WO2000052118A1 - Procede de traitement d'une huile utilisant un fluide a l'etat supercritique - Google Patents
Procede de traitement d'une huile utilisant un fluide a l'etat supercritique Download PDFInfo
- Publication number
- WO2000052118A1 WO2000052118A1 PCT/FR2000/000508 FR0000508W WO0052118A1 WO 2000052118 A1 WO2000052118 A1 WO 2000052118A1 FR 0000508 W FR0000508 W FR 0000508W WO 0052118 A1 WO0052118 A1 WO 0052118A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- oil
- fluid
- oils
- filtration
- supercritical
- Prior art date
Links
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
- C10M175/0058—Working-up used lubricants to recover useful products ; Cleaning by filtration and centrifugation processes; apparatus therefor
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/0025—Working-up used lubricants to recover useful products ; Cleaning by thermal processes
- C10M175/0041—Working-up used lubricants to recover useful products ; Cleaning by thermal processes by hydrogenation processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M175/00—Working-up used lubricants to recover useful products ; Cleaning
- C10M175/005—Working-up used lubricants to recover useful products ; Cleaning using extraction processes; apparatus therefor
Definitions
- the present invention relates to a method of treating an oil using a fluid in the supercritical state.
- the invention relates to a process for refining an oil in order to separate the pollutants therefrom and to recover a refined oil.
- the method according to the invention makes it possible to treat organic, biological as well as mineral oils and applies, in particular, to the re-refining of petroleum oils and in particular used motor oils and using C0 2 in the supercritical state.
- the technical field of the invention can be defined as that of the treatment of oils in order to remove pollutants therefrom and to obtain a refined oil and interesting compounds.
- oils in particular petroleum oils
- the refining of oils essentially uses distillation operations and catalyzed stages, such as catalytic hydrogenation.
- the distillation can be vacuum or atmospheric distillation.
- gases When gases are used at medium or high pressure, they are generally light alkanes and hydrogen.
- the object of the invention is to provide a method of treating an oil which meets, inter alia, all of the needs mentioned above, which does not have the drawbacks, limitations, defects and disadvantages of the methods of prior art and which solves the problems of the processes of the prior art.
- a process for treating an oil comprising an initial step of bringing said oil into contact with a fluid in the supercritical state, in order to separate a light fraction, heavy fraction and majority intermediate fraction; then the processing of said intermediate fraction in separation and / or reaction stages, said stages all being carried out in the presence of said fluid in the (in phase) supercritical state. Due to the implementation of the fluid in the supercritical state in all the stages of the process, a significant overall energy gain is obtained by the process of the invention.
- This gain is also due to the fact that the same operating conditions or quasi-constant operating conditions are generally implemented throughout the process, that is to say during the initial step and subsequent processing steps. , which avoids variations in temperature and pressure and optimizes energy.
- the dissolution of 15% by mass of C0 2 in the liquid phase will cause an increase in the total volume by a factor of approximately 1.15 , but at the same time, a reduction in viscosity by a factor of 4 to 5.
- the constant operating conditions depend on the fluid in the supercritical state used and are, for example, from 50 to 350 bars and from 40 to 200 ° C, preferably from 150 to 200 bars and from 60 to 150 ° C, more preferably from 60 to 120 ° C, in the case where the supercritical fluid is C0 2 .
- the use of the same operating conditions from the start to the end of the process makes it possible to avoid the compression, expansion, decompression stages inherent in conventional processes.
- the almost constant operating conditions are generally those prevailing in the initial stage.
- the initial contacting step is a liquid-fluid extraction step in the supercritical state which is preferably carried out in a column against the current.
- the stage or stages of distillation of conventional processes for refining fluid oils is (are) replaced by a stage of extraction with C0 2 which is much more advantageous for energy consumption.
- the so-called intermediate fraction which is generally the majority fraction of the oil, is then treated first by filtration, generally by tangential monophasic filtration.
- filtration generally by tangential monophasic filtration.
- This operation takes advantage of the lowering of the viscosity due to the solubilization of the gas under pressure in the oil causing a fluidization of the oily medium.
