METHOD AND DEVICE FOR OILING HYDROGEN-CONTAINING RECYCLABLE MATERIALS

Description

[0001] The invention relates to a process for the oiling of hydrocarbon-containing recycled materials by Depolymerization of the recycled materials, introduction of the oil-containing vapor generated in the depolymerization step into a condenser to form condensed oils, and collection of the oils condensed in the condenser.

[0002] The invention further relates to a device for the oiling of hydrocarbon-containing recycling materials with an evaporator having an evaporation chamber for receiving the recycling materials and a heater for heating the recycling materials, and with a condenser connected to the evaporator and designed to form condensed oils from oil-containing vapor generated in the evaporator.

[0003] Hydrocarbon-containing recyclables, especially plastics, can be recycled by incineration. This process involves the depolymerization of the recyclables and the simultaneous oxidation of the resulting hydrocarbons. A disadvantage of recycling plastics is that a large proportion of other additives pass into the exhaust gas and must be removed from it in a very complex and costly manner. Furthermore, highly toxic new compounds can be formed during the combustion process, which may also require extensive removal.

[0004] Hydrocarbon-containing recycled materials can also be oiled. This has the advantage that problematic contaminants and additives can be removed either during the oiling process or from the liquid end product. This is easier to manage than cleaning a hot exhaust gas stream.

[0005] DE 103 16 969 A1 describes a process and a device for the catalytic treatment of residual materials in continuously cleaned and heated tube bundle reactors. In this process, an oil suitable for diesel engine use is produced using ion-exchange catalysts in an oil-catalyst suspension cycle. The waste materials are introduced into a heated reactor vessel, with liquid input materials being introduced into the lower section of the reactor vessel via mechanical and thermal water separation. Steam is generated through a catalytic depolymerization process within the reactor vessel.

[0006] DE 100 49 377 C2 describes a process for the oiling of hydrocarbon-containing waste, in which a catalyst made of sodium aluminum silicates is stirred in a circulating evaporator in a cycle with a high-boiling hydrocarbon and the hydrocarbon-containing waste is added in the reactor part below a distillation plant.

[0007] DE 10 2011 111 526 B4 discloses a process for converting recyclable materials using a thermally insulated material converter, wherein the recyclable materials are heated to approximately 110°C in a first heating phase, causing any water vapor produced to escape completely and any already vaporized oil to escape from the converter. This is immediately followed by a second heating phase, now free of water and oxygen, with a temperature range of approximately 110°C to approximately 280°C, in which the recyclable materials, aided by an auxiliary mixture, convert 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.

[0008] US 2007 / 062104 A1 relates to a process and apparatus for converting a process material such as plastic powder into fossil fuel. For this purpose, a cylinder with a movable piston is provided, into which powdered plastic is introduced and heated to approximately 600°C. The resulting oil vapors are compressed by the piston and expelled into a main condenser. In the main condenser, oil and water separate due to the initial cooling and are separated from each other based on their density differences. The remaining oil fractions rise as gases and cool down in further containers connected in series.

[0009] US 2015 / 087871 A1 relates to the production of hydrocarbon-containing liquids from plastic waste. This involves a process in which solid plastic waste is melted in an aerobic atmosphere, at least a portion of the molten plastic waste is distilled, and the distillate is collected. Based on this, the object of the present invention is to provide an improved process and a device for the oiling of hydrocarbon-containing recycled materials.

[0010] WO 2012 / 110990 A1 discloses a microwave pyrolysis process for plastics, which are oiled at a continuously increasing temperature. The various components of the resulting mineral oil are collected in several fractions for different temperature ranges.

[0011] Based on this, the object of the present invention is to create an improved method and a device for the oiling of hydrocarbon-containing recycled materials.

[0012] The problem is solved by the method with the features of claim 1 and by the device with the features of claim 10. Advantageous embodiments are described in the dependent claims.

[0013] The depolymerization step is carried out in several stages at different temperatures, and the fractions of condensed oils formed in each stage are collected separately. Switching between depolymerization stages is achieved by increasing the depolymerization temperature when the temperature of the cooling medium in the condenser decreases. It is proposed that switching between depolymerization stages occurs when the temperature of the cooling medium in the condenser decreases.

