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WO2022248698A1 - Procédé et dispositif destinés à la purification d'huile usagée - Google Patents

Procédé et dispositif destinés à la purification d'huile usagée Download PDF

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Publication number
WO2022248698A1
WO2022248698A1 PCT/EP2022/064463 EP2022064463W WO2022248698A1 WO 2022248698 A1 WO2022248698 A1 WO 2022248698A1 EP 2022064463 W EP2022064463 W EP 2022064463W WO 2022248698 A1 WO2022248698 A1 WO 2022248698A1
Authority
WO
WIPO (PCT)
Prior art keywords
bath
oil
rectification column
reactor
waste oil
Prior art date
Application number
PCT/EP2022/064463
Other languages
German (de)
English (en)
Inventor
Michael Richter
Original Assignee
Biofabrik Black Refinery Gmbh
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Biofabrik Black Refinery Gmbh filed Critical Biofabrik Black Refinery Gmbh
Publication of WO2022248698A1 publication Critical patent/WO2022248698A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B01D1/0041—Use of fluids
    • B01D1/0052—Use of a liquid transfer medium or intermediate fluid, e.g. bain-marie
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/02—Evaporators with heating coils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/30—Accessories for evaporators ; Constructional details thereof
    • B01D1/305—Demister (vapour-liquid separation)
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
    • B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
    • B01D3/322—Reboiler specifications
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/006—Distillation of hydrocarbon oils of waste oils other than lubricating oils, e.g. PCB's containing oils
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/06—Vacuum distillation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • C10G2300/1007—Used oils

