EP0574272B1 - Procédé amelioré pour la production d'huiles de base à partir d'huile usée - Google Patents

Procédé amelioré pour la production d'huiles de base à partir d'huile usée Download PDF

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Publication number
EP0574272B1
EP0574272B1 EP93304584A EP93304584A EP0574272B1 EP 0574272 B1 EP0574272 B1 EP 0574272B1 EP 93304584 A EP93304584 A EP 93304584A EP 93304584 A EP93304584 A EP 93304584A EP 0574272 B1 EP0574272 B1 EP 0574272B1
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EP
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Prior art keywords
process according
oil
sodium
alkali compound
lube
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EP93304584A
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German (de)
English (en)
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EP0574272A2 (fr
EP0574272A3 (fr
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Louis M. Magnabosco
William A. Rondeau
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CHEMICAL ENGINEERING PARTNERS
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CHEMICAL ENGINEERING PARTNERS
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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

Definitions

  • the present invention provides for an improved process of producing base stock oil from spent or used lube oils.
  • Lube base oils are among the most valuable constituents in crude oil. Virgin lube oils are recovered from so-called lube-crudes by solvent extraction followed by wax (i.e. paraffin) removal. To enhance color and stability, the raw lube oil is catalytically hydrotreated. Average crude oils contain 3-8% lube base oils, whereas lube crudes have typically 12-16% lube base oils. This compares with 60 to 65% of lube base oils contained in spent automotive oils. Thus, it is quite evident that mere disposal of spent lube oil destroys a valuable natural resource that should be reclaimed.
  • lubricating base oils from used oil has been plagued by a myriad of problems, most of them associated with inordinate corrosion and fouling due to decomposition of the additives in formulated oils.
  • typical automotive lube oils consist of about 75% base oil and about 25% additives.
  • additives include: viscosity index (VI) improvers, anti-oxidants, anti-wear improvers, pour-point depressants, detergents, etc. While the base lube stock components deteriorate only slightly, the additives undergo severe changes which make re-refining a difficult endeavor.
  • Used oil typically consists of about 66% base oil, about 10% water, about 12% additives and about 12% fuel. In addition, these spent oils frequently contain glycols, chlorinated solvents, gasoline, carbon, solid particles and metals.
  • Metals in a typical used oil include the following: lead about 100 ppm, calcium about 875 ppm, phosphorous about 730 ppm, magnesium about 230 ppm, zinc about 710 ppm, sodium about 130 ppm, cadmium about 2 ppm and chromium about 3 ppm. These metals are primarily present in the form of metallo-organic compounds and are present to a minor extent as metal oxides or sulfides. Decomposition of certain metallo-sulfur additives may generate sulfuric acid and, thus, may lead to problems with fouling and corrosion in subsequent steps in the re-refining process.
  • Decomposition of base lube oil components may result in production of lower boiling hydrocarbons which comprise materials boiling in the gasoline, kerosene and light gasoil boiling ranges respectively. These materials can be separated by distillation.
  • Another process proposed to re-refine used lubricating oils using an extraction process.
  • the used lube oil was contacted with a light hydrocarbon solvent, for example propane, in a first extraction zone to give a first extract and a raffinate. Removal of solvent from the first extract gave the desired lube oil base stock.
  • the first raffinate was then solvent extracted using the same solvent to produce a second extract and a second raffinate. Removal of solvent from the second extract yielded an oil which could be further refined.
  • Other processes which involve solvent extraction have been proposed; however, these solvent extraction processes are economically disadvantageous (i.e., expensive) due to the high energy requirements for solvent evaporation which has limited their acceptance.
  • a process involving a heat soak step (at a temperature of about 300°C) prior to distillation was proposed.
  • the used oil was then passed first over a guard bed containing adsorbents and then over the hydrotreating catalyst to yield a high quality base lube stock.
  • Phosphorus content of the material was said to be responsible for short catalyst life.
