Method and system for processing plastic waste materials

Abstract

A method and system for pretreating plastic waste, and a method and system for producing automotive fuel from plastic waste, are disclosed. The method for pretreating plastic waste includes step 1) contacting the plastic waste with a pretreatment agent and a solvent oil for impurity removal; and step 2) subjecting the effluent solution from step 1) to solid-liquid separation to obtain an insoluble material and an impurity-removed plastic-containing solution. The impurity-removed plastic-containing solution has low metal, chlorine, and silicon contents, thereby reducing the impact on downstream processing equipment.

Description

Detailed Description of the Invention

[0001] (CROSS-REFERENCE TO RELATED APPLICATIONS) This application claims priority to Chinese Patent Application No. 202010617815.X, filed on June 30, 2020, entitled "Method and System for Producing Automotive Fuel from Plastic Waste," and Chinese Patent Application No. 202011171603.X, filed on October 28, 2020, entitled "Method and System for Pretreating Plastic Waste," the contents of which are incorporated herein by reference in their entireties.

[0002] (Technical field) The present application relates to the technical field of solid plastic waste treatment, and in particular to methods and systems for treating plastic waste.

[0003] (Background technology) The development of the plastics industry has made significant contributions to social development. China's current annual plastic production capacity is high, at approximately 120 million tons, and the majority of plastic is discarded into the environment after a single use. Statistics show that China's plastic waste output is approximately 2.4 million to 4.8 million tons per year; by 2035, approximately 800 million tons of plastic waste may exist in the natural environment. Since the time required for complete decomposition of plastic may be 200 to 500 years, the continuous accumulation of plastic waste not only causes serious environmental pollution but also affects the ecological balance of the natural environment.

[0004] Existing plastic waste disposal technologies mainly include two types: landfilling and incineration. Landfilling occupies a large amount of land and is prone to secondary pollution, making it essentially ineffective. However, there are currently only approximately 400 waste incineration power plants in China capable of processing plastic waste. To process all plastic waste for power generation by incineration would require the construction of over 1,000 waste incineration power plants, which is clearly unfeasible. Furthermore, physical plastic waste recovery is expensive and has low economic value, resulting in insufficient profits for companies. It is also prone to secondary pollution during the recovery process, which has led to the slow development of plastic waste resource recovery.

[0005] Chemical conversion of plastic waste is an effective means for realizing rapid recovery and conversion of plastic waste. In particular, thermoplastic plastic waste can be converted into oil and gas through the pyrolysis process, so pyrolysis is currently one of the main process routes for the chemical conversion of plastic waste.

[0006] Chinese Patent No. CN106635115B discloses a method and hydrothermal reaction system for efficiently and cleanly producing oil from mixed plastic waste. The method involves hydrothermal decomposition of mixed plastic waste using an alkaline aqueous solution under conditions including a temperature of 160°C to 300°C and a pressure of 20 bar to 220 bar; the mixed plastic waste contains one or more of polyethylene (PE), polypropylene (PP), and polystyrene (PS), as well as PET. Optionally, the mixed plastic waste may also contain polyvinyl chloride (PVC); the aqueous layer of the material obtained after the hydrothermal treatment is separated from the solid layer, and oil is produced from the separated solid layer. This method avoids the adverse effects of PET and PVC in the mixed plastic waste on the oil, and can efficiently and cleanly produce oil, leading to the production of high-value-added products such as TA powder or particles and PS recycled plastic.

[0007] Chinese Patent Application No. CN108456328A discloses a method for treating plastic waste, which comprises adding plastic waste, a reforming catalyst, and a reaction solvent to a catalytic cracking reactor, mixing them uniformly, and then carrying out a catalytic cracking reaction. The reforming catalyst is a HZSM-5 and HY composite molecular sieve catalyst modified with a modifying oxide, the modifier is one or more selected from the group consisting of Sn, Fe, Ti, and Zn, the reaction solvent is a mixture of tetralin and n-hexadecane, and the catalytic cracking conditions include a reaction temperature of 150°C to 300°C, a reaction time of 120 to 240 minutes, a stirring speed of 600 rpm to 1000 rpm, and introduction of hydrogen at a hydrogen partial pressure of 4 MPa to 7 MPa.