Definitions

  • the invention relates to the processing of waste oil within the meaning of the Waste Oil Ordinance.
  • oils that are generated as waste and consist entirely or partly of mineral oil, synthetic or biogenic oil.
  • this includes liquid, oily residues such as contaminated diesel, heating oil or shipping oils.
  • This waste oil is used as a feedstock in the process.
  • the cleaning of the used oil can be done via pure
  • Distillation can take place without changing the molecular structures.
  • the invention can also be used in a temperature range in which so-called cracking takes place, i.e. long molecular chains are broken up into shorter ones.
  • the invention relates to a method for cleaning waste oil, in which the starting material is heated to the gas phase and the resulting vapor is rectified, with cleaned oil being removed as condensate from a vent in a rectification column.
  • the invention also relates to a device for cleaning used oil with a main reactor and a rectification column connected to it.
  • DE 19820 635 A1 discloses a process for processing used oil, in which the used oil is subjected to a rough cleaning and subsequent drying, then thermally cracked at 400 to 500° C. and the cracked product is subjected to distillation. To lower the chlorine content alkaline compounds are added to the pre-cleaned waste oil.
  • the starting material comes into contact with a hot gas via a heat exchanger.
  • a heat exchanger For sufficient heating of the starting material, it is necessary to choose such a temperature difference that allows heating up to the target temperature.
  • the inner tube of the heat exchanger tends to clog because combustion residues adhere to the inside.
  • the outside is also exposed to heavy stress from the heating gas. This results in a not inconsiderable maintenance effort. This is not a problem in large stationary plants, since several reactors can be used, so that one or more are always available for operation, even if others have to undergo maintenance. In smaller and mobile systems the choice of such a redundancy is not possible, but at least disadvantageous.
  • DE 102012 008 458 A1 discloses a reactor for gasifying starting material which is filled with a filler and a metal which can be brought into the liquid phase by external heating elements.
  • the starting material is introduced into this liquid metal bath on the underside. It is intended to use solid starting material in granular form. This starting material will undergo depolymerization due to the temperature of the metal bath.
  • the starting material thereby changes to the liquid phase and, due to the delayed penetration of the filler, into the vapor phase and is condensed in a condenser into an output material and collected in an accumulator.
  • EP 0592 057 B1 describes a method in which solid starting material is also subjected to pyrolysis in a metal bath.
  • WO 2014/106650 A2 describes a process for converting hydrocarbon-containing starting material into oil, also in a metal bath.
  • a treatment of waste oil as a starting material with a metal bath is known from WO 2020/104472 A1, the content of which is included here.
  • a disadvantage is seen in their disclosure, according to which the starting material was fed directly through the melt bath, that acidifiers and other uncontrollable side reactions occur, which lead to the product quality suffering. Carbon deposits also occur on the outer wall. This causes the carbon to form an insulating layer, which can burn through the heating sleeves. The object of the invention is then to avoid the disadvantages of the prior art.
  • the method can combine known methods of the crude oil industry with a depolymerization method of hydrocarbon-containing raw materials designed according to the invention and so-called cold cracking technologies.
  • Plastics are usually made from petroleum and - to put it simply - their hydrocarbons are linked together (polymerization) in such a way that solid materials are made from a formerly liquid substance. Depolymerization reverses this process. The chains are going through
  • oils medium length
  • waxes lightly longer chains, also liquid when heated
  • gases very short chains
  • the inventive method provides that the waste oil as Starting material used and an evaporation by at least indirect contacting of the starting material with a molten bath whose melting temperature is above the evaporation temperature but below the ignition temperature of the waste oil, and the vapor is rectified in the rectification column.
  • the used oil is distilled in the process.
  • the special energy input system in the main reactor ensures very controllable and rapid heating of the used oil.
  • the process is carried out under vacuum.
  • a procedural solution had to be created in which the products distilled off under vacuum are continuously transported into an atmospherically open environment.
  • the starting material is supplied to the molten bath indirectly, in that it is passed through the molten bath without a direct connection and via a thermally conductive connection with the latter.
  • This thermally conductive evaporation ensures an even transfer of energy into the waste oil, which prevents slagging on the heat exchanger surfaces and, at least as a result, significantly reduces the maintenance effort.
  • the gas phase is separated into predefined and controlled fractions of high to low boilers in a special rectification process previously reserved for the heavy oil industry. This is how different distillate qualities are created. Fuels suitable for engines are discharged, unclean fractions can repeat the process until they are also completely separated into usable and waste components. The different oil fractions are further depending on the area of application refined or delivered to distributors or end customers in the form of finished products. In the waste discharge, 5 to 10 percent of the raw material accumulates as tar-like waste. This can be used for bitumen production in road construction or as a substitute fuel. No other waste is generated.
  • the focus of the invention is the use of the rectification process in the small plant sector, combined with melt bath evaporation.
  • the main reactor is designed as a melt bath evaporator, in that a reactor chamber is filled with a melt bath material whose melting temperature is above the evaporation temperature but below the ignition temperature of the waste oil, the reactor chamber is provided with a heating device and in the reactor there is an inlet for the Waste oil is arranged.
  • the dividing wall is formed by a long spiral in which the input material is circulated at high speed and lies in the molten bath, with the molten bath being formed by a stainless steel tube which is filled with liquid metal and fitted with heating sleeves on the outside and which Melting pool absorbs the energy and absorbs it over the entire spiral distributed.
  • the high convection energies for heat transfer that occur in molten baths are able to supply the stored energy to the fluid to be evaporated in milliseconds.
  • the solution to the problem according to the invention is aimed at avoiding the interruption of operating times.