  • Phosphorus levels in the lube distillate were reduced from the range of about 50 to 350 ppm to less than 6 ppm by heat soaking the de-watered and de-gasoiled raw waste oil and then separating the bottoms (asphalt) from the raw lube distillate by thin filter evaporation (see U.S. Patent No. 4,512,878).
  • DE-A-1594531 describes a process for purifying contaminated waste oil which comprises the steps of eliminating water from the waste oil, heating the contaminated waste oil with an alkaline earth metal hydroxide and simultaneously or subsequently vacuum distilling the waste oil.
  • the present invention is directed to an improved process of re-refining used oil to produce a base stock oil which is suitable for use in automobile lubricating oil and which is substantially equivalent to a base stock oil produced from virgin crude oil.
  • a process which comprises (a) pretreating used oil to remove hydrofinishing catalyst fouling materials to give a pretreated mixture; (b) distilling the pretreated mixture from step (a) to separate lower boiling materials (less than 150°C), gasoil and lube oil distillate from asphalt; and (c) hydrofinishing the lube oil distillate from step (b) wherein said pretreating of step (a) includes adding a sufficient amount of an alkali compound, to the used oil under vigorous mixing conditions to give a pH of at least 5 in the gas phase of all the distillates produced in step (b), the amount of alkali compound being insufficient to cause gelling of the asphalt fraction, and wherein said pretreated mixture comprises at least 3% water.
  • Suitable alkali compounds include an alkali metal or a weak acid salt of an alkali metal or an alkaline earth or a combination thereof.
  • alkali compounds which comprise an alkali metal, or an alkali metal or alkaline earth hydroxide, oxide, aluminate, carbonate, bicarbonate, sulfite or bisulfite, or a combination thereof.
  • the alkali compound is selected from sodium hydroxide, potassium hydroxide, sodium aluminate, sodium carbonate, sodium bicarbonate, sodium sulfite, sodium bisulfite or a combination thereof.
  • At least about 3% water is present in the pretreated mixture.
  • the pretreated mixture comprises 3% to 20% water, more preferably 5% to 15% water.
  • pretreating step (a) is carried out at a temperature of 80°C to 170°C, more preferably at a temperature of 90°C to 150°C; especially preferred is the temperature range of 100°C to 130°C.
  • the alkali compound comprises sodium hydroxide added in step (a) in an amount sufficient to give a pH of 6.5 or greater for gasoil fractions boiling in a range of 150°C to 300°C.
  • the alkali compound comprises sodium aluminate, sodium carbonate, sodium bicarbonate, sodium sulfite, sodium bisulfite or a combination thereof, or alternatively, the alkali compound comprises sodium hydroxide in combination with sodium aluminate.
  • the present invention provides a process for reducing the phosphorus content in lube oil distillate produced by refining used oils.
  • This process comprises steps (a), (b) and (c) as defined above wherein the amount of alkali compound added in pretreating step (a) is sufficient to convert substantially all free phosphorus to an insoluble phosphate or phosphoro compound.
  • Suitable alkali compounds include an alkali metal or an alkali metal salt or an alkaline earth salt of a weak acid.
  • Preferred alkali compounds include an alkali metal or a salt selected from an alkali metal or alkaline earth hydroxide, oxide, aluminate, carbonate, bicarbonate, sulfite, or bisulfite or a combination thereof.
  • pretreating step (a) is conducted at a temperature of 80°C to 170°C under well-mixed conditions. More preferably pretreating step (a) is conducted at 90°C to 150°C, an especially preferred temperature range is from 100°C to 130°C.
  • distilling step (b) includes holding the pretreated mixture at a temperature of about 300°C with good mixing for 30 minutes to 2 hours, more preferably for 45 to 75 minutes.
  • the present invention is based on the surprising finding that the present process results not only in distillates (produced in the distillation step) having an advantageous basic pH which are less corrosive to refinery equipment, but also produces an asphalt fraction which does not gel and, thus, foul and block piping and associated equipment.
  • use of the process of the present invention removes metallo-sulfur compounds which are present in the lubricating oil additives and/or result from the decomposition of lubricating oil additives and which in later processing steps may cause serious fouling and corrosion due to acid-catalyzed polymerization reactions.
  • overtreatment with these compounds, particularly when using sodium hydroxide leads to serious plant operational problems in addition to being expensive.
