EP0230543B1 - Verfahren zur Aufarbeitung von Altöl - Google Patents
Verfahren zur Aufarbeitung von Altöl Download PDFInfo
- Publication number
- EP0230543B1 EP0230543B1 EP86116200A EP86116200A EP0230543B1 EP 0230543 B1 EP0230543 B1 EP 0230543B1 EP 86116200 A EP86116200 A EP 86116200A EP 86116200 A EP86116200 A EP 86116200A EP 0230543 B1 EP0230543 B1 EP 0230543B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- oil
- solvent
- extraction
- process according
- extraction residue
- 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
Links
- 238000000034 method Methods 0.000 title claims abstract description 48
- 238000004064 recycling Methods 0.000 title 1
- 238000000605 extraction Methods 0.000 claims abstract description 46
- 239000002904 solvent Substances 0.000 claims abstract description 34
- 238000002309 gasification Methods 0.000 claims abstract description 12
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000000194 supercritical-fluid extraction Methods 0.000 claims abstract description 5
- 238000007669 thermal treatment Methods 0.000 claims abstract description 4
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 3
- 238000009903 catalytic hydrogenation reaction Methods 0.000 claims abstract description 3
- 239000001294 propane Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 39
- 239000002699 waste material Substances 0.000 claims description 27
- 238000004061 bleaching Methods 0.000 claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 238000004821 distillation Methods 0.000 claims description 14
- 238000005984 hydrogenation reaction Methods 0.000 claims description 9
- 238000005292 vacuum distillation Methods 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 5
- 239000000654 additive Substances 0.000 claims description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 4
- 239000000470 constituent Substances 0.000 claims description 4
- 238000001914 filtration Methods 0.000 claims description 4
- 229910052760 oxygen Inorganic materials 0.000 claims description 4
- 239000001301 oxygen Substances 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 239000012535 impurity Substances 0.000 claims description 3
- 239000007788 liquid Substances 0.000 claims description 3
- 150000002736 metal compounds Chemical class 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000003807 solvent-free extraction Methods 0.000 claims description 3
- 239000004215 Carbon black (E152) Substances 0.000 claims description 2
- 238000000746 purification Methods 0.000 claims description 2
- 238000005201 scrubbing Methods 0.000 claims 2
- 239000001273 butane Substances 0.000 claims 1
- 230000006835 compression Effects 0.000 claims 1
- 238000007906 compression Methods 0.000 claims 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims 1
- 238000012958 reprocessing Methods 0.000 claims 1
- 239000010802 sludge Substances 0.000 claims 1
- 150000002366 halogen compounds Chemical class 0.000 abstract description 3
- 239000006227 byproduct Substances 0.000 abstract description 2
- 230000008021 deposition Effects 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 58
- 235000019198 oils Nutrition 0.000 description 57
- 239000000047 product Substances 0.000 description 22
- 238000000926 separation method Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 238000007670 refining Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000010913 used oil Substances 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- 239000002199 base oil Substances 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000010801 sewage sludge Substances 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 239000010409 thin film Substances 0.000 description 3
- 239000002918 waste heat Substances 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000000356 contaminant Substances 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 229910052736 halogen Inorganic materials 0.000 description 2
- 150000002367 halogens Chemical class 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000004254 Ammonium phosphate Substances 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- KEAYESYHFKHZAL-UHFFFAOYSA-N Sodium Chemical compound [Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 150000001348 alkyl chlorides Chemical class 0.000 description 1
- 150000001350 alkyl halides Chemical class 0.000 description 1
- ZRIUUUJAJJNDSS-UHFFFAOYSA-N ammonium phosphates Chemical class [NH4+].[NH4+].[NH4+].[O-]P([O-])([O-])=O ZRIUUUJAJJNDSS-UHFFFAOYSA-N 0.000 description 1
- 235000019289 ammonium phosphates Nutrition 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 150000008282 halocarbons Chemical class 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 239000010687 lubricating oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010327 methods by industry Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 235000019476 oil-water mixture Nutrition 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 150000003071 polychlorinated biphenyls Chemical class 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 150000003464 sulfur compounds Chemical class 0.000 description 1
- 239000000725 suspension 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
- C10M175/02—Working-up used lubricants to recover useful products ; Cleaning mineral-oil based
Definitions
- the invention relates to a process for working up waste oil, in which the previously dewatered waste oil is subjected to extraction under supercritical conditions using a solvent which is gaseous under normal conditions and the extracted components are then separated from the separated supercritical gas phase by reducing the pressure and / or changing the temperature.
