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A system and method of converting waste plastics into hydrocarbon oil comprises a thermal cracking reactor, into which the waste plastics are cracked at a temperature in the range of 270-800° C. to obtain partly gaseous hydrocarbons, partly liquid hydrocarbons, and remaining residues. A continu

A system and method of converting waste plastics into hydrocarbon oil comprises a thermal cracking reactor, into which the waste plastics are cracked at a temperature in the range of 270-800° C. to obtain partly gaseous hydrocarbons, partly liquid hydrocarbons, and remaining residues. A continuous thermal cracking and residual discharging portion is connected to have the liquid hydrocarbons gradually and fully cracked into gaseous hydrocarbons, while the residues are discharged at a residual discharge outlet. A chlorine removal portion is connected to receive the gaseous hydrocarbons to remove chlorine from it. A catalytic cracking reactor is connected to the chlorine removal portion to have the gaseous hydrocarbons catalytic cracking with an acid catalyst. A three-stage cooling portion is adopted to have the catalytically cracked gaseous hydrocarbons fully converted into liquid hydrocarbons, i.e., hydrocarbon oil. A pressurized activation reaction portion is provided to remove few amount of S. N. P. from the liquid hydrocarbons to obtain purified hydrocarbon oils.

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1. A system of converting waste plastics into hydrocarbon oil, said system comprising:(1) an oven thermal cracking reactor, into which solid waste plastics are fed and in which said waste plastics are cracked at a temperature in a range of 270-800° C. to obtain a thermal cracking product of par

1. A system of converting waste plastics into hydrocarbon oil, said system comprising:(1) an oven thermal cracking reactor, into which solid waste plastics are fed and in which said waste plastics are cracked at a temperature in a range of 270-800° C. to obtain a thermal cracking product of partly gaseous hydrocarbons and partly a mixture of liquid hydrocarbons and residues;(2) a catalytic cracking portion coupled to receive said gaseous hydrocarbons, in which the gaseous hydrocarbons are cracked with an acidic catalyst;(3) a cooling portion in which the gaseous hydrocarbons after the catalytic cracking are substantially converted into liquid hydrocarbons of smaller molecules, and remaining non-convertible gaseous hydrocarbon substances are transported back to compensate the heating of the thermal cracking reactor; and(4) tubular continuous thermal cracking and residual discharging portion being connected to receive the mixture of liquid hydrocarbons and residues from said thermal cracking reactor, such that the liquid hydrocarbons are gradually thermally cracked into gaseous hydrocarbons when passing through the tubular continuous thermal cracking and residual discharging portion, while the dry residues from the previous thermal cracking and residues generated from the further thermal cracking are discharged at a residual discharge outlet of the continuous thermal cracking and residual discharging portion. 2. The system of claim 1, further comprising a hydrochloric acid removal portion connected before the catalytic cracking portion to receive the gaseous hydrocarbons, respectively, from the thermal cracking reactor and the continuous thermal cracking and residual discharging portion, in which the gaseous hydrocarbons are subject to reaction with an alkaline metallic substance at a high temperate said catalytic cracking reactor being connected to said hydrochloric acid removal portion to receive the chlorine-free gaseous hydrocarbons and having said gaseous hydrocarbons subjected to catalytic with said acid catalyst. 3. The system of claim 1, further comprising a pressurized activating reaction portion provided to receive said liquid hydrocarbons from the cooling portion to solidify sulfur, nitrogen, and phosphorus contained in said liquid hydrocarbons so as to obtain purified hydrocarbons oils. 4. The system of claim 1, wherein said continuous thermal cracking and residual discharging portion comprises a plurality of sets of reaction tubes arranged in parallel with one another, in which screw conveyors are provided, each screw conveyer rotating in an opposite direction with the rotation of adjacent screw conveyors such that the mixture of liquid hydrocarbons and residues is pushed continuously forward from the beginning of the tubes to the tubes, while all of the liquid hydrocarbons are gasified, and the residues are discharged from a residual discharging outlet. 5. The system of claim 2, wherein said hydrochloric acid removal action is carried out at a temperature of 270-800° C., chloride ion being replaced from hydrochloric acid contained in said gaseous hydrocarbons and the resulting chlorine gas being expelled out of the hydrochloric acid removal portion. 