- This single-phase filtration makes it possible, for example, in the case of the treatment of petroleum oils, such as used engine oils, to retain in particular the metals and the asphaltenes which were not precipitated during the initial stage d 'extraction.
- the retentate from said single-phase tangential filtration is subjected to a biphasic filtration, after addition of excess supercritical fluid, whereby one obtains at the end of this biphasic filtration operation, as concentrate a very viscous or solid residue and, as a permeat, a purified high viscosity liquid.
- high viscosity is generally meant a viscosity greater than or equal to 120 cSt at 40 ° C.
- This biphasic filtration operation is an important step in the process according to the invention and it also takes advantage of the lowering of the viscosity of the liquid treated during this step.
- the permeate consisted only of the liquid phase containing little fluid (such as CO), namely generally from 15 to 20%, while the biphasic mixture of the retentate generally contains from 80 to 95%.
- the biphasic filtration according to the invention is particularly beneficial, since the energy necessary for recycling the fluid, such as C0 2 , remains low and corresponds to the proportion actually dissolved and not to the total proportion present in the retentate.
- the permeate when the mixture (which constitutes the retentate) conveyed on the membrane is composed of 80 to 95% of fluid, such as C0 2 , it would be logical that the permeate has the same proportions, or even contains a higher proportion of -fluid, such as C0 2 , which is the smaller compound of the mixture.
- the permeate consists of an oily liquid monophase containing only 15 to 20% of C0 2 found in dissolved form. This unexpected effect makes biphasic filtration energetically profitable. This unexpected effect is neither suggested nor mentioned in the prior art.
- the second unexpected effect of this biphasic filtration step is the fact that a highly viscous residue, generally solid and "dry", for example of bitumen type, is obtained as a concentrate.
- the residue for example of the bituminous type obtained during biphasic filtration, generally corresponds to a concentration of the retentate from 10 to 100 times, preferably from 20 to 60 times.
- the polluting compounds are coated in an extremely stable matrix and the whole can be considered to be chemically and physically inert and stable under ambient atmospheric conditions.
- the residue for example of the bituminous type, can be recovered by conventional channels and reused for the manufacture of roads, joints and others.
- the residue is subjected to expansion in order to separate the fluid, such as C0 2 , which it contains, with a view to its recycling.
- the permeate from this two-phase filtration operation is recovered. This is, for example in the case of the treatment of a petroleum oil, of a “Bright stock” type product, with a viscosity generally greater than or equal to 120 cSt at 40 ° C.
- this permeate is generally subjected to expansion in order to separate the fluid such as C0 2 , which it contains, in view of its recycling to the initial stage.
- the permeate resulting from the monophasic tangential filtration operation and which essentially comprises the intermediate compounds of the oil is subjected to a nanofiltration operation.
- nanofiltration has the meaning generally known in this field of the technique: that is to say that it is a filtration carried out on an organic or mineral membrane - preferably mineral in the process of l invention - whose pore diameter is generally 0.5 to 3 n.
- nanofiltration of the intermediate compounds is essentially to separate them as a function of their average molar mass which varies, for example, from 200 to 600 g.mol -1 .
- the retentate resulting from this nanofiltration operation essentially comprises the intermediate compounds of medium viscosity which are also the heavier and have the highest boiling point.
- this fraction has a viscosity of the order of 50 to 80 cSt at 40 ° C.
- this fraction corresponds to petroleum fractions obtained conventionally by distillation, the viscosity of which is the highest.
- the permeate of this nanofiltration operation essentially comprises the intermediate compounds of low viscosity, by low viscosity, it is generally understood that this fraction has a viscosity of the order of 20 cSt at 40 ° C.
- Said retentate and said permeate, coming from the nanofiltration operation, are then subjected to a refining or purification operation comprising, for example, adsorption on solid particles, for example, on activated earth, or a catalytic treatment , preferably a catalytic hydrogenation or hydrorefining.
- this step is a step carried out in a biphasic medium in the presence of fluid in the supercritical state, which implements a solid phase and a liquid phase, instead of three phases, namely a solid phase, a phase liquid (adsorbed or not) and a gas phase, in conventional processes.
