Pyrolysis system for producing hydrocarbon compounds from plastic residues

Abstract

The present invention relates to a pyrolysis system such as a pyrolysis plant (100) for generating hydrocarbon compounds from polymer residues such as synthetic polymers, the system comprising: - an agglomeration device (101) configured to receive and heat the polymer residue; - a degassing feeder configured to transfer the polymer residue from the agglomeration device and add a pH adjustment additive such as calcium oxide (CaO) to the polymer residue; - a degassing device conveyor (112) such as a degassing device screw conveyor configured to move the polymer residue to a degassing device outlet (122a), and a heater configured to heat the polymer residue to a temperature within the range of 240 to 280°C, the degassing device (102) configured to receive the polymer residue from the degassing feeder; and - a pyrolysis reactor (103) comprising at least one reactor conveyor (113) configured to move the solid portion of the polymer residue towards a black carbon outlet (123b), and a heater configured to heat the polymer residue to generate pyrolysis vapor, the pyrolysis reactor (103) having an inlet (123a) configured to receive the polymer residue from the gas device, and the pyrolysis reactor having a reactor vapor outlet (123c) for discharging the pyrolysis vapor containing the hydrocarbon compound.

Description

Technical Field

[0001] The present invention relates to a pyrolysis system, and more particularly to a pyrolysis plant for converting a plastic material, preferably waste plastic, into hydrocarbon products such as oil.

Background Art

[0002] To increase the amount of recyclable plastic waste, it is necessary to recycle plastic to make new plastic products. However, currently, only a very small part of plastic waste is directly recycled into new products, and most of it is discarded in incinerators, landfills, or the natural environment.

[0003] It is known to use a pyrolysis plant to convert waste plastic into oil products, and many different pyrolysis plants have been proposed.

[0004] However, such known pyrolysis plants still have the problem that it is difficult to process waste plastic on a large scale.

[0005] Therefore, there is a need for a pyrolysis plant that can process plastic waste on a large scale, efficiently and practically.

[0006] U.S. Patent Application Publication No. 2016 / 0024390 (A1) discloses a pyrolysis apparatus divided into two zones for continuously converting a hydrocarbonaceous material into condensable and non-condensable, solid hydrocarbon products. This apparatus includes at least one extruder capable of applying shear force and heat supply, having three or more processing zones, a continuous process heat kiln reactor (the extruder and the kiln reactor in fluid communication are in liquid communication), and means for transporting the hydrocarbonaceous material throughout the apparatus. The hydrocarbonaceous material has at least three zones and is retained within those zones of the extruder having at least two zones and the kiln reactor within a predetermined temperature and time range.

[0007] International Publication No. 2019 / 202546 (A1) pamphlet discloses a pyrolysis plant for pyrolyzing plastic materials. This plant includes a sealed reactor connected to a feeder for supplying plastic materials. This reaction vessel has a portion for outputting the decomposition gas product after depolymerization, a mechanical mixer, and an output terminal for removing unevaporated heavy fractions. In the said feeder, the plastic material is compressed and adjusted so as to be continuously movable to the reaction vessel. The said feeder is equipped with a device for heating the plastic material, and the flow rate of the discharged plastic material is adjusted according to the level of the material in the reaction vessel in the said feeder.

[0008] International Publication No. 2022 / 013712 (A1) pamphlet discloses a method for pyrolyzing a mass of waste. The said method includes arranging a screw for supplying heat to the said mass by mechanical shear, after arranging the said screw, preparing a reactor for supplying heat to the said mass in the absence of oxygen by heating the reactor wall, heating the said mass to the outlet temperature and raising the pressure to the outlet pressure under the said screw arrangement, and subjecting the said mass to an extreme state under the said screw arrangement at the said outlet temperature and outlet pressure to cause pyrolysis during pressure drop, thereby forming gaseous hydrocarbons in the said connecting element, that is, performing pyrolysis of the said mass in the said reactor.

[0009] Japanese Patent Application Laid-Open No. 2000-309781 discloses a continuous dry pyrolysis apparatus for plastics, especially waste plastics. This apparatus includes a compression unit, a melting unit, a first decomposition unit, a second decomposition unit, and a separation unit.

[0010] The above-mentioned publication discloses a pyrolysis plant for treating waste plastics, but the present invention was devised with the aim of further improving such a pyrolysis plant, especially with the idea of efficiently and practically treating large-scale plastic waste.

Summary of the Invention

Problems to be Solved by the Invention

[0011] An object of the present invention is to provide an improved pyrolysis plant for converting waste plastics into hydrocarbon components. In particular, it provides a solution to address the above problems in existing pyrolysis plants and provides a pyrolysis plant on an industrial scale.

Means for Solving the Problems

[0012] In a first aspect of the present invention, a pyrolysis system such as a pyrolysis plant for generating hydrocarbon compounds from polymer residues such as synthetic polymers is provided, and the system includes: - An agglomeration device configured to receive and heat the polymer residue; - A degassing feeder configured to transfer the polymer residue from the agglomeration device and add a pH adjustment additive such as calcium oxide (CaO) to the polymer residue; - A degassing device including a degassing device conveyor such as a degassing device screw conveyor configured to move the polymer residue to a degassing device outlet and a heater configured to heat the polymer residue to a temperature within the range of 240 to 280 °C, and the degassing device configured to receive the polymer residue from the degassing feeder, and - A pyrolysis reactor including at least one reactor conveyor configured to move the solid portion of the polymer residue toward a black carbon discharge port and a heater configured to heat the polymer residue to generate pyrolysis vapor, and the pyrolysis reactor including a reactor vapor discharge port for discharging the pyrolysis vapor containing the hydrocarbon compound, and the pyrolysis reactor configured to receive the polymer residue from the degassing device and including an inlet.

[0013] The hydrocarbon compound refers to hydrocarbon vapor and gas that are condensed in other parts of the pyrolysis plant to form one or more hydrocarbon oils.

[0014] In the present disclosure, the terms steam, hydrocarbon vapor, and gas are used interchangeably. Thus, steam may also be referred to as gas, and vice versa. Steam may contain various liquids and solids in the gas phase, and gas may contain substances in the vapor phase.

[0015] An advantage of the present disclosure is that the manufacturing process includes the following three steps. 1) The polymer residue such as waste plastic is first heated and compressed in the agglomerator. In the first treatment, a large amount of steam and unnecessary chemicals are removed, and the polymer product is heated to adjust its viscosity so that it can be conveyed to the degassing device without completely melting the polymer product. 2) By further heating in the degassing device, it is ensured that the polymer product is substantially melted. By heating in the range of 240 to 280 °C, advantageously, undesirable vapors, chemicals, and gases such as corrosive vapors and gases are released, so that the undesirable gas-phase substances are not trapped in the pyrolysis oil, and the downstream plant unit can be manufactured from a metal with low corrosion resistance. Furthermore, by making the temperature range of 240 to 280 °C low enough, the generation of the desired hydrocarbon vapor can be avoided, so that the desired hydrocarbon vapor can be released only in the pyrolysis reactor. The temperature of the degassing device may be, in particular, 260 °C or substantially 260 °C, or a temperature in the range of 255 to 265 °C. The undesirable volatile substances may be released from the degassing device through the degassing device steam outlet. The undesirable gas may be used for other purposes such as power supply to a gas motor or fuel supply to a gas boiler. 3) The molten polymer residue can be continuously pyrolyzed and continuously discharged from the black carbon outlet by the screw conveyor system pyrolysis reactor.

