WO2005071043A1

WO2005071043A1 - Device and method for recovering fractional hydrocarbons from recycled plastic fractions and/or from oily residues

Info

Publication number: WO2005071043A1
Application number: PCT/EP2005/000661
Authority: WO
Inventors: Wolf-Eberhard Nill; Anton Schmillen; Gerold Weser
Original assignee: Nill Tech Gmbh
Priority date: 2004-01-24
Filing date: 2005-01-24
Publication date: 2005-08-04
Also published as: CA2558347C; EP1745115B1; DK1745115T3; SI1745115T1; CA2558347A1; PT1745115E; DE502005010684D1; PL1745115T3; EP1745115A1; ATE491771T1

Abstract

The invention relates to a method for recovering fractional hydrocarbons from recycled plastic fractions, which are sorted according to type and compacted under the exclusion of air using a feed system (1, 2, 3, 4), the compacted mass being supplied to a fusion container (7), where it is heated. The mass is separated into a first liquid phase, a first gas phase and a residual fraction, the liquid phase and the first gas phase are then transported to an evaporation container (20), in which a second liquid phase and a second gas phase are produced by the application of heat. The second liquid phase is transferred to a secondary heater (23) and heated further to produce a third gas phase. The second gas phase and the third gas phase are then supplied to a cracking tower (27), in which further cracking of the long-chained hydrocarbons occurs and short-chained hydrocarbons are produced. The oil gas is supplied to a primary condenser (30), in which it is condensed to liquid oil, the latter constituting the target product.

Description

DEVICE AND METHOD FOR OBTAINING FRACTURED CARBON HYDROCARBONS FROM PLASTIC MATERIALS AND / OR OIL-RESISTANT RESINS

Technical field: The invention relates to a method for obtaining fractionated hydrocarbons from plastic materials and / or from oily residues, wherein the plastic materials and / or residues are sorted by grade and compacted using a registration system and the compacted mass is fed to a melting vessel and heated therein ; Likewise, the invention relates to an apparatus for carrying out the method for obtaining fractionated hydrocarbons from plastic materials and / or oil-containing residues.

PRIOR ART: Plastics are used today in almost all areas of life and must be recycled after use and / or disposed of. At the same time, health-friendly disposal poses considerable problems. Plastics such as polypropylene (PP), polyethylene (PE) or polystyrene, which consist of long-chain macromolecules, must be split into small molecules for their utilization. Through a conversion plant, such plastics can be converted in a low-temperature cracking process into an oil-like product with gaseous admixtures and a solid residue.

The gas resulting from the cracking process consists of a mixture of methane, ethane, ethene, propane, propylene, i-butene, i-butane, 1-butene, 1-butane, pentane and the like, as well as a small amount of water vapor. The polystyrene-derived oil consists of more than 50% styrenes and also contains 2-methyl-styrenes, toluene, ethylbenzene and benzene. The oil obtained from polyethylene and polypropylene consists mainly of paraffins and olefins and contains only small amounts of aromatics. The low-volatile residues consist of cokes, heavy oil long-chain hydrocarbons. The oil-like residue can in a further process step

BESTATIGUNGSKOPIE be mixed with water. This produces an oil / water emulsion, which can be utilized energetically, for example as a lighting agent.

CN 1284537A has disclosed a process for recovering hydrocarbons, such as gases or oils, from plastic materials, which has a melting and cracking process with subsequent oil gas separation and distillation of the oil mixture. For this purpose, plastic raw materials are melted and vaporized within a container (melting and cracking reactor). The plastic raw materials are heated to 280 ° C to 380 ° C and cracked. The disadvantage here is the single-stage entry of the necessary heat energy. The high heat flow density leads to strong partial overheating. These then lead to the formation of clogs, which worsen the further heat input. As a result, the heat consumption is high in relation to the yield. Furthermore, CN 2435146Y has disclosed a similar method.