- lubricating oils used technically are contaminated waste oils and can, as far as they are accessible to a collection, be used for further purposes. This can be done either by incineration for the purpose of energy production or by refining the used oil for the purpose of re-use as a lubricant.
- the used oil to be processed contains impurities of all kinds, e.g. as so-called additives serving metal compounds, wear and aging residues and contaminants that result from improper storage of the used oil.
- these contaminants of various types require special measures to protect the environment when burning waste oil and, on the other hand, must be completely separated from the product to be reused when refining the waste oil.
- the sulfuric acid / bleaching earth process has so far been used to a particularly large extent for refining used oils.
- the advantages of a simple technique are offset by low yields, inadequate selectivity and larger amounts of problematic waste materials, essentially acid resins and bleaching earth residues.
- this process does not guarantee the harmless disposal of particularly problematic pollutants such as polychlorinated biphenyls, polychlorinated phenyls, haloalkanes and polycondensed aromatics.
- Thin-film evaporation however, consists in fouling the heat exchanger surfaces and in the comparatively low selectivity of the process.
- the invention is therefore based on the object of further developing the process for the processing of waste oil using a supercritical extraction in such a way that the above-described disposal problem is solved in a satisfactory manner, so that the processing of the waste oil without the occurrence of residues or unacceptably polluting the environment By-products can be carried out.
- the method according to the invention basically provides two options for the disposal of the resulting solvent-free extraction residue. If conditions permit, efforts will be made to dispose of the extraction residue by storage in a landfill for cost reasons. However, if this is not possible, the extraction residue will be disposed of by thermal treatment (gasification).
- the waste oil to be processed is fed from the collecting container 1 via line 2 to the filter system 3, in which the solid particles are separated from the waste oil by filtration and are withdrawn via line 4.
- the waste oil freed from the solid particles passes via line 5 and the pump 6 into the distillation column 7.
- the waste oil is subjected to a distillation in the temperature range between 120 ° C. and 250 ° C. under atmospheric pressure.
- the gas oil-water mixture escaping overhead from the distillation column 7 is introduced via line 8 into the separating tank 9, in which the water is separated from the gas oil (so-called gas oil I) by phase separation.
- the gas oil is discharged through line 10 and the water through line 11 deducted from the separating container 9.
- the pre-distilled and dewatered waste oil drawn off from the distillation column 7 via the line 12 is introduced into the central part of the extraction column 13, which works at a pressure between 50 and 150 bar and a temperature between 20 ° C. and 80 ° C.
- the pump 14 brings the waste oil to the required operating pressure of the extraction column 13, and the heat exchanger 15 ensures that the required operating temperature of the waste oil is reached.
- the waste oil can also be fed into the extraction column 13 in its upper or lower part.
- the required solvent is introduced via line 16 into the lower part of the extraction column 13.
- the solvent absorbs the components of the waste oil that are soluble under the specified operating conditions, while the insoluble components collect together with the impurities in the bottom of the extraction column 13 and are withdrawn from there via line 17 under level control.
- the valve 18 serves to regulate the extraction of the extraction residue from the extraction column 13.
- the necessary expansion of the extraction residue to a pressure of 1 to 0.01 bar takes place in the expansion tank 19.
- the gaseous solvent released in this process is drawn off via line 20.
- the expansion tank 19 can be heated and provided with an agitator.
- the upper part of the extraction column 13 acts as an amplifier section.
- the top product obtained there is drawn off via line 21 and enters the steam-heated heat exchanger 22, in which the required reflux is generated by a slight increase in temperature, since the solubility of the oil in the supercritical solvent decreases as the temperature increases.
- the downstream separator 23 the condensed oil is separated off and returned to the extraction column 13 by the pump 24 via line 25, where it is added as reflux to the top of the column.
- the loaded solvent passes from the separator 23 via the line 26 into the high-pressure separator 27, in which, in the present case, the oil phase is completely separated from the solvent.
- the separated oil phase which is the extract
- the separated oil phase is withdrawn from the lower part of the high-pressure separator 27 under level control and passes via line 28 into the low-pressure separator 29, in which the solvent residues still present in the oil phase are separated off.
- the amount of the extract withdrawn via line 28 is regulated by valve 30.
- the solvent-free product oil is withdrawn via line 31 from the low-pressure separator 29 and passes via line 31 into the collecting container 32.