- the liquid is fluidized by the fluid, such as dissolved C0 2 , which itself contains the cosolubilized hydrogen.
- the fluid such as dissolved C0 2
- the liquid phase contains a mixture of fluid, such as C0 2 and hydrogen dissolved in the required proportions, namely, for example, from 5 to 80 mol%, preferably from 7 to 50 mol%.
- the dissolved hydrogen is directly in contact with the molecules of the oil to be treated, for example the hydrocarbon molecules, in order to carry out the chemical reaction, such as hydrogenation, unlike what happens when hydrogen is in gaseous form.
- the catalyst is separated by filtration, then optionally recycled in the catalytic treatment stage.
- This filtration is generally a microfiltration and has the essential aim of separating the catalyst fines from the refined oil resulting from the catalytic treatment.
- the separated catalyst fines are returned to the catalytic treatment steps, for example, catalytic hydrogenation or refining.
- This catalyst is contained in the retentate of these filtration operations of the catalyst by filtration, and this retentate resulting from filtration is thus recycled with the catalyst to the catalytic treatment.
- the permeate obtained in these catalyst filtration operations is formed from a refined oil of low viscosity, that is to say generally from 20 to 40 cSt at 40 ° C or of medium viscosity, that is to say generally from 40 to 80 cSt at 40 ° C; these oils constitute the final product of the process according to the invention.
- This final product, or valued main fraction, which is in fact formed by all of the intermediate fractions treated and refined corresponds substantially to a depolluted base oil, for example, free of metallic compounds, and which generally represents 85 to 95% of the mass of the initial oil charge.
- Refined oil of low or medium viscosity is generally subjected to an expansion, in order to separate the fluid, such as the C0 2 which it contains, with a view to its recycling towards the initial stage.
- the heavy fraction resulting from the initial separation step, is separated by decantation, precipitation under the action of gravity, at the bottom of said extraction column against the current.
- This heavy fraction generally includes the heaviest compounds, such as tars and solids.
- the heavy fraction is discharged from the bottom of the column, preferably continuously, and it can optionally be mixed with the retentate of the monophasic tangential filtration to undergo the biphasic filtration.
- the light fraction extracted from the oil resulting from the initial separation step is generally treated by successive detents to separate the light compounds from the oil, while the fluid, such as the recovered C0 2 , is recycled to the initial stage of the process after being reconditioned to the supercritical state.
- Successive detents may be, for example, 1 to 3 in number.
- oil treated by the process of the invention can be any and can be chosen from both organic and mineral oils.
- oil or oily product according to the invention generally means products mainly composed of triglycerides, or else aromatic, naphthenic or paraffinic hydrocarbons, glycol products, glycol esters alone or in mixtures or any other organic solvent. .
- These products can contain water in varying concentrations, for example, from 0 to 80%, preferably from 0 to 50%.
- This organic oil can be chosen from these vegetable organic oils, and animal oils.
- the organic vegetable oils are generally chosen from triglyceride oils, such as sunflower oil, peanut oil, rapeseed oil, corn oil, olive oil, copra, palm oil, and non-triglyceride oils, such as jojoba oil.
- the organic animal oils are generally chosen from oils from fish, marine mammals, terrestrial mammals, such as beef, pork or mutton oils, etc.
- the oil treated by the process of the invention is preferably a mineral oil comprising petroleum products, more preferably it is a used engine oil.
- the process according to the invention is then defined as being a process for re-refining used motor oils, the aim of such a process being to rid the oil of light fractions or gasolines (that is to say of “Desessencier” the oil) and pollutants: asphaltenes, metals, solids they contain, in order to recover a refined oil or oils (possibly reusable).
- the fluid in the supercritical state is generally chosen from C0 2 , N? 0, SF 6 and the other gaseous compounds, which are not completely miscible in the oily liquid phase.
- the preferred fluid is C0 2 , in particular when the treatment of an oil comprising petroleum products is carried out, such as a used engine oil.
- the safety of the process of the invention is thus improved due to the reduction of fire risks, thanks to the permanent presence in all stages of the process of a compound, neither fuel nor fuel, such as C0 2 - This can also replace the light alkanes usually used in certain stages refining with the same positive influence on process safety.