  • the metal bath losses that occur in continuous operation are counteracted in molten bath reactors.
  • baffle plates are placed one behind the other above the molten bath in the steam flow direction, each of these baffle plates having a lateral opening and these openings being offset in such a way that they do not lie one above the other in the steam flow direction, but cover one another.
  • the baffle plates can be arranged in the reactor space of the main reactor.
  • a metal bath return can also be provided.
  • the metal bath return is a component that was specially built for this application in order to collect the smallest amounts of liquid metal in the reactor space above the metal bath surface and to feed it back into the reactor zone. Despite the steel balls, small amounts can still occur, which get caught in the metal bath return and returned to the reactor are returned.
  • the component ensures that gas can flow through but liquid metal is trapped and flows back into the actual metal bath.
  • thermal energy is introduced into the waste oil through thermal conduction, whereby the excellent properties of the molten bath, which equalize the temperature differences, are used to cause evaporation without slagging or similar phenomena occurring at the thermally conductive connection, as is the case, for example, with the known tube furnaces is the case.
  • a heat exchanger can be introduced into the reactor space of the main reactor, which has an inlet and an outlet, the inlet forming the inlet for the waste oil and the outlet of which opens into the inlet of the rectification column.
  • a heat exchanger of this type achieves a highly efficient and uniform input of energy into the used oil, without there being any losses in the melt pool as a result of gas bubbles bursting in the melt pool.
  • the heat exchanger can be designed as a tube whose one side is the entrance and the other side is the exit. This tube can be spirally wound.
  • the molten bath in particular a metal bath, surrounds the heat exchanger.
  • the molten pool causes the uniform input of energy, because newly fed in waste oil must first be heated.
  • the large thermal capacity of the melt pool allows the waste oil to be heated quickly without the temperature of the melt pool falling significantly or slagging when the energy is input.
  • the invention is based on a first
  • FIG. 1 is a representation of the prior art
  • Fig. 2 is a schematic overview of a
  • FIG. 3 shows a design of a main reactor for a once-through principle
  • FIG. 4 shows a design of a main reactor for a countercurrent principle
  • FIG. 6 shows the main reactor according to FIG. 4 with a bubble distribution of the depolymerization material
  • Fig. 7 shows the main reactor in the countercurrent principle with a bubble distribution of the depolymerization material
  • FIG. 8 shows the main reactor in the countercurrent principle with filling elements and bubble distribution of the depolymerization material
  • FIG. 11 shows an arrangement of the metal bath return on the main reactor
  • FIG. 12 shows the arrangement of the metal bath return according to FIG
  • FIG. 16 shows a front view of a device according to the invention according to the second exemplary embodiment
  • Fig. 17 is a sectional view corresponding to section line B - B in Fig. 16, Fig. 18 shows a cross-sectional representation according to the line A - A in Fig. 17,
  • FIG. 19 shows a plan view of the arrangement according to the invention of the second exemplary embodiment
  • FIG. 20 shows a tank management system
  • the crude oil is heated to over 360° C. in the tube furnace TI, so that the components largely evaporate.
  • the distillates T4 to T9 of the individual fractions collect in the bubble trays T3.
  • the tube T10 in which the used oil is conducted, comes into direct contact with the heating gas generated by the combustion chamber TU.
  • the heating gas is not evenly distributed in the tube furnace TI, so that the tube T10 partially overheats.
  • the thermal capacity of the heating gas is also low, so that high temperature differences have to be used, ie the heating gas is heated up considerably, which in turn can lead to overheating of the tube T10.
  • waste oil is provided in an external input tank 1 according to FIG. 2 for the purpose of cleaning by the device according to the invention shown. From this input tank 1, this waste oil is using a template pump 2 in an internal Reservoir 3 and pumped from there into the main reactor 5. The amount of waste oil fed in is controlled via the temperature in the rectification column 6 as a controlled variable.
  • the used oil mixes with the distillate and bottom returns described below to form a depolymerization material 4, which is fed to the main reactor 5 and abruptly evaporated there by means of so-called flash evaporation.
  • the main reactor in the second embodiment does not perform flash evaporation but conduction heat evaporation. In both exemplary embodiments, however, steam is produced which is fed to a rectification column 6 .
  • the vapor condenses in different stages, i.e. at different temperatures. Deductions 7 to 10 are provided at these levels. While the condensate at the first side draw 7 and the second side draw 8, cooled via heat exchanger 11, is fed back to receiver 3, the product, i.e. a cleaned oil, is removed from the third side draw 9 and top draw 10 and also cooled via heat exchanger 11 , a product tank 12 is supplied. From here it is then conveyed into an output tank 14 by means of a product pump 13 .
  • Condensate which is not derived from the deductions 7 to 10, and components of the Depolymerisationsgutes 4, the are not evaporated and float in the metal bath of the main reactor 5 are fed back to the main reactor 5 via a circulation line 31 by means of a circulation pump 32 for renewed evaporation as depolymerization material 4 .
  • the condensate that can no longer be distilled collects as a sump at the bottom of the rectification column. From there, the sump is fed to the disposal container 15 via a sump return 16 . From there, the content of the
  • the main reactor 5 can be designed on the once-through principle.
  • the entrance 17 for the is located at the lower end
  • a metal bath 19 which consists of a metal which has a melting point above the vaporization temperature of the
  • Depolymerisationsgutes 4 has.
  • the metal is kept in the liquid phase by heating collars 20 . Since the Depolymerisationsgut 4 by the temperature of the metal bath
  • Evaporation temperature must be, is immediately evaporated as soon as it enters the metal bath 19, this is referred to as a flash evaporation.
  • Fig. 3 represents the flow principle, in which the Deploymerizationsgut 4 arranged directly on the underside of the main reactor 5 inlet 17 directly Underside of the metal bath 19 is fed and evaporated there immediately.
  • FIG. 4 represents the counterflow principle, in which the inlet 17 has a counterflow tube 21 .
  • the depolymerization material 4 is passed through the metal bath 19 through this counterflow tube 21 .
  • the depolymerization material 4 already heats up almost to the vaporization temperature, so that the flash vaporization proceeds even faster when it exits from the inlet 17 .