[0008] Chinese Patent No. CN102786980B discloses a method and production line for producing oil from plastic waste. The method includes steps 1) pretreating plastic waste; 2) cracking; 3) catalytic reaction; 4) concentration; and 5) filtration and water removal. By subjecting plastic waste to oil treatment, the method achieves high oil yield and low slagging rate. The production line includes a feeding device, a high-frequency electric heating reactor, a catalytic tower, a cooling filter tank, a liquefaction tower, and an oil storage tank. The feeding device is connected to the high-frequency electric heating reactor, the high-frequency electric heating reactor is connected to the catalytic tower via a pipeline, the catalytic tower is connected to the cooling filter tank via a pipeline, the cooling filter tank is connected to the liquefaction tower via a pipeline, and the liquefaction tower is connected to the oil storage tank via a pipeline.

[0009] Plastic waste has a complex composition and contains a large amount of heteroatoms; during the plastic production process, a large amount of various organic or inorganic additives are added to improve its performance; and a large amount of impurities can easily adhere to discarded plastic. For the reasons mentioned above, existing pyrolysis methods have had problems with the quality of pyrolysis oil, particularly the high content of Cl and Si impurities. The Cl in pyrolysis oil mainly comes from the decomposition of PVC in plastic waste. Most of the Cl exists as small organic chlorides, which can easily decompose to form HCl during subsequent oil product processing, thereby causing serious corrosion. In conventional techniques, alkaline substances are mainly used to dechlorinate pyrolysis oil, which generates a large amount of solid waste and ultimately converts PVC into inorganic salts such as NaCl and CaCl, essentially reducing the value of the PVC. The silicon in pyrolysis oil is mainly derived from the decomposition of polymer additives such as silicone oil, silicone resin, and silicone rubber powder. Inorganic additives such as SiO2, which exist mainly as alkylepoxysilanes, are poisons for catalysts used in subsequent processing and can cause permanent deactivation of the catalyst.

[0010] Therefore, there is still an urgent need for new plastic waste treatment technologies to solve the problems faced by conventional technologies, such as the high content of harmful elements Cl and Si contained in pyrolysis oil produced from plastic waste, which leads to corrosion of pipelines and equipment and easy deactivation of catalysts in subsequent processes.

[0011] DISCLOSURE OF THE INVENTION It is an object of the present application to provide a novel method and system for treating plastic waste that can overcome one or more of the problems encountered in the prior art discussed above.

[0012] To achieve the above object, in one aspect, the present application provides a method for pretreating plastic waste, comprising the following steps: Step 1) contacting plastic waste with a pretreatment agent and a solvent oil for impurity removal, wherein the pretreatment agent is selected from humus soil, red mud, waste catalyst from an oil refinery unit, kaolin, semi-coke, activated carbon, gasification ash and gasification slag, or a combination thereof; and Step 2) A step of subjecting the effluent from step 1) to solid-liquid separation to obtain insoluble materials and a solution containing impurities-removed plastics.

[0013] Preferably, at least a part of the plastic waste used in step 1) has been subjected to a dechlorination treatment comprising the steps of: step i) dissolving the plastic waste in a first organic solvent selected from tetrahydrofuran, a ketone solvent, a chlorinated aliphatic hydrocarbon, or a combination thereof; and Step ii) A step of subjecting the mixture obtained in step i) to solid-liquid separation to obtain a chlorine-containing solution and chlorine-removed plastic waste.

[0014] In another embodiment, the present application provides a plastic waste pretreatment system for carrying out the plastic waste pretreatment method described herein, comprising a plastic waste pretreatment device and a solid-liquid separation device, the plastic waste pretreatment device having a plastic waste inlet, an optional chlorine-removed plastic waste inlet, a pretreatment agent inlet, a solvent oil inlet, and a pretreated effluent outlet, the solid-liquid separation device having an inlet, an insoluble material outlet, and an impurity-removed plastic-containing solution outlet, and the pretreated effluent outlet of the plastic waste pretreatment device is in communication with the inlet of the solid-liquid separation device.

[0015] Preferably, the plastic waste pretreatment system further includes a plastic waste dissolution-dechlorination apparatus having a plastic waste inlet, a first organic solvent inlet and a dissolution effluent outlet, and a dechlorination-separation apparatus having an inlet, a chlorine-containing solution outlet and a chlorine-removed plastic waste outlet, wherein the dissolution effluent outlet of the plastic waste dissolution-dechlorination apparatus is communicated with the inlet of the dechlorination-separation apparatus, and the chlorine-removed plastic waste outlet of the dechlorination-separation apparatus is communicated with the chlorine-removed plastic waste inlet of the plastic waste pretreatment apparatus.

