WO2003044141A2 - Process for the purification of contaminated oils - Google Patents
Process for the purification of contaminated oils Download PDFInfo
- Publication number
- WO2003044141A2 WO2003044141A2 PCT/HU2002/000119 HU0200119W WO03044141A2 WO 2003044141 A2 WO2003044141 A2 WO 2003044141A2 HU 0200119 W HU0200119 W HU 0200119W WO 03044141 A2 WO03044141 A2 WO 03044141A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- oils
- purification
- adsorbent
- contaminated
- distillation
- Prior art date
Links
- 239000003921 oil Substances 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000000746 purification Methods 0.000 title claims abstract description 7
- 239000003463 adsorbent Substances 0.000 claims abstract description 9
- 238000004821 distillation Methods 0.000 claims abstract description 8
- 239000012535 impurity Substances 0.000 claims abstract description 8
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 7
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 239000004721 Polyphenylene oxide Substances 0.000 claims abstract description 4
- 229920000570 polyether Polymers 0.000 claims abstract description 4
- 238000001914 filtration Methods 0.000 claims abstract description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 5
- 229910021536 Zeolite Inorganic materials 0.000 claims description 3
- 239000000908 ammonium hydroxide Substances 0.000 claims description 3
- 229940043379 ammonium hydroxide Drugs 0.000 claims description 3
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical group O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 3
- 239000010457 zeolite Substances 0.000 claims description 3
- 239000005909 Kieselgur Substances 0.000 claims description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 2
- 239000012670 alkaline solution Substances 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 2
- 239000007791 liquid phase Substances 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 description 14
- 239000010687 lubricating oil Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 239000002585 base Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- 239000012071 phase Substances 0.000 description 4
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 3
- 238000005299 abrasion Methods 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 238000000354 decomposition reaction Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000011701 zinc Substances 0.000 description 3
- 229910052725 zinc Inorganic materials 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- 239000004411 aluminium Substances 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000012065 filter cake Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 150000001399 aluminium compounds Chemical class 0.000 description 1
- 229940077746 antacid containing aluminium compound Drugs 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 238000000998 batch distillation Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000004880 explosion Methods 0.000 description 1
- 239000003925 fat Substances 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 238000005187 foaming Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 238000005461 lubrication Methods 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- 239000011733 molybdenum Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000010773 plant oil Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000001577 simple distillation Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- -1 such as Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
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
Definitions
- the subject of the invention is a process for the purification of contaminated oils, such as, hydrocarbon oils or polyether oils.
- U.S. Patent 5,527,449 comprises the distillation of the mixture of waste oils, animal fats and plant oils simultaneously cracking of them.
- the resulted unstabilized material obtained this way can not be considered as a product and according to the description it needs further processing.
- Our target was to develop a procedure with low quantity of waste for cleaning the contaminated hydrocarbon oils and polyether oils with which the oils are purified from the toxic components and become applicable for energy-supply in ' general-purpose furnaces or become utilizable in other types of technologies.
- Impurity components of them comprise additives (containing zinc, magnesium, calcium, aluminium, sulphur, chlorine), abrasion residues (cadmium, iron, stannum, nickel, molybdenum, chromium, lead, copper, cobalt) and degradation products formed in use.
- the invention is based upon the recognition that after an treatment of the oils with a base, the separation of the liquid phases is not necessary, since the decomposition products in the aqueous phase can be adsorbed on an appropriate adsorbent and water can be separated by means of distillation without redissolving the impurities into the oily phase.
- Preferred adsorbents are diatomaceous earth or zeolite. The adsorbents with adsorbed impurity components and abrasion residues can then be filtered out as mechanical impurities.
- ammonium-hydroxide as a base makes more simple the process. Namely ammonium-hydroxide can be distilled off and recycled at the end of the process. Consequently the raw material cost of the process is lower and less dangerous waste is formed.
- the reactor is evacuated by the compressor 3 and filled with N . Under continuous and intensive stirring the reactor is heated up to 110 °C, while the steam generated as a result of heating is transferred under 4 bar pressure by the compressor 3 through the cooler and condensed (in the reactor the operational pressure is about 0,5 bar). The condensate (water and light hydrocarbon) is collected in the drain tank 4 till the end of dripping.