- the product oil is pressed into the hydrogenation reactor 36 via the pump 34 located in line 33 and the heat exchanger 35 which the catalytic hydrogenation of the product oil takes place in the presence of commercially available hydrogenation catalysts which contain, for example, nickel as the active component.
- the hydrogen required for this is introduced into the hydrogenation reactor 36 via line 37.
- the halogen and sulfur compounds contained therein are converted into hydrogen or hydrogen sulfide.
- These products are withdrawn in gaseous form from the hydrogenation reactor 36 via line 38.
- the hydrogenated product oil in the meantime passes via line 39 into the addition container 40, into which bleaching earth can be introduced via line 41, which is mixed in the addition container 40 with stirring with the hydrogenated product oil.
- the bleaching earth / oil mixture is then introduced via pump 42 and line 43 into vacuum distillation column 44, in which it is distilled under a vacuum of 0.002 to 0.1 bar and is thus broken down into different fractions. If it is possible to dispense with the addition of bleaching earth, the hydrogenated product oil passes directly into the vacuum distillation column 44 via line 39. Gas oil II is withdrawn via line 45 and spindle oil is removed via line 46. The distillation residue obtained in the vacuum distillation column 44 is conveyed by means of the pump 48 in line 47 into the filter system 49, in which the bleaching earth is separated off by filtration. This oily bleaching earth passes through line 51 into the gasifier 52, while the base oil obtained during the filtration is drawn off from the filter system 49 via line 50.
- the following products are also introduced into the gasifier 52: the extraction residue from the expansion tank 19 via the line 53 and the pump 54, the gas oil from the separating tank 9 via the line 10 and the sewage sludge from the biological wastewater treatment 55 via the line 56.
- the carburetor 52 can be an entrained-flow carburetor that works according to the known Koppers-Totzek method. Oxygen and / or air and possibly small amounts of water vapor serve as the gasification medium.
- the gasification can be carried out under normal or increased pressure. If liquids or suspensions are to be gasified, the gasifier is equipped with so-called atomizing burners. The burners can also be preceded by heat exchangers in which the product to be gasified is brought to the temperature required for setting the required viscosity.
- the products introduced into the carburetor 52 are gasified in a flame reaction at temperatures between 1300 ° C and 2000 ° C.
- the additional fuel which may be required for this purpose passes through line 57 and the necessary air or oxygen via line 58 into the gasifier 52.
- the gas which results essentially consisting of the components CO, H 2 , C0 2 , H 2 0 and N 2 is drawn off from the carburetor 52 via the line 59 and reaches the pressurized water scrubber 61 via the waste heat boiler 60.
- the gas stream from the line 38 is also introduced into this, so that both gas streams carry out the subsequent gas treatment go through together.
- This consists of the pressurized water wash 61 and the pressurized wash 62, the individual stages being connected to one another via the lines 63 and 64.
- This gas treatment removes both halogen and hydrogen sulfide as well as the metal compounds originating from the oil additives from the gas. Since the gas in the waste heat boiler 60 has already been pre-cooled to the required extent, the gas drawn off via line 65 after passing through the two washing stages can be used without problems as heating gas.
- the gasification residue (slag) obtained in the gasification is drawn off in the molten state via line 66 from the gasifier and granulated and cooled in a water bath (not shown).
- the solvent escaping overhead from the high-pressure separator 27 is drawn off via line 67 and returns via the heat exchanger 68 to line 16, via which the solvent is reintroduced into the extraction column 13. Since the solvent circuit is almost isobaric, only a slight increase in pressure has to be brought about by the circuit compressor 69.
- the heat exchangers 68 and 70 are used here to adjust the temperature of the solvent.
- the solvent escaping from the low-pressure separator 29 is drawn off via the line 71 and, after having been compressed to condensation pressure in the compressor 72, reaches the condenser 73, in which it is liquefied.
- the heat exchanger 74 in turn serves the required temperature setting.
- the line 20 opens into the line 71 in front of the heat exchanger 74, via which line the solvent released in the expansion tank 19 is drawn off.
- the liquefied solvent is collected in the template 75 and fed from there through the compressor 76 via line 77 into line 16, if necessary.
- the water separated in the separating container 9 passes via line 11 into the biological wastewater treatment 55, from which the cleaned wastewater is introduced via line 78 into the receiving water.
- the sewage sludge resulting from the wastewater treatment is, as already mentioned, fed to the gasifier 52 via line 56.
