EP0372276B1 - Procédé pour régénérer des huiles usagées - Google Patents
Procédé pour régénérer des huiles usagées Download PDFInfo
- Publication number
- EP0372276B1 EP0372276B1 EP89121255A EP89121255A EP0372276B1 EP 0372276 B1 EP0372276 B1 EP 0372276B1 EP 89121255 A EP89121255 A EP 89121255A EP 89121255 A EP89121255 A EP 89121255A EP 0372276 B1 EP0372276 B1 EP 0372276B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- distillation
- oils
- thermal treatment
- thermal
- contaminated
- 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
Links
- 239000003921 oil Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000007669 thermal treatment Methods 0.000 claims abstract description 11
- 150000001805 chlorine compounds Chemical class 0.000 claims abstract description 5
- 238000004821 distillation Methods 0.000 claims description 20
- 238000004227 thermal cracking Methods 0.000 claims description 11
- 238000005292 vacuum distillation Methods 0.000 claims description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 238000004523 catalytic cracking Methods 0.000 claims description 8
- 230000015572 biosynthetic process Effects 0.000 claims description 6
- 238000002309 gasification Methods 0.000 claims description 5
- 238000012958 reprocessing Methods 0.000 claims description 4
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 238000003786 synthesis reaction Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims 1
- 238000007670 refining Methods 0.000 abstract description 12
- 238000007700 distillative separation Methods 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 description 17
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 11
- 239000010913 used oil Substances 0.000 description 9
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 8
- 239000000460 chlorine Substances 0.000 description 8
- 229910052801 chlorine Inorganic materials 0.000 description 8
- 239000000654 additive Substances 0.000 description 7
- 150000001875 compounds Chemical class 0.000 description 7
- 239000007789 gas Substances 0.000 description 6
- 239000002184 metal Substances 0.000 description 6
- 229910052751 metal Inorganic materials 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 150000002739 metals Chemical class 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000005336 cracking Methods 0.000 description 4
- 239000010779 crude oil Substances 0.000 description 4
- -1 for example Chemical compound 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000000314 lubricant Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 150000001735 carboxylic acids Chemical class 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 3
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 3
- 238000005984 hydrogenation reaction Methods 0.000 description 3
- 239000003112 inhibitor Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical class S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000010306 acid treatment Methods 0.000 description 2
- 125000004429 atom Chemical group 0.000 description 2
- 238000004061 bleaching Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 238000005187 foaming Methods 0.000 description 2
- 125000005842 heteroatom Chemical group 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000011835 investigation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 229920005989 resin Polymers 0.000 description 2
- 239000011347 resin Substances 0.000 description 2
- 229910052721 tungsten Inorganic materials 0.000 description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 238000005299 abrasion Methods 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000011280 coal tar Substances 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 150000002013 dioxins Chemical class 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 150000002019 disulfides Chemical class 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 239000003995 emulsifying agent Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 230000020169 heat generation Effects 0.000 description 1
- 239000010763 heavy fuel oil Substances 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 239000006078 metal deactivator Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 229920001296 polysiloxane Polymers 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000003381 stabilizer Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 235000013311 vegetables Nutrition 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Images
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
Definitions
- the present invention relates to a process for working up contaminated oils by thermal treatment in a thermal or catalytic cracking stage, working up the product by distillation and then hydrogenating treatment of distillate fractions.
- waste oil Although a precise definition of the term “waste oil” is missing (see, for example, Chapter 1, K. Müller “waste oil recycling”, Erich Schmidt Verlag, Berlin 1982), in the broadest sense it is mostly used lubricants and functional fluids that are no longer directly reusable based on petroleum, but also those based on coal tar, vegetable, animal or synthetic. These materials can also be substances that are solid or semi-solid at normal temperature.
- the new lubricants and functional fluids contain numerous additives, such as Corrosion inhibitors, oxidation inhibitors, foam inhibitors, detergents, dispersants, metal deactivators, color stabilizers, viscosity index improvers, pour point depressants, wear control additives, emulsifiers and others.
- additives such as Corrosion inhibitors, oxidation inhibitors, foam inhibitors, detergents, dispersants, metal deactivators, color stabilizers, viscosity index improvers, pour point depressants, wear control additives, emulsifiers and others.