- Step 2 Degradation of impurities: Oil is then heated preferably to 150°C and from the alkali storage vessel 7 concentrated ammonia solution in a portion (w/w) from 5 to 15, preferably 10 is added to it and stirred vigorously for 30 min.
- Step 3) Removal of ammonia solution When the heating is completed the exhaust gases of the reactor 2 are transferred by the compressor 3 through the heat exchanger 8 and condensed. In order to avoid foaming of the content of the reactor a foam sensor is installed. NH OH is condensed in the heat exchanger and till the end of dripping it is collected in the drain tank 4 and then transferred into the alkali storage vessel 7.
- the holding tank 9 vents through the adsorbent 16.
- Oil is transferred into the mud filter 10, where in order to build up the necessary filter cake it is circulated for 10 to 120 min, preferably for 60 min.
- the filter cake having been built up the re-circulating section of the filtration loop is closed and from the filter the oil as a product is harvested through the heat exchanger 1 simultaneously pre-heating the sequential batch.
- Benefit of the process of the invention is that it can be carried out very easily and small quantity of waste is obtained while the concentration of abrasion residues, zinc and aluminium compounds and halogenated aliphatic hydrocarbons of contaminated oils is reduced.
Landscapes
- 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)
Abstract
The present invention relates to a process for the purification of contaminated oils, mainly hydrocarbon oils or polyether oils wherein the contaminated oil is treated by an base solution in the presence of an adsorbent and then water is removed by distillation without the separation of the liquid-phases and the impurities adsorbed on adsorbent are separated preferably by filtration. The oils purified by the process become applicable for energy-supply in commercial furnaces or become utilizable in other types of technologies.
Description
Process for the purification of contaminated oils
Field if the invention:
The subject of the invention is a process for the purification of contaminated oils, such as, hydrocarbon oils or polyether oils.
The handling of used lubricating oils (dead oils) continuously raises serious difficulties to the consumers, therefore great efforts have already been made for the purification of these wastes and for recycling them.
Background of the invention:
Extended experiments were performed in the 1970's for the regeneration of waste lubricating oils (dead oils) in Hungary, however those did not fulfil the expectations. Essentially the procedure consisted of the refinement of dead oils by sulphuric acid and then the re-admixture of them The quality of the obtained oil was very low and the regeneration procedure resulted in large quantity of wastes being dangerous to the environment, furthermore their handling and storage could hardly be solved. Further disadvantage of the procedure was that it was applicable only in cases of natural based lubricating oils having a low admixture level. Nowadays the powerful lubricating oils with high admixture levels are used and they very often made of synthetic base oils.
There are known procedures for the regeneration of the lubricating oil wastes comprising of concentrated base treatment. For example the French Patent No. 93 03275 and the Italian Patent No. MI92A002271 comprise the combination of an alkaline extraction with a batch distillation. Products of the process are the oily distillates taken at different boiling point range. Major disadvantage of the described procedures is that due to the inconsistent quality of the gathered lubricating oil wastes the manufacturing of lubrication oil in standard quality is very difficult. A further disadvantage of the processes is that the distillation residue as a waste is significantly high occasionally exceeding 30%.
U.S. Patent No. 08/925 279 and German Patent No. 198 52 007 describe procedures comprising the distillation of dead oils, then the extraction of distillate. Disadvantage of the procedures are similar to the ones described previously.
The process of U.S. Patent 5,527,449 comprises the distillation of the mixture of waste oils, animal fats and plant oils simultaneously cracking of them. The resulted unstabilized material obtained this way can not be considered as a product and according to the description it needs further processing.
The process disclosed in International Patent Application No. WO 9921945 comprises the distillation of oily wastes and cracking of them under hydrogen gas introduction. In this case the product is also equal to the distillate. In this case, due to the cracking, the quantity of the distillation residue is low relative to the simple distillation procedures described above. The high price of the hydrogen gas manufactured by the decomposition of hydrocarbons considerably reduces the economy of the process.
An other problem is that since these procedures have to be carried out in large scale in refinery plants, a centralised gathering of wastes is needed for processing, which further raises the costs of the procedure.
Summary of the invention:
Our target was to develop a procedure with low quantity of waste for cleaning the contaminated hydrocarbon oils and polyether oils with which the oils are purified from the toxic components and become applicable for energy-supply in 'general-purpose furnaces or become utilizable in other types of technologies.