  • Fats and fatty oils present in the used oils may be hydrolyzed, producing soaps which cause gelling of the oil.
  • Excess sodium hydroxide may also increase the viscosity of the distillation residue, resulting in associated problems in pumps and mechanical equipment.
  • Certain processing problems are also associated with overtreatment and include an apparent lack of performance of heat transfer equipment which may be caused by changes in chemical and physical properties of the oil in the liquid phase, due to ion exchange and/or hydrolysis reactions during treatment. Also, the radical increase in viscosity of the distillation residue may lead to difficulties in extracting the material from the process equipment, which must be avoided, particularly in view of vacuum operating conditions which may be employed for certain processing steps.
  • the improved process described herein substantially avoids overtreatment in the pretreating of step (a).
  • pretreatment with alkali metal hydroxide results in a reduced phosphorus content in lube distillate.
  • use of sodium aluminate in the pre-treating step is particularly effective in reducing phosphorus content in the lube oil distillate fraction (see Table VI). This reduction in phosphorus content is believed to occur by formation of aluminum phosphates and/or aluminum phosphoro esters.
  • sodium aluminate other suitable alkali compounds which form low-solubility phosphorus products may be used.
  • Such suitable alkali compounds include magnesium aluminate, calcium oxide, calcium hydroxide, magnesium oxide, calcium aluminate, and magnesium hydroxide and other compounds which form insoluble phosphorus compounds that end up in the bottom (asphalt) fraction upon evaporation (or distillation).
  • Other suitable alkali compounds include the sodium salts of weak acids and include sodium carbonates, bicarbonates, sulfites and bisulfites. Phosphorus is an undesirable component in lube distillates, since its presence deactivates hydrotreating catalyst in subsequent hydroprocessing operations that are conducted to improve a variety of important quality/stability parameters of the lube oil base stock.
  • the catalyst life of the hydroprocessing catalyst was typically about 3 to 4 weeks. After application of the process according to a preferred embodiment of the present invention, catalyst life was typically about 3 to 6 months which represents, a significant extension in catalyst life.
  • FIG. 1 A simplified block flow diagram of the overall re-refining process is depicted in Figure 1.
  • This process comprises high-efficiency re-refining technology. Key steps include the pretreatment and subsequent base lube oil recovery via thin-film vacuum distillation that produces base lube oils in the overhead product and asphalt in the bottoms. Deleterious metals wind up encapsulated in the asphalt fraction. The asphalt fraction meets the leaching test criteria.
  • the asphalt produced in this manner is suitable for use as a blending component for road paving asphalt or for production of roofing shingles.
  • the raw lube base distillates are catalytically hydrotreated to improve color and stability.
  • the resulting finished lube base oils are of equal or better quality than virgin oil produced via extraction from lube crudes.
  • the pretreatment steps assure low maintenance and continuous, trouble-free operation, by minimizing fouling and corrosion.
  • Table I An analysis of a typical used oil used in re-refining is set forth in Table I.
  • Table I Analysis of Typical Used Oil for Re-Refining Viscosity centistokes @ 100 deg Fahrenheit ( ⁇ 37.7°C) 40-140 API Gravity - degrees 20-32 Composition - Volume Percentages Water 5-15% Light Ends 1-4% Gas Oil Fraction 10-15% Lube Oil Fraction 55-70% Asphalt Flux 10-15% Sulphur - weight percentage 0.13-0.35% Nitrogen - weight percentage 0.03-0.06% Chlorine - ppm 600-1500 Sulphated Ash - weight percentage 0.5-1.5% Flash Point (degrees Fahrenheit) 100 ( ⁇ 37.7°C) Metals - ppm Lead 100 Calcium 875 Phosphorus 730 Magnesium 230 Zinc 710 Sodium 130 Cadmium 2 Chromium 3 Silicon 50
  • An important aspect of the processes of this invention comprises the pretreatment of the used oil to reduce fouling of catalyst and equipment and corrosion of equipment and to reduce the phosphorous content of the lube distillate that results from such pretreatment.
  • a major obstacle in the re-refining of used automotive oils is the presence of a wide variety of additives, including organo-metallic compounds, that have been added to lube base oils to impart desirable properties in a lubricating oil.
  • additives involve a considerable spectrum of compounds and include, but are not limited to, the following: antiwear compounds, corrosion inhibitors, pour point depressants, oxidation inhibitors, antifoam agents, etc.