[0016] In a preferred embodiment of the present disclosure, the reactor conveyor comprises at least one screw conveyor. However, it can be seen that other suitable conveyor means may be used.

[0017] An advantage of the present disclosure is that the degassing feeder may include a heating pipe, the heated screw conveyor, and the agglomeration device, or an input section for adding a pH adjustment additive, preferably calcium oxide (CaO), may be provided in the inlet region of the degassing feeder along the flow of the polymer residue. Advantageously, the calcium oxide reduces the acidity of the polymer product, thereby reducing the risk of corrosion. Furthermore, the calcium oxide is generally added as a process additive for the purpose of improving the process. It can be seen that the reduction in acidity can avoid crystallization of the product processed in the pyrolysis plant, thereby reducing the risk of pipe blockage. As a result, the amount of expensive stainless steel parts can be reduced, and the cost of process equipment can also be reduced. According to the present invention, it can also be seen that the effect of CaO addition is remarkable not only in terms of the amount of the additive but also in terms of the residence time of the additive in the system.

[0018] According to one embodiment, the agglomeration device is configured to heat the polymer residue within a range of 150 to 250 °C, for example, to a temperature of about 200 °C. The initial heating temperature is low enough that no required gas is generated, and further, the temperature is low enough that the polymer residue can be compressed or its viscosity can be changed (for example, softening of the polymer product). By heating the polymer product in the agglomeration device, a part of the polymer product may melt, but the polymer product does not completely melt. By this heating, water and optionally unnecessary chemicals coming out of the polymer product can be released from the agglomeration device as water vapor through a vapor outlet for releasing water vapor generated in the process of agglomerating the polymer residue. Thereby, oxidation of the pyrolysis oil generated in the latter half of the process can be avoided. In a preferred embodiment of the present disclosure, the agglomeration device is configured to compress the polymer residue at a compression ratio of 2 to 3.5.

[0019] According to one embodiment, the degassing feeder comprises a heated pipe, an input section for adding calcium oxide, and / or a heated screw conveyor for transferring the polymer residue from the agglomerator to the degassing device. Advantageously, the heated degassing feeder enables the heated and compressed polymer residue to be transported over a long distance without concern of clogging.

[0020] An advantage of the degassing device is that it further comprises a degassing device steam outlet for discharging unwanted volatiles generated by heating the polymer residue within the degassing device. Preferably, the degassing device is arranged substantially horizontally.

[0021] In a preferred embodiment of the present disclosure, the degassing device and the pyrolysis reactor are connected such that they are in fluid communication with each other between the lower part of the degassing device and the lower part of the pyrolysis reactor. Further, the pyrolysis reactor is arranged at an incline such that the solid portion of the polymer residue moves from the lower part to the upper part within the pyrolysis reactor by the reactor screw conveyor, and the pyrolysis reactor has a black carbon outlet arranged at the uppermost part thereof (the black carbon is received at this outlet and discharged by gravity from this outlet), and a black carbon screw conveyor for transferring the black carbon to a container is arranged.

[0022] An advantage is that the degassing device is arranged substantially horizontally, and further the inclination angle of the pyrolysis reactor can be adjusted.

[0023] The pyrolysis reactor preferably includes a plurality of reactor screw conveyors that move the solid portion of the polymer residue toward the black carbon discharge port. The plurality of reactor screw conveyors, for example, two screw conveyors, are arranged in parallel in the reactor. As a result, the capacity of the reactor increases, and further, during heating, heating by electric heating becomes possible, so it is advantageous that only the screw needs to be moved. As a result, the polymer residue is heated to a high temperature of up to 500 °C, such as a temperature in the range of 420 to 460 °C, in the pyrolysis reactor.

[0024] According to the pyrolysis plant of the present disclosure, it is advantageous that the pressures in the degassing device, the pyrolysis reactor, and the oil reactor are in the range of 0.1 to 1 bar, for example, 0.2 to 0.45 bar.

[0025] According to one embodiment, the black carbon discharge port is arranged to receive the black carbon by gravity, and the black carbon screw conveyor is arranged to transfer the black carbon to a container. Advantageously, the black carbon is separated from the liquid polymer product by the screw conveyor in the pyrolysis reactor so that the black carbon falls by gravity to the black carbon discharge port and is continuously discharged from the pyrolysis reactor through the black carbon discharge port. An advantage of the black carbon screw conveyor is that it can continuously transfer the black carbon from the black carbon discharge port to the black carbon container. Other means for transferring black carbon other than the black carbon screw conveyor may be used. Also, the configuration of the plant can be such that the black carbon received at the black carbon discharge port is transferred to the black carbon container without going against gravity. In this case, the black carbon screw conveyor becomes unnecessary.

[0026] According to one embodiment, the pyrolysis reactor is arranged in an inclined manner such that the solid portion of the polymer residue can be moved from the lower part to the upper part of the reactor by the one or more reactor screw conveyors. By inclining in this way, the liquid components in the reactor due to pyrolysis remain in the lower part of the reactor and are further decomposed into pyrolysis vapor and / or gas.

[0027] Advantageously, by taking such an inclined arrangement, the solid portion is carried above the liquid level in the reactor. And the solid black carbon is lifted by the screw conveyor to the upper dry part. The thus-produced black carbon is advantageously dried or substantially dry when exiting the pyrolysis reactor through the black carbon discharge port. The black carbon can be used in various manufacturing processes. To keep the upper part in a dry state, it can be achieved by taking such an inclined arrangement and controlling the liquid level in the reactor, for example, by controlling the inflow from the degassing device of the molten polymer product to the pyrolysis reactor and / or the inflow to the agglomeration device of the polymer residue. Such flow control can be carried out based on the measurement of the liquid level in the pyrolysis reactor. Advantageously, due to the dry part of the pyrolysis reactor, the black carbon can be continuously removed from the reactor.

[0028] According to one embodiment, the pyrolysis reactor is configured such that its inclination can be adjusted to change the height level of the upper end of the polymer residue in the reactor by tilting the reactor. For example, by being able to adjust the inclination in this way, during the initial trial operation of the pyrolysis plant, the inclination angle of the agglomerator can be set to an optimal angle according to a predetermined desired inflow amount of the polymer product into the agglomerator or a desired inflow amount into the pyrolysis reactor. In this case, the inclination adjustment may be performed manually. However, the way of inclination adjustment may be electric, or in some cases, by automatic feedback control, so that such an inclination can be adjusted according to measurement conditions such as the inflow amounts into the agglomerator and the pyrolysis reactor, the liquid level in the reactor, or a combination thereof. By adjusting the inclination of the pyrolysis reactor, especially with the degassing device arranged horizontally, not only can the height level of the liquid polymer residue in the pyrolysis reactor be adjusted, but also the volume capacity and size of the drying part corresponding to the length of the drying part of the pyrolysis screw conveyor can be adjusted.

