EP3710560A1 - Procédé et dispositif de transformation en huiles de substances de valorisation hydrocarbonées - Google Patents

Procédé et dispositif de transformation en huiles de substances de valorisation hydrocarbonées

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Publication number
EP3710560A1
EP3710560A1 EP18807244.1A EP18807244A EP3710560A1 EP 3710560 A1 EP3710560 A1 EP 3710560A1 EP 18807244 A EP18807244 A EP 18807244A EP 3710560 A1 EP3710560 A1 EP 3710560A1
Authority
EP
European Patent Office
Prior art keywords
evaporator
depolymerization
condenser
temperature
condensed
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.)
Granted
Application number
EP18807244.1A
Other languages
German (de)
English (en)
Other versions
EP3710560B1 (fr
Inventor
Burkhart Schulte
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Reset International GmbH
Original Assignee
Reset 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 Reset GmbH filed Critical Reset GmbH
Publication of EP3710560A1 publication Critical patent/EP3710560A1/fr
Application granted granted Critical
Publication of EP3710560B1 publication Critical patent/EP3710560B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

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Classifications

    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • 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
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • 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

Definitions

  • the invention relates to a process for the oilation of hydrocarbon-containing Verêtsstoffen by
  • the invention further relates to a device for the oilation of hydrocarbon-containing recycling materials with an evaporator, which has a vaporization chamber for receiving the utilization materials and a heater for heating the Verwer- materials, and with a condenser, which is connected to the evaporator and condensed to form Oils from vapor-generated vapor in the evaporator is set up.
  • hydrocarbon-containing recycling materials in particular of plastics
  • plastics can be effected by burning them.
  • Depolymerization of the recycling substances takes place during simultaneous oxidation of the resulting hydrocarbons.
  • a disadvantage of using plastics is that a large part of other additives passes into the exhaust gas phase and has to be removed from the exhaust gas in a very expensive way.
  • highly toxic new compounds can be formed during the combustion process, which may need to be laboriously removed.
  • Hydrocarbon-containing recycling materials can also be oiled. This has the advantage that the problematic interfering and additives can be removed either already during the oiling or from the liquid end product. This is easier to handle than cleaning a hot exhaust stream.
  • DE 103 16 969 A1 describes a method and a device for the catalytic treatment of residues in continuously cleaned and heated tube bundle reactors.
  • an oil is produced with ion-exchanging catalysts in an oil-catalyst suspension circuit, which can be used diesel engineisch.
  • the recycling materials are introduced into a heated reactor vessel, wherein liquid input materials are introduced via a mechanical and thermal Wasserab- divorce in the lower part of the reactor vessel. Steam is generated by a catalytic depolymerization process in the reactor vessel.
  • DE 100 49 377 C2 describes a process for the oilification of hydrocarbon-containing wastes, in which a catalyst of sodium aluminum silicates in a circulation evaporator is stirred in circulation with a high-boiling hydrocarbon and in the reactor part under a distillation unit, the hydrocarbon-containing waste is added.
  • DE 10 2011 111 526 B4 discloses a process for the conversion of valuable materials with a thermally insulated recyclable material converter, wherein the valuable materials are heated in a first heating phase to about 110 ° C, thereby resulting water vapor completely and additionally escape already vaporized oil from the recyclable material converter. This is immediately followed by a second now water- and oxygen-free heating phase with a temperature range of about 110 ° C to about 280 ° C, in which convert the valuable materials supported by an excipient mixture to oil vapors.
  • the water and oil vapors are condensed and separated in at least one condensation element and the vaporized oil from the second heating phase is condensed in at least one further condensation element.
  • this incremental increase in the depolymerization temperature can reduce the total energy required, since not all the material needs to be heated to the maximum temperature, but each substance is only heated to a specific gasification temperature and then escapes and the volume for the next Depolymerisations- level is further reduced.
  • a combustible gas fraction may be supplied to an ignition jet engine (eg, gas engine and / or oil burning engine) or even a gas turbine to convert energy from this gas fraction into mechanical energy, electrical energy, and / or heat energy.