[0016] In yet another aspect, the present application provides a method for producing motor fuel from plastic waste, comprising the steps of: Step I) A step of pretreating plastic waste using the plastic waste pretreatment method or the plastic waste pretreatment system described herein to obtain an impurity-removed plastic-containing solution; Step II) contacting the impurity-removed plastic-containing solution and any catalytic cracking feedstock with a catalytic cracking catalyst for reaction; and Step III) Separating the reaction product of step II) to obtain a gasoline fraction and / or a diesel fraction.

[0017] In yet another aspect, the present application provides a system for carrying out the method for producing motor fuel from plastic waste of the present application, comprising the plastic waste pretreatment system described herein and a catalytic cracking apparatus, wherein the catalytic cracking apparatus has an impurity-removed plastic-containing solution inlet, an optional catalytic cracking feedstock inlet, and at least one outlet, and the impurity-removed plastic-containing solution outlet of the solid-liquid separation apparatus of the plastic waste pretreatment system is in communication with the impurity-removed plastic-containing solution inlet of the catalytic cracking apparatus.

[0018] The method and system for pretreating plastic waste according to the present invention can effectively remove metal impurities, chlorine impurities, and silicon impurities from plastic waste, thereby avoiding the impact of the metal impurities and chlorine impurities on subsequent treatment equipment; the silicon impurities are removed in the original form of the organosilicon polymer added during the treatment of the plastic, thereby effectively avoiding the problem of catalyst deactivation in subsequent treatment equipment. Furthermore, the method and system for pretreating plastic waste according to the present invention has the advantages of small pollution emissions, good environmental protection, and reduced carbon emissions during operation.

[0019] The method and system for producing automotive fuel from plastic waste can be used to produce automotive fuel from plastic waste, and thus is beneficial to solving the problem of white pollution, and has good environmental, social, and economic benefits.

[0020] Other features and advantages of the present application are explained in detail in the detailed description that follows.

[0021] BRIEF DESCRIPTION OF THE DRAWINGS The drawings that form part of this specification are provided to aid in the understanding of the application and should not be considered limiting. The application can be read with reference to the drawings in combination with the following detailed description. In the drawings: FIG. 1 shows a schematic diagram of a preferred embodiment of the method and system for pre-treating plastic waste according to the present application; and FIG. 2 shows a schematic diagram of a preferred embodiment of the method and system for producing motor fuel from plastic waste according to the present application.

[0022] (Detailed Description of the Invention) The present application will be described in further detail below with reference to specific embodiments thereof and drawings. It should be noted that the specific embodiments of the present application are provided for illustrative purposes only and are not intended to be limiting in any way.

[0023] Any specific numerical value, including the endpoints of a numerical range, set forth in the context of this application should not be limited to that exact value, but should also be interpreted as encompassing all values ​​close to that exact value, such as, for example, all values ​​within ±5% of that exact value. Furthermore, with respect to any numerical range described herein, any combination between the endpoints of the range, between each endpoint and any specific value within the range, or between any two specific values ​​within the range, can be made to provide one or more new numerical ranges, which new numerical ranges should also be considered to be specifically set forth in this application.

[0024] Unless otherwise specified, terms used herein have the same meaning as commonly understood by one of ordinary skill in the art; if a term is defined herein and that definition differs from the common understanding in the art, the definition provided herein shall control.

[0025] As used herein, the term "humus" refers to a mixture formed by various decayed plant matter and organic waste that is mixed with plastic waste excavated from a landfill.

[0026] As used herein, the term "semi-coke" refers to the solid product produced by pyrolysis of carbonaceous materials such as coal, biomass and plastic waste at temperatures between 350°C and 600°C.

[0027] As used herein, the terms "gasification ash and gasification slag" refer to solid residues obtained by reacting carbonaceous materials, such as coal, semi-coke, coke, biomass, petroleum coke, plastic waste, etc., with a gasifying agent at temperatures above 600°C under atmospheric or pressurized conditions.

[0028] As used herein, the term "red mud" refers to the industrial solid waste product discharged after the extraction of alumina from bauxite.

[0029] As used herein, the term "solvent oil" has the meaning known in the art and typically refers to a complex mixture of hydrocarbons. Preferably, the "solvent oil" is a distillate oil rich in aromatic hydrocarbons, which may be one of liquid distillate oils obtained from petroleum refining, coal pyrolysis, direct coal liquefaction, pyrolysis of biomass and / or plastic waste, or a mixture of two or more liquid distillate oils.