[0029] According to one embodiment, the pyrolysis plant includes controlled conveyor means such as a controlled screw conveyor for transferring the polymer residue from the degassing device to the pyrolysis reactor.

[0030] In the controlled conveyor means, the flow rate of the polymer residue, that is, the inflow amount into the pyrolysis reactor, can be controlled. For example, the inflow amount can be controlled according to the liquid level in the pyrolysis reactor, the liquid level in the degassing device, or both liquid levels. For example, it can be controlled by adjusting the liquid levels of both to a specific ratio so that the liquid levels in the pyrolysis reactor and the degassing device are the same or substantially the same.

[0031] According to one embodiment, the pyrolysis plant includes an oil reactor arranged to separate the pyrolysis vapor received from the pyrolysis reactor into a vapor component and a liquid component. In the pyrolysis plant, the oil reactor has one or more separator outlets for transferring the vapor component to one or more reflux condensers and a liquid outlet for returning the liquid component to the pyrolysis reactor.

[0032] According to one embodiment, the oil reactor is configured to adjust the temperature inside the separator within a set temperature range of 350 to 450 °C.

[0033] According to one embodiment, the oil reactor is configured to receive the condensed residue obtained after condensation of the pyrolysis vapor. For example, it may be returned to the oil reactor for further cracking of non-volatile heavy hydrocarbon oil.

[0034] According to one embodiment, the pyrolysis plant further includes one or more reflux condensers arranged to receive the vapor component from the oil reactor and condense at least a part of the vapor component into a liquid component. The one or more reflux condensers may have a liquid outlet for returning the liquid component to the oil reactor.

[0035] According to one embodiment, the pyrolysis plant further includes one or more raw pyrolysis oil (RPO) condensers arranged to receive the vapor component from the one or more reflux condensers and condense at least a part of the vapor component into a heavier hydrocarbon liquid such as raw pyrolysis oil.

[0036] According to one embodiment, the pyrolysis plant includes first and second reflux condensers and first and second raw pyrolysis oil condensers, and each of the first and second raw pyrolysis oil condensers is arranged to receive the vapor component from any one of the first and second reflux condensers. Advantageously, by providing a plurality of sets in which the reflux condenser and the raw pyrolysis oil condenser are paired, one set can be removed from the process for cleaning and the other set can be operated.

[0037] According to one embodiment, the plant includes a naphtha condenser arranged to receive a vapor component from one or more raw pyrolysis oil condensers and to condense at least a part of the vapor component into a lighter hydrocarbon liquid such as a naphtha liquid.

[0038] According to one embodiment, the pyrolysis plant further includes a gas storage tank arranged to receive the vapor containing the gas coming out of the plant. For example, the gas storage tank can store the vapor coming out of the degassing device vapor outlet and the non-condensable vapor coming out of the naphtha condenser. Advantageously, the vapor contains, for example, a gas that can be used as an energy source for generating, for example, heat, steam or electricity in the pyrolysis plant. Therefore, the pyrolysis plant may include a gas-driven unit such as a gas generator configured to be supplied with fuel derived from the gas coming out of the gas storage tank. For example, the gas-driven unit may be a generator or a gas turbine arranged to drive the gas-driven unit.

[0039] According to one embodiment, the pyrolysis plant further comprises a boiling point correction device arranged to receive the heavier hydrocarbon liquid before it exits from the one or more raw pyrolysis oil condensers. This boiling point correction device comprises reboilers arranged in a cascade. Each reboiler is arranged to heat the received liquid, transfer the generated vapor to a manifold tank, and transfer the remaining liquid to the next reboiler in the cascade of reboilers, and the last reboiler is arranged to return the remaining liquid to the oil reactor. A second aspect of the present invention relates to a manufacturing process for producing hydrocarbon compounds from polymer residues such as synthetic polymers. This manufacturing method comprises: as follows: - receiving the polymer residue in an agglomeration device, heating and compressing it; - adding a pH adjustment additive such as calcium oxide (CaO) to the polymer residue, and transferring the polymer residue from the agglomeration device to a degassing device using a degassing feeder; - heating the polymer residue in the degassing device to a temperature in the range of 240 to 380 °C, preferably 240 to 280 °C, and transferring the polymer residue to the degassing device outlet using a degassing device conveyor such as a degassing device screw conveyor; - transferring the solid portion of the polymer residue towards a black carbon discharge port using at least one reactor conveyor, for example at least one screw conveyor, and heating the polymer residue to generate pyrolysis vapor, discharging the pyrolysis vapor containing the hydrocarbon compound through the reactor vapor discharge port of the pyrolysis reactor, further condensing the pyrolysis vapor to form a hydrocarbon oil product, and transferring the polymer residue from the degassing device to the pyrolysis reactor; including.

[0040] According to one embodiment, the pyrolysis reactor and the reactor screw conveyor are arranged at an inclination so that at least one of the reactor screw conveyors can transfer the solid portion of the polymer residue from the lower part to the upper part of the pyrolysis reactor, and the liquid level in the pyrolysis reactor is controlled to be lower than the upper part of the pyrolysis reactor.

[0041] For example, the conveyor means arranged to transfer the molten polymer product from the degassing device to the pyrolysis reactor may be controlled so that the inflow rate of the molten polymer into the pyrolysis reactor is adjusted based on, for example, the measurement result of the liquid level in the pyrolysis reactor. Alternatively or as an additional means, a conveyor such as a belt conveyor that supplies the polymer residue to the agglomerator may be controlled based on the measurement result of the liquid level in the pyrolysis reactor, and the inflow into the pyrolysis reactor may be controlled by controlling the inflow into the agglomerator.

[0042] A third aspect of the present invention relates to the use of the pyrolysis system according to the first aspect for producing hydrocarbon compounds from polymer residues.

[0043] In general, various aspects and embodiments of the present invention may be combined in any way possible within the scope of the present invention, or together with each other. These and other aspects, features and / or advantages of the present invention will become apparent by reference to the embodiments described below.

Brief Description of the Drawings

[0044] Embodiments of the present invention will be described by way of example only with reference to the drawings.

Figure 1

Figure 2

Figure 3

Figure 4

DETAILED DESCRIPTION OF THE INVENTION

[0045] FIGS. 1, 2, and 3 show a pyrolysis plant 100 configured to produce hydrocarbon compounds from polymer residues. The polymer residues generally refer to synthetic polymers. In FIGS. 2 and 3, the components of the pyrolysis plant 100 that are the same as those shown in FIG. 1 are shown enlarged and are labeled with reference numerals.