  • a depolymerization at a temperature in the range of 100 ° C to 150 ° C for the evaporation of water and for draining condensed water from the condenser This has the advantage that the recycling substances are dried in this first depolymerization stage and air oxygen is displaced from the gas space.
  • additives to the hydrocarbon-containing recycling materials for the catalytic support of depolymerization and / or for chemical neutralization or for binding constituents of the recycling materials.
  • the decomposition temperature can be lowered.
  • catalysts By adding catalysts, the conversion of long-chain hydrocarbons and short-chain hydrocarbons can be supported.
  • Disturbing component of waste materials used, such as Nitrogen, chlorine, sulfur, etc. can already be neutralized in the liquid phase in the evaporator (i.e., the depolymerizer) by adding suitable chemicals, or bound as salts, oxides, hydroxides, etc., in the solid state of the process.
  • the step of condensing may be done with at least one selected capacitor of a plurality of capacitors. It is conceivable that at least two capacitors are connected in series or in parallel. This makes it possible that two different temperature ranges of the cooling medium are possible. It is desirable that the condensed oil is not warmer than 50 ° C for emission protection and fire protection reasons. When using a single Condenser, the exit temperature of the cooling medium would be correspondingly low, so that the heat of the cooling medium is not economically useful. In the case of a multistage condenser, however, at least the first condenser in a series can have a considerably higher outlet temperature of the cooling medium of more than 100 ° C. At this temperature level, the waste heat of the cooling medium is technically usable and can be recycled as energy.
  • a reheating of the oily vapor rising in the evaporator is advantageous in such a way that the formation of condensate which flows back into the evaporator is reduced.
  • This reheating can take place, for example, with an additional heater on the lid and / or in the region of the outlet line of the evaporator.
  • Such postheating ensures that condensation of the vapor phase only takes place in the condenser and that the depolymerization process in the evaporator is not impaired by refluxing condensate.
  • This reheating can advantageously also be used independently of a specific control of the switching of Depolymerisationstressn.
  • inert gas such as carbon dioxide
  • inert gas such as carbon dioxide
  • the plant is supplied with hydrogen in the depolymerization process or thereafter in order to bind free carbon ends of the condensed oils with hydrogen and to prevent oxidation during storage. This also prevents a dark discoloration of the oils.
  • the supply of hydrogen can be carried out in a simple manner by switching over the gas feeds provided for inerting.
  • the direct use of hydrogen in the evaporator enables hydrogenation of the oil vapors as soon as they are formed. This can prevent the free carbon ends resulting from depolymerization from being mixed with another substance, e.g. Oxygen, connect. Any unused hydrogen components can easily be processed into energy in an ignition jet engine.
  • Additives can be fed into the at least one condenser for washing or neutralizing substances contained in the condensed oil.
  • the capacitors may have a rinsing or spraying device in order to use the condenser as a scrubber at the same time.
  • This is e.g. advantageous in the processing of PVC, which decomposes into HCl and HC components (hydrocarbon) when heated to over 180 ° C.
  • HCl hydrochloric acid
  • the bottom of the evaporator may have tapered elevations. For example, it can be combed or wavy. As a result of the resulting larger surface, a significantly more favorable heat input into the material to be processed is possible.
  • the material to be processed can be deposited on the sieve plate.
  • the plastic components melt and flow down between the heating elements. There they are exposed to a higher temperature and are evaporated.
  • the non-volatile components remain on the sieve bottom and can be easily removed.
  • the heat introduced is used much more effectively by the arrangement of the heating elements in these heating pockets, as it radiates on both sides of the material and not with one side in the insulation.
  • FIG. 1 shows a block diagram of a device for the oiling of hydrocarbonaceous substances
  • FIG. 2 shows a sketch of an evaporator bottom having a tapered elevations and a sieve plate placed thereon.
  • FIG. 1 shows a block diagram of a device 1 for the oiling of hydrocarbon-containing recycling substances.
  • Such recycling materials can be, for example, composite materials with plastic components or plastics.
  • a so-called batch process is carried out continuously in which quantities of waste materials are introduced batchwise into an evaporator 2 (depolymerizer).
  • the evaporator 2 has a heat-insulated evaporation chamber 3, into which the recycling substances are introduced.