- chlorinated compounds in particular of polychlorodiphenyls, -terphenyls, polychlorodiphenylmethanes and other chlorine-containing additives, is of particular importance in the case of waste oils or the mixtures mentioned.
- An improvement is the sulfuric acid / bleaching earth method, in which after the sulfuric acid treatment is treated with bleaching earth and then distilled in vacuo (R. Meixlsperger in W. Kumpf, K. Maas, H. Straub: Müll und Abfallbesorgung, 395, no . 4010).
- the applicant has surprisingly succeeded in developing a process that is already used on a large industrial scale with great success in a refinery and that allows waste oils to be processed with excellent results within the framework of conventional refinery technology, characterized in that a thermal treatment of the contaminated Oil consisting of a thermal or catalytic cracking stage is carried out, that the distillative separation of chlorine-containing distillates and that a hydrogenative refining of the chlorine-containing distillates takes place.
- Thermal cracking has the advantage that heavy, relatively heavily contaminated oils can be used.
- Typical thermal cracking processes are visbreaking, which is carried out at relatively low temperatures of approx. 400-500 ° C, normal thermal cracking at approx. 500-600 ° C and coking, which is carried out at approx. 500 ° C.
- Catalytic cracking processes are generally carried out in a fixed bed, fluidized bed or fluidized bed at about 400-500 ° C. According to the invention, these cracking processes are also suitable as a thermal treatment stage.
- the refining of refinery streams serves to remove the heteroatoms, especially nitrogen and sulfur, which are present in the crude fractions in the form of compounds.
- refining processes can also consist of chemical reactions, such as the oxidation of strong-smelling mercaptans to low-smelling disulfides, refining by hydrogenation in the presence of sulfur-resistant catalysts, which usually contain combinations of Ni, Co, Mo and W as metal components, is the most most procedures used.
- the heteroatoms S, N and O occur as H2S, NH3 and H2O. Unsaturated compounds are converted into saturated hydrocarbons.
- the hydrogenating refining can be used under very different conditions, for example 25-100 bar and 300-400 ° C are typical, but also significantly higher pressures up to e.g. 300 bar can be used.
- contaminated oil such as e.g. Used oil without pre-cleaning in a Visbreaker one of the under standard conditions of approx. 10 bar and 20 min. Dwell time and operated at a temperature up to about 450 ° C, there are significant chemical conversions that can lead to the elimination of HCl and formation of the carboxylic acids. The details of the course of these conversions are not known.
- the carboxylic acids mainly as acetic acid, are removed via the top of the atmospheric distillation column downstream of the Visbreaker or at an upper side draw, and HCl also escapes.
- Corrosion protection additives are advantageously added to the condensation system on the head in order to avoid corrosion there too.
- Gas oil cutting which usually has a boiling range of 170-360 ° C, but can also be cut differently if required, still contains chlorine-containing compounds.
- the bottom of atmospheric distillation is a vacuum subjected to distillation, the vacuum distillate also contains chlorine-containing compounds.
- distillate that boils more easily in the atmospheric distillation than gas oil can, however, be obtained free of critical chlorine-containing components such as polychlorobi- and -terphenylene or polychlorodiphenylmethanes, as can the bottom of the vacuum distillation.
- gas oil and / or vacuum distillate are now subjected to a hydrogenating catalytic refining, the hydrogenation-active metals, in particular combinations of Ni / Co / Mo and tungsten, being on conventional supports such as amorphous or crystalline zeolites, Al2O3, aluminum silicates, SiO2 and the like.
- the hydrogenating refining can take place in a wide pressure range of 25-300 bar and 280-500 ° C.
- a preferred mode of operation is 25-100 bar and 280-400 ° C, particularly preferred are 30-70 bar and 300-380 ° C.
- the products obtained are completely chlorine-free and can be used or processed like conventional refinery cuts.
- a base in particular NaOH, is preferably added to the thermal or, if appropriate, catalytic cracking stage.
- 20-40 mol% of gram atom of chlorine can be used in the feed product, but NaOH can be varied within wide limits up to stoichiometric or even stoichiometric amounts. An amount less than 20 mol% per gram atom of chlorine is less advantageous.
- the amount of contaminated oil used e.g. Waste oil can be> 0 to 35% by weight of the total use in the thermal treatment stage, preferably> 0-20% by weight and particularly preferably> 0-15% by weight.