[0014] By gradually increasing the depolymerization temperature, it is not only possible to initially dry the recycled material and remove water. These multiple depolymerization stages ensure that only the substance that depolymerizes at the reached depolymerization temperature, then rises and condenses, is present in the gas phase. This conversion to the gas phase, including evaporation, is also referred to as vaporization in the broadest sense, even though the boiling point is not yet reached. This prevents secondary reactions between different substances in the gas phase and the condenser, which could impede the process. Furthermore, only the specific oils from the respective vapor phase are produced in the condenser and collected in separate fraction collection containers. This makes it possible to separate different oils simply by their different rates of vaporization (i.e.,Evaporation and, if necessary, vaporization) are achieved directly, rather than in a rectification column. Furthermore, this stepwise increase in the depolymerization temperature reduces the total energy required, as the entire substance does not need to be heated to its maximum temperature. Instead, each component is heated only to a specific vaporization temperature, at which point it escapes, and the volume for the next depolymerization stage is continuously reduced.

[0015] During the depolymerization of specific substances in the depolymerization stage, the available volume of these substances decreases over time. This leads to a noticeable drop in the temperature of the cooling medium in the condenser when the specific amount of substance has been largely depleted. Therefore, the temperature of the cooling medium can be used to control the depolymerization process in a simple and reliable manner and to switch to the next depolymerization stage with a higher depolymerization temperature.

[0016] A combustible gas fraction can be fed to a pilot-ignition engine (e.g., a gas engine and / or oil-fired combustion engine) or, potentially, even a gas turbine to convert energy from this gas fraction into mechanical energy, electrical energy, and / or thermal energy. This means that during the oiling of hydrocarbon-containing waste materials, not only are oil fractions captured, but the gas phase can also be directly converted into usable energy. It is also conceivable that the combustible gas fraction is captured and collected for later use. By connecting it to a pilot-ignition engine that extracts the gas fraction, the entire system can be operated under negative pressure. This reduces or even eliminates the need for filters to the environment.

[0017] As a first step, depolymerization can be carried out at a temperature in the range of 100°C to 150°C to evaporate water and allow the condensed water to drain from the condenser. This has the advantage that the recycled materials are dried in this first depolymerization stage and atmospheric oxygen is displaced from the gas space.

[0018] It is also conceivable to add additives to the hydrocarbon-containing waste materials to catalytically support depolymerization and / or to chemically neutralize or bind components of the waste materials. The use of such catalysts can lower the decomposition temperature. The addition of catalysts can also support the conversion of long-chain and short-chain hydrocarbons. Interfering components of the waste materials used, such as nitrogen, chlorine, sulfur, etc., can be neutralized in the liquid phase of the evaporator (i.e., the depolymerizer) by adding suitable chemicals, or bound as salts, oxides, hydroxides, etc., in the solid state of the process.

[0019] The condensation step can be performed using at least one selected condenser from a plurality of condensers. It is conceivable that at least two condensers are connected in series or parallel. This allows for two different temperature ranges of the cooling medium. For emission and fire safety reasons, it is desirable that the condensed oil does not exceed 50°C. Using a single condenser would result in a correspondingly low outlet temperature of the cooling medium, making further heat utilization uneconomical. However, with a multi-stage condenser, at least the first condenser in a series can achieve a significantly higher outlet temperature of the cooling medium, exceeding 100°C. At this temperature level, the waste heat from the cooling medium is technically usable and can be further utilized as energy.

[0020] Connecting multiple capacitors in parallel not only doubles the power output but also allows one of the capacitors to be used as a cold trap. This is particularly useful for substances that transition directly from the vapor phase to the solid state (sublimation). Sulfur, for example, undergoes sublimation, which can cause the substance to solidify and clog the capacitor. With multiple capacitors operating in parallel, one can be specifically designated as a cold trap for these substances. Since the vapor phase contains only the substance that evaporates at the set depolymerization temperature, no other substances are condensed in the cold trap that would then need to be reheated. Once the respective substance has been collected, the process can be switched back to the other capacitor, and the one serving as the cold trap can be cleaned.