  • a heater 4 is arranged at the bottom portion of the evaporation chamber 3. After closing the evaporation chamber 3, the evaporator 2 with the heater 4 is first in a first stage to about
  • the water-containing vapor in the first stage rises and is removed via a vapor line 5 in the lid region of the evaporation chamber 3 and introduced into at least one condenser 6a, 6b.
  • the condensers 6a, 6b are flowed through by coolant 7, so that the vapor, for example, by evaporation or after reaching the saturation vapor pressure by vaporization gaseous vapor on the capacitors 6a, 6b (heat exchanger) is cooled again and condensed.
  • the condensate is then collected in selectable fraction collection containers 8a, 8b, 8c, 8d, 8e, 8f.
  • the condensate drains of the condensers 6a, 6b are each connectable via shut-off valves 9 with at least one selectable fraction collecting container 8a to 8f.
  • shut-off valves 9 At a gas inlet of the capacitors 6a, 6b are also shut-off valves 10a and 10b, with which the capacitors can be switched either individually or in parallel.
  • a bypass valve 11 At the output of the first capacitor 6a there is likewise a bypass valve 11, which is connected via a bypass line 12 to the input of the second capacitor 6b.
  • the output of the capacitors 6a, 6b is further connected to a gas filter 13 for the respective capacitor 6a, 6b, which in turn is coupled via a gas line 14 to a gas reservoir 15 and an ignition jet motor 16 or a gas turbine connectable thereto.
  • the gas line 14 can be directly connected to the ignition jet motor 16 via a direct line 17 without intermediate control circuit of the gas reservoir 14.
  • the gas line 14 is preferably arranged vertically in at least one section so that condensate can be collected in a further condensate tank 18. Again controllable shut-off valves 19 are present.
  • the depolymerization temperature is increased in several steps. In each step, depending on the depolymerization temperature, by controlling the shut-off valves 9, a fraction collector 8a to 8f is selected in which the condensed oil formed at the respective depolymerization temperature is then collected.
  • a chemical-physical process takes place in which, by supplying heat and excluding oxygen, the utilization substances are heated under normal pressure to such an extent that the organic components depolymerize and change into the gaseous state (ie in the vaporizing the broadest sense).
  • thermoplastics are heated, they begin to soften and then form a melting point. At these temperatures, usually in the range from 200 ° C to 500 ° C (without the use of catalysts), the decomposition of macromolecules into a wide variety of low molecular weight molecules takes place. These gases are formed, such as methane, ethane, liquid organic compounds, water and solid carbon. In addition, heteroatoms such as nitrogen, sulfur, oxygen and / or chlorine are split off.
  • each substance is only heated until it has reached its gasification temperature. With water, the heating is thus only up to approx. 100 ° C and for other substances according to their respective properties. This reduces the energy required compared to the situation where the entire recovery material is heated to the maximum temperature.
  • the switching of the depolymerization stages by increasing the depolymerization and evaporation temperature takes place by measuring the temperature of the cooling medium 7 in the capacitors 6a, 6b. If the temperature of this cooling medium 7 in the at least one selected condenser 6a, 6b drops, this is a sign that no material suitable for the respective depolymerization temperature is present in the evaporator 2. Threshold values can be specified for this temperature reduction observed for switching over. In this case, absolute threshold values or preferably relative threshold values, such as, for example, a reduction by 10% of the temperature present hitherto can be used.
  • the evaporator 2 further has an additional heater 20, which is arranged in the ceiling space of the evaporation chamber 3 and / or in the outlet area of the evaporator 2. This heats the resulting vapors to prevent the rising oil-containing steam is not already condensed again on the lid of the evaporator 2 and drips back. This would mean that the depolymerization temperature in the evaporator 2 would have to be significantly above the actual depolymerization temperature of the respective substance so that the temperature on leaving the evaporator 2 is still above the condensate temperature. In that case, a precise separation of the substances due to different depolymerization temperatures would be problematic.
  • an inert gas source 21 a is connected to the steam line 5. This can be done inerting of the atmosphere in the device 1 by feeding eg. Of carbon dioxide CO2. This avoids reactions of the oil vapors with air and improves fire protection and emission protection since the device 1 can first be flushed with carbon dioxide before each discharge, before air enters the system.
  • a hydrogen source 21b e.g. reversibly connected to the steam line 5 to supply hydrogen-containing gas to the condensed oils during the Verkölungsvonen, sporadically between or after completion of the Verkölungsvones.