  • Modern automotive lubricants may contain up to about 25 percent additives.
  • Such additives decompose much more rapidly than the base oils. The decomposition of these additives dictates the frequency of lube oil changes, since base oils are reported to be considerably more stable than additives. See, e.g. , P.C.
  • Figure 2 depicts a proposed reaction scheme.
  • the reaction is not instantaneous. Depending on conditions, the reaction takes about 15 to 20 minutes and in some instances up to 60 minutes, to go to completion. Mixing is important to assure thorough contacting of the aqueous phase with the hydrocarbon phase.
  • Some release of ammonia is triggered, if the alkali compound is dosed properly, due to decomposition of amines, amides and similar nitrogen containing compounds which keep the vapor space alkaline and allow use of carbon steel equipment without corrosion protection measures being required. If the alkali compound is improperly dosed, acidic gasoil fractions will be obtained that cause fouling and corrosion of equipment.
  • Gelling of asphalt due to over-treatment with sodium hydroxide is principally due to formation of soaps from fats and fatty oils. This gelling is also believed to be due to formation of sodium alcoholates and, in general, sodium oxygenates, all of which may cause gelling.
  • insoluble sulfates helps to shift the reaction to the right, i.e., to complete sulfonate conversion.
  • presence of Ca, and to a lesser extent Mg shifts the sulfonate hydrolysis reaction to the right.
  • This observation applies, but is not limited, to this type of reaction, it is only noted here as an example. Similar considerations apply to other hydrolysis reactions in used oil processing of the present invention that are shifted to completion in the presence of certain metal ions such as Ca and Al, notably conversion of phosphorous compounds such as phosphorous esters, thiophosphates, dithiophosphates and the like.
  • phosphorous content in the lube distillate produced can be decreased by addition of an alkali compound and/or materials that promote hydrolysis of the phosphorous-bearing compounds.
  • Particularly useful is sodium aluminate per se or in combination with another alkali compound.
  • the alkali compound used in the pretreating of step (a) comprises a combination of an alkali metal or alkaline earth hydroxide and an alkali metal or alkaline earth aluminate.
  • a combination of sodium hydroxide and sodium aluminate we have found the use of a combination of sodium hydroxide and sodium aluminate to be particularly advantageous. Also advantageous is the use of sodium aluminate alone.
  • Runs 1 and 2 clearly showed the beneficial effect of NaAlO 2 in that phosphorous was reduced to 0.3 ppm with NaAlO 2 whereas NaOH added alone resulted in a phosphorous content of 1.9 ppm. Elimination of the 60 minute holding time increased the phosphorous contents of the respective distillates to 28 ppm for NaOH and to 18 ppm for the NaAlO 2 . Thus, there was a 30% improvement in phosphorous reduction when using NaAlO 2 . In the experiments 5 and 6, the heat up from 12°-300° was changed as well as the holding time at 300°C. Again, there was an advantage for NaAlO 2 .
  • FIG. 3 A graphic representation of the results in Table VII is depicted in Figure 3, where the phosphorous content of the lube distillate and the pH of the 150°C-200°C gasoil boiling range fraction are plotted as a function of sodium hydroxide added.
  • Figure 3 clearly indicates that the phosphorous content of the lube distillate decreases as a function of sodium hydroxide added.
  • the pH of the gasoil fraction 150°C-200°C boiling range, is observed to increase with increasing amounts of sodium hydroxide added, whereby a steep increase is observed between 1.1 ml and 2.0 ml aqueous sodium hydroxide solution (30% NaOH).
  • This steep slope of the curve occurs between pH 3 and 7, and it is similar to a titration curve.
  • this behavior suggests the concept of neutralisation stoichiometry involving sodium hydroxide on one hand and waste oil content of the predominant metals magnesium, calcium and zinc on the other hand.
  • the values of the pH's for all gasoil fractions are above 6.5 at a point where about 1.7 ml sodium hydroxide solution (30% NaOH) had been added.
  • Table IV WASTE OIL FEED COMPOSITION Component ppm Ca 950 Mg 300 Zn 845 P 830 H 2 O, % by weight 10.5 Table V Gas Phase PH as a Function of Reflux Time pH Reaction Time Before Cold Finger 1 2 3 0 7.7 8.8 10.0 10 7.4 9.4 10.4 20 8.7 9.3 10.1 30 8.0 9.1 9.8 40 8.7 9.3 9.8 50 8.4 9.2 9.9 1 Waste Oil only. 2. 0.5 ml NaOH 30% added. 3. 2.1 ml NaOH 30% added.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Lubricants (AREA)
  • Fats And Perfumes (AREA)