[0030] As used herein, the term "optionally / optionally" means that the corresponding step, device, component or ingredient is not essential but optional, i.e., said step, device, component or ingredient may or may not be present.

[0031] In the context of this application, all reaction and process pressures given are gauge pressures unless otherwise specified.

[0032] In the context of this application, in addition to what is explicitly stated, what is not mentioned or any thing shall be considered to be the same as what is known in the art without any changes.In addition, any of the embodiments described herein can be freely combined with one or more of the embodiments described herein, and the technical solutions or ideas thus obtained shall be considered as part of the original disclosure or original description of this application, and shall not be considered as new matters not disclosed or anticipated in this specification, unless it is obvious to a person skilled in the art that such combination is obviously unreasonable.

[0033] All patent and non-patent literature cited herein, including but not limited to textbooks and journal articles, is hereby incorporated by reference in its entirety.

[0034] In a first aspect, the present application provides a method for pre-treatment of plastic waste, comprising the steps of: Step 1) contacting plastic waste with a pretreatment agent and a solvent oil for impurity removal, wherein the pretreatment agent is selected from humus soil, red mud, waste catalyst from an oil refinery, kaolin, semi-coke, activated carbon, gasification ash and gasification slag, or a combination thereof, and optionally further comprises an alkaline oxide; and Step 2) A step of subjecting the effluent from step 1) to solid-liquid separation to obtain insoluble materials and a solution containing impurities-removed plastics.

[0035] In a preferred embodiment, step 1) is carried out at a temperature of 200°C to 450°C; more preferably, the treatment conditions for step 1) include a temperature of 250°C to 410°C, a pressure of 0.1 to 5 MPa, and a time period (i.e., a residence time of the plastic waste) of 10 to 60 minutes. In some further preferred embodiments, the treatment conditions for step 1) include a temperature of 320°C to 390°C, a pressure of 0.5 MPa to 4.0 MPa, and a time period of 15 to 45 minutes. In some other further preferred embodiments, the treatment conditions for step 1) include a temperature of 280°C to 390°C, a pressure of 0.1 MPa to 5 MPa, and a time period of 10 to 30 minutes.

[0036] In a preferred embodiment, the distillation range of the solvent oil used in step 1) is between 80°C and 550°C, and the solvent oil has a total aromatics content of more than 50% by mass and a monocyclic aromatics content of more than 20% by mass. More preferably, the solvent oil has a monocyclic aromatics content of more than 40% by mass. For example, the solvent oil may be vacuum gas oil (VGO), hydrogenated light cycle oil (HLCO), straight-run diesel (i.e., straight-run diesel oil), coal tar, etc.

[0037] In a preferred embodiment, the weight ratio of the solvent oil to the plastic waste in step 1) is 1:10 to 10:1, more preferably 1:1 to 7:1.

[0038] According to the present application, the pretreatment agent used in step 1) may be one of humus, red mud, waste catalyst from an oil refinery, kaolin, semi-coke, activated carbon, and gasification ash and gasification slag, or a mixture of two or more thereof, and optionally contains an alkaline oxide. In a preferred embodiment, the pretreatment agent used in step 1) is selected from the group consisting of waste catalytic cracking catalyst, humus, activated carbon, or a combination thereof, and optionally contains an alkaline oxide.

[0039] In a preferred embodiment, the particle size of the pretreatment agent used in step 1) is within the range of 75 μm to 150 μm; more preferably, the weight ratio of the pretreatment agent to the plastic waste in step 1) is 1:10 to 2:1, more preferably 1:7 to 1:5. For example, in some particularly preferred embodiments, the pretreatment agent is used in an amount of 1 wt % to 10 wt % based on the total weight of the mixed material obtained in step 1).

[0040] In a preferred embodiment, the plastic waste used in step 1) is washed, dried and crushed, and the crushed plastic waste has a particle size of 1 mm to 200 mm, preferably 1 mm to 50 mm.

[0041] In a preferred embodiment, the operating temperature of the solid-liquid separation in step 2) is 250°C to 410°C.

[0042] In the method of the present application, by carefully selecting the type of pretreatment agent and solvent oil, as well as the treatment conditions, the impurity content in the resulting impurity-removed plastic-containing solution can be controlled within a desired range to facilitate subsequent further steps and treatments, such as catalytic cracking. In a preferred embodiment, the impurity-removed plastic-containing solution has a metal content of less than 5 μg / g, a chlorine content of less than 20 μg / g, and a silicon content of less than 3 μg / g; more preferably, the impurity-removed plastic-containing solution has a metal content of less than 5 μg / g, a chlorine content of less than 3 μg / g, and a silicon content of less than 3 μg / g; particularly preferably, the impurity-removed plastic-containing solution has a metal content of less than 3 μg / g, a chlorine content of less than 1 μg / g, and a silicon content of less than 1 μg / g.