- the supercritical fluid such as C0 2
- the supercritical fluid can be used alone or at least one solvent compound can be added to the supercritical fluid.
- Said solvent compound is chosen, for example, from alcohols of 1 to 5 carbon atoms, ketones, such as acetone, alkanes of 1 to 5 carbon atoms, alkenes of 2 to 5 carbon atoms, aromatic compounds of 6 to 10 carbon atoms and, in general, among all the compounds miscible with the liquid solution under pressure constituted by the oil and the supercritical fluid.
- Figure 1 is a diagram of the method according to the invention.
- Figure 2 is a graph showing the evolution of the flux density D in kg.h _ ⁇ .m -2
- a liquid phase essentially comprising the oil and, on the other hand, a phase supercritical essentially comprising C0 2 is carried out in the counter-current column (1).
- the oil to be treated is introduced at the top (2), and flows downwardly (3) into the column, while the supercritical fluid, for example C0 2 , is introduced at the bottom of this column
- the optimal operation of the column is generally at a pressure of 100 bars to 300 bars for a temperature of 40 to 150 ° C, preferably the pressure is 150 to 200 bars and the temperature of 60 ° C to 120 ° C.
- the density of pure C0 2 is then close to 600 to 700 kg.m "3 , creating a difference in density between the liquid phase rich in oil, and the supercritical phase, rich in C0 2 , close to 250 to 300 kg .m -3 .
- the temperature and pressure are the same as those described above in the context of setting up phase contact.
- the important parameter is the ratio of the C0 2 and oil flow rates.
- This ratio typically ranges from 1 to 50, preferably from 3 to 10.
- a flow rate ratio C0 2 of oil equal to 10 and with a suitably chosen interior trim (e.g. type Sulzer BX ®), the specific flow rate of will be close to
- the counter-current column may or may not be equipped with a thermal reflux zone at the top, the aim of which is to concentrate the lightest fractions.
- the light and aromatic compounds are removed at the top of the column (8) and are subjected to a stepwise separation in separators (9, 10, 11).
- the stepped separation makes it possible to lower, by a succession of stages, for example in three stages (9, 10, 11), the density of C0 2 • This lowering of the density can be achieved by a series of concentric detents to reheating, or only by reheating the supercritical phase.
- the water sets at the first separator and is evacuated with the products Cil to C14 (12).
- these extracts will be richer in aromatic compounds. This is interesting because at the same time the intermediate compounds are enriched with paraffinic molecules which promote the obtaining of a good viscosity index of the final oil.
- the CO 2 is recycled (15) either by pumping or by compression and returned to the contacting column against the current (1).
- a fraction is recovered which contains the predominantly paraffinic intermediate compounds.
- This fraction is subjected to a single-phase filtration operation (16) of the intermediate compounds, in order to retain metals and asphaltenes.
- This filtration is generally a tangential filtration operation, the operating conditions of which will be fixed by the previous step.
- the pressure is generally 150 to 200 bars, and the temperature from 60 to 120 ° C.
- the transmembrane pressure has a value generally between 1 and 10 bars.
- the membrane used is a microfiltration or ultrafiltration membrane, preferably an inorganic membrane, the cutoff threshold of which is preferably from 50 kD to 300 kD.
- the filtrate flow will vary as the concentration sought.
- the permeate obtained (17), which is purified from the polluting metals initially contained, is directed to a nanofiltration operation (18).
- the retentate (19) obtained during the monophasic filtration operation of the fraction containing the intermediate compounds, described above, is subjected to a tangential or even frontal biphasic filtration operation (20).
- the heavy settling residues from the column (1) taken from (6) are added (21) to this retentate from the single-phase filtration.
- this two-phase filtration operation must be preceded by an addition (22) of excess CO 2 to lead to the two phases present at the membrane level, namely: the phase consisting of supercritical C0 2 (or possibly liquid ) and the phase consisting of the oil, pollutants, heavy compounds and possibly dissolved C0 2 mixture.
- This second phase can take on a bituminous or purely solid appearance when all the oil present has been removed and an ultimate dry residue is then obtained.