Technical task:

The invention has for its object to further develop the aforementioned method and the device such that the energy input is improved and that in particular by an optimal and targeted use of energy and heat recovery in untersc different areas, the efficiency of the method and the device is verb essert ,

DISCLOSURE OF THE INVENTION AND ITS ADVANTAGES: This object is achieved according to the invention by a process for obtaining fractionated hydrocarbons from plastic materials and / or from oily residues, wherein the plastic materials and / or residues are sorted by type and compacted using an entry system with exclusion of air and the compressed mass is supplied to a melting vessel and heated therein, so that a separation into a first liquid phase, a first gas phase and a residue portion takes place, after which the liquid phase and the first gas phase are transported into an evaporation vessel in which further heat input a second liquid phase and a second gas phase is formed, the second liquid phase is transferred to a reheater and further heated there with further heat input, so that a third gas phase is formed, after which the second gas phase from the evaporation tank and third gas phase from the reheater are fed to a cracking tower, where further breakage (cracking) of the long-chain hydrocarbons into short-chain hydrocarbons takes place and the resulting oil gas is then fed to a condenser in which the oil gas is condensed to liquid oil, the oil being the target product.

In a further embodiment of the method according to the invention, this is carried out using a multi-circuit, indirect heating system which generates the process heat for the melting tank, the evaporation tank and the reheater, it being possible to use oil or salt or gas as the heat carrier. For this purpose, a non-condensable fraction of the oil gas for thermal utilization can be supplied to the heating system for firing the same in an advantageous manner. The heating system thus comprises all components for the supply of the melting vessel and the evaporation vessel with energy. The thermally recoverable by-products formed in the process, such as a fraction of an oil-water emulsion from the residue components from the melting tank and otherwise unusable gas fractions from the crack tower and a gas fraction from a flame arrester, are advantageously used in the heating system for generating the primary process heat.

In addition, a maximum of heat from the area of the oil gas and residue precooling from a cooling system is advantageously returned to the heating system. For this purpose, the capacitor can consist of a precondensator and a main capacitor, which can be connected to a multi-circuit cooling system. The excess heat from the pre-condenser, the main condenser and the residual pre-cooling tank is thus fed to the heating system. Likewise, the oil-water emulsion for thermal utilization can be supplied to the heating system for firing. The inventive method advantageously has a low energy consumption and optimum energy utilization by means of heat recovery, based on the yield. In particular, the heating circuit in the different process areas advantageously heats indirectly and specifically. In particular, by means of the method according to the invention, plastic materials can be recycled in accordance with the regulations on waste recycling.

In a further embodiment according to the invention, a precondensator and a main capacitor are used as the capacitor, the excess heat from the precondensator, the main capacitor and the residual precooling vessel being supplied to the heating system, and the main capacitor being connected to a multicircular condensation system.

In a further embodiment according to the invention, the plastic materials and / or oily residues are comminuted in a pretreatment process after sorting and optionally dried before the cracking process is carried out. The plastic materials are sorted by PP, PE and PS into hard and soft plastic parts. Since the water content of the plastics should be below 1% for energy reasons, plastics with a higher water content are dried beforehand. To enter the plastic materials and / or the oil-containing residues in the melting container can be used within the registration system a stuffing screw or a Stopfwerk, which compacts the residues for oxygen deprivation. Likewise, the plastic materials should be fed fine shredded the stuffing screw or Stopfwerk.

In a further embodiment of the method according to the invention, the residue fraction within the melting vessel is transported to a sedimentation compartment underneath, where the residue fraction is concentrated and then the concentrated residue fraction is transferred to a residue precooling vessel, in which the residue fraction is cooled by means of a cooling medium, preferably below 120 ° C. The cooled residue fraction can be fed to an emulsion unit in which an oil-water emulsion is prepared from the residue fraction.

In a further embodiment of the method, a precondensator is arranged between the cracking tower and the main condenser, which pre-cools the oil gas and recovers heat at a high temperature level and reduces the temperature gradient between cracking tower and main condenser. Furthermore, the main capacitor and optionally the precondensator can be connected to a multi-circuit cooling system.

The inventive method is preferably carried out between 300 to 450 degrees Celsius and normal pressure up to 2 bar overpressure.