[0043] In a preferred embodiment, at least a part of the plastic waste used in step 1) has been subjected to a dechlorination treatment comprising the following steps: step i) dissolving the plastic waste in a first organic solvent selected from tetrahydrofuran, a ketone solvent, a chlorinated aliphatic hydrocarbon, or a combination thereof; and Step ii) A step of subjecting the mixture obtained in step i) to solid-liquid separation to obtain a chlorine-containing solution and chlorine-removed plastic waste.

[0044] According to the preferred embodiment, the chlorine-containing plastic in the plastic waste is dissolved in a solution by selectively dissolving the plastic waste with the first organic solvent in step i). When polystyrene is contained in the plastic waste, both the chlorine-containing plastic and the polystyrene are dissolved in the first organic solvent in step i). According to the present application, the chlorine-containing plastic may be one or more selected from the group consisting of polyvinyl chloride, polyvinylidene chloride, and copolymers thereof.

[0045] In this preferred embodiment, step i) preferably uses a first organic solvent that has a good dissolving effect and high dissolving efficiency for the chlorine-containing plastic. In a further preferred embodiment, the first organic solvent used in step i) is a mixed solvent of tetrahydrofuran and a ketone solvent in any weight ratio, more preferably a mixed solvent of tetrahydrofuran and a ketone solvent in a weight ratio of 1:3 to 3:1, more preferably 1:2 to 2:1, and the ketone solvent is selected from methyl ethyl ketone, methyl isobutyl ketone, cyclohexanone, isophorone, or a combination thereof, preferably methyl ethyl ketone, cyclohexanone, or a combination thereof, more preferably methyl ethyl ketone.

[0046] In a further preferred embodiment, in step i), the plastic waste is dissolved in the first organic solvent at 50° C. to 100° C. for 30 minutes to 60 minutes.

[0047] In a further preferred embodiment, the weight ratio of the first organic solvent to the plastic waste used in step i) is 1:10 to 10:1.

[0048] In some further preferred embodiments, the first organic solvent used in step i) is preheated to a temperature of 40°C to 60°C.

[0049] In a further preferred embodiment, the operating temperature of the solid-liquid separation in step ii) is 50° C. to 100° C. Preferably, the chlorine content in the chlorine-removed plastic waste is less than 20 μg / g.

[0050] In a further preferred embodiment, the dechlorination treatment further comprises the steps of: Step iii) subjecting the chlorine-containing solution obtained in step ii) to a precipitation and separation treatment selected from back-extraction, simple distillation, flash evaporation, rectification or a combination thereof to obtain plastic (e.g., PVC and / or PS) particles and recovered first organic solvent.

[0051] In a more preferred embodiment, the precipitation treatment in step iii) is stripping-distillation combined with distillation, the stripping solvent being water, the stripping temperature being 70°C to 100°C, and the distillation temperature being 80°C to 100°C. In some particularly preferred embodiments, after contacting the chlorine-containing solution with the stripping aqueous solution in step iii), the dissolved plastic (e.g., PVC and / or PS) precipitates as solid particles, and the remaining liquid portion can be a first organic solvent containing water; the first organic solvent containing water can be distilled to obtain water and a recovered first organic solvent, which can then be reused. In some specific embodiments, the stripped effluent is separated by filtration to obtain wastewater containing plastic (e.g., PVC and / or PS) particles and an organic solvent.

[0052] In a preferred embodiment, the method for pre-treatment of plastic waste according to the present application further comprises the steps of: Step 3) contacting the insoluble material obtained in step 2) with a second organic solvent for solvent extraction, and subjecting the obtained product to solid-liquid separation to obtain a solid material and a liquid material, wherein the second organic solvent is selected from benzene, toluene, trichloromethane, cyclohexanone, ethyl acetate, butyl acetate, carbon disulfide, tetrahydrofuran, gasoline, or a combination thereof; step 4) treating the solid material obtained in step 3) to recover the pretreatment agent, and recycling at least a portion of the recovered pretreatment agent to step 1), wherein the treatment is selected from screening, regeneration, or a combination thereof; and Step 5) subjecting the liquid material obtained in step 3) to a precipitation treatment and separation to obtain solid plastic particles and a recovered second organic solvent, wherein the precipitation treatment is selected from back-extraction, simple distillation, flash evaporation, rectification or a combination thereof.