[0021] It is advantageous to reheat the oil-containing vapor rising in the evaporator in such a way as to reduce the formation of condensate that flows back into the evaporator. This reheating can be achieved, for example, with an additional heater on the lid and / or in the area of ​​the evaporator's outlet line. Such reheating ensures that condensation of the vapor phase only occurs in the condenser and that the depolymerization process in the evaporator is not impaired by backflowing condensate. This reheating can also be advantageously used independently of a specific control system for switching between the depolymerization stages.

[0022] One possibility is to introduce an inert gas, such as carbon dioxide, into the device. This would inertize the atmosphere within the system, preventing the oil vapors from reacting with the air. Furthermore, this method improves fire safety and emission control, as the device can be purged with carbon dioxide before each emptying, preventing air from entering.

[0023] It is advantageous to supply hydrogen to the system during or after the depolymerization process to bind free carbon ends in the condensed oils and prevent oxidation during storage. This also prevents the oils from darkening. Hydrogen can be easily supplied by switching the gas inlets provided for inerting.

[0024] By directly introducing hydrogen into the vaporizer, the oil vapors are hydrogenated as they are generated. This prevents the free carbon ends produced during depolymerization from combining with other substances, such as oxygen. Any unused hydrogen can then be easily converted into energy in a spark-ignition engine.

[0025] Additives can be introduced into at least one condenser to wash out or neutralize substances contained in the condensed oil. For example, the condensers can be equipped with a rinsing or spray system to simultaneously function as scrubbers. This is advantageous, for instance, when processing PVC, which decomposes into HCl and HC (hydrocarbons) when heated above 180°C. HCl (hydrogen chloride) reacts with water to form aggressive, corrosive hydrochloric acid, so the HCl should be washed out as quickly as possible. Therefore, it is conceivable to use sodium hydroxide (NaOH) in the condenser, which directly neutralizes the hydrochloric acid and converts the chlorine to sodium chloride (NaCl).

[0026] The base of the evaporator can have tapered elevations. For example, it can be comb-shaped or wavy. The resulting larger surface area allows for significantly more efficient heat transfer into the material being processed.

[0027] If a sieve plate is placed on the raised areas, such as the comb tips, the material to be processed can be placed on the sieve plate. At the appropriate temperature, the plastic components melt and flow downwards between the heating elements. There, they are exposed to a higher temperature and evaporate. The non-evaporable components remain on the sieve base and can thus be easily removed. Furthermore, the arrangement of the heating elements in these heating pockets allows for significantly more efficient use of the applied heat, as it radiates into the material from both sides and not just into the insulation.

[0028] The invention is explained in more detail below with reference to the accompanying drawing. The drawing shows: Figure 1 - Block diagram of a device for the oiling of hydrocarbon-containing oiling substances; Figure 2 - Sketch of an evaporator bottom with tapered elevations and a sieve plate placed on it.

[0029] Figure 1Figure 1 shows a block diagram of a device 1 for the de-oiling of hydrocarbon-containing recycled materials. Such recycled materials can be, for example, composite materials with plastic components or plastics. A so-called batch process is carried out, in which quantities of recycled materials are introduced discontinuously into an evaporator 2 (depolymerizer). The evaporator 2 has a thermally insulated evaporation chamber 3 into which the recycled materials are introduced. A heater 4 is arranged at the bottom of the evaporation chamber 3. After the evaporation chamber 3 is closed, the evaporator 2 is first heated in a first stage to approximately 100°C to 120°C by the heater 4 in order to drive off water and oxygen. The steam, which contains water in the first stage, rises and is discharged via a steam line 5 in the lid area of ​​the evaporation chamber 3 and introduced into at least one condenser 6a, 6b.The condensers 6a, 6b are supplied with coolant 7, so that the gaseous vapor, e.g., through evaporation or after reaching saturation vapor pressure through evaporation, is cooled again via the condensers 6a, 6b (heat exchangers) and condenses. The condensate is then collected in selectable fraction collection containers 8a, 8b, 8c, 8d, 8e, 8f.