- phase C0 2 The role of phase C0 2 is to constitute a sufficiently dense medium to convey the second phase consisting essentially of oil and pollutants at the start of filtration or pollutants in essentially solid form at the end of filtration.
- the mixture of the two phases is easily pumpable, in order to achieve a tangential speed of 3 to 6 m. s -1 in the membrane, the densities of one and the other must be sufficiently close.
- This Bright Stock (24) can undergo a discoloration treatment by adsorption (37) on activated earth whose purpose is to trap polar, oxygenated or sulfur compounds.
- the fluidization of Bright Stock by dissolved C0 2 is beneficial from an energy point of view by reducing the pressure drops in the adsorbent bed.
- the “Bright Stock” (24) possibly treated by adsorption (37) is expanded (41) in order to separate the included C0 which is recycled to the column (4) by the pipes (43) and (15) .
- the permeate from the monophasic filtration step (17) is subjected to nanofiltration (18) of the intermediate compounds, in order to separate them according to their average molar mass ranging from 200 to 600 g.mol "1.
- This step is carried out under the operating conditions of single-phase filtration (16), that is to say generally from 150 to 200 bars and from 60 to 120 ° C, using a membrane whose cut-off threshold is close to 400 g.
- ol -1 preferably a mineral membrane.
- the transmembrane pressure is between 5 and 50 bars.
- the heaviest compounds will be mainly retained by the membrane. These compounds are also those whose boiling point is They correspond to the petroleum fractions traditionally obtained by distillation with the highest viscosity. This step therefore makes it possible to obtain a fraction of medium viscosity (25), conventionally of the order of 50 to 80 cSt at 40 °. C, and a more fluid fraction (26) whose viscosity is lower on the order of 20 cSt at 40 ° C.
- the medium viscosity (25) and low viscosity (26) fractions obtained at the end of the nanofiltration step (18) are subjected to a refining operation, of adsorption type on activated earth, or of hydrogenation type. catalytic (at 27, respectively 28) or hydrorefining in H 2 / C0 2 medium, the hydrogen being supplied respectively by the pipes (29) and (30) in the catalytic hydrogenation reactors (27) and (28).
- This step is carried out if possible under operating conditions close to those used during the single-phase filtration operation, that is to say from 150 to 200 bars and from 60 to 120 ° C.
- the porous medium also serves as a hydrogen diffuser or as a C0 2 and H 2 mixer.
- the liquid medium is fluidized by dissolved C0 2 .
- the catalysts and supports used in this step are known to those skilled in the art and will not be described in more detail, by way of example there may be mentioned: Ni, Mo, Pt, Ag, etc., fixed on particles of Si0 2 , A1 2 0 3 , and other ceramics.
- the catalyst fines from the hydrorefining operations are then separated. This separation is essential in the case of catalytic reactions in a fluidized bed.
- the retentates (33, 34) from the two filtration operations (31, 32) of catalyst fines are recycled to the hydrorefining operations (27, 28).
- the permeates obtained respectively by filtration of the hydrorefining product of the medium viscosity fraction (25) and by filtration of the hydrorefining product of the low viscosity fraction (26) are recovered respectively in the form of a refined oil of viscosity from 50 to 80 cSt (35) and a refined oil with a viscosity of around 20 cSt (36).
- a de-essenced paraffinic used oil that is to say having previously undergone a counter-current column extraction operation, which can be considered as standard, is treated.
- the analytical characteristics of this oil are grouped in Tables I, II and III, below.
- the viscosity of this oil at 40 ° C is 57 cSt for an average molar mass of 426 g.mol "1 and its total metal content, coming from the wear of engines and additives is close to 5000 ppm.
- This oil is treated by a single-phase filtration operation under the following conditions:
- the initial flow of filtrate at equilibrium is close to 55 kg.h -1 .m -2 and when the concentration factor is of the order of 10, the flow of filtrate drops to a value close to 10 kg. h "1 .m -2 (see also figure 2).
- Table IV shows the metal concentrations in the feed and the permeate and shows the decrease in the metal content and the lowering of the viscosity after the filtration operation.
- the permeate obtained is purified from the polluting metals initially contained.