- the drying oil emerging from the distillation column 7 was cooled to 43 ° C. via the heat exchanger 15, compressed to 100 bar with the pump 14 and then fed to the extraction column 13 at half the height. At the foot of the extraction column 13, ethane was fed in as a solvent at 43 ° C. and 100 bar.
- the cleaned, loaded solvent phase was freed from the dissolved products following the heat exchanger 22 in the downstream high-pressure separator 27 by heating to 150 ° C. at 100 bar.
- the separated product in an amount of 126 kg / h was drawn off at the bottom of the high-pressure separator 27 and expanded to 1 bar in the low-pressure separator 29 in order to separate off the solvent still dissolved in it.
- the solvent released was recompressed and combined with the main solvent stream.
- the separated product was subjected to hydrogenation in the hydrogenation reactor 36 to break down the halogenated hydrocarbons present in it and then separated into the products base oil, spindle oil and gas oil II in the vacuum distillation column 44. 2.8 kg / h of bleaching earth were added to the product given to the vacuum distillation.
- the oily bleaching earth was filtered off from the bottom product of the vacuum distillation in the filter system 49. 74 kg / h base oil, 35 kg / h spindle oil and 14 kg / h gas oil II as well as 5.6 kg / h oiled bleaching earth were obtained.
- the extraction residue preheated to 150 ° C. was compressed to the required pre-pressure of the carburetor 52.
- the gas oil 1 was mixed with the oil-laden bleaching earth and the small amount of sewage sludge obtained in the biological wastewater treatment 55, and the resulting mixture was also compressed to the required admission pressure of the gasifier 52 and fed to the gasifier 52 together with the extraction residue at approx. 150 ° C.
- This mixture was gasified in the gasifier 52 with the addition of 0.95 kg of oxygen per kg of mixture as an oxidizing agent in a flame reaction at temperatures above 1500 ° C.
- the product of the gasification was CO and H 2 in a ratio of 2.1: 1 as well as small amounts of CO 2 and water vapor as well as traces of H 2 S and HCl.
- the metal contents of the residue were oxidized and removed from the gasifier as ash or fly dust.
- the hot raw gas which was still loaded with small amounts of flying dust, was subjected to the gas treatment described above, whereby heating gas, waste heat steam and saline solution were obtained.
- it was mixed with the raw gas from the gasification before the gas treatment.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Extraction Or Liquid Replacement (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Processing Of Solid Wastes (AREA)
- Lubricants (AREA)
- Fats And Perfumes (AREA)
- Treatment Of Sludge (AREA)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AT86116200T ATE41029T1 (de) | 1986-01-29 | 1986-11-21 | Verfahren zur aufarbeitung von altoel. |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19863602586 DE3602586A1 (de) | 1986-01-29 | 1986-01-29 | Verfahren zur aufarbeitung von altoel |
| DE3602586 | 1986-01-29 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| EP0230543A1 EP0230543A1 (de) | 1987-08-05 |
| EP0230543B1 true EP0230543B1 (de) | 1989-03-01 |
Family
ID=6292841
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| EP86116200A Expired EP0230543B1 (de) | 1986-01-29 | 1986-11-21 | Verfahren zur Aufarbeitung von Altöl |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US4797198A (ja) |
| EP (1) | EP0230543B1 (ja) |
| JP (1) | JPS62184097A (ja) |
| AT (1) | ATE41029T1 (ja) |
| DE (2) | DE3602586A1 (ja) |
| ES (1) | ES2006695B3 (ja) |
Families Citing this family (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3839799A1 (de) * | 1988-11-25 | 1990-07-05 | Rwe Entsorgung Ag | Verfahren zur aufarbeitung kontaminierter oele |
| US5143597A (en) * | 1991-01-10 | 1992-09-01 | Mobil Oil Corporation | Process of used lubricant oil recycling |
| US5316743A (en) * | 1992-09-28 | 1994-05-31 | Leblanc Ralph W | Diesel fuel cracking unit |