A device according to the invention for the extraction of fractionated ohlen hydrogen from plastic materials and / or from oil-containing residues, wherein the plastic materials and / or the residues are sorted by variety, is characterized by a registration system for the compression of the plastic material and / or the oily residues with exclusion of air, and by a downstream melting tank for heating and melting the compacted mass to produce a first liquid phase, a first gas phase and a residue portion, wherein after the AufschmelzbehäHer for generating further heat input of a second liquid phase and a second gas phase, an evaporation tank is disposed on welc to Initiation and further heating of the second liquid phase, a reheater follows the emergence of a third gas phase, and the evaporation tank and the reheater to separate the resulting oil gas from black a cracking tower is connected to the oil and unvaporised plastic parts, to which a main condenser is connected to condense the oil to liquid oil.

In a further refinement of the device, a stuffing screw or a stuffing plant for compacting the plastic substances and / or the oil-containing residues in the melting container within the registration system of the plastic material and / or the oily residues, in front of which, if necessary, a spherical transfer container for transfer into the stuffing screw or Stopfwerk is located. The exit of the plug screw or the stuffing machine opens below the liquid level of the molten mass into the melting container.

In a further embodiment of the device, the same has a multi-circuit heating system for generating the necessary process heat at this optimized temperature levels, serving as a heat carrier oil or salt or gas.

In a further embodiment of the device, a sedimentation compartment for receiving the residue fraction is arranged below the melting tank. To the sedimentation compartment can be arranged a residue precooling container as well as an emulsion unit for producing an oil-water emulsion from the residue portion.

In a further embodiment of the device, the capacitor is formed of a main capacitor and a precondensator, wherein between the cracking tower and the main capacitor for precooling of the oil gas, the precondensator is arranged. Furthermore, a multi-circuit cooling system can be connected to the main capacitor.

In a further embodiment, the device for generating the process heat for the melting tank, the evaporation tank and the reheater on a multi-circuit heating system.

Furthermore, the melting tank and the evaporation tank and, if appropriate, the after-heating tank have an externally arranged heating jacket and / or internal heating coils which can be heated by the common heat carrier heating system.

Short name of the drawing, in which show:

1a, 1b and 1c a process plant distributed over three figures, to win 2 is a modified registration system compared to that of Figure 1 Figure 3 is a similar to Figures 1a, 1 B and 1c process plant in which the heat transfer and cooling circuits are shown in more detail Figure 4 is another registration system a process plant

Figure 5 shows another registration system of a process plant with a cooling jacket around the supply pipe and plug screw shell in front of another melting tank

Figure 6 shows another example of a main capacitor and

FIG. 7 shows a further process plant similar to FIG.

PREFERRED EMBODIMENT OF THE INVENTION The process plant for obtaining fractionated hydrocarbons, from plastic materials and / or oily residues shown in the figures, consists of a silo installation 1, in which the plastic materials to be treated, preferably in the shredded state, are stored. The storage can also be done in a bunker. To remove the plastic materials is a marked by the letter "M" motor-driven trough screw conveyor 2 connected to the silo 1, which promotes a transfer container 3, for example, a flanged ball housing for flexible adaptation to different local conditions. At the transfer container 3, a stuffing screw 4 or a Stopfwerk connects, which compresses the plastic materials and thus largely expels the air and thus the oxygen. The lower end of the plug screw 4 or Stopfwerks opens into a melting tank 7 and that below or above its level. Between the end of the screw conveyor 4 or the Stopfwerks and the confluence with the Aufschmelzbehälter 7 a pneumatically operated throttle-check valve 5 is arranged, which is followed by an entry fitting 6 in the form of a ball valve 6. The melting tank 7 has at its lower end a sedimentation compartment 10 for receiving and concentrating a residue fraction which precipitates out of the liquid phase of the compacted mass. The sedimentation compartment 10 is conductively connected via three successive residue discharge fittings 11, 12 and 13 to a residue precooling vessel 15, which has an outer cooling jacket 14. Within the residue Vorkühlbehälters 15 an accumulation of the residue and a cooling of the residue by means of a cooling medium from a cooling system 34, preferably below 120 ° C. The pre-cooling of the residue takes place under the possibility of heat recovery in the heating system, thereby reducing the temperature gradient between Melting tank 7 and a subsequent emulsion unit 16 is given.

The cooled residue is fed to the emulsion unit 16 in which an oil-water emulsion is produced by means of a motor-driven agitator from the residue fraction. By reducing the temperature gradient also reduces the necessary water mask in the emulsion unit 16, whereby a higher oil concentration in the oil-water emulsion is possible and thus the calorific value of the same is raised.