- Defoamers can be added to reduce or prevent foaming in the entire application area.
- the expert known defoamers suitable for such purposes are used.
- the bottom of the atmospheric distillation can, for example, be fed directly to gasification. The soot in the gasification largely absorbs the ashes of the contaminated oils.
- the figure serves as an example for a more detailed explanation.
- the bottom product is used in vacuum distillation 11.
- Vacuum distillate reaches hydrogenation reactor 13 via 12. Via 9 gas oil can also be used directly in 13. Hydrogen is added via 14.
- a hydrocarbon product above 15 which is completely chlorine-free is withdrawn from the hydrogenation reactor.
- the system was operated without problems for 16 weeks in the manner described.
- the present invention therefore represents a method for the first time ready, which allows large quantities of contaminated oils to be processed in normal refining operations without operational disruptions, whereby flawless hydrocarbon streams which can be fed to customary further processing are obtained.
- the bottom product of the vacuum distillation 11 can be supplied to gasification, for example a shell or Texaco gasification 17, or can be drawn off as heavy fuel oil via 18.
- gasification for example a shell or Texaco gasification 17
- the bottom product of column 6 can also be fed directly via 17 or 18 via 19. Over 20 synthesis gas is withdrawn.
Landscapes
- Chemical & Material Sciences (AREA)
- Physics & Mathematics (AREA)
- Thermal 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)
- Treatment Of Liquids With Adsorbents In General (AREA)
Claims (10)
1. Procédé d'épuration d'huiles usagées, caractérisé en ce qu'on effectue un traitement thermique de l'huile usagée consistant en une étape de craquage thermique ou catalytique, en ce qu'on effectue la séparation par distillation de distillats contenant des quantités chlorées et en ce qu'on effectue un raffinage par hydrogénation des distillats contenant des composés chlorés.
2. Procédé suivant la revendication 1, caractérisé en ce que l'épuration par distillation consiste en une distillation atmosphérique suivie d'une distillation sous vide.
3. Procédé suivant la revendication 2, caractérisé en ce que la fraction de gazole provenant de la distillation atmosphérique et le distillat sous vide sont soumis à un traitement d'hydrogénation catalytique.
4. Procédé suivant les revendications 2 et 3, caractérisé en ce que la température de tête de la distillation atmosphérique est maintenue au-dessus de 150°C, de préférence au-dessus de 180°C.
5. Procédé suivant les revendications 1 à 4, caractérisé en ce qu'une base est ajoutée dans l'étape de traitement thermique.
6. Procédé suivant les revendications 1 à 5, caractérisé en ce que de l'hydroxyde de sodium est ajouté dans l'étape de traitement thermique.
7. Procédé suivant les revendications 1 à 6, caractérisé en ce que le traitement d'hydrogénation est conduit à 25-300 bars et à 280-500°C, de préférence à 25-100 bars et à 300-400°C et notamment à 30-70 bars et à 320-380°C.
8. Procédé suivant les revendications 1 à 7, caractérisé en ce qu'on utilise une opération de viscoréduction comme étape de traitement thermique.
9. Procédé suivant les revendications 1 à 8, caractérisé en ce que la quantité d'huile usagée, par rapport à la charge totale introduite dans l'étape de traitement thermique, va de plus de 0 à 35% en poids, de préférence de plus de 0 à 20% en poids et notamment de plus de 0 à 15% en poids.