The oily wastes evolve mainly as a result of running down of lubricating oils. Impurity components of them comprise additives (containing zinc, magnesium, calcium, aluminium, sulphur, chlorine), abrasion residues (cadmium, iron, stannum, nickel, molybdenum, chromium, lead, copper, cobalt) and degradation products formed in use.
It is known that after the treatment of oils with concentrated base the compounds containing zinc and aluminium, furthermore halogenated aliphatic hydrocarbons degrade
under the effect of bases and the decomposition products become extractable into the aqueous phase.
The invention is based upon the recognition that after an treatment of the oils with a base, the separation of the liquid phases is not necessary, since the decomposition products in the aqueous phase can be adsorbed on an appropriate adsorbent and water can be separated by means of distillation without redissolving the impurities into the oily phase. Preferred adsorbents are diatomaceous earth or zeolite. The adsorbents with adsorbed impurity components and abrasion residues can then be filtered out as mechanical impurities.
Our further recognition is that the application of ammonium-hydroxide as a base makes more simple the process. Namely ammonium-hydroxide can be distilled off and recycled at the end of the process. Consequently the raw material cost of the process is lower and less dangerous waste is formed.
A detailed demonstration of our invention is presented in the following example without limiting our claims only on it.
Example:
Step 1) Flashing point adjustment: Pre-heated 100 portion (w/w) of dead oil is introduced through the heat exchanger 2 into the reaction tank being equipped with a mixer 1. During introduction zeolite activated properly is mixed in 0.1-4 portion (w/w), preferably in 1 portion (w/w) into the oil stream. The reactor is evacuated by the compressor 3 and filled with N . Under continuous and intensive stirring the reactor is heated up to 110 °C, while the steam generated as a result of heating is transferred under 4 bar pressure by the compressor 3 through the cooler and condensed (in the reactor the operational pressure is about 0,5 bar). The condensate (water and light hydrocarbon) is collected in the drain tank 4 till the end of dripping. Phases of the collected condensate are separated and the upper phase is transferred into the hydrocarbon storage vessel 5 while the lower phase is transferred into the water storage tank 6. Condensates are handled as dangerous wastes (expected quantity is about 0-2 portion /w/w/ per batch). Explosion of the reactor is protected by the release valve 11 connected after the safety vessel 12, while other part of the equipment is protected by the release valve 13 venting through the scrubber 14 and adsorbent 15 being connected in series.
Step 2) Degradation of impurities: Oil is then heated preferably to 150°C and from the alkali storage vessel 7 concentrated ammonia solution in a portion (w/w) from 5 to 15, preferably 10 is added to it and stirred vigorously for 30 min.
Step 3) Removal of ammonia solution: When the heating is completed the exhaust gases of the reactor 2 are transferred by the compressor 3 through the heat exchanger 8 and condensed. In order to avoid foaming of the content of the reactor a foam sensor is installed. NH OH is condensed in the heat exchanger and till the end of dripping it is collected in the drain tank 4 and then transferred into the alkali storage vessel 7.
Step 4) Removal of impurities: Treated oil is pumped into the holding tank 9. The holding tank 9 vents through the adsorbent 16. Oil is transferred into the mud filter 10, where in order to build up the necessary filter cake it is circulated for 10 to 120 min, preferably for 60 min. When the filter cake having been built up the re-circulating section of the filtration loop is closed and from the filter the oil as a product is harvested through the heat exchanger 1 simultaneously pre-heating the sequential batch.
Benefit of the process of the invention is that it can be carried out very easily and small quantity of waste is obtained while the concentration of abrasion residues, zinc and aluminium compounds and halogenated aliphatic hydrocarbons of contaminated oils is reduced.
Claims
1.) A process for the purification of contaminated hydrocarbon oils or polyether oils wherein the purification comprises the treatment by alkaline solution, preferably by ammonium- hydroxide and adding of adsorbent for yield increasing and then removal of water by distillation and the impurities by filtration.