| FR2725725B1 (fr) * | 1994-10-17 | 1996-12-13 | Inst Francais Du Petrole | Procede et installation pour la purification des huiles usagees |
| US6066350A (en) | 1997-02-07 | 2000-05-23 | Cargill Incorporated | Method and arrangement for processing cocoa mass |
| US7045038B1 (en) * | 1999-12-21 | 2006-05-16 | Industrial Microwave Technologies, Inc. | Process for treating waste oil |
| EP1279722A1 (de) * | 2001-07-18 | 2003-01-29 | Minitec Engineering GmbH | Verfahren zur Reinigung von Ölen und zur Entfernung von Feststoffablagerungen in ölführenden Anlagen, Rohrbündelwärmeübertragern, Transformatoren, Tankbehälter oder ähnlichem |
| US7201934B2 (en) * | 2002-10-15 | 2007-04-10 | Cargill, Incorporated | Dispersible cocoa products |
| US20040071848A1 (en) * | 2002-10-15 | 2004-04-15 | Cargill Inc. | Process for producing cocoa butter and cocoa powder by liquefied gas extraction |
| US20040071847A1 (en) * | 2002-10-15 | 2004-04-15 | Cargill, Inc. | Producing cocoa powders with different cocoa butter contents by liquefied gas extraction on substantially the same production line |
| US8088276B2 (en) * | 2008-08-08 | 2012-01-03 | CleanOil Limited | Oil re-refining system and method |
| WO2020160662A1 (en) * | 2019-02-05 | 2020-08-13 | Gen Iii Oil Corporation | Method and system for re-refining and upgrading used oil |
Family Cites Families (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3074882A (en) * | 1959-02-02 | 1963-01-22 | Texaco Inc | Petroleum treating process involving solvent deasphalting and propane fractionation |
| US3507777A (en) * | 1968-01-25 | 1970-04-21 | Exxon Research Engineering Co | Cracking process |
| DE2030609A1 (de) * | 1969-09-09 | 1971-03-18 | Petrolchemisches Kombinat | Verfahren zur Aufarbeitung von ge brauchten Schmierölen |
| US3594308A (en) * | 1970-06-22 | 1971-07-20 | Universal Oil Prod Co | Petroleum crude oil conversion process |
| US3864242A (en) * | 1973-12-13 | 1975-02-04 | Imamura Seisakusho Kk | Treating muddy-like waste oily material |
| US3919076A (en) * | 1974-07-18 | 1975-11-11 | Pilot Res & Dev Co | Re-refining used automotive lubricating oil |
| US4021333A (en) * | 1975-08-27 | 1977-05-03 | The Lubrizol Corporation | Method of rerefining oil by distillation and extraction |
| IT1091961B (it) * | 1978-01-12 | 1985-07-06 | Snam Progetti | Procedimento per la rigenerazione degli oli esausti |
| DE2850540C2 (de) * | 1978-11-22 | 1982-12-23 | Fried. Krupp Gmbh, 4300 Essen | Verfahren zur Aufbereitung von Altöl |
| CS209612B1 (en) * | 1979-11-10 | 1981-12-31 | Alexander Tkac | Method of treating the spent motor oils |
| US4363717A (en) * | 1981-01-15 | 1982-12-14 | Mobil Oil Corporation | Conversion of heavy hydrocarbon oils |
| IT1137280B (it) * | 1981-07-07 | 1986-09-03 | Assoreni E Snamprogetti Spa | Procedimento per recupero di oli esausti |
| US4482453A (en) * | 1982-08-17 | 1984-11-13 | Phillips Petroleum Company | Supercritical extraction process |
| DE3321356A1 (de) * | 1983-06-14 | 1984-12-20 | Drägerwerk AG, 2400 Lübeck | Gasdosimeter in einer halterung, ein diffusionspruefroehrchen enthaltend |
| US4431523A (en) * | 1983-06-24 | 1984-02-14 | Phillips Petroleum Company | Upgrading fuel fractions in a re-refined oil process |
-
1986
- 1986-01-29 DE DE19863602586 patent/DE3602586A1/de not_active Withdrawn
- 1986-11-21 ES ES86116200T patent/ES2006695B3/es not_active Expired
- 1986-11-21 EP EP86116200A patent/EP0230543B1/de not_active Expired
- 1986-11-21 AT AT86116200T patent/ATE41029T1/de not_active IP Right Cessation
- 1986-11-21 DE DE8686116200T patent/DE3662205D1/de not_active Expired
-
1987
- 1987-01-27 JP JP62015349A patent/JPS62184097A/ja active Pending
- 1987-01-27 US US07/007,358 patent/US4797198A/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| ATE41029T1 (de) | 1989-03-15 |
| US4797198A (en) | 1989-01-10 |
| EP0230543A1 (de) | 1987-08-05 |
| JPS62184097A (ja) | 1987-08-12 |
| DE3662205D1 (en) | 1989-04-06 |
| ES2006695B3 (es) | 1989-10-16 |
| DE3602586A1 (de) | 1987-07-30 |
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