[0053] The plastic waste suitable for use in this application may be any common plastic waste material, such as plastic waste in fresh household waste, plastic waste from industrial and agricultural production, and waste plastic in mature waste, preferably low-quality plastic waste that cannot be physically recycled. The plastic waste may be in the form of plastic waste rods, plastic waste pellets, plastic waste flakes, or a combination thereof, obtained by initial processing of the plastic waste. The plastic waste may include any one or more of PE, PP, PS, and PVC plastics.

[0054] In some preferred embodiments, the method for pretreatment of plastic waste of the present application comprises the following steps: Step 1) contacting plastic waste with a pretreatment agent and a solvent oil in a plastic waste pretreatment device to remove impurities; and Step 2) Separating the effluent of step 1) in a solid-liquid separation device to obtain insoluble materials and an impurity-removed plastic-containing solution, wherein the impurity-removed plastic-containing solution has a metal content of less than 5 μg / g, a chlorine content of less than 20 μg / g, and a silicon content of less than 3 μg / g.

[0055] In some further preferred embodiments, the method for pretreatment of plastic waste further comprises the steps of: Step 3) in an extractor, contacting the insoluble material obtained in step 2) with a second organic solvent for solvent extraction, and subjecting the resulting product to solid-liquid separation to obtain a solid material and a liquid material; Step 4) treating the solid material obtained in step 3) in a pretreatment agent recovery device to recover the pretreatment agent, and recycling at least a portion of the recovered pretreatment agent as a circulating pretreatment agent in the plastic waste pretreatment device of step 1); and Step 5) The liquid material obtained in step 3) is subjected to precipitation treatment and separation in a second solvent recovery device to obtain solid plastic particles and recovered second organic solvent.

[0056] In some other preferred embodiments, the present method for pretreatment of plastic waste comprises the steps of: Step a) completely dissolving the plastic waste in a first organic solvent in a plastic waste dissolving-dechlorination device; Step b) subjecting the dissolved effluent obtained in step a) to solid-liquid separation in a dechlorination-separation device to obtain a chlorine-containing solution and chlorine-removed plastic waste; Step c) contacting the chlorine-removed plastic waste obtained in step b) and optionally additional plastic waste with a pretreatment agent and a solvent oil in a plastic waste pretreatment device for impurity removal; Step d) separating the effluent in step c) in a solid-liquid separator to obtain insoluble materials and a removed plastic-containing solution having a metal content of less than 5 μg / g, a chlorine content of less than 20 μg / g, and a silicon content of less than 3 μg / g; Process.

[0057] In a further preferred embodiment, in step a), the plastic waste is completely dissolved in a first organic solvent in a plastic waste dissolution-dechlorination apparatus at a temperature of 50°C to 100°C. In step a), the residence time of the plastic waste is 30 minutes to 60 minutes; and in step b), the dissolution effluent is subjected to solid-liquid separation in a dechlorination-separation apparatus. The operating temperature of the dechlorination-separation apparatus is 50°C to 100°C.

[0058] In a further preferred embodiment, in step b), the chlorine-containing solution obtained from the dechlorination-separation device is subjected to precipitation and separation in a first solvent recovery device to obtain plastic (such as PVC and / or PS) particles and a recovered first organic solvent, and the operation and conditions of the precipitation treatment are as described above and will not be repeated here.

[0059] In some further preferred embodiments, the method for pretreatment of plastic waste further comprises the steps of: Step e) contacting the insoluble material obtained in step d) with a second organic solvent in an extractor for solvent extraction, and subjecting the obtained product to solid-liquid separation to obtain a solid material and a liquid material; Step f) treating the solid material obtained in step e) in a pretreatment agent recovery device to recover the pretreatment agent, and recycling at least a portion of the recovered pretreatment agent as a recycled pretreatment agent to the plastic waste pretreatment device in step c); and Step g) subjecting the liquid material obtained in step e) to precipitation and separation in a second solvent recovery device to obtain solid plastic particles and recovered second organic solvent.

[0060] In the above-mentioned further preferred embodiment, the operating conditions of the extraction device in step 3) or step e) are consistent with the second organic solvent used, and the purpose of the extraction is to remove the solvent oil adhering to the discharged solid material, reduce the total amount of the discharged solid material, and ultimately achieve the purpose of emission reduction.