  • FIG. 7 parts of the depolymerization material 4 are not vaporized by the temperature of the metal bath 19.
  • FIG. The non-evaporated part 22 is mostly higher-chain compounds, which largely come from the contamination of the used oil in the input tank. As can be seen from FIG. 7, this part 22 floats on the metal bath 19 and flows into the bottom container 15 at the connecting edge between the main reactor 3 and the rectification column.
  • a metal bath return line 24 is arranged above the metal bath 19.
  • This metal bath return 24 can, for example, be in the reactor space of the main reactor 5 or in the rectification column 6 to be ordered.
  • This metal bath return has baffle plates 26 lying in the steam flow direction 25, as shown in FIGS.
  • Each of these baffle plates 26 has a lateral opening 27, these openings being offset in such a way that they do not lie one above the other in the steam flow direction, but cover one another.
  • the baffle plates 26 can be braced in the metal bath return 24 by means of a nut 28 which is screwed onto a tie rod 29 .
  • FIG. 12 shows the principle of the outflow of the non-evaporated part as shown in FIG. 7, but with the metal bath return flow.
  • the unevaporated part 22 also floats on the metal bath 19, but fills the metal bath return flow 24 up to its upper edge. Since the unevaporated part 22 is always growing, the excess flows over the upper edge of the metal bath return 24 into the sump tank 15.
  • baffle plates 26 than in the non-evaporated part 22. The metal tips of the metal bath 19 therefore reach the baffle plates 26 within the non-evaporated part 22 and flow from there through the non-evaporated part 22 back into the metal bath 19.
  • a further measure to prevent the material being discharged from the metal bath can consist in introducing packing 27 into the main reactor 5 .
  • These fillers can be made of a metal with a higher melting temperature than the metal bath 19 or other--possibly inert--materials, such as ceramics.
  • Such a filling with filler bodies 30 is possible both with the continuous flow principle according to FIG. 3, shown in FIGS. 5 and 6, and with the counterflow principle according to FIG. 4, shown in FIGS. 7 and 8.
  • a combination of the packing 30 with a metal bath return 24, as shown in FIGS. 11 to 13, is also possible.
  • the effect can be seen in the fact that the vapor bubbles 23 that emerge from the inlet are still quite large and are broken up into smaller bubbles by the packing 30. Vapor bubbles 23 reduced in size in this way only have less energy to emit metal spatter when they burst on the surface of the metal bath 19 .
  • tin is used as the metal for the metal bath 19 for the purpose of evaporating waste oil, since its melting point of 300° C. optimally matches the vaporization temperature of the waste oil.
  • the use of other melting materials is also possible. The only decisive factor is that the melting temperature of the melting material used is equal to or higher than the vaporization temperature of the depolymerization material. However, the melting temperature selected must not be so high that the depolymerization material is not even partially burned.
  • the material to be depolymerized is heated directly, i.e. without a molten bath, e.g. by an input of thermal energy from outside through the wall of the main reactor, the temperature gradient will inevitably lead to overheating of the material to be depolymerized on the wall and thus to the deposit of combustion residues, which will soon require complex cleaning of the main reactor become necessary.
  • melt pool solution This also reveals other areas of application for the melt pool solution. This makes it possible, for example, to process contaminated solvents or cleaning agents or fuels. Then, in particular, a design of the device will be chosen that works under vacuum. However, it is also possible to feed granulated plastics to a molten bath, preferably made of metal. The vapors emitted as a result of heating can then be rectified into valuable raw materials. But other heat carriers, such as saturated salt solutions, melting plastics, and even liquid gases, in addition to the metals already described above, can be used as melt bath materials for various fields of application.
  • the second exemplary embodiment as illustrated in FIGS. 14 to 19, is also aimed at preventing a melt pool loss and avoiding combustion residues.
  • FIG. 14 shows a main reactor 5 which has a reactor vessel 34 .
  • Heating jackets 20 are arranged on the outside of the reactor vessel.
  • the heaters can also be designed differently, for example alternatively as induction heaters.
  • the metal bath 19 is located inside the reactor vessel 34.
  • a heat exchanger or heating register 35 is completely immersed in this bath.
  • the metal bath 19 flows around the heating register when it has liquefied.
  • At the top is the reactor vessel 34 with a
  • Flange 36 is provided, by means of which the reactor vessel 34 can be connected to the main reactor 5.
  • a drain hole 37 is provided in this flange 36, through which non-condensable liquid can be drained directly into the sump.
  • the heating register consists of a spirally bent tube with a first end 38 and a second end 39.
  • the cold waste oil is introduced into the first end 38 and guided to the heating register 35 at its end facing the flange 36.
  • the used oil which has been heated to the vapor phase, enters the rectification column 6 connected to it at the second end 39.
  • the distillation already described takes place there.
  • the pipe jacket of the pipe of the heating register 35 thus forms the partition between the used oil and the metal bath 19.
  • the dividing wall consists of the pipe shell of a 15 meter long spiral pipe in which the input material is circulated at high speed and lies in the melt pool. (0.1mmx10mm).
  • the weld pool is a 1000mm x 80mm long stainless steel tube filled with liquid metal.
  • the heating sleeves on the outside fire this tube with a maximum of 650°C.
  • the weld pool absorbs the energy and distributes it over the entire spiral.
  • the heat transfer is very good and the space requirement is minimal.
  • the device according to the invention is arranged in a frame 40 as a transportable mobile device. It contains the storage container 3, the product tank 12 and the disposal container 15. There are four to increase the production capacity
  • Main reactors 5.1 to 5.4 and of the type according to FIG. 14 are provided, the second ends of which each open into the rectification column 6, which is arranged centrally.
  • a controller 41 is provided for the proper operation of the system.
  • TMS tank management system
  • Each rectification column outlet has a product lock.
  • the two tanks (top 44 and bottom 45) are under vacuum. They are connected to a central vacuum system 46 .
  • the lower tank 45 is emptied (about 10 seconds). Then the ventilation valve 48 closes again, the vacuum valve 47 to the buffer tank (upper tank 44) is opened and the lower one
  • Tank 45 is again placed under vacuum. Due to the small filling volume of the tanks 44 and 45, the pressure fluctuations that cannot be ruled out are negligible.
  • the control is fully automatic via a PLC