The reflow vessel 7 has a stirrer 9 for homogenizing the molten plastic mass and a Abrakeleinrichtung 17 for stripping the inner wall of the reflow vessel 7 in the region of the mouth of the screw conveyor 4 or Stopfwerks. Furthermore, the melting tank 7 is closed at the top and has a lateral outlet A in the upper area. This provides great strength in the area of the upper tank bottom by reducing the number of openings. Furthermore, the melting container 7 is surrounded by an outer heating jacket 8, which is constructed such that a homogeneous heat input is given and in particular heat peaks are avoided during operation. Likewise, the outer heating jacket 8 allows heat removal, condensation, before maintenance or even in case of an accident. Furthermore, the melting tank 7 and the evaporation tank 20 may be equipped with hinged concentric coiled tubing, for example two. By using coiled tubing for heat transfer, a larger transfer area is achieved.

Within the melting tank 7, a heating of the plastic mass takes place, so that a separation into a first liquid phase, a first gas phase and a residue portion takes place, after which the liquid phase and the first gas phase via the outlet A are transported in a conduit in a Verdampfungs- 20, in which under further heat input into the mass a second liquid phase and a second gas phase is formed. The evaporation vessel 20 is used for evaporation of valuable parts with higher evaporation temperatures. The outlet A of the melting tank 7 and the inlet A of the evaporation tank 20 may have an additional heater 18, such as electric immersion heater, to which a further reheater 19 can connect to increase the heat input in the inlet of the evaporation tank 20.

The heat input into the evaporation tank 20 is controlled by a heating jacket 21 and / or heating coils at a higher level than in the melting tank 7 in a reduced amount of plastic, whereby a reduction in the amount of energy is given at a high temperature level. Also, the evaporation vessel 20 has a motor-driven agitator 22 for homogenizing the molten recyclable material. Within the evaporation container 20, the formation of a second liquid phase and a second gas phase takes place.

Parallel to the evaporation tank 20 a Nachheizbehälter 23 is connected by line, which has its own heater 24, which may be an electric heater E. The Nachheizbehälter 23 is used for further reheating and vaporizing an even smaller amount of recyclables than in the evaporation vessel 20 with the highest evaporation temperatures of the recyclables, so that in him a third gas phase is formed. The evaporation tank 20 is down by means of a residue discharge fitting 25, for example of the type ball valve, closed to discharge residues. The Nachheizbehälter 23 has in turn at its lower end an emptying valve 26 for emptying the Nachheizbehälters 23.

On the evaporation vessel 20, a cracking tower 27 is placed, which serves to break up the long-chain molecules into short-chain molecules; in Crackturm 27 there is a separation of the resulting oil gas from high-boiling components. Also, the Nachheizbehälter 23 is connected in line with the cracking tower 27, so that in the same both the second gas phase from the evaporation tank 20 and the third gas phase is introduced from the Nachheizbehälter 23. Via a product gas line 28, namely a pipe 28, the discharge of the product gas formed in the cracking tower in a pre-condenser 29 can be carried out, which works as a heat exchanger to recover heat at a high temperature level, so that this pre-cooling of the product gas with the possibility of heat recovery in the Heating system is done. The oil is then fed to the main condenser 30, in which the oil gas is condensed to liquid oil.

The main condenser 30 has two cooling circuits, namely a sump cooling condenser 31 and a head cooling condenser 32. The main condenser 30 has an incoming and outgoing line with a circulating pump 35 for circulating the oil. Also located in the line are two automatic valves with a throttle function for switching and dividing the recirculation flow to the main condenser 30 or into a transfer line 37 to a separator (not shown). The conduit further has a metering point 40 as an injection site for delivery of additives, for example, to condition, stabilize and adjust product properties of the product oil.

Addition of an additive can also be made in the line between cracking tower and main condenser. Furthermore, the main condenser 30 is conductively connected via a residual gas outlet 39 to a heating system 38 of the process plant, via the residual gas outlet 39, a derivation of the non-condensable portion of the product gas in the heating system 38 of the process plant for thermal utilization in the heating system.

The main condenser achieves a very rapid cooling and condensation of the hot product gas (shock cooling) to an average temperature level of 80-200 ° C by applying the process principle quenching.