Claims (17)

  1. Procédé pour le ré-raffinage d'huiles usées pour fournir une huile de base qui est essentiellement équivalente à une huile de base obtenue à partir d'une huile de pétrole vierge qui comprend :
    (a) le prétraitement de l'huile usée pour éliminer les matières d'encrassement du catalyseur d'hydrofinition et conduire à un mélange prétraité,
    (b) la distillation du mélange prétraité de l'étape (a) pour séparer, d'une fraction d'asphalte, une fraction de distillat de faible point d'ébullition qui bout à moins de 150° C, une fraction de gasoil et une fraction d'huile lubrifiante, et
    (c) l'hydrofinition de la fraction d'huile lubrifiante de l'étape (b),
    procédé dans lequel l'étape de prétraitement comprend l'addition à la dite huile usée, dans des conditions d'agitation vigoureuses, d'une quantité suffisante d'un composé alcalin pour conduire à un pH d'au moins 5 dans la phase gazeuse de tous les distillats obtenus à l'étape (b), la quantité du composé alcalin étant insuffisante pour provoquer la gélification de la fraction d'asphalte et dans lequel le mélange prétraité contient au moins 3 % d'eau.
  2. Procédé selon la revendication 1 dans lequel ledit mélange de prétraitement contient de 3 à 20 % d'eau.
  3. Procédé selon la revendication 1 ou 2 dans lequel le composé alcalin est choisi parmi les métaux alcalins et les sels d'acides faibles d'un métal alcalin ou alcalino-terreux.
  4. Procédé selon la revendication 3 dans lequel le composé alcalin comprend un métal alcalin ou un sel choisi parmi les hydroxydes, oxides, aluminates, carbonates bicarbonates ou bisulfites d'un métal alcalin ou alcalino-terreux ou un mélange de ceux-ci.
  5. Procédé selon la revendication 4 dans lequel ledit composé alcalin comprend de l'hydroxyde de sodium, de l'hydroxyde de potassium, de l'aluminate de sodium, du carbonate de sodium, du bicarbonate de sodium, du sulfite de sodium, du bisulfite de sodium ou un mélange de ceux-ci.
  6. Procédé selon la revendication 5 dans lequel le composé alcalin comprend de l'aluminate de sodium, du carbonate de sodium, du bicarbonate de sodium, du sulfite de sodium, du bisulfite de sodium ou un mélange de ceux-ci.
  7. Procédé selon la revendication 5 dans lequel le composé alcalin comprend de l'hydroxyde de sodium en mélange avec de l'aluminate de sodium.
  8. Procédé selon la revendication 5 dans lequel ledit composé alcalin comprend de l'hydroxyde de sodium additionné à l'étape (a) en une quantité suffisante pour donner un pH de 6,5 ou supérieur aux fractions de gasoils de point d'ébullition compris entre 150° C et 300° C.
  9. Procédé selon l'une quelconque des revendications 1 à 7 dans lequel ledit composé alcalin est additionné à l'étape (a) en une quantité suffisante pour donner un pH d'au moins 6 dan la phase gazeuse de tous les distillats obtenus à l'étape (b).
  10. Procédé selon la revendication 9 dans lequel ledit composé alcalin est additionné à l'étape (a) en une quantité suffisante pour donner un pH d'au moins 6,5 dans la phase gazeuse de tous les distillats obtenus à l'étape (b).
  11. Procédé selon l'une quelconque des revendications 1 à 10 dans lequel la quantité du composé alcalin additionnée à l'étape de prétraitement (a) est suffisante pour convertir essentiellement tout le soufre libre en un composé phosphate ou phosphoro insoluble.
  12. Procédé selon la revendication 11 dans lequel ledit composé alcalin comprend de l'hydroxyde de sodium.
  13. Procédé selon l'une quelconque des revendications 1 à 12 dans lequel ladite étape de prétraitement (a) est réalisée à une température de 80° C à 170° C.
  14. Procédé selon la revendication 13 dans lequel ladite étape de prétraitement (a) est réalisée à une température de 90° C à 150° C.
  15. Procédé selon la revendication 14 dans lequel ladite étape de prétraitement (a) est réalisée à une température de 100° C à 130° C.
  16. Procédé selon l'une quelconque des revendications 1 à 15 dans lequel l'étape de distillation (b) consiste à maintenir le mélange prétraité à une température d'environ 300° C pendant 30 minutes à 2 heures sous bonne agitation.
  17. Procédé selon la revendication 16 dans lequel le temps de contact, à environ 300° C, est de 45 à 75 minutes.
EP93304584A 1992-06-12 1993-06-14 Procédé amelioré pour la production d'huiles de base à partir d'huile usée Expired - Lifetime EP0574272B1 (fr)