[0046] Examples of the polymer residues and synthetic polymer products equivalent thereto include thermoplastic plastics and other plastic materials including processed products such as granules obtained from the synthetic polymer products. The polymer residues may include multilayer plastics and composite plastics, that is, products containing different types of polymer products.

[0047] Examples of the thermoplastic resins include polyethylene, polypropylene, polyvinyl chloride, polystyrene, polyamide, polyester, polyurethane, polyetheretherketone, liquid crystal polymer, polysulfone, polyphenylene sulfide, and combinations thereof.

[0048] Advantageously, the polymer residues may be waste, used products, or recycled products. Therefore, the synthetic polymer products can be processed into oil and gas without landfilling or incinerating the waste. The thermoplastic product decomposes into a mixture of waste, steam, and gas. This mixture can be treated with one or more condensers that condense steam into oil.

[0049] The generated hydrocarbon compounds include gas products and oil products such as pyrolysis oil, naphtha oil, and marine gas oil.

[0050] The polymer residue may take the form of a mixture of different types of polymer residues obtained by sorting. By mixing the pre-sorted polymer products so that the ratio of each product is the desired ratio or the ratio of a specific component does not exceed the upper limit, the final mixture of the polymer residue can be obtained. For example, the mixture of the polymer residue can be prepared by maximizing the ratio of polyethylene terephthalate (PET) and polyvinyl chloride (PVC). The ratio of another synthetic polymer product or plastic can be selected to make it a specific condition in the pyrolysis process. An advantage of the polymer residue is that it may contain chloride, flour, and terephthalate components.

[0051] The polymer residue may contain contaminated waste plastics. In this case, it is preferably shredded before the product is fed into the agglomeration device. The mixture of the polymer residue or the sorted polymer products is supplied to the agglomeration device 101 by, for example, a conveyor belt. The polymer residue is compressed in the agglomeration device. Such compression is performed by one or more screw conveyors 111 included in the agglomeration device 101. The polymer residue is heated by the frictional effect during compression. Due to this heating, at least a part of the polymer product may melt, but since the heating temperature is sufficiently low, substantially no chemical reaction occurs. However, some water vapor may be generated from the polymer product due to this heating. The agglomeration device may be configured to include a water vapor discharge port 121 through which the water vapor is discharged.

[0052] The agglomeration device may be configured to heat the polymer residue to a temperature within a range of about 200°C, for example, 150°C to 200°C.

[0053] The compressed, heated, and in some cases partially melted polymer product is transferred to the degassing device 102 through a heating pipe 131 such as a heat trace pipe using hot oil.

[0054] Alternatively or in addition to the above, the polymer product sent from the agglomerator 101 may be transferred toward the degassing device 102 using, for example, a screw conveyor heated by an electric heater. As a means for transferring from the agglomerator 101, for example, a heated screw conveyor connected in series with the heated pipe 131 such that the heated pipe is disposed downstream of the heated screw conveyor may be mentioned.

[0055] The degassing device 102 includes a screw conveyor 112 configured such that the polymer residue moves from the inlet to the degassing device outlet 122a. The degassing device 102 includes a heater such as an electric heater that heats the polymer residue to a temperature within the range of 240 to 280°C. The preferred output temperature of the molten polymer residue at the degassing device outlet 122a is a temperature within the range of 250 to 270°C, for example, 255 to 265°C, for example, a temperature near 260°C. Therefore, a temperature of 260°C or another temperature within the range of 240 to 280°C may be controlled using a controller arranged to control the heater of the degassing device 102 and used as a set temperature. A temperature deviation of + / -1 to 2°C or the like may occur as the temperature deviation from the set temperature.

[0056] By heating in the degassing device 102, substantially all moisture evaporates, and not only other volatile substances and undesirable volatile substances but also gas, that is, non-condensable gas evaporates. Such undesirable volatile substances may include undesirable vapors such as corrosive gases and vapors. By removing such undesirable volatile substances, materials with low corrosion resistance can be used for components downstream such as the pyrolysis reactor.

[0057] For the purpose of discharging the undesirable volatile substances and the remaining water vapor, the degassing device is provided with a degassing device steam discharge port 122b.

[0058] The volatile substances and gases released from the degassing device are transferred to the storage tank 180. The released volatile substances include gases such as synthesis gas that can be used as fuel for gas-driven units 181 such as gas turbines and boilers.

[0059] In order to improve the quality of the pyrolysis liquid generated in the process, calcium oxide (CaO) may be supplied to the system as an additive / catalyst. For this purpose, an input part 132 for adding the calcium oxide into the flow of the polymer residue (also referred to as plastic pulp) is configured in the heating pipe 131 or, alternatively, in the agglomeration device 101.

[0060] The molten polymer residue is transferred from the degassing device 102 to the inlet 123a of the pyrolysis reactor 103 via a pipe or, optionally, a conveyor means 150 such as a screw conveyor, a piston, or other conveyor means capable of controlling the transfer of the molten polymer residue. The conveyor means 150, preferably a screw conveyor, can be controlled according to the measurement results of the liquid level in the degassing device and / or the pyrolysis reactor 103 to control the liquid level height 191 in the degassing device 102 and / or the pyrolysis reactor 103. For example, the control of the conveyor means 150 is performed by controlling, for example, the speed and, in some cases, the rotation direction of the screw conveyor, and the liquid level height 191 in the degassing device 102 and the pyrolysis reactor 103 can be ensured to be horizontal.

[0061] The pyrolysis reactor 103 is provided with a reactor screw conveyor 113 that moves and mixes the polymer residue toward the black carbon discharge port 123b. The pyrolysis liquid in the reactor is heated by a heater such as an electric heater that heats the polymer residue to a temperature within the range of 420 to 500 °C to generate pyrolysis vapor. When the polymer residue is heated to a temperature exceeding about 430 °C, the polymer residue is chemically decomposed into pyrolysis vapor, that is, a mixture of hydrocarbon compounds that become gaseous at a predetermined temperature. The pyrolysis vapor is discharged from the reactor 103 through the reactor vapor discharge port 123c. It is advantageous to dispose the reactor vapor discharge port 123c at an intermediate portion in the longitudinal direction of the reactor screw conveyor 113 or at least at a position away from the drying portion of the reactor, whereby it is possible to avoid the vapor from dripping onto the dried black carbon.

[0062] Nearly all of the polymer residue is decomposed as it moves toward the end of the reactor screw conveyor 113, and a solid portion containing black carbon residue exits the process at the end of the reactor. After transporting the black carbon out of the reactor through the black carbon discharge port 123b disposed in the reactor, the black carbon is received by dropping it by gravity. The plant 100 may be provided with a black carbon screw conveyor 133 disposed on an extension line of the black carbon discharge port 123b that transfers the black carbon to a container.

[0063] The solid portion containing the black carbon of the polymer residue is generated in the pyrolysis reactor 103 by chemical decomposition.