The quench medium used is cooled condensate (product oil). The quenching can be carried out in two different ways: The hot gas stream is sucked into the liquid recycle stream from cooled condensate, where due to the high turbulence intensive heat exchange and instantaneous condensation of the product gas occurs. Or alternatively, the quench can be carried out as a packed column, wherein a liquid recycle stream of cooled condensate is trickled over the packing and hot product gas flows in countercurrent from bottom to top and thereby condenses. Due to the large surface of the packing, an intensive heat exchange between cold condensate and hot product gas is achieved, so that the latter condenses immediately.

Thus, by arranging two packed columns, the one can be regenerated while the other is operating normally, with the regeneration of the recycle stream in the packed column to be regenerated being shut off and the hot gas stream coming from the cracking tower being passed through the packed column to be regenerated, thereby causing the bed to fill is heated and deposits are replaced. The regeneration of the packed columns thus happens alternately.

In a further modification of the invention, the heat exchangers of the main capacitor do not necessarily have to be inside the condenser, for example be arranged as bottom and head cooling, but it is sufficient a heat exchanger in the line of the circulating flow.

The heating system is preferably multi-circuit for generating the necessary process heat at this optimized temperature levels. As a heat carrier oil or salt or gas can be used for heat transfer with adjustable maximum heating temperature. The efficiency of the heating system is thereby maximized by providing heat recovery to the system using the residual gas to fire the heating system. Thus, the method according to the invention does not require the separate gas combustion, gas flare, required in the prior art. The maximum energy utilization is also given because flexible heating of the heating system is possible by means of several optimized temperature levels, namely by the product oil, by the product gas and by the oil-water emulsion, as well as electrically or by a combination of the various aforementioned energy sources. In order to record and monitor the amounts of energy, the resulting temperature differences, the different pressures as well as the different flow rates of the heat transfer medium circuits can be used.

FIG. 2 shows a modified registration system compared to that of FIG. 1. The connecting tube of the melting container 7 for connecting the screw conveyor 4 or the stuffing mechanism is here formed at an acute angle to the melting container; otherwise the design is the same.

FIG. 3 shows a process plant which is very similar to that of FIGS. 1a, 1b and 1c and in which the heat transfer and cooling circuits are shown completely. The heating system 38 is divided into five heat carrier circuits WT 1 to WT 5. WT 1 is connected via lines to the reflow tank 7 and supplies it with heat energy; Similarly, WT2 is connected to the evaporation vessel 20. WT 3 or WT 4 or WT 5 is connected to the heat removal with the precondensator 29 or with the cooling system 34 or with the residue precooling container 15. Figures 4 and 5 show two further examples of different registration systems of a process plant according to the invention. The reflow containers 39 shown here have an upper filler neck 40, through which a feed tube 41 is guided, whose opening is below the liquid level 42 of the liquid melt. In FIG. 5, the feed tube 41 and the screw plug are additionally surrounded by a cooling jacket 43, through which cooling water flows.

FIG. 6 shows a further example of a main capacitor 44 of the process plant according to the invention. The hot gas enters through the opening 45 in the main condenser 44 and flows through packed columns 46, in which there are Füllkörperschüttungen, such as rings made of stainless steel. Liquefied condensate is withdrawn from the sump 54 via a line 47 and fed via a pump 48 two series-connected heat exchangers 49, 50 and further cooled, which are connected to a cooling system 55 with two cooling circuits, cooling circuit I and cooling circuit II. By means of a return line 51 to the second heat exchanger 50, cooled condensate is fed back into the main condenser 44 in countercurrent, as can be seen in FIG. As a result, the gas flowing through the packed columns 46 is cooled shock-like. Via the overhead outlet 53, which corresponds to the outlet 39 in FIG. 1c, non-condensed residual gas is either used as combustion gas or a further condenser can follow here, by means of which remaining portions of HCs within the residual gas are condensed. Via a branch line 52 to the second heat exchanger 50 and before the return line 51, the liquid oil, the target product of the process plant, is removed.