[0030] For this purpose, the condensate drains of the condensers 6a and 6b can each be connected to at least one selectable fraction collection container 8a to 8f via shut-off valves 9. Shut-off valves 10a and 10b are also located at a gas inlet of the condensers 6a and 6b, allowing the condensers to be connected either individually or in parallel. A bypass valve 11 is also located at the outlet of the first condenser 6a and is connected to the inlet of the second condenser 6b via a bypass line 12. In this way, by opening shut-off valve 10a and closing shut-off valve 10b, and actuating bypass valve 11 so that the outlet of the first condenser 6a is connected to the inlet of the second condenser 6b, the two condensers 6a and 6b can be connected in series.

[0031] The output of the capacitors 6a, 6b is 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 storage tank 15 and a pilot-ignition engine 16 or a gas turbine that can be connected to it. The gas line 14 can also be connected directly to the pilot-ignition engine 16 via a direct line 17 without an intermediate control circuit of the gas storage tank 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. Controllable shut-off valves 19 are also provided here. By drawing in the gas fraction through the pilot-ignition engine 16, the system can be operated under negative pressure, which reduces the requirements for gas filters facing the environment or even makes them completely unnecessary. A negative pressure allows the gas flow in the system to be optimized.

[0032] After the recycling materials have been dried and oxygen driven off in the first stage, the depolymerization temperature is increased in several steps. In each step, depending on the depolymerization temperature, a fraction collection container 8a to 8f is selected by controlling the shut-off valves 9, in which the condensed oil formed at the respective depolymerization temperature is then collected. In the evaporator 2, a chemical-physical process takes place in which, by supplying heat and excluding oxygen, the recycling materials are heated under normal pressure to such an extent that the organic components depolymerize and transition into the gaseous state (i.e., evaporate in the broadest sense).

[0033] When thermoplastic materials are heated, for example, they begin to soften and then reach a melting point. At these temperatures, typically in the range of 200°C to 500°C (without the use of catalysts), the decomposition of macromolecules into a wide variety of lower-molecular-weight molecules takes place. This process produces gases such as methane and ethane, liquid organic compounds, water, and solid carbon. Heteroatoms such as nitrogen, sulfur, oxygen, and / or chlorine are also released. By heating in stages at different depolymerization temperatures, each substance is heated only until it reaches its depolymerization temperature. For water, this means heating only to approximately 100°C, and for other substances, the temperature is adjusted according to their specific properties. This reduces the energy required compared to heating the entire material to its maximum temperature.

[0034] The gas phase then contains only the substance that evaporates at the reached temperature. This prevents secondary reactions in condensers 6a and 6b, such as polycondensation or polyaddition between different substances, which could lead to the formation of new substances like waxes, paraffin, etc. This prevents any disruption to the process.

[0035] Since the vapor phase always contains only the substance that evaporates at the respective depolymerization temperature, only the specific oils from this vapor phase are produced in condensers 6a and 6b. These are collected in the respective, selected fraction collection vessels 8a to 8f. This makes it possible to separate the different oils directly through their differential evaporation rates, rather than requiring a rectification column into which the entire vapor mixture of all components flows.

[0036] The switching of the depolymerization stages by increasing the depolymerization and evaporation temperatures is achieved by measuring the temperature of the cooling medium 7 in the condensers 6a, 6b. If the temperature of this cooling medium 7 drops in the at least one selected condenser 6a, 6b, this indicates that no substance suitable for the respective depolymerization temperature is present in the evaporator 2. Threshold values ​​can be specified for this temperature drop observed during switching. These threshold values ​​can be absolute or, preferably, relative threshold values, such as a reduction of 10% of the previously observed temperature.

[0037] Evaporator 2 also has an additional heater 20, which is located in the ceiling area of ​​evaporation chamber 3 and / or in the outlet area of ​​evaporator 2. This reheats the vapors to prevent the rising oil-containing vapor from condensing back onto the lid of evaporator 2 and dripping back down. This would require the depolymerization temperature in evaporator 2 to be significantly higher than the actual depolymerization temperature of the respective substance so that the temperature at the outlet of evaporator 2 is still above the condensate temperature. In that case, precise separation of the substances due to differing depolymerization temperatures would be problematic.