[0064] The liquid exiting the reactor (i.e., the heaviest fraction of the pyrolysis vapor) is supplied to the bottom of the pyrolysis reactor to facilitate further decomposition of these compounds.

[0065] The pyrolysis reactor 103 is arranged in an inclined manner such that at least the solid portion of the polymer residue moves from the lower portion 141 near the inlet 123a to the upper portion 142 of the reactor near the black carbon discharge port 123b by means of the reactor screw conveyor. Arranging the reactor in this inclined manner means arranging the reactor screw conveyor in an inclined manner, that is, arranging one end of the screw conveyor near the inlet 123a at a position lower than the other end of the screw conveyor near the black carbon discharge port 123b with respect to the horizontal plane.

[0066] The inclination angles of the pyrolysis reactor 103 and the reactor screw conveyor 123 are in the range of 5 degrees to 35 degrees with respect to the horizontal, for example, 15 degrees to 25 degrees, preferably about 20 degrees.

[0067] The solid black carbon moves upward along the reactor screw conveyor 123 toward the black carbon discharge port 123b. On the other hand, the liquid component obtained by the pyrolysis moves toward the lower portion near the inlet 123a of the reactor and is further decomposed into pyrolysis vapor there. In the reactor screw conveyor 123, holes are formed in the flange of the screw portion so that the liquid component can easily move to the lower portion 141. On the other hand, the heavier solid portion moves upward through the outer portion of the screw flange without holes.

[0068] FIG. 2 shows an example in which the liquid level 191 is shown. In this example, the liquid level 191 is substantially the same as the liquid levels in the degassing device 102 and the pyrolysis reactor 103. Due to the inclination of the pyrolysis reactor 103, the upper part 142 of the reactor can be dried, so that the black carbon is drying or substantially dry in the upper part 142 and is thus discharged from the pyrolysis reactor as dry black carbon. The upper part of the liquid part where the reactor is dry is called the dry part of the pyrolysis reactor 103. This dry part is related to the length of the pyrolysis screw conveyor, i.e., the final part of the pyrolysis screw conveyor above the liquid level.

[0069] The inclination angle of the pyrolysis reactor may be adjustable. By adjusting the inclination angle, the height level of the liquid polymer residue in the pyrolysis reactor 103 can be adjusted, and its volume capacity and size corresponding to the length of the dry part of the pyrolysis screw conveyor can be adjusted.

[0070] For example, when the inflow rate of the polymer residue is low, or when the polymer residue is promptly processed into pyrolysis vapor, the height level of the liquid polymer residue decreases, and thus the height level of the polymer residue in the degassing device 102 also decreases. Therefore, in order to perform efficient processing in the degassing device, the level may become too low. That is, the level in the degassing device must be set to a level high enough to sufficiently raise the degassing device screw conveyor 112 to mix the polymer residue. In this case, by increasing the inclination angle and reducing the volume capacity in the pyrolysis reactor, the liquid level in the pyrolysis reactor can be raised. Since the fluid in the containers of the degassing device 102 and the pyrolysis reactor 103 can flow between the containers via the conveyor means 150, the flow in the containers behaves as if the fluid were a fluid communicating between the containers. Therefore, when the inclination angle is increased, the liquid level in the pyrolysis reactor 103 rises and flows back to the degassing device 102, and the liquid level in the degassing device also continues to rise until equilibrium is reached.

[0071] If the liquid level at the upper end of the liquid polymer residue in the pyrolysis reactor is too high, the drying portion may become too small. Therefore, when the level in the pyrolysis reactor 103 is too high, the inclination angle can be increased to reduce its volume capacity. However, even if the liquid level can be raised in this way, the drying portion will rise in an attempt to hold or increase that portion. Conversely, if the drying portion becomes too large, the inclination angle can be reduced to suppress the rise of the drying portion and shorten the length of the drying portion of the pyrolysis screw conveyor.

[0072] The pyrolysis vapor is discharged from the pyrolysis reactor 103 through a pipe, via the reactor vapor discharge port 123c at the upper end of the reactor, and is directly transferred to the oil reactor 104.

[0073] The oil reactor 104 is a tank configured to separate the pyrolysis vapor received from the pyrolysis reactor 103 into a vapor component and a liquid component. In the oil reactor 104, all black carbon is separated and sent back to the pyrolysis reactor together with the liquid component.

[0074] The oil reactor 104 may be equipped with a stirrer for mixing the contents. The pyrolysis vapor enters into the liquid phase in the tank through a nozzle and a dip pipe at its upper end. The tank temperature can be adjusted within a temperature range of 350 to 450 °C. For example, a temperature control system for controlling the tank temperature to a set temperature can be provided. The temperature inside the oil reactor 104 can be controlled, for example, by adjusting the heating degree of the condensate in the separator in combination with an electric heater.

[0075] In addition to the pyrolysis vapor, the configuration of the oil reactor 104 may be such that the condensed residue can be received from the condensate of the pyrolysis vapor through the pipe connection 124d. Such a condensed residue contains the liquid product received from the reactor feeder tank 202i.

[0076] The liquid from the oil reactor 104 is returned to the pyrolysis reactor 103 through the liquid discharge port 124c and further decomposed into pyrolysis vapor.

[0077] The oil reactor 104 is provided with two separator outlets 124a and 124b for sending the vapor component through the respective pipes of the reflux condensers 105a and 105b. Through the same pipes, the condensate from the reflux condensers 105a and 105b is returned to the oil reactor 104 through the liquid discharge ports 125a and 125b of the reflux condensers. Therefore, these liquid discharge ports also function as vapor inlets.

[0078] The reflux condensers 105a and 105b are arranged to condense at least a part of the vapor components exiting the oil reactor 104 into liquid components. As the configuration of the two reflux condensers, a shell & tube type (multi-tube heat exchanger) heat exchanger can be adopted, in which heat transfers to the hot oil side during the condensation of the pyrolysis vapor between the pyrolysis vapor on the tube side and the hot oil on the shell side.

[0079] In the configuration of the pyrolysis plant 100, the reflux condensers 105a and 105b are designed to be operable one by one at a time. That is, each of the reflux condensers is designed to match the capacity of the pyrolysis reactor 103 (100% capacity). Therefore, while one of the reflux condensers is operating, the other can be cleaned.

[0080] Therefore, each of the reflux condensers can be separated / cut off from the pyrolysis process. Various components such as crystals and waxes generated from PET may precipitate in the reflux condenser, and these can be cleaned mechanically and / or using steam.

[0081] The supply control of the hot oil for cooling the pyrolysis vapor in the reflux condensers 105a and 105b can be carried out based on the temperature of the vapor discharged from the reflux condenser, that is, the temperature of the pyrolysis vapor discharged from the reflux condenser and supplied to the downstream raw pyrolysis oil condensers 106a and 106b. The set temperature of the outlet vapor is, for example, about 250°C. However, the set temperature of the reflux condenser is adjustable, whereby the hydrocarbon compounds produced in the plant can have desired properties.