[0061] In the above-mentioned further preferred embodiment, the precipitation treatment in step 5) or step g) is preferably selected from back-extraction, simple distillation, flash evaporation, rectification or a combination thereof, and the operating temperature can be flexibly controlled according to the type and amount of the solvent used.

[0062] The plastic waste pretreatment method of the present application can effectively remove metal impurities, chlorine impurities, and silicon impurities from plastic waste, and the resulting impurity-removed plastic-containing solution can be used as a hydrocarbon feedstock and subjected to further processing to produce chemical raw materials such as olefins and aromatics, or to produce products such as automobile fuel. In particular, the silicon impurities can be removed in the form of organosilicon polymers added during plastic processing, thereby effectively avoiding the impact of the silicon impurities on catalysts used in subsequent processing equipment. Meanwhile, reducing the chlorine content in plastic waste can effectively avoid the impact of chlorine impurities on subsequent processing equipment.

[0063] In a second aspect, the present application provides a method for producing a pharmaceutical composition comprising: There is provided a plastic waste pretreatment system for carrying out the plastic waste pretreatment method of the present application, comprising a plastic waste pretreatment device and a solid-liquid separation device, the plastic waste pretreatment device having a plastic waste inlet, an optional chlorine-removed plastic waste inlet, a pretreatment agent inlet, a solvent oil inlet, and a pretreated effluent outlet, the solid-liquid separation device having an inlet, an insoluble material outlet, and an impurity-removed plastic-containing solution outlet, and the pretreated effluent outlet of the plastic waste pretreatment device is in communication with the inlet of the solid-liquid separation device.

[0064] In the plastic waste pretreatment system of the present application, the majority of the plastics are dissolved in the solvent oil in the plastic waste pretreatment device and subjected to desiliconization and demetallization in the presence of the pretreatment agent, and the PVC in the plastic waste is appropriately decomposed into HCl and captured by the pretreatment agent, thereby achieving a dechlorination effect. The effluent obtained after impurity removal is sent to a solid-liquid separator and separated into insoluble materials and a solution containing impurities-removed plastics.

[0065] In the plastic waste pretreatment system of the present application, the plastic waste pretreatment device can effectively remove metal impurities, chlorine impurities, and silicon impurities from the plastic waste. The resulting impurity-removed plastic-containing solution preferably has a metal content of less than 5 μg / g, a chlorine content of less than 20 μg / g, and a silicon content of less than 3 μg / g; more preferably a metal content of less than 5 μg / g, a chlorine content of less than 3 μg / g, and a silicon content of less than 3 μg / g; particularly preferably a metal content of less than 3 μg / g, a chlorine content of less than 1 μg / g, and a silicon content of less than 1 μg / g. In particular, the silicon impurities are removed in the original form of the organosilicon polymer added during the processing of the plastic, thereby effectively preventing the silicon impurities from affecting the catalyst used in subsequent processing equipment. Meanwhile, the impact of chlorine impurities on subsequent processing equipment is effectively prevented by reducing the chlorine content in the plastic waste.

[0066] In a preferred embodiment, the plastic waste pretreatment device may be a single-stage kettle dissolver, a multi-stage kettle dissolver connected in series or parallel, a profiled dissolver with dissolving action, or a continuous screw extractor, or other devices with the same function. More preferably, the plastic waste pretreatment device is provided with a stirrer and a heater. The stirrer may be electrically or magnetically driven and may be one or more of a paddle type, anchor type, frame type, and spiral type. The stirring speed of the stirrer may be 1 r / min to 300 r / min, preferably 60 r / min to 100 r / min. The heater may be one or more of an internal heater and / or an external heater. For example, the external heater may be one or more of a jacket type or a semicircular coil pipe heater, and the internal heater may be various built-in coil pipes. The heat source may be one or more of electricity, heat-conducting oil, steam, and direct flame.