[0038] Furthermore, an inert gas source 21a is connected to the steam line 5. This allows the atmosphere in the device 1 to be inerted by the injection of, for example, carbon dioxide (CO2). This prevents reactions of the oil vapors with air and improves fire protection and emission control, since the device 1 can be purged with carbon dioxide before each emptying, before air enters the system.

[0039] Optionally, a hydrogen source 21b can be connected, for example, to the steam line 5 in a switchable manner, to supply hydrogen-containing gas to the condensed oils during the oiling process, sporadically in between, or after completion of the oiling process. This binds the free carbon ends of the recovered oils with hydrogen and reduces or completely prevents the tendency of the oils to oxidize. This prevents the oils from darkening and allows them to retain their typically honey-brown color.

[0040] The at least two capacitors 6a and 6b allow for both series and parallel connection. This enables the use of two different temperature ranges for the cooling medium 7. Since the oil condensate should not exceed 50°C for emission and fire safety reasons, a single cooler would have to operate with a cooling medium 7 outlet temperature above 50°C. This heat would be technically unusable. With a two-stage cooler, the first stage can easily have an outlet temperature exceeding 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 is technically usable. Since almost all the energy of the process is contained in the oil vapor as evaporation energy, this represents economically significant quantities of heat and energy.

[0041] Connecting capacitors 6a and 6b in parallel not only doubles the power output but also allows one of the capacitors to be used as a cold trap. This is particularly useful for substances that sublimate directly from the vapor phase to the solid state. Sulfur, for example, can be a substance that, in this process, can become trapped and clogged within capacitors 6a and 6b. With two capacitors 6a and 6b connected in parallel, one can be specifically used as a cold trap for these substances. Of course, more than two capacitors 6a and 6b can also be connected in parallel. A combination of parallel and series connections of more than two capacitors is also possible.

[0042] The control of the heater 4 and, if applicable, the auxiliary heater 20 is based, for example, on the heat absorption of the cooling medium 7. When a substance evaporates and condenses again in the condenser 6a, 6b, it releases the heat of condensation to the cooling medium 7, which consequently heats up. Once the substance evaporating at the respective evaporation temperature in the evaporator 2 has completely evaporated, no more heat reaches the condenser 6a, 6b, and the temperature of the cooling medium 7 drops significantly, even though the temperature in the evaporator 2 remains constant. This means that the correct time has come to increase the temperature in the evaporator 2 to the next stage and simultaneously switch the condensate drain from the condensers 6a, 6b to the next fraction collection container 8a to 8f (condensate tank).

[0043] Condensers 6a and 6b can be extended with a rinsing or spray device to allow at least one of them to also function as a scrubber. This is particularly useful when processing PVC, which decomposes into HCl and HC components when heated above 180°C. HCl reacts with water to form hydrochloric acid, an aggressive and corrosive substance. Therefore, it is advantageous to wash out the HCl as quickly as possible. For this purpose, sodium hydroxide (NaOH) can be used in condensers 6a and 6b, directly neutralizing the hydrochloric acid and converting the chlorine to sodium chloride (NaCl).

[0044] The oils collected in the fraction collection containers 8a to 8b can be fed to a pilot-ignition engine 16 or a turbine to convert the energy contained in the oils into mechanical, electrical and / or thermal energy.

[0045] The ignition jet engine 16, which is located in the Figure 1It is actually powered by a gas mixture. It is conceivable that the pilot-injection engine 16 is a pure gas engine. The recovered oils can be supplied to an optional additional oil combustion engine for further energy conversion into electrical and thermal energy. However, it is also possible that the pilot-injection engine 16 is a combined gas and oil engine that is powered by both the gas fraction and the liquid oil fraction.

[0046] By using a pilot-ignition engine 16, it is also possible to use other gaseous fuels, such as landfill gas or wood gas.

[0047] The device 1 can be combined with a combined heat and power plant to utilize the heat W and electrical energy E generated in the device 1 for further use.