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US89802592A 1992-06-12 1992-06-12
US898025 1992-06-12

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EP0574272A2 EP0574272A2 (fr) 1993-12-15
EP0574272A3 EP0574272A3 (fr) 1994-02-23
EP0574272B1 true EP0574272B1 (fr) 2000-04-05

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JP (1) JPH06158086A (fr)
AT (1) ATE191496T1 (fr)
DE (1) DE69328274T2 (fr)

Cited By (2)

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US7226533B2 (en) 2002-07-15 2007-06-05 Sener Grupo De Ingenieria, S.A. Process for re-refining used oils by solvent extraction
US9932530B2 (en) 2014-06-17 2018-04-03 Air Products And Chemicals, Inc. Refining used motor oil through successive hydrotreating processes

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JP2005505681A (ja) 2001-10-16 2005-02-24 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 予備処理した使用済み油の品質向上
US9074159B2 (en) * 2010-10-06 2015-07-07 Uop Llc Process for improving a re-refined lube oil stream
US9708565B2 (en) * 2012-01-27 2017-07-18 Vertellus Performance Chemicals, LLC Method for reducing color in used lubricating oil
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.
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
FI128911B (en) * 2018-07-20 2021-03-15 Neste Oyj Purification of recycled and renewable organic material
FI128174B (en) 2018-07-20 2019-11-29 Neste Oyj Purification of recycled and renewable organic material
FI128069B2 (en) * 2018-07-20 2024-04-24 Neste Oyj Cleaning of recycled and renewable organic material
FI128121B (en) 2018-07-20 2019-10-15 Neste Oyj Production of hydrocarbons from recycled or renewable organic material
FI128115B2 (en) * 2018-07-20 2024-08-20 Neste Oyj Cleaning of recycled and renewable organic material
FI129367B (en) 2018-12-28 2021-12-31 Neste Oyj METHOD FOR HANDLING LIPID - CONTAINING MATERIALS
FI128517B (en) 2018-12-28 2020-07-15 Neste Oyj Apparatus and method for heat treating input materials comprising lipid materials
CN110923052B (zh) * 2019-12-06 2022-04-12 烟台立衡环保科技有限公司 一种用于废润滑油再生的蒸馏回收装置
US11034895B1 (en) * 2020-01-22 2021-06-15 Axens SA Process for production of on specification group III/III+ base oils while preserving base oil yield
CN111334368A (zh) * 2020-04-15 2020-06-26 南京车全新能源科技有限公司 一种废旧润滑油净化装置

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Cited By (2)

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Publication number Priority date Publication date Assignee Title
US7226533B2 (en) 2002-07-15 2007-06-05 Sener Grupo De Ingenieria, S.A. Process for re-refining used oils by solvent extraction
US9932530B2 (en) 2014-06-17 2018-04-03 Air Products And Chemicals, Inc. Refining used motor oil through successive hydrotreating processes

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Publication number Publication date
EP0574272A2 (fr) 1993-12-15
JPH06158086A (ja) 1994-06-07
DE69328274D1 (de) 2000-05-11
ATE191496T1 (de) 2000-04-15
DE69328274T2 (de) 2000-11-30
EP0574272A3 (fr) 1994-02-23

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