[0067] The plastic waste pretreatment system of the present application does not have any specific requirements regarding the form of the solid-liquid separation device, and various forms of filters, centrifuges, or combinations thereof may be used. In a preferred embodiment, the solid-liquid separation device may be one or more stages of continuous automatic solid-liquid separation devices connected in series, each having heat preservation function, oil resistance, and organic solvent resistance, or may be one or more of various types of filters with automatic filter sieve replacement, a press filter with a scraper plate, a cross-flow filter, a horizontal screw centrifuge, and a screw press desolventizer. More preferably, the solid-liquid separation device may include a heating device and a heat preservation device. The heating device may be one or more of an external heating device or an internal heating device. The external heating device may be one or more of a jacket-type or semicircular coil pipe heating device, and the internal heating device may be various built-in coil pipes. The heat source may be one or more of electricity, heat-conducting oil, steam, and direct flame. Preferably, the operating temperature of the solid-liquid separator may be, for example, 250° C. to 410° C. When the solid-liquid separator is a filter, the mesh diameter of the filter may be 0.1 mm to 1 mm, preferably 0.1 μm to 10 μm.

[0068] In a preferred embodiment, the plastic waste pretreatment system further includes a plastic waste dissolution-dechlorination apparatus having a plastic waste inlet, a first organic solvent inlet, and a dissolution effluent outlet, and a dechlorination-separation apparatus having an inlet, a chlorine-containing solution outlet, and a chlorine-removed plastic waste outlet, wherein the dissolution effluent outlet of the plastic waste dissolution-dechlorination apparatus is communicated with the inlet of the dechlorination-separation apparatus, and the chlorine-removed plastic waste outlet of the dechlorination-separation apparatus is communicated with the chlorine-removed plastic waste inlet of the plastic waste pretreatment apparatus.

[0069] In this preferred embodiment, the plastic waste may be subjected to an appropriate dissolution treatment in the first organic solvent in the plastic waste dissolution-dechlorination device at a temperature of, for example, 50°C to 100°C, and the residence time of the plastic waste may be, for example, 30 minutes to 60 minutes. The treated material is subjected to solid-liquid separation in the dechlorination-separation device, which may be operated at a temperature of, for example, 50°C to 100°C, to obtain a chlorine-containing liquid and chlorine-removed plastic waste.

[0070] In this preferred embodiment, the plastic waste is passed through the plastic waste dissolution-dechlorination device, where most of the chlorine-containing plastic waste in the plastic waste is removed, and the chlorine-removed plastic waste obtained after the separation in the dechlorination-separation device may have a chlorine content of less than 20 μg / g.

[0071] In a more preferred embodiment, the plastic waste dissolving-dechlorination apparatus may be a single-stage kettle dissolver, a multi-stage kettle dissolver connected in series or parallel, a profiled dissolver with dissolving action, or a device having the same function (e.g., a continuous screw extractor). More preferably, a stirring device and a heating device are provided in the plastic waste dissolving-dechlorination apparatus. The stirring device may be electrically or magnetically driven and may be one or more of a paddle type, anchor type, frame type, and spiral type. The stirring speed of the stirring device may be 1 r / min to 300 r / min, preferably 60 r / min to 100 r / min. The heating device may be one or more of an internal heating device and / or an external heating device. For example, the external heating device may be one or more of a jacket type or a semicircular coil pipe heating device, and the internal heating device may be various built-in coil pipes. The heat source may be one or more of electricity, heat-conducting oil, steam, and direct flame.

[0072] In a more preferred embodiment, the dechlorination-separation device may be one or more serially connected continuous automatic solid-liquid separation devices having various forms of heat preservation function, oil resistance, and organic solvent resistance, or may be one or more of various types of filters with automatic filter sieve replacement, a press filter with a scraper plate, a cross-flow filter, a horizontal screw centrifuge, and a screw press desolvator. More preferably, the dechlorination-separation device may be equipped with a heating device and a heat preservation device. The heating device may be one or more of an external heating device or an internal heating device. The external heating device may be one or more of a jacket-type or semicircular coil pipe heating device, and the internal heating device may be various built-in coil pipes. The heat source may be one or more of electricity, heat-conducting oil, steam, and direct flame. When the dechlorination-separation device is a filter, the mesh diameter of the filter may be 0.1 mm to 10 mm, more preferably 0.1 mm to 1 mm.

[0073] In a further preferred embodiment, the plastic waste pretreatment system further comprises a first solvent recovery device having a chlorine-containing solution inlet, a plastic particle outlet, and a recovered first organic solvent outlet, and the chlorine-containing solution outlet of the plastic waste dissolution-dechlorination device is in communication with the chlorine-containing solution inlet of the first solvent recovery device.

[0074] In this further preferred embodiment, the chlorine-containing solution obtained from the dechlorination-separation device is subjected to precipitation treatment and separation in the first solvent recovery device to obtain plastic (such as PVC and / or PS) particles and recovered first organic solvent. Preferably, the precipitation treatment is