 1999-11-11 ES ES99971836T patent/ES2222051T3/es not_active Expired - Lifetime
- 1999-11-11 BR BRPI9916606-2A patent/BR9916606B1/pt not_active IP Right Cessation
- 1999-11-11 UA UA2001063912A patent/UA69426C2/uk unknown
- 1999-11-11 PT PT99971836T patent/PT1141181E/pt unknown
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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 |
Also Published As
Publication number | Publication date |
---|---|
EP1141181A1 (de) | 2001-10-10 |
HU226925B1 (en) | 2010-03-01 |
ATE259405T1 (de) | 2004-02-15 |
DE19852007A1 (de) | 2000-05-18 |
SK285213B6 (sk) | 2006-09-07 |
BR9916606A (pt) | 2001-08-14 |
CN1185327C (zh) | 2005-01-19 |
ES2222051T3 (es) | 2005-01-16 |
HUP0104072A2 (hu) | 2002-05-29 |
BR9916606B1 (pt) | 2011-10-18 |
HUP0104072A3 (en) | 2004-08-30 |
UA69426C2 (en) | 2004-09-15 |
AU1161900A (en) | 2000-05-29 |
JP2002529579A (ja) | 2002-09-10 |
WO2000027957A1 (de) | 2000-05-18 |
JP4246397B2 (ja) | 2009-04-02 |
CN1326498A (zh) | 2001-12-12 |
SK6362001A3 (en) | 2001-11-06 |
CZ20011559A3 (cs) | 2001-12-12 |
PL348757A1 (en) | 2002-06-03 |
CZ298571B6 (cs) | 2007-11-07 |
CA2351606A1 (en) | 2000-05-18 |
PL191398B1 (pl) | 2006-05-31 |
DE19852007C2 (de) | 2002-06-13 |
RU2217484C2 (ru) | 2003-11-27 |
US6712954B1 (en) | 2004-03-30 |
DK1141181T3 (da) | 2004-06-14 |
DE59908537D1 (de) | 2004-03-18 |
CA2351606C (en) | 2005-06-07 |
PT1141181E (pt) | 2004-06-30 |
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