10. Procédé suivant les revendications 1 à 9, caractérisé en ce que le résidu de distillation atmosphérique et/ou le résidu de distillation sous vide sont envoyés à une installation de gazéification pour la production de gaz de synthèse.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT89121255T ATE71136T1 (de) | 1988-11-25 | 1989-11-17 | Verfahren zur aufarbeitung kontaminierter oele. |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE3839799A DE3839799A1 (de) | 1988-11-25 | 1988-11-25 | Verfahren zur aufarbeitung kontaminierter oele |
| DE3839799 | 1988-11-25 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0372276A1 EP0372276A1 (fr) | 1990-06-13 |
| EP0372276B1 true EP0372276B1 (fr) | 1992-01-02 |
Family
ID=6367865
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP89121255A Expired - Lifetime EP0372276B1 (fr) | 1988-11-25 | 1989-11-17 | Procédé pour régénérer des huiles usagées |
Country Status (5)
| Country | Link |
|---|---|
| US (1) | US5049258A (fr) |
| EP (1) | EP0372276B1 (fr) |
| AT (1) | ATE71136T1 (fr) |
| DD (1) | DD290211A5 (fr) |
| DE (2) | DE3839799A1 (fr) |
Families Citing this family (21)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5300212A (en) * | 1992-10-22 | 1994-04-05 | Exxon Research & Engineering Co. | Hydroconversion process with slurry hydrotreating |
| US5885444A (en) * | 1992-11-17 | 1999-03-23 | Green Oasis Environmental, Inc. | Process for converting waste motor oil to diesel fuel |
| US5362381A (en) * | 1993-03-25 | 1994-11-08 | Stanton D. Brown | Method and apparatus for conversion of waste oils |
| US5527449A (en) * | 1993-03-25 | 1996-06-18 | Stanton D. Brown | Conversion of waste oils, animal fats and vegetable oils |
| BR9707470A (pt) * | 1996-01-26 | 2000-01-04 | Heshui Yu | Processo e aparelho para o tratamento de óleos de refugo |
| US5676711A (en) * | 1996-02-21 | 1997-10-14 | Kuzara; Joseph K. | Oil conversion process |
| KR0171501B1 (ko) * | 1996-08-28 | 1999-03-20 | 이성래 | 폐유 재생 장치 및 방법 |
| US6132596A (en) * | 1997-01-24 | 2000-10-17 | Yu; Heshui | Process and apparatus for the treatment of waste oils |
| EP0860183B1 (fr) * | 1997-02-24 | 2002-11-13 | Kabushiki Kaisha Meidensha | Procédé et système d'élimination des composés nocifs |
| GB0327178D0 (en) * | 2003-11-21 | 2003-12-24 | Taylor John | Production of hydrocarbon fuel |
| US8366912B1 (en) | 2005-03-08 | 2013-02-05 | Ari Technologies, Llc | Method for producing base lubricating oil from waste oil |
| US20140257008A1 (en) | 2013-03-07 | 2014-09-11 | Verolube, Inc. | Method and apparatus for recovering synthetic oils from composite oil streams |
| CN103351939B (zh) * | 2013-06-28 | 2015-01-21 | 姜皓 | 一种废润滑油的精制再生方法及其再生装置 |
| WO2019116108A2 (fr) | 2017-12-13 | 2019-06-20 | Karl Ip Holdings Inc. | Conversion catalytique à basse pression d'huile pour moteur usagée en carburant diesel |
| FI129867B (en) | 2017-12-29 | 2022-10-14 | Neste Oyj | A method for reducing fouling in catalytic cracking |
| FI128121B (en) | 2018-07-20 | 2019-10-15 | Neste Oyj | Production of hydrocarbons from recycled or renewable organic material |
| FI128069B2 (en) * | 2018-07-20 | 2024-04-24 | Neste Oyj | Cleaning of recycled and renewable organic material |
| FI128115B (en) | 2018-07-20 | 2019-10-15 | 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 |
| FI128911B (en) | 2018-07-20 | 2021-03-15 | Neste Oyj | Purification of recycled and renewable organic material |
| FI128237B (en) * | 2018-12-21 | 2020-01-15 | Neste Oyj | METHOD FOR UPGRADING GAME OILS |
Family Cites Families (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT262479B (de) * | 1965-10-21 | 1968-06-10 | Oemv Ag | Verfahren zur Aufarbeitung von gebrauchten Schmierölen |
| US3755141A (en) * | 1971-02-11 | 1973-08-28 | Texaco Inc | Catalytic cracking |