6. The system of claim 1, wherein said cooling portion comprises three stages, through which most of the catalytically cracked gaseous hydrocarbons are converted into liquid hydrocarbons, while certain gaseous hydrocarbons that are non-convertible at room temperature and pressure are collected and transported back to compensate the heating capacity of the thermal cracking. 7. A system of converting waste plastics into hydrocarbon oil, said system comprising:(1) an oven thermal cracking reactor, into which solid waste plastics are fed and in which said waste plastics are cracked at a temperature in a range of 270-800° C. thermal cracking product of partly gaseous hydrocarbons and partly a mixture of liquid hydrocarbons and residues;(2) a catalytic crackin g reactor being connected to receive the gaseous hydrocarbons and having said gaseous hydrocarbons subjected to catalytic cracking with an acid catalyst;(3) a cooling portion in which the gaseous hydrocarbons after the catalytic cracking are substantially converted into liquid hydrocarbons of smaller molecules and remaining non-convertible gaseous hydrocarbon substances;(4) a tubular continuous thermal cracking and residual discharging portion being connected to receive the mixture of liquid hydrocarbons and residues from the thermal cracking reactor, in which the liquid hydrocarbons are gradually and cracked into gaseous hydrocarbons when passing through the tubular continuous thermal cracking and residual discharge portion, while the dry residues from the previous thermal cracking and residues newly generated from the further thermal cracking are discharged at a residual discharge outlet of the continuous thermal cracking and residual discharge portion; and(5) a hydrochloric acid removal portion being connected to receive the gaseous hydrocarbons, respectively, from the thermal cracking reactor and from the continuous thermal cracking and residue discharging portion. 8. The system of claim 7, wherein a pressurized activation reaction portion is provided to receive the liquid hydrocarbons from the cooling portion to solidify sulfur, nitrogen, and phosphorus contained in the liquid hydrocarbons so as to obtain purified hydrocarbon oils. 9. The system of claim 7, wherein the thermal cracking and residual discharging portion comprises a plurality of continuous reacting tubes of parallel arrangement, and screw-propelling conveyors mounted inside the tubes, wherein the mixture of the liquid hydrocarbons and residues is pushed forward by said screw conveyors, and passes through the reaction tubes, while the mixture is maintained at a high temperature sufficient to enable complete gasification of the liquid hydrocarbons. 10. The system of claim 7, wherein, in said hydrochloric acid removal portion, the thermal cracking products is in reaction with alkaline substances to replace the chlorine from the hydrochloric acid contained in the thermal cracking resultants so as to obtain purified gaseous hydrocarbons, and the hydrochloric acid removal reaction is carried out at a high temperature in a range of 270-800° C. 11. The system of claim 7, wherein the cooling portion comprises three stages of cooling, whereby the catalytically cracked gaseous hydrocarbons are substantially converted into liquid hydrocarbons of smaller molecules of eight to twenty carbon atoms, with gaseous hydrocarbon substances equal to or less than four carbon atoms remaining. 12. The system of claim 11, wherein said gaseous hydrocarbons become said liquid hydrocarbons through said three cooling stages, and said few gaseous hydrocarbon substances that are non-convertible at room temperature and pressure are returned to the thermal cracking reactor and continuous thermal cracking and residual discharge portion to compensate the heating supply for the thermal cracking reaction. 13. A method of converting waste plastics into hydrocarbon oil, said method comprising the following steps of:(1) feeding solid waste plastics into an oven thermal cracking reactor;(2) subjecting said solid waste plastics to thermal cracking at a temperature in a range of 270-800° C. to obtain a thermal cracking product of partly gaseous hydrocarbons and partly a mixture of liquid hydrocarbons and residues;(3) passing said gaseous hydrocarbons into a catalytic cracking reactor for catalytic cracking with an acid catalyst;(4) sending said catalytically cracked gaseous hydrocarbons into a cooling portion to obtain liquid hydrocarbons of smaller molecules; and(5) said mixture of liquid hydrocarbons and residues from the thermal cracking portion being sent into a tubular continuous thermal cracking and residual discharging portion, in which the liquid hydrocarbons are gradually cracked in to gaseous hydrocarbons when passing through the tubular continuous thermal cracking and residual discharge portion, while the dry residues from the previous thermal cracking and residues generated from the further thermal cracking are discharged at a residual discharging outlet of the continuous thermal cracking and residual discharge portion. 