[0048] The exhaust gas flow A from the pilot-ignition engine 16 can also be used, under certain circumstances, with the help of a heat exchanger to generate energy and optimize the efficiency of the device 1.

[0049] Device 1 has the advantage that the oiling process produces an easily stored and transportable energy-rich product that can be used in a variety of ways, both as a fuel and as a basic chemical feedstock. The purification of the produced oil takes place in the liquid phase and can be repeated as often as needed. Batch oiling is economically viable even in small units and is therefore very well suited for decentralized systems. Operating the batch oiling system is significantly simpler than operating a combustion plant, with the process being able to be switched on and off very quickly and being very easy to operate. The excellent storage capacity of the recovered oils in the fraction collection containers 8a to 8f makes it possible to operate power plants that are only switched on during peak demand. Device 1 can therefore be used to complement wind and solar energy plants.

[0050] It is also conceivable to add catalysts to evaporator 2. This can support the conversion of long-chain hydrocarbons into short-chain hydrocarbons. Undesirable components of the waste materials used, such as nitrogen, chlorine, sulfur, etc., can be neutralized in the liquid phase of evaporator 2 by adding suitable chemicals, or bound as salts, oxides, hydroxides, etc., in the solid residue of the process. The evaporation temperature is increased in several stages, starting with an initial stage of approximately 100°C (80°C to 120°C) and then in at least two further stages to approximately 340°C. In the first evaporation stage, water-containing vapor is generated, which may also contain small amounts of oil. In the next two or more evaporation stages, after the water has been driven off, oil-containing vapor is generated, which in at least two further stages contains different oil fractions.This means that at least three evaporation stages are provided.

[0051] Suitable materials for recycling include mixtures or composite materials containing a significant proportion of organic matter, such as all types of plastics including PVC, rubber, waste oils, waxes, fats, transformer oils, hydraulic oils, refinery residues, concrete, tars and hospital waste, which are completely sterilized in evaporator 2.

[0052] The non-gasifiable components of the recycled materials remain in the evaporator 2 and can be disposed of. In addition to the condensable gases, gases that do not condense at room temperature, such as butane, propane, and methane, are also produced. Depending on the recycled material, this can amount to approximately 10% to 15% of the total recycled material. These gases can be fed directly into a gas engine for electricity generation. The electricity generated can be used for the self-sufficiency of the device 1, for example, to power the heater 4, and any surplus electricity can be fed into a power grid. A second combustion engine 16 or an emergency flare may be required to provide redundancy.

[0053] Depending on the level of contamination, the oil collected in the fraction collection containers 8a to 8f can be subjected to further cleaning or can be used directly for use in a diesel engine of a combined heat and power plant.

[0054] The heat generated by the heat exchangers (condensers 6a, 6b) and the pilot-ignition engines 16 can optionally be used for pre-drying the recycled materials or, if necessary, for other purposes. Pre-drying reduces the residence time in the evaporator 2 and thus the energy input required in the evaporator.

[0055] It is conceivable to connect several evaporators 2 in parallel to increase the throughput.

[0056] Once oil production is complete, i.e., when no more vaporizable substances remain in evaporator 2, evaporator 2 is cooled down. During this time, a second evaporator can be connected to steam line 5 to continue operating the downstream system. The cooled evaporator 2 is then emptied and reloaded with new raw materials. To reduce emissions from the system, particularly when evaporator 2 is opened, it should be purged internally with an inert gas, such as carbon dioxide, before being opened. The gas escaping during this purging process should then be adequately filtered.

[0057] The fraction collection containers 8a to 8f should also have suitable air filters 22 for ventilation.

[0058] Figure 2Figure 1 shows a sketch of an evaporator base 30, which has tapered projections 31 and a sieve plate 32 placed on the projections 31. Heating elements 33 are arranged in the outer space of the evaporator 2 between the projections 31, below the horizontal sections of the evaporator base 30, and optionally on the side walls. The plastic recycling products to be melted are placed on the sieve plate 32, which is preferably loosely placed on the comb tips. The plastic components melt at the appropriate temperature and flow downwards into the trough-shaped sections adjacent to the heating elements 33. There, they are exposed to higher temperatures and are evaporated. The non-evaporable components remain on the sieve plate 32 and can thus be easily removed.