| US3738931A (en) * | 1971-05-13 | 1973-06-12 | Atlantic Richfield Co | Method for treating synthetic crude oil for pour point reduction |
| GB1537822A (en) * | 1975-01-22 | 1979-01-04 | Shell Int Research | Process for the production of normally gaseous olefins |
| DE2508713C3 (de) * | 1975-02-28 | 1979-04-12 | Adolf Schmids Erben Ag, Bern | Verfahren zur Aufarbeitung von gebrauchtem Mineralöl |
| US4167533A (en) * | 1978-04-07 | 1979-09-11 | Uop Inc. | Co-production of ethylene and benzene |
| DE2818521A1 (de) * | 1978-04-27 | 1979-11-08 | Degussa | Verfahren zur wiederaufbereitung von gebrauchten schmieroelen (ii) |
| JPS57123290A (en) * | 1981-01-25 | 1982-07-31 | Chiyoda Chem Eng & Constr Co Ltd | Method for converting heavy hydrocarbon oil into light fractions |
| US4512878A (en) * | 1983-02-16 | 1985-04-23 | Exxon Research And Engineering Co. | Used oil re-refining |
| MX165696B (es) * | 1983-02-16 | 1992-12-01 | Exxon Research Engineering Co | Redepuracion de aceites usados |
| DE3600024C1 (de) * | 1986-01-02 | 1987-06-19 | Union Rheinische Braunkohlen | Verfahren zur Gewinnung hochwertiger Schmierstoffe aus Altoelen |
| DE3602586A1 (de) * | 1986-01-29 | 1987-07-30 | Krupp Koppers Gmbh | Verfahren zur aufarbeitung von altoel |
| FR2598089B1 (fr) * | 1986-04-30 | 1989-07-21 | Labofina Sa | Procede de decomposition de composes organiques halogenes applicable notamment aux huiles minerales |
| DE3623430A1 (de) * | 1986-07-11 | 1988-01-28 | Veba Oel Entwicklungs Gmbh | Verfahren zur hydrierenden behandlung von mit chlorbiphenylen u. dgl. kontaminierten mineraloelen |
| US4773986A (en) * | 1986-12-18 | 1988-09-27 | Lummus Crest, Inc. | High severity visbreaking |
-
1988
- 1988-11-25 DE DE3839799A patent/DE3839799A1/de not_active Withdrawn
-
1989
- 1989-11-17 AT AT89121255T patent/ATE71136T1/de not_active IP Right Cessation
- 1989-11-17 EP EP89121255A patent/EP0372276B1/fr not_active Expired - Lifetime
- 1989-11-17 DE DE8989121255T patent/DE58900667D1/de not_active Expired - Lifetime
- 1989-11-22 US US07/440,504 patent/US5049258A/en not_active Expired - Fee Related
- 1989-11-24 DD DD89334841A patent/DD290211A5/de not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| ATE71136T1 (de) | 1992-01-15 |
| DE3839799A1 (de) | 1990-07-05 |
| EP0372276A1 (fr) | 1990-06-13 |
| DE58900667D1 (de) | 1992-02-13 |
| US5049258A (en) | 1991-09-17 |
| DD290211A5 (de) | 1991-05-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP0372276B1 (fr) | Procédé pour régénérer des huiles usagées | |
| EP0182309B1 (fr) | Procédé pour la réutilisation par hydration de déchets contenant du carbone d'origine synthétique | |
| DE2215664C3 (fr) | ||
| DE3737370C1 (de) | Verfahren zur hydrierenden Konversion von Schwer- und Rueckstandsoelen,Alt- und Abfalloelen in Mischung mit Klaerschlaemmen | |
| DE2639775A1 (de) | Verfahren zur erzeugung von einem oder mehreren atmosphaerischen kohlenwasserstoffoeldestillaten aus einem atmosphaerischen rueckstandsoel | |
| DE2215665C3 (de) | Verfahren zum Herstellen von Benzin und raffinierten flüssigen Kohlenwasserstoffen | |
| DE2601875A1 (de) | Gesamtverfahren zur erzeugung von unter normalbedingungen gasfoermigen olefinen | |
| DE2953190A1 (de) | Verfahren zum herstellen von hochwertigem koks | |
| DE3207069A1 (de) | Krackverfahren unter anwendung eines wasserstoffabgebenden loesungsmittels zur qualitaetsverbesserung von hochsiedenden, kohlenstoffhaltigen fluessigkeiten | |
| DE2927251C2 (fr) | ||
| DE976855C (de) | Verfahren zum Hydrofinieren von rohem Erdoel | |
| DE1470628A1 (de) | Verfahren zur Befreiung von Kohlenwasserstoffoelen von Verunreinigungen | |
| DE1276264B (de) | Verfahren zur Herstellung von Schmieroelfraktionen mit hohem Viskositaetsindex | |
| DE3529795A1 (de) | Verfahren zur verfluessigung von kohle | |
| DE2813200C2 (de) | Verfahren zur Wiederaufbereitung von gebrauchten Schmierölen | |