  • a hydrogen source 21b e.g. reversibly connected to the steam line 5 to supply hydrogen-containing gas to the condensed oils during the Verkölungsvon, sporadically between or after completion of the Verkölungsvonsky.
  • the at least two capacitors 6a, 6b By the at least two capacitors 6a, 6b, it is possible to switch them both in series and in parallel. This makes it possible that two different temperature ranges of the cooling medium 7 are used. Since the oil condensate for emission protection and fire protection reasons should not be warmer than 50 ° C, would have a single cooler with an outlet temperature of the cooling medium 7 of> 50 ° C work. This heat would not be technically usable. For a two-stage cooler, the first stage may well have an outlet temperature of over 100 ° C. The cooling medium 7, such as thermal oil, would then have an outlet temperature of more than 100 ° C. At this temperature level, the waste heat can definitely be used technically. Since almost the entire energy of the process as vaporization energy in the oil vapor is, here are economically interesting amounts of heat and energy.
  • a condenser 6a, 6b can be specifically used as a cold trap for these substances.
  • more than two capacitors 6a, 6b can be connected in parallel.
  • a combination of parallel and series connection of more than two capacitors is conceivable.
  • the control of the heater 4 and optionally the auxiliary heater 20 takes place, for example, depending on the heat absorption of the cooling medium 7.
  • a substance evaporates and condenses again in the condenser 6a, 6b, it releases the condensation heat to the cooling medium 7, which warmed up accordingly. If the material evaporating in the evaporator 2 at the respective evaporation temperature is then completely vaporized, then heat is no longer present at the capacitor 6a, 6b and the temperature of the cooling medium 7 drops significantly, although the temperature in the evaporator 2 remains the same.
  • the capacitors 6a, 6b can be extended by a rinsing or spraying device in order to use at least one of the capacitors 6a, 6b also as a scrubber.
  • a rinsing or spraying device in order to use at least one of the capacitors 6a, 6b also as a scrubber.
  • This is particularly interesting in the processing of PVC, which decomposes when heated to over 180 ° C in HCl and HC components.
  • HCl forms with hydrochloric acid, ie an aggressive corrosive substance. Therefore, it is advantageous if the HCl is washed out as quickly as possible.
  • sodium hydroxide NaOH can be used, whereby the hydrochloric acid is directly neutralized and the chlorine is converted to sodium chloride NaCl.
  • the oils collected in the fraction collection containers 8a to 8b may be supplied to a priming motor 16 or a turbine to convert the energy contained in the oils into mechanical, electrical and / or thermal energy.
  • the Zündstrahlmotor 16 can be shared, which is actually fed in Figure 1 with gas mixture. It is conceivable that the ignition jet engine 16 is a pure gas engine. The oils obtained can be fed to an optional additional oil-burning engine for further energy conversion into electrical and thermal energy. But it is also possible that the ignition jet engine 16 is a combined gas and oil engine, which is fed with both the gas fraction, as well as with the liquid oil fraction.
  • the device 1 can be combined with a combined heat and power plant in order to utilize the heat W and the electrical energy E generated in the device 1 for further utilization.
  • the exhaust gas flow A from the ignition jet engine 16 can also be used with the aid of a heat exchanger to generate energy and optimize the efficiency of the device 1.
  • the device 1 has the advantage that due to the oiling an easily stored and transported energy-containing product is produced, which is versatile as a fuel, as well as a raw material in chemistry. The cleaning of the oil produced takes place in the liquid phase and can be repeated as desired.
  • the batch-wise oiling is already economically interesting in small units and therefore very well suited for decentralized plants.
  • the operation of the batch-wise oiling plant is much simpler than the operation of an incinerator, whereby the process can be switched on and off very quickly and is very easy to operate. Due to the very good storage possibility of the oils obtained in the fraction collection containers 8a to 8f, it is possible to operate hereby power plants that are switched on only in need of a peak load.
  • the device 1 can thus be used in addition to wind and solar energy systems.
  • evaporator 2 It is also conceivable to add catalysts to the evaporator 2. This can be used to support the conversion of long-chain hydrocarbons into short-chain hydrocarbons. Disturbing constituents of the waste materials used, such as nitrogen, chlorine, sulfur, etc., can already be neutralized in the liquid phase in evaporator 2 or added as salts, oxides, hydroxides, etc. in the solid residue of the process by adding suitable chemicals.