FIG. 7 essentially differs from FIG. 3 only in that heating coils 56, 57 are additionally installed in the melting tank 7 and in the evaporation tank 20 in order to increase the introduction of heat into the masses. These heating coils 56, 57 are connected to their supply according to the figure 7 to own heat transfer medium circuits WT circuit 1 and WT circuit 2 of the heat transfer heating system 58, which either gas-fired ÖI - for example, with the residual gas from the main capacitors 30 and 44 - or electrically heated. When using heating coils, the outer heating jacket can also be omitted.

From 100 kg of dry, clean and pure plastic materials, about 75-90 kg of product oil, 2-12 kg of residues and 2-15 kg of non-condensable gases are produced for thermal utilization in the heating system. The yield of product oil depends, among other things, on the types of plastic that are registered.

Industrial Applicability:

The inventive method or cracking method and the device are industrially applicable in the industries of hygienic workup for the recovery of plastic materials and / or oily residues or plastic waste and / or oily waste.

List of references: 1 Silo plant 2 Trough screw conveyor 3 Transfer container 4 Plug screw or Stopfwerk 5 Throttle check valve 6 Entry fitting 7, 39 Melting tank 8. 21 Heating jackets 9. 22 Agitators 10 Sedimentation compartment 11, 12, 13, 25, 26 Residual discharge fittings 14, 43 Cooling jacket 15 Residue pre-cooling tank 16 emulsion unit Spreader Heater reheater heater 19 Reheater Evaporator tank Reheater Crack tower Pipeline 28 Precondensator, 44 Main condenser Cooling system Heating system, 53 outlets Upper filler neck Supply tube Liquid level Main condenser opening Columns Pump, 50 Heat exchanger Return branching branch, 57 Heating coil Outlet

Claims

claims:

1. A method for obtaining fractionated hydrocarbons from plastic and / or from oil-containing residues, wherein the plastic materials and / or residues sorted by variety and compacted using an entry system (1, 2,3,4) with exclusion of air and the compressed mass is fed to a melting tank (7) preferably below the liquid level and heated therein, so that separation into a first liquid phase, a first gas phase and a residue portion takes place, after which the liquid phase and the first gas phase are transported into an evaporation tank (20), in which with further heat input, a second liquid phase and a second gas phase is formed, wherein the second liquid phase is transferred to a reheater (23) and further heated there with further heat input, so that a third gas phase is formed, after which the second gas phase from the evaporation tank (20 ) and dr The gas phase from the reheater (23) is fed to a cracking tower (27) where further cracking of the long-chain hydrocarbons into short-chain hydrocarbons takes place and the resulting oil gas is then fed to a condenser (30) in which the oil gas becomes liquid oil is condensed, wherein the oil is the target product.

2. The method according to claim 1, characterized in that it is carried out using a multi-circuit heating system (38) for generating the necessary process heat, which generates the process heat for the reflow tank (7), the evaporation tank (20) and the reheater (23) , where oil or salt or gas is used as a heat carrier.

3. The method according to any one of the preceding claims, characterized in that for entering the plastic materials and / or the oil-containing residues in the melting tank (7) within the registration system a stuffing screw (4) or a Stopfwerk is used, which the residues for Extracts oxygen deprived and enters into the Aufschmelzbehälter below the liquid level.

4. The method according to claim 1, characterized in that the middle and heavy fraction of the hot oil or cracking gas is quenched by quenching with cold condensate abruptly cooled to an intermediate temperature level and thereby condensed, so that simultaneously condense hydrocarbons medium to large chain length.

5. The method according to claim 4, characterized in that for carrying out the Quenchenprinzips the gas stream is either sucked into the cold, liquid recycle or over two Füllkörperschüt- lines within Füllkörperkolonnen, which are operated in countercurrent out, with cold condensate on the Sprinkles are sprinkled.

6. The method according to claim 4, characterized in that by the arrangement of two packed columns one can be regenerated while the other operates in control mode, being switched off for regeneration of the recycle stream in the packed column to be regenerated and coming from the Crackurm hot gas stream through the regenerated Passage column is passed, whereby the bed is heated in the same and deposits are detached.

7. The method according to any one of the preceding claims, characterized in that for generating the primary process heat, a non-condensable fraction of the oil gas for thermal utilization of the same is supplied to the heating system for firing.

8. The method according to any one of the preceding claims, characterized in that the oil-water emulsion for thermal utilization of the heating system (38) is supplied to the firing.