[0082] Furthermore, when using the hot oil system of the reflux condenser, it is necessary to ensure that when starting the pyrolysis process of the plant 100 from a cold state, or when using the non-operating reflux condenser 105a in the tax increase process after the cleaning process, the reflux condensers 105a and 105b are preheated to an appropriate process temperature.

[0083] The plant can be composed of only one reflux condenser 105a or a plurality of reflux condensers arranged to operate in parallel.

[0084] The pyrolysis vapor released by the one or more reflux condensers 105a is condensed in the downstream raw pyrolysis oil condensers 106a, 106b and the naphtha condenser 107.

[0085] The raw pyrolysis oil condensers 106a, 106b can be configured as a shell & tube type (multi-tube heat exchanger) heat exchanger in which pyrolysis vapor passes through the tube side and hot oil passes through the shell side. Heat conduction occurs when the pyrolysis vapor is partially condensed in the liquid phase of marine gas oil (MGO).

[0086] Similar to the reflux condensers 105a and 105b, the raw pyrolysis oil condensers 106a and 106b are designed to operate only one unit at a time. That is, each of the raw material pyrolysis oil condensers is designed such that its capacity exactly matches 100 percent of the capacity of the pyrolysis reactor 103 and one or more of the reflux condensers. Therefore, for example, even if one of the raw pyrolysis oil condensers is stopped for cleaning, only the other one needs to be operated. Thus, each of the raw pyrolysis oil condensers 106a and 106b can be configured to be separated / disconnected from the pyrolysis process. However, this is only an example configuration shown, and the pyrolysis plant 100 may instead be composed of only the one raw pyrolysis oil condenser 105a, or may be composed of a plurality of raw pyrolysis oil condensers 106a and 106b arranged to operate in parallel.

[0087] In the duplicate configuration in the pyrolysis plant 100, the first and second reflux condensers 105a and 105b and the first and second raw pyrolysis oil condensers 106a and 106b are connected via pipes and shut-off valves so that each of the first and second raw pyrolysis oil condensers can be in fluid connection with any one of the first and second reflux condensers. That is, each of the first and second raw pyrolysis oil condensers 106a and 106b can receive a vapor component from each of the first and second reflux condensers 105a and 105b.

[0088] Regarding the hot oil for cooling the pyrolysis vapor in the raw pyrolysis oil condensers 106a and 106b, its supply amount can be controlled based on the temperature at the outlet of the vapor discharge of the raw pyrolysis oil condensers 106a and 106b. The set temperature of the outlet temperature can be controlled in the range of 100 ° C to 180 ° C, for example, in the range of 130 to 180 ° C, according to the desired oil characteristics.

[0089] The pyrolysis vapor exiting the raw pyrolysis oil condensers 106a and 106b is sent to the naphtha condenser 107. The naphtha condenser may be a shell & tube type (multi-tube heat exchanger) in which the pyrolysis vapor passes through the tube side and cold water passes through the shell side. The pyrolysis vapor enters the exchanger at a temperature of 130 to 180°C and is cooled and condensed to a temperature of about 20°C.

[0090] The temperature of the cold water supplied to the naphtha pyrolysis oil (NPO) condenser 107 can be controlled based on the temperature at the outlet of the naphtha exiting the naphtha pyrolysis oil condenser. The set temperature of the outlet temperature of the naphtha pyrolysis oil condenser can be 20 to 30°C (for example, 20°C, etc.).

[0091] Even if the raw pyrolysis oil and the naphtha pyrolysis oil condensers are respectively labeled 106a, 106b, and 107, the raw pyrolysis oil condensers 106a and 106b are not limited to the production of raw pyrolysis oil, and the naphtha pyrolysis oil condenser is not limited to the production of naphtha. Generally, the operation of the raw pyrolysis oil (RPO) condensers and the naphtha pyrolysis oil (NPO) condensers 106a, 106b, and 107 can be carried out such that heavier oils such as C12 - C45 oils are produced in the raw pyrolysis oil condensers 106a and 106b, and lighter oils such as C5 - C12 oils are produced in the naphtha pyrolysis oil (NPO) condenser 107. However, the operation of the raw pyrolysis oil condensers and the naphtha condensers 106a, 106b, and 107 can be carried out such that other groups of hydrocarbons C1 - C45 processed in the plant 100 are produced. Therefore, the raw pyrolysis oil condenser is also called a heavy oil condenser, and the naphtha condenser may also be called a light oil condenser.

[0092] The pyrolysis plant 100 further includes a gas storage tank 180. This gas storage tank 180 receives steam from the degassing device steam outlet 122b through fluid communication (not shown) with the degassing device 102, and receives non-condensable gas from the naphtha condenser 107 through fluid communication (not shown). The gas (which may be called synthesis gas) stored in the gas storage tank 180 may be used as fuel for a gas turbine driving an electric generator, or as fuel for a gas-driven boiler or steam generator. The electric power generated based on the gas exiting the pyrolysis plant can be used to supply power to the power-consuming devices of the power plant 100 such as electric heaters. The steam exiting the boiler can be used for the heating process of the plant 100.

[0093] The pyrolysis plant 100 may include a raw pyrolysis oil (RPO) storage tank (not shown) that receives and stores condensate from the raw pyrolysis oil condensers 106a and 106b. The raw pyrolysis oil storage tank may be provided with heating means configured to maintain or slightly increase the temperature of the incoming liquid. The normal operating temperature of the raw pyrolysis oil storage tank may be in the temperature range of 130 to 180°C. The raw pyrolysis oil tank is provided with a steam outlet connected to the steam outlets of the raw pyrolysis oil condensers 106a and 106b, and can balance the respective pressures.

[0094] The pyrolysis plant 100 may further include a naphtha (NPO) storage tank (not shown) that receives and stores condensate from the naphtha condenser 107. In an embodiment, the RPO and NPO are stored in the same tank.

[0095] Optionally, the pyrolysis plant may comprise a boiling point correction device 201 arranged to receive the condensate from the one or more raw pyrolysis oil condensers 106a, 106b via a branch pipe 210. The boiling point correction device 201 comprises, for example, a reboiler 202 arranged in a cascade to gradually heat the liquid, and heats, for example, from an output temperature of the raw pyrolysis oil condenser, for example a temperature in the range of 130 to 180°C, to, for example, 300°C (maximum temperature 450°C), or generally heats at a temperature of 100°C to 450°C. The reboiler comprises a heating element arranged to heat the received liquid. The first reboiler 202a receives the condensate from the one or more raw pyrolysis oil condensers 106a, 106b. The first reboiler 202a heats the liquid to a first temperature T1, for example 130°C. The vapor generated in the first boiler 202a is transferred to a manifold tank 203, and the remaining liquid is transferred to a second reboiler 202b. The second reboiler 202b heats the liquid exiting the first reboiler 202a to a second temperature T2. Here, T2>T1. The vapor generated in the second reboiler 202b is sent to the manifold tank 203, and the remaining liquid is sent to a third reboiler 202c. One or more subsequent downstream reboilers 202d to 202h (their configuration is the same as that of the previous upstream boiler) have boiling points that increase to T3 to T8. The last ninth boiler 202i heats the liquid exiting the previous boiler 202h to a final temperature Tf. Here, Tf>T8. For example, Tf is 450°C. The vapor generated in the last boiler 202i is sent to the manifold tank 203, and the remaining liquid is returned to the oil reactor 104 via the pipe connection 124d. The vapor in the manifold tank 203 is transferred to the condenser 204, and the condensate exiting the condenser 204 is sent to a subcooler 205 and cooled to an appropriate temperature, for example 20°C.