  • the evaporation temperature is increased in several stages, starting with a first stage by about 100 ° C (80 ° C to 120 ° C) and then in at least two further stages to about 340 ° C. In the first evaporation stage, water-containing steam is produced, which optionally also contains lower proportions of oil. In the next at least two evaporation stages, after the water has been expelled, oily vapor is generated which contains different oil fractions in at least two further stages. Thus, at least three evaporation stages are provided.
  • Useful substances are mixtures or composites in which a considerable proportion of organic components is present, such as, for example, Plastics of all kinds, including PVC, rubber, used oils, waxes, greases, transformer oils, hydraulic oils, refinery residues, concrete, tars and hospital waste, which are completely sterilized in the evaporator 2.
  • Plastics of all kinds including PVC, rubber, used oils, waxes, greases, transformer oils, hydraulic oils, refinery residues, concrete, tars and hospital waste, which are completely sterilized in the evaporator 2.
  • the non-gasifiable components of the utilization substances then remain in the evaporator 2 and can be disposed of.
  • gases that do not condense at room temperature such as butane, propane and methane, are also formed. Depending on the recycling material, this may be about 10% to 15% of the recycling substance.
  • gases can be passed directly to a gas engine for power generation.
  • the resulting amount of electricity can be used for self-supply of the device 1, for example, for the supply of the heater 4 and any surplus electricity can be fed into a power supply network.
  • a second internal combustion engine 16 or an emergency flare is to be provided.
  • the oil collected in the fraction collection containers 8a to 8f can be specifically subjected to further purification or can also be used directly for use in a diesel engine of a combined heat and power plant.
  • the heat arising from the heat exchangers (capacitors 6a, 6b) and the ignition jet motors 16 can optionally be used for the predrying of the utilization substances or, if appropriate, also elsewhere.
  • the evaporator 2 When the oil production has come to an end, i. If there are no more vaporizable substances in the evaporator 2, the evaporator 2 is cooled again. During this period, a second evaporator can already be connected to the steam line 5 in order to continue to operate the subsequent system. The cooled evaporator 2 is then unloaded and loaded again with new recovery materials. In order to reduce emissions from the plant, in particular when the evaporator 2 is opened, the evaporator 2 should be connected before cooling by an internal purge by an inert gas, such as carbon dioxide, with cooling effect. The gas exiting during the flushing process should then be adequately filtered.
  • an inert gas such as carbon dioxide
  • the fraction collecting containers 8a to 8f should also have suitable air filters 22 for venting.
  • FIG. 2 shows a sketch of an evaporator bottom 30, which has tapered elevations 31 and a screen plate 32 placed on the elevations 31.
  • Heating elements 33 are arranged in the outer space of the evaporator 2 between the elevations 31, below the horizontal sections of the evaporator bottom 30 and optionally on the side walls.
  • the Bennettschmelzenden plastic recovery products are placed on the preferably loosely placed on the comb tips screen plate 32.
  • the plastic components melt at the appropriate temperature and flow down into the trough-shaped sections which are adjacent to the heating elements 33. There they are exposed to higher temperatures and are evaporated. The non-volatile components remain on the screen plate 32 back and can be easily removed.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention concerne un procédé pour transformer en huiles des substances de valorisation hydrocarbonées, par la dépolymérisation des substances de valorisation, l'introduction, dans un condensateur (6a, 6b), de la vapeur huileuse produite au cours de l'étape de la dépolymérisation pour former des huiles condensées, et la collecte des huiles condensées dans le condensateur (6a, 6b). L'étape de la dépolymérisation a lieu au cours de plusieurs phases à différentes températures. Les fractions d'huiles condensées formées respectivement au cours des phases sont collectées séparément les unes des autres, une inversion des phases d'évaporation ayant lieu par augmentation de la température d'évaporation lors de la baisse de la température de fluide de refroidissement (7) dans le condensateur (6a, 6b).
EP18807244.1A 2017-11-17 2018-11-15 Procédé et dispositif de transformation en huiles de substances de valorisation hydrocarbonées Active EP3710560B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102017127132.5A DE102017127132B4 (de) 2017-11-17 2017-11-17 Verfahren und Vorrichtung zur Verölung von kohlenwasserstoffhaltigen Verwertungsstoffen
PCT/EP2018/081390 WO2019096915A1 (fr) 2017-11-17 2018-11-15 Procédé et dispositif de transformation en huiles de substances de valorisation hydrocarbonées