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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)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Lubricants (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Extraction Or Liquid Replacement (AREA)
- Fats And Perfumes (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2000602731A JP2002538267A (ja) | 1999-03-02 | 2000-03-01 | 超臨界状態の流体を用いたオイル処理方法 |
EP00909398A EP1165728A1 (fr) | 1999-03-02 | 2000-03-01 | Procede de traitement d'une huile utilisant un fluide a l'etat supercritique |
NO20014201A NO20014201L (no) | 1999-03-02 | 2001-08-29 | Fremgangsmåte for å behandle en olje ved å anvende et fluid i superkritisk tilstand |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR99/02558 | 1999-03-02 | ||
FR9902558A FR2790479B1 (fr) | 1999-03-02 | 1999-03-02 | Procede de traitement d'une huile utilisant un fluide a l'etat supercritique |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2000052118A1 true WO2000052118A1 (fr) | 2000-09-08 |
Family
ID=9542701
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2000/000508 WO2000052118A1 (fr) | 1999-03-02 | 2000-03-01 | Procede de traitement d'une huile utilisant un fluide a l'etat supercritique |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP1165728A1 (fr) |
JP (1) | JP2002538267A (fr) |
FR (1) | FR2790479B1 (fr) |
NO (1) | NO20014201L (fr) |
WO (1) | WO2000052118A1 (fr) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
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EP1245662A2 (fr) * | 2001-03-31 | 2002-10-02 | Clariant International Ltd. | Additifs à base de pétrole brut améliorant l'écoulement à froid du brut et des distillats pétroliers |
US7045038B1 (en) | 1999-12-21 | 2006-05-16 | Industrial Microwave Technologies, Inc. | Process for treating waste oil |
WO2011110585A1 (fr) | 2010-03-10 | 2011-09-15 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procede de regeneration d'une charge hydrocarbonee |
WO2011161378A1 (fr) | 2010-06-22 | 2011-12-29 | Societe De Conception D'equipements Pour L'environnement Et L'industrie | Procédé de purification d'une charge hydrocarbonée usagée |
ES2395320A1 (es) * | 2011-07-14 | 2013-02-11 | Soluciones Extractivas Alimentarias, S.L. | Nuevo método para la reducción de contaminantes en grasas y aceites a partir de aceites y sus derivados. |
CN109456785A (zh) * | 2018-08-29 | 2019-03-12 | 山西洪旭环保科技有限公司 | 一种工业危废hw11类及hw08类危险废弃物的处置方法 |
CN115838600A (zh) * | 2022-12-07 | 2023-03-24 | 陕西延长石油(集团)有限责任公司 | 超临界二氧化碳混合煤焦油预处理降粘除杂系统及方法 |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT514774B1 (de) * | 2013-08-30 | 2016-08-15 | Avl List Gmbh | Betriebsmittel für einen Kondensationskernzähler für Abgase von Verbrennungsmotoren |
KR102350370B1 (ko) * | 2021-06-21 | 2022-01-14 | 김진성 | 폐산성백토의 재생방법 |
EP4183462A1 (fr) | 2021-11-23 | 2023-05-24 | TotalEnergies OneTech | Procédé de désodorisation d'huiles lubrifiantes régénérées utilisant du co2 supercritique |
EP4183463A1 (fr) | 2021-11-23 | 2023-05-24 | TotalEnergies OneTech | Procédé de régénération de lubrifiants usagés à l'aide de co2 supercritique |
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GB2032789A (en) * | 1978-10-09 | 1980-05-14 | Krupp Gmbh | Method of refining crude vegetable fats and oils |
EP0055492A1 (fr) * | 1980-12-31 | 1982-07-07 | Phillips Petroleum Company | Procédé pour la régénération des huiles de moteur usagées |
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WO1991018067A1 (fr) * | 1990-05-16 | 1991-11-28 | The Procter & Gamble Company | Extraction liquide/liquide a contre-courant pour fractionner des melanges complexes contenant des triglycerides d'acide gras a chaines moyennes et longues |