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

Abstract

L'invention concerne un procédé et un dispositif destinés à la purification d'huile usagée, procédé selon lequel la matière de départ est chauffée jusqu'à la phase gazeuse et la vapeur ainsi produite est rectifiée, l'huile purifiée étant soutirée sous forme de condensat depuis un point de soutirage ménagé dans une colonne de rectification. L'invention a pour but de fournir un procédé et un dispositif destinés à la purification d'huile usagée permettant un travail efficace même dans de très petites installations, de telle sorte qu'une configuration d'installation compacte et ainsi, en particulier, une utilisation mobile sont rendues possibles grâce à une structure de type conteneur. L'invention vise également à réduire la complexité de maintenance. À cet effet, l'huile usagée est soumise à une évaporation par mise en contact au moins indirect de la matière de départ avec un bain de fusion dont la température de fusion est supérieure à la température d'évaporation, mais inférieure à la température d'inflammation de l'huile usagée, et la vapeur est rectifiée dans la colonne de rectification.
PCT/EP2022/064463 2021-05-26 2022-05-27 Procédé et dispositif destinés à la purification d'huile usagée WO2022248698A1 (fr)

Applications Claiming Priority (2)

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DE102021113616 2021-05-26
DE102021113616.4 2021-05-26

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EP0592057B1 (fr) 1992-10-06 1997-10-08 FORMEX TRADING GmbH Procédé de pyrolyse de déchets organiques
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EP1664240A1 (fr) * 2004-02-18 2006-06-07 Technologie Ekologiczne Procede et dispositif pour la conversion continue de dechets organiques
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US20120116142A1 (en) * 2009-05-14 2012-05-10 Adam Handerek Method and System for Performing Chemical Proceses
DE102012008458A1 (de) 2012-04-24 2013-10-24 Adam Handerek Reaktor zum Vergasen und/oder Reinigen eines Ausgangsmaterials
WO2014106650A2 (fr) 2013-01-03 2014-07-10 EZER, Argun Procédés et dispositifs de dépolymérisation d'une matière première hydrocarbonée
US9243191B1 (en) * 2010-07-16 2016-01-26 Delta Technologies LLC Re-refining used motor oil
WO2020104472A1 (fr) 2018-11-19 2020-05-28 Biofabrik Hoyerswerda Gmbh Procédé et dispositif de nettoyage d'huiles usées contaminées

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Publication number Priority date Publication date Assignee Title
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