2.) A process of claim 1 wherein the adsorbent is zeolite or diatomaceous earth.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2002366004A AU2002366004A1 (en) | 2001-11-20 | 2002-11-13 | Process for the purification of contaminated oils |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| HU0105022A HU225697B1 (en) | 2001-11-20 | 2001-11-20 | Method for purifying of used oils |
| HUP0105022 | 2001-11-20 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2003044141A2 true WO2003044141A2 (en) | 2003-05-30 |
| WO2003044141A3 WO2003044141A3 (en) | 2003-07-17 |
Family
ID=89979917
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| PCT/HU2002/000119 WO2003044141A2 (en) | 2001-11-20 | 2002-11-13 | Process for the purification of contaminated oils |
Country Status (3)
| Country | Link |
|---|---|
| AU (1) | AU2002366004A1 (en) |
| HU (1) | HU225697B1 (en) |
| WO (1) | WO2003044141A2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008032129A1 (en) * | 2006-09-14 | 2008-03-20 | David Tamas | Improved method for purifying contaminated oils |
| NO20064993L (en) * | 2006-10-31 | 2008-05-02 | Due Miljoe As | Procedure for purifying oils and their use in food and feed |
| CN103146423A (en) * | 2013-04-01 | 2013-06-12 | 佛山市和挚承环保科技有限公司 | Method for regenerating and extracting waste mineral oil by filling nitrogen extracting |
| CN109957448A (en) * | 2017-12-26 | 2019-07-02 | 丰益(上海)生物技术研发中心有限公司 | A kind of crude oil cleaning technology |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1919655A (en) * | 1929-07-12 | 1933-07-25 | Bocjl Corp | Purification of oil |
| DE2704469A1 (en) * | 1977-02-03 | 1978-08-10 | Krupp Ag Huettenwerke | Reclamation of used phosphate hydraulic fluid - by treating with water, alkali and bleaching earth |
| WO1987004455A1 (en) * | 1986-01-27 | 1987-07-30 | Strahorn David A | Process for purifying used lubricating oil |
| FR2703067A1 (en) * | 1993-03-22 | 1994-09-30 | Sotulub | Method and installation for regenerating lubricating oils |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2619264B2 (en) * | 1988-06-23 | 1997-06-11 | トヨタ自動車株式会社 | Reprocessing of lubricating waste oil |
-
2001
- 2001-11-20 HU HU0105022A patent/HU225697B1/en not_active IP Right Cessation
-
2002
- 2002-11-13 WO PCT/HU2002/000119 patent/WO2003044141A2/en not_active Application Discontinuation
- 2002-11-13 AU AU2002366004A patent/AU2002366004A1/en not_active Abandoned
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1919655A (en) * | 1929-07-12 | 1933-07-25 | Bocjl Corp | Purification of oil |
| DE2704469A1 (en) * | 1977-02-03 | 1978-08-10 | Krupp Ag Huettenwerke | Reclamation of used phosphate hydraulic fluid - by treating with water, alkali and bleaching earth |
| WO1987004455A1 (en) * | 1986-01-27 | 1987-07-30 | Strahorn David A | Process for purifying used lubricating oil |
| FR2703067A1 (en) * | 1993-03-22 | 1994-09-30 | Sotulub | Method and installation for regenerating lubricating oils |
Non-Patent Citations (1)
| Title |
|---|
| PATENT ABSTRACTS OF JAPAN vol. 014, no. 131 (C-0700), 13 March 1990 (1990-03-13) & JP 02 004898 A (TOYOTA MOTOR CORP;OTHERS: 01), 9 January 1990 (1990-01-09) * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2008032129A1 (en) * | 2006-09-14 | 2008-03-20 | David Tamas | Improved method for purifying contaminated oils |
| NO20064993L (en) * | 2006-10-31 | 2008-05-02 | Due Miljoe As | Procedure for purifying oils and their use in food and feed |
| CN103146423A (en) * | 2013-04-01 | 2013-06-12 | 佛山市和挚承环保科技有限公司 | Method for regenerating and extracting waste mineral oil by filling nitrogen extracting |
| CN109957448A (en) * | 2017-12-26 | 2019-07-02 | 丰益(上海)生物技术研发中心有限公司 | A kind of crude oil cleaning technology |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2003044141A3 (en) | 2003-07-17 |
| HUP0105022A3 (en) | 2005-04-28 |
| HU225697B1 (en) | 2007-06-28 |
| HUP0105022A2 (en) | 2004-04-28 |
| HU0105022D0 (en) | 2002-01-28 |
| AU2002366004A1 (en) | 2003-06-10 |
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