[0096] The boiling point correction device 201 is provided optionally, but may be provided to adjust the boiling point of the produced oil. For example, the boiling point of the heavy oil produced by the pyrolysis oil condensers 206a and 206b may be in the range of 450 to 550°C, for example, 500°C. Therefore, if necessary, the boiling point correction device 201 can be used to lower the boiling point to a temperature in the range of 400 to 450°C, for example, around 410°C.

[0097] In FIG. 3, a first branch pipe 210 connecting the pyrolysis oil condensers 106a and 106b to the boiling point correction device 201 and a second branch pipe 211 connecting the pyrolysis oil condensers 106a and 106b directly to the sub-cooler 205 are shown. In the configuration of the pyrolysis plant including the boiling point correction device 201, a valve for selecting either the first or second branch pipe 210, 211 is provided.

[0098] It should be noted that the oil condenser may be arranged in a layout other than that shown in FIG. 1. For example, the naphtha condenser 107 may be arranged in series with the duplicate pyrolysis oil condensers 106a and 106b to cool the pyrolysis oil that has been condensed in advance, condense the naphtha vapor, and produce pyrolysis oil instead of pyrolysis oil and naphtha.

[0099] FIG. 4 shows a further embodiment of the pyrolysis plant according to the present invention, and the rising conditions and mutual sizes of the reactor and the condenser conform to those of the preferred embodiment of the pyrolysis plant of the present disclosure.

[0100] Similar to the plant shown in FIGS. 1 to 3, the polymer residue is fed to the agglomerator 101, which is preferably compressed by the screw conveyor 111 at a ratio of 2 to 3.5. A steam outlet 121 is provided to discharge the water vapor released from the polymer residue during compression. By removing the water vapor, steam explosion within the system can be avoided, and oxidation of the pyrolysis oil after production can be avoided. Calcium oxide (CaO), which is a pH adjustment additive, is preferably added via an inlet 132 at the inlet of the degassing feeder 101a, and the polymer residue after compression is carried forward via the degassing feeder 101a. Next, calcium oxide is immediately mixed with the polymer residue in the degassing feeder 101a. While the polymer residue passes through the degassing feeder, it is heated in a heating pipe 131. In the first section, the product is heated to 180 to 220 °C, and in the second section, it is further heated at about 200 to 280 °C. Next, the polymer residue is fed to the degassing device 102. In the degassing device 102, the polymer residue is passed through while being moved substantially horizontally by the screw conveyor 112 to the three heating zones 102a, 102b, and 102c. The degassing device 102 heats each zone. For example, in the first zone 102a, the medium, i.e., the polymer residue, is heated to a maximum temperature of 240 °C, in the second zone 102b, the medium is heated to a maximum temperature of 260 °C, and in the third zone 102c, the medium is heated to a maximum temperature of 280 °C. As shown in FIG. 4, a gas outlet 122b is provided at least above the zones 102b and 102c. The pressure inside the degassing device 102 is in the range of 0.1 to 1 bar, for example, 0.2 to 0.45 bar.

[0101] The polymer residue (also called the medium or plastic pulp) is transferred to the pyrolysis reactor 103 via the pipe conveyor 150. The horizontally arranged degassing device and the upwardly inclined pyrolysis reactor are connected so as to be in fluid communication between the discharge port 122a at the bottom of the degassing device 102 and the inlet 123a at the lowermost part of the inclined pyrolysis reactor 103. As shown in FIG. 4, the liquid level 191 is substantially the same as that referred to and described in FIG. 2.

[0102] The pyrolysis reactor 103 preferably includes two screw conveyors 113 arranged parallel to it, and only one of them is shown in FIG. 4. The screw conveyor 113 conveys the polymer residue, mixes the products, lifts them upward out of the liquid level, and transfers them to the black carbon discharge port 123b at the upper end of the reactor 103. The pyrolysis liquid in the reactor 103 is heated by a heater such as an electric heater that heats the polymer residue to a temperature of up to 500°C to generate pyrolysis vapor. The heating means can be arranged in the heating zone. The pressure in the pyrolysis reactor 103 is about the same as the pressure in the degassing device, that is, 0.1 to 1 bar, for example, 0.2 to 0.45 bar.

[0103] The pyrolysis vapor is discharged from the reactor 103 through the reactor vapor discharge port 123c. The reactor vapor discharge port 123c is arranged away from the drying part of the reactor to avoid any condensed vapor from dripping onto the dried black carbon. As the polymer residue moves towards the end of the reactor screw conveyor 113, all of it is substantially decomposed, and the solid part containing the black carbon residue is discharged from the process at the end of the reactor 103. The black carbon is transported through the black carbon discharge port 123b arranged in the reactor for receiving the black carbon and exits the reactor 103. At the discharge port 123b, a black carbon screw conveyor 133 for transferring the black carbon to a container may be arranged on the extension of the black carbon discharge port 123b. More preferably, a gas lock valve (not shown) may be provided so that no gas leaks from the black carbon discharge port 123b.

[0104] The pyrolysis vapor discharged from the reactor 103 through the reactor vapor discharge port 123c is supplied to the oil reactor 104. The oil reactor 104 functions as a gas-liquid separator. The reactor vapor discharge port pipe 123c is installed in the oil reactor 104 such that the pipe outlet 123d is lower than the liquid level 104d in the oil reactor 104. As shown in FIG. 4, the oil reactor 104 is heated in three zones 104a, 104b, and 104c. In each zone, the pyrolysis vapor product is heated to a maximum temperature of 450 °C. As shown in FIG. 4, the pyrolysis vapor is discharged into the oil reactor 104 below the liquid level. When the product liquefies and falls to the bottom in the oil reactor 104, this heavy oil and solid particles are returned to the pyrolysis reactor 103 through the pipe 124c and further decomposed in the pyrolysis reactor 103.