Publications (2)

Publication Number Publication Date
EP3710560A1 true EP3710560A1 (fr) 2020-09-23
EP3710560B1 EP3710560B1 (fr) 2026-03-11

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EP18807244.1A Active EP3710560B1 (fr) 2017-11-17 2018-11-15 Procédé et dispositif de transformation en huiles de substances de valorisation hydrocarbonées

Country Status (3)

Country Link
EP (1) EP3710560B1 (fr)
DE (1) DE102017127132B4 (fr)
WO (1) WO2019096915A1 (fr)

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012110990A1 (fr) * 2011-02-18 2012-08-23 Cooperativa Autotrasportatori Fiorentini C.A.F. - Societa' Cooperativa A R.L. Production d'hydrocarbures à partir de copyrolyse de matières plastiques et de matériaux de pneu avec chauffage par micro-ondes

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5771821A (en) * 1994-03-25 1998-06-30 Science-Technical And Product-Innovative Center "Tokema" Method of treating plastic waste
DE10049377C2 (de) 2000-10-05 2002-10-31 Evk Dr Oberlaender Gmbh & Co K Katalytische Erzeugung von Dieselöl und Benzinen aus kohlenwasserstoffhaltigen Abfällen und Ölen
DE10316969A1 (de) 2003-04-14 2004-12-02 Jochen Herrlinger Verfahren und Vorrichtung zur katalytischen Behandlung von Reststoffen in kontinuierlich gereinigten und beheizten Rohrbündelreaktoren
US7588665B2 (en) * 2005-09-20 2009-09-15 Smith Steven W Apparatus for converting waste products into usable fossil fuel
DE102007057827A1 (de) * 2007-11-29 2010-05-12 Klaus Sommer Sekundäre Energieträger aus schockbehandelten Biomassen und Verfahren der Herstellung
WO2009145884A1 (fr) * 2008-05-30 2009-12-03 Natural State Research, Inc. Méthodes et dispositifs de dégagement des obstructions de tubes médicaux
DE102011111526B4 (de) 2011-08-31 2014-06-26 Georg Bogdanow Verfahren zur Konvertierung von Wertstoffen

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012110990A1 (fr) * 2011-02-18 2012-08-23 Cooperativa Autotrasportatori Fiorentini C.A.F. - Societa' Cooperativa A R.L. Production d'hydrocarbures à partir de copyrolyse de matières plastiques et de matériaux de pneu avec chauffage par micro-ondes

Also Published As

Publication number Publication date
DE102017127132A1 (de) 2019-05-23
EP3710560B1 (fr) 2026-03-11
DE102017127132B4 (de) 2022-01-13
WO2019096915A1 (fr) 2019-05-23

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