14. The method of claim 13, wherein gaseous hydrochloric acid contained in said gaseous hydrocarbons from the thermal cracking reactor and the continuous thermal cracking and residual discharging portion are sent to a hydrochloric acid removal portion for removing hydrochloric acid from said gaseous hydrocarbons to obtain chlorine free gaseous hydrocarbons before said catalytic cracking. 15. The method of claim 13, wherein said liquid hydrocarbons obtained from the cooling portion are passed into a pressurized activation reaction portion in which sulfur, nitrogen, and phosphorus contained in the liquid hydrocarbons are solidified so as to obtain purified hydrocarbon oils. 16. The method of claim 13, wherein said continuous thermal cracking in said continuous thermal cracking and residual discharging portion is carried out at a temperature range of 270-800° C. 17. The method of claim 14, wherein said hydrochloric acid removal reaction is carried out in presence of alkaline metallic substances at a temperature of 270-800° C. 18. The method of claim 13, wherein said cooling is a three-stage cooling, through which most of the gaseous hydrocarbons are turned into liquid hydrocarbons, and gaseous substances that are not convertible at room temperature and pressure are returned to the thermal cracking reactor and the continuous thermal cracking and residual discharge portion to generate additional heating for the thermal cracking. 19. The method of claim 15, further comprising a step of separation of hydrocarbon oils from the pressured activation reactor to obtain further purified hydrocarbon oils by means of a centrifuge. 20. A method of converting waste plastics into hydrocarbon oil, said method comprising the following steps of:(1) feeding solid waste plastics into an oven thermal cracking reactor;(2) subjecting said solid waste plastics to thermal cracking at a temperature in a range of 270-800° C. to obtain a thermal cracking product of partly gaseous hydrocarbons and partly a mixture of liquid hydrocarbons and residues;(3) passing said gaseous hydrocarbons into a catalytic cracking reactor for catalytic cracking with an acid catalyst;(4) sending said catalytically cracked gaseous hydrocarbons into a cooling portion to obtain liquid hydrocarbons of smaller molecules;(5) passing said mixture of liquid hydrocarbons and residues into a continuous thermal cracking and residual discharging portion, in which the liquid hydrocarbons are gradually cracked into gaseous hydrocarbons when passing through the continuous thermal cracking and residual discharging portion, while the dry residues from the previous thermal cracking and residues newly generated from the further thermal cracking are discharged at a residual discharging outlet of the continuous thermal cracking and residual discharge portion; and(6) sending said gaseous hydrocarbons from the thermal cracking reactor and from the continuous thermal cracking and residual discharging portion to a hydrochloric acid removal portion for removing hydrochloric acid from said gaseous hydrocarbons to obtain chlorine free gaseous hydrocarbons before said catalytic cracking. 21. The method of claim 20, further comprising a step of passing said liquid hydrocarbons from said cooling stage into a pressurized activation reaction portion to have sulfur, nitrogen, and phosphorus contained in the liquid hydrocarbons solidified so as to obtain purified hydrocarbon oils. 22. The method of claim 20, wherein said continuous thermal cracking is carried out in a plurality of continuous reaction tubes of predetermined length parallel arranged at a temp erature range of 270-800° C. 23. The method of claim 20, wherein said hydrochloric acid removal reaction is carried out in presence of alkaline metallic substances at a temperature range of 270-800° C. 24. The method of claim 20, wherein said catalytically cracked gaseous hydrocarbons are passed through three stages of cooling, such that most of the gaseous hydrocarbons are converted into liquid hydrocarbons of smaller molecules, while certain gaseous hydrocarbons that are not convertible at room temperature and pressure are led back the thermal cracking reactor and the continuous thermal cracking and residual discharge portion to compensate the heating capacity of thermal cracking. 25. The method of claim 21, wherein the liquid hydrocarbon oils is subject to a separation process by means of a centrifuge.