[0105] At the upper end of the oil reactor 104, two discharge ports 124a and 124b for transferring the vapor component to the two reflux condensers 105a and 105b are provided. All of the pyrolysis vapor enters from the bottom of each of the reflux condensers 105 and is discharged from the upper ends of the reflux condensers 105a and 105b at a maximum temperature of 260°C. The pyrolysis vapor is led from the upper ends of the reflux condensers 105a and 105b to the raw pyrolysis oil (RPO) condensers 106a and 106b, where the vapor is condensed into a heavy product (Raw Pyrolysis Oil or RPO) with a discharge port temperature of about 150 - 180°C. Further, the pyrolysis vapor is sent to the naphtha pyrolysis oil condenser 107, where the vapor is condensed and cooled and discharged as a light product at a temperature of 10 - 35°C.

Claims

1. A manufacturing process for producing hydrocarbon compounds from polymer residues, wherein the manufacturing process is as follows: - The polymer residue is received by the agglomeration device (101), heated, and compressed. - Transferring the compressed polymer residue from the flocculation device to the degassing device (102) via the degassing supply (101a), and in which a pH adjusting additive is added to the compressed polymer residue, and transferring the compressed polymer residue from the flocculation device to the degassing device (102) via the degassing supply (101a), - While the polymer residue is moved to the degassing device outlet (122a) using the degassing device conveyor (112), the polymer residue is heated in the degassing device (102) within the range of 240 to 380°C, -Transferring the polymer residue from the degassing device to the pyrolysis reactor (103), wherein the solid portion of the polymer residue is transported toward the black carbon outlet (123b) using at least one reactor conveyor (113), and the polymer residue is heated to generate pyrolysis vapor, and the pyrolysis vapor containing the hydrocarbon compound is released through the reactor vapor outlet (123c) of the pyrolysis reactor to further condense the pyrolysis vapor to produce hydrocarbon oil products, and The separation of the pyrolysis vapor received from the pyrolysis reactor (103) into a vapor component and a liquid component in an oil reactor (104), wherein the oil reactor (104) is equipped with one or more separator outlets (124b) for transferring the vapor component to one or more reflux condensers (105a, 105b) and a bottom liquid outlet (124c) for returning the liquid component to the pyrolysis reactor (103) for further decomposition, and the separation of the pyrolysis vapor received from the pyrolysis reactor (103) into a vapor component and a liquid component in the oil reactor (104), Includes, The degassing device (102) is arranged horizontally. The pyrolysis reactor (103) is positioned at an angle such that the solid portion of the polymer residue is moved from the lower part (141) to the upper part (142) of the pyrolysis reactor by a reactor screw conveyor. Manufacturing process.

2. The manufacturing process according to claim 1, wherein the pyrolysis reactor is tilted so as to move the solid portion of the polymer residue from the lower part to the upper part of the pyrolysis reactor by a reactor screw conveyor, and the liquid level in the pyrolysis reactor is controlled to be lower than that in the upper part of the pyrolysis reactor.

3. A pyrolysis system for producing hydrocarbon compounds from polymer residues by performing the manufacturing process described in claim 1 or 2, The aforementioned system, - A flocculation device (101) configured to receive, heat, and compress the polymer residue, - A degassing feeder (101a) configured to transfer the polymer residue after compression from the flocculation device, which adds a pH adjusting additive to the polymer residue after compression. - The degassing device (102) is configured to receive the polymer residue from the degassing supply, and the degassing device (102) is equipped with a degassing device conveyor (112) for moving the polymer residue to the degassing device outlet (122a), and a heater for heating the polymer residue to a temperature in the range of 240 to 280°C, and the degassing device (102) is configured to receive the polymer residue from the degassing supply, - A pyrolysis reactor (103) having an inlet (123a) configured to receive the polymer residue from the degassing device, wherein the pyrolysis reactor (103) has at least one reactor conveyor (113) that moves the solid portion of the polymer residue toward a black carbon outlet (123b), and a heater that heats the polymer residue to generate pyrolysis vapor, and a reactor vapor outlet (123c) that releases the pyrolysis vapor containing the hydrocarbon compound, Equipped with, The pyrolysis plant (100) further comprises an oil reactor (104) arranged to separate the pyrolysis vapor received from the pyrolysis reactor (103) into a vapor component and a liquid component, the oil reactor (104) comprising one or more separator outlets (124b) for transferring the vapor component to one or more reflux condensers (105a, 105b), and a bottom liquid outlet (124c) for returning the liquid component back to the pyrolysis reactor (103) for further decomposition. The degassing device (102) is arranged horizontally. The pyrolysis reactor (103) is positioned at an angle such that the solid portion of the polymer residue is moved from the lower part (141) to the upper part (142) of the pyrolysis reactor by a reactor screw conveyor. Pyrolysis system.

4. The reactor conveyor comprises at least one screw conveyor. The system according to claim 3.

5. The flocculation device is equipped with an outlet for releasing water vapor generated during the process of flocculating the polymer residue, and / or the flocculation device is configured to compress the polymer residue at a compression ratio of 2 to 3.

5. The system according to claim 3.

6. The degassing supply unit comprises a heated pipe (131), an inlet (132) for adding calcium oxide, and a heated screw conveyor for transferring the polymer residue from the coagulation device to the degassing device. The system according to claim 3.

7. The degassing device (102) is equipped with a degassing device vapor outlet (122b) that releases undesirable volatile substances generated by heating the polymer residue. The system according to claim 3.

8. The degassing device (102) and the pyrolysis reactor (103) are connected to each other by a fluid communication pipe between the lower part of the degassing device (102) and the lower part of the pyrolysis reactor (103). The system further includes a conveyor means (150) for transferring the polymer residue from the degassing device (102) to the pyrolysis reactor (103), wherein the conveyor means (150) is capable of controlling the flow rate of the polymer residue. The system according to claim 3.

9. The degassing apparatus is positioned horizontally, and the tilt angle of the pyrolysis reactor (103) is adjustable. The system according to claim 3.

10. The pyrolysis reactor (103) is equipped with a plurality of reactor screw conveyors (113) that move the solid portion of the polymer residue toward the black carbon outlet (123b), The black carbon outlet (123b) is positioned at the top of the pyrolysis reactor (103) to receive the black carbon, and the black carbon is discharged from the outlet by gravity. A black carbon screw conveyor (133) is also provided to transfer the black carbon to a container. The system according to claim 3.

11. The polymer residue is heated to a high temperature of up to 500°C in the pyrolysis reactor (103), and / or The pressure inside the degassing apparatus, the pyrolysis reactor, and the oil reactor is within the range of 0.1 to 1 bar. The system according to claim 3.

12. The pyrolysis plant (100) further comprises one or more reflux condensers (105a, 105b) arranged to receive the vapor component from the oil reactor (104) and to condense at least a portion of the vapor component into a liquid component, and further comprises one or more biopyrolysis oil condensers (106a, 106b) arranged to receive the vapor component from the one or more reflux condensers and to condense at least a portion of the vapor component into a heavier hydrocarbon liquid, The system according to claim 3.

13. The plant comprises a naphtha condenser (107) which is configured to receive vapor components from one or more biopyrolysis oil condensers and to condense at least a portion of the vapor components into a lighter hydrocarbon liquid, The system according to claim 12.

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