WO1993022022A1 (fr) * | 1992-04-29 | 1993-11-11 | Institut Français Du Petrole | Procede et dispositif de fractionnement d'un melange en lit mobile simule en presence d'un gaz comprime, d'un fluide supercritique ou d'un liquide subcritique |
WO1996018445A1 (fr) * | 1994-12-12 | 1996-06-20 | Commissariat A L'energie Atomique | Procede et installation de separation de composes lourds et legers, par extraction par un fluide supercritique et nanofiltration |
WO1998032819A1 (fr) * | 1997-01-28 | 1998-07-30 | Norsk Hydro Asa | Epuration de glycerides d'acides gras polyinsatures |
WO1998046337A1 (fr) * | 1997-04-15 | 1998-10-22 | Commissariat A L'energie Atomique | Procede et installation de filtration tangentielle d'un liquide visqueux |
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1999
- 1999-03-02 FR FR9902558A patent/FR2790479B1/fr not_active Expired - Lifetime
-
2000
- 2000-03-01 JP JP2000602731A patent/JP2002538267A/ja not_active Withdrawn
- 2000-03-01 EP EP00909398A patent/EP1165728A1/fr not_active Withdrawn
- 2000-03-01 WO PCT/FR2000/000508 patent/WO2000052118A1/fr not_active Application Discontinuation
-
2001
- 2001-08-29 NO NO20014201A patent/NO20014201L/no unknown
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US7045038B1 (en) | 1999-12-21 | 2006-05-16 | Industrial Microwave Technologies, Inc. | Process for treating waste oil |
EP1245662A2 (fr) * | 2001-03-31 | 2002-10-02 | Clariant International Ltd. | Additifs à base de pétrole brut améliorant l'écoulement à froid du brut et des distillats pétroliers |
DE10116267A1 (de) * | 2001-03-31 | 2002-10-10 | Clariant Internat Ltd Muttenz | Additive auf erdöleigener Basis zur Verbesserung der Kaltfließeigenschaften von Roh- und Destillatölen |
EP1245662A3 (fr) * | 2001-03-31 | 2004-01-02 | Clariant International Ltd. | Additifs à base de pétrole brut améliorant l'écoulement à froid du brut et des distillats pétroliers |
US6803492B2 (en) | 2001-03-31 | 2004-10-12 | Clariant International Ltd. | Additives based on components present in petroleum for improving the cold flow properties of crude and distillate oils |
WO2011110585A1 (fr) | 2010-03-10 | 2011-09-15 | Commissariat A L'energie Atomique Et Aux Energies Alternatives | Procede de regeneration d'une charge hydrocarbonee |
FR2957353A1 (fr) * | 2010-03-10 | 2011-09-16 | Commissariat Energie Atomique | Procede d'elimination d'un ou plusieurs composes contenus dans une charge hydrocarbonee |
WO2011161378A1 (fr) | 2010-06-22 | 2011-12-29 | Societe De Conception D'equipements Pour L'environnement Et L'industrie | Procédé de purification d'une charge hydrocarbonée usagée |
ES2395320A1 (es) * | 2011-07-14 | 2013-02-11 | Soluciones Extractivas Alimentarias, S.L. | Nuevo método para la reducción de contaminantes en grasas y aceites a partir de aceites y sus derivados. |
US9309484B2 (en) | 2011-07-14 | 2016-04-12 | Soluciones Extractivas Alimentarias, S.L. | Process for reducing pollutants in fats and oils and their derivatives |
CN109456785A (zh) * | 2018-08-29 | 2019-03-12 | 山西洪旭环保科技有限公司 | 一种工业危废hw11类及hw08类危险废弃物的处置方法 |
CN115838600A (zh) * | 2022-12-07 | 2023-03-24 | 陕西延长石油(集团)有限责任公司 | 超临界二氧化碳混合煤焦油预处理降粘除杂系统及方法 |
Also Published As
Publication number | Publication date |
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NO20014201D0 (no) | 2001-08-29 |
FR2790479B1 (fr) | 2001-04-13 |
JP2002538267A (ja) | 2002-11-12 |
EP1165728A1 (fr) | 2002-01-02 |
FR2790479A1 (fr) | 2000-09-08 |
NO20014201L (no) | 2001-11-02 |
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