9. The method according to claim 1, characterized in that a precondensator (29) and a main capacitor (30) is used as the capacitor and the excess heat from the precondensator (29), the main capacitor (30) and the Rückkorkkühlbehälter (15) the heating System (38) is supplied, wherein the main capacitor is connected to a multi-circuit condensation system.

10. The method according to claim 1, characterized in that the plastic materials and / or oily residues are comminuted after sorting and optionally dried before performing the cracking process.

11. The method according to claim 1, characterized in that the residue fraction within the melting vessel (7) is transported to a sedimentation compartment below (10), where a concentration of the residue fraction takes place and then the concentrated residue fraction is transferred to a residue precooling vessel (15), in which a cooling of the residue fraction takes place by means of a cooling medium from a cooling system (34), preferably below 120 ° C.

12. The method according to any one of the preceding claims, characterized in that the cooled residue portion of an emulsion unit (16) is supplied, in which from the residue portion, an oil-water emulsion is prepared.

13. The method according to any one of the preceding claims, characterized in that between the cracking tower (27) and the main condenser (30) a precondensator (29) is arranged, which pre-cools the Olgas for recovering energy at a high temperature level and thereby the temperature gradient between Crackturm (27) and main capacitor (30) is reduced.

14. The method according to any one of the preceding claims, characterized in that the main capacitor (30) and optionally the precondensator (29) to a multi-circuit cooling system (34) is connected.

15. Apparatus for recovering fractionated hydrocarbons from plastic materials and / or from oil-containing residues, wherein the plastic materials and / or the residues are sorted by variety, characterized by a registration system (1, 2,3,4) for compacting the plastic materials and / or the oil-containing residues under exclusion of air, and by a downstream melting tank (7) for heating and melting the compacted mass to produce a first liquid phase, a first gas phase and a residue portion, wherein after the melting tank (7) for generating under further heat input of a second liquid phase and a reboiler (23) follows for the formation of a third gas phase, and to the evaporation vessel (20) and the reheater (23) for breaking up (cracking) a second gas phase an evaporation tank (20) is arranged on soft for initiation and further heating of the second liquid phase ) the long A cracking tower (27) is connected to the chain-like hydrocarbons in short-chain hydrocarbons, to which a condenser (30) is connected for condensing the oil gas into liquid oil.

16. The apparatus according to claim 15, characterized in that for introducing the plastic materials and / or oil-containing residues in the melting tank (7) within the registration system a plug screw (4) or a Stopfwerk for compacting the plastic material and / or the oil-containing residues is arranged in front of which, if appropriate, a spherical transfer container (3) for transfer to the packing screw (4) or the Stopfwerk is located.

17. The apparatus according to claim 15, characterized in that the output of the plug screw (4) or Stopfwerks below the liquid level of the molten mass within the Aufschmelzbehälters (7) opens into the same.

18. The apparatus according to claim 15, characterized in that the same has a multi-circuit heating system (38) for generating the necessary process heat at this optimized temperature levels, being used as the heat transfer oil or salt or gas.

19. The apparatus according to claim 15, characterized in that below the melting vessel (7) a sedimentation (10) for receiving the residue portion is arranged.

20. The device according to any one of claims 17 to 18, characterized in that the sedimentation (10) a Rückkorkühlbehälter (15) and thereon an emulsion unit (16) is arranged for producing an oil-water emulsion from the residue portion.

21. The apparatus according to claim 16, characterized in that the capacitor of a main capacitor (30) and a precondensator (29) is formed and arranged between the cracking tower (27) and the main capacitor (30) for precooling of the oil gas of the precondensator (29) is.

22. The apparatus according to claim 16, characterized in that to the main capacitor (30) a multi-circuit cooling system (34) is connected.

23. The device according to claim 16, characterized in that the same for generating the process heat for the reflow tank (7), the evaporation tank (20) and the reheater (23) comprises a multi-circuit heating system (38).

24. The device according to claim 16, characterized in that the reflow container (7) and the evaporation container (20) and, where appropriate, the Nachheizbehälter (23) has an outboard heating jacket (8,21) and / or coiled tubing (56, 57) which heating jackets (8,21) on the common heat carrier heating system (38) are heatable.