| DE102019133911A1 (de) | Verfahren zur Co-Verarbeitung | |
| DE2202526A1 (de) | Reinigungsverfahren fuer Kohlenwasserstoff-Einsatzmaterial u.dgl. sowie Verwendung der gereinigten Kohlenwasserstoffe zum katalytischen Cracken | |
| DE2417977A1 (de) | Verfahren zur herstellung von heizoel mit niedrigem schwefelgehalt | |
| DE3405858A1 (de) | Verfahren zur wiederaufbereitung von altoelen | |
| DE60016755T2 (de) | Verfahren zur behandlung von rohöl | |
| DE3600024C1 (de) | Verfahren zur Gewinnung hochwertiger Schmierstoffe aus Altoelen | |
| DE1271869B (de) | Verfahren zur gleichzeitigen Herstellung von Schmieroel und Heizoel und bzw. oder niedriger siedenden Kohlenwasserstoffen | |
| DE3039263A1 (de) | Solvensextraktionsverfahren fuer die kohleumwandlung | |
| DE1200459B (de) | Verfahren zum Vergueten von schweren Kohlenwasserstoffen | |
| DD200891B5 (de) | Verfahren zur Gewinnung von Kohlenwasserstoffen aud Polyolefinen |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
| AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AT BE CH DE ES FR GB GR IT LI NL SE |
|
| 17P | Request for examination filed |
Effective date: 19901024 |
|
| 17Q | First examination report despatched |
Effective date: 19910503 |
|
| ITF | It: translation for a ep patent filed |
Owner name: GUZZI E RAVIZZA S.R.L. |
|
| GRAA | (expected) grant |
Free format text: ORIGINAL CODE: 0009210 |
|
| AK | Designated contracting states |
Kind code of ref document: B1 Designated state(s): AT BE CH DE ES FR GB GR IT LI NL SE |
|
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: SE Effective date: 19920102 Ref country code: GR Free format text: LAPSE BECAUSE OF FAILURE TO SUBMIT A TRANSLATION OF THE DESCRIPTION OR TO PAY THE FEE WITHIN THE PRESCRIBED TIME-LIMIT Effective date: 19920102 Ref country code: ES Free format text: THE PATENT HAS BEEN ANNULLED BY A DECISION OF A NATIONAL AUTHORITY Effective date: 19920102 Ref country code: BE Effective date: 19920102 |
|
| REF | Corresponds to: |
Ref document number: 71136 Country of ref document: AT Date of ref document: 19920115 Kind code of ref document: T |
|
| GBT | Gb: translation of ep patent filed (gb section 77(6)(a)/1977) | ||
| REF | Corresponds to: |
Ref document number: 58900667 Country of ref document: DE Date of ref document: 19920213 |
|
| ET | Fr: translation filed | ||
| PLBE | No opposition filed within time limit |
Free format text: ORIGINAL CODE: 0009261 |
|
| STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT |
|
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: AT Effective date: 19921117 |
|
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: LI Effective date: 19921130 Ref country code: CH Effective date: 19921130 |
|
| 26N | No opposition filed | ||
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: NL Effective date: 19930601 |
|
| NLV4 | Nl: lapsed or anulled due to non-payment of the annual fee | ||
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: FR Effective date: 19930730 |
|
| REG | Reference to a national code |
Ref country code: CH Ref legal event code: PL |
|
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: DE Effective date: 19930803 |
|
| REG | Reference to a national code |
Ref country code: FR Ref legal event code: ST |
|
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: GB Effective date: 19931117 |
|
| GBPC | Gb: european patent ceased through non-payment of renewal fee |
Effective date: 19931117 |
|
| PG25 | Lapsed in a contracting state [announced via postgrant information from national office to epo] |
Ref country code: IT Free format text: LAPSE BECAUSE OF NON-PAYMENT OF DUE FEES;WARNING: LAPSES OF ITALIAN PATENTS WITH EFFECTIVE DATE BEFORE 2007 MAY HAVE OCCURRED AT ANY TIME BEFORE 2007. THE CORRECT EFFECTIVE DATE MAY BE DIFFERENT FROM THE ONE RECORDED. Effective date: 20051117 |