Claims

1. Method for oiling hydrocarbon-containing recyclable materials by - depolymerizing the recyclable materials, - introducing the oil-containing vapor produced in the depolymerization step into a condenser (6a, 6b) to form condensed oils, and - collecting the oils condensed in the condenser (6a, 6b), wherein the depolymerization step is carried out in several stages at different temperatures and the fractions of condensed oils formed in each stage are collected separately from one another, characterized in that switching between the depolymerization stages is effected by increasing the depolymerization temperature when the temperature of the cooling medium (7) in the condenser (6a, 6b) drops.

2. Method according to claim 1, characterized by feeding a combustible gas fraction to an internal combustion engine (16) or a gas turbine for converting energy from this gas fraction into mechanical energy, electrical energy, and / or thermal energy.

3. Method according to claim 1 or 2, characterized in that, in a first step, depolymerization takes place at a temperature in the range from 100°C to 150°C to evaporate water and to remove condensed water from the condenser (6a, 6b).

4. Method according to one of the preceding claims, characterized by the addition of additives to the hydrocarbon-containing recyclable materials for catalytic support of the depolymerization and / or for chemical neutralization or binding of components of the recyclable materials.

5. Method according to one of claims 1 to 4, characterized in that the condensation step is carried out with at least one selected condenser (6a, 6b) from a plurality of condensers (6a, 6b).

6. Method according to one of the preceding claims, characterized by reheating the oil-containing vapor rising in the evaporator (2) in such a way that the formation of condensate flowing back into the evaporator (2) is reduced.

7. Method according to one of the preceding claims, characterized by supplying inert gas into the device at the beginning and / or at the end of a depolymerization process.

8. Method according to one of the preceding claims, characterized in that the oil-containing vapor is introduced into a plurality of condensers (6a, 6b) connected in series one after the other or parallel or condensers (6a, 6b) connected in parallel.

9. Method according to one of the preceding claims, characterized by supplying additives into the at least one condenser (6a, 6b) for washing out or neutralizing substances contained in the condensed oil.

10. Apparatus (1) for oiling hydrocarbon-containing oiling substances, comprising an evaporator (2) having an evaporation chamber (3) for receiving the oiling substances and a heater (4) for heating the oiling substances, a condenser (6a, 6b) connected to the evaporator (2) and designed to form condensed oils from oil-containing vapor produced in the evaporator (2), wherein the outlet of the condenser (6a, 6b) can be selectively connected to a fraction collection container (8a-8f), and wherein the device (1) is designed to control the heating (4) of the evaporator (2) in stages in order to evaporate the recyclable materials in several stages at different temperatures and to collect the fractions of condensed oils formed in each stage separately from one another in selected fraction collection containers (8a-8b), characterized in that the device (1) is designed to switch between the depolymerization stages by increasing the depolymerization temperature when the temperature of the cooling medium (7) in the condenser (6a, 6b) drops.

11. Device (1) according to claim 10, characterized in that the device (1) has an internal combustion engine (16) or a gas turbine which is designed to convert energy from a combustible gas fraction of the depolymerized recyclable materials supplied to the internal combustion engine (16) or the gas turbine into mechanical energy, electrical energy and / or thermal energy.

12. Device (1) according to claim 10 or 11, characterized in that an additional heater (20) is arranged in the ceiling space and / or in the outlet area of the evaporator (2).

13. Device (1) according to one of claims 10 to 12, characterized in that an inert gas feed (21, 19) is provided in the connecting line (5) between the evaporator (2) and the condenser (6a, 6b).

14. Device (1) according to one of claims 10 to 13, characterized in that several condensers (6a, 6b) connected in series or in parallel and / or several evaporators (2) connected in series or in parallel are provided.

15. Device (1) according to one of claims 10 to 14, characterized in that the evaporator (2) has tapered projections (31).

16. Device (1) according to claim 15, characterized in that a screen plate (32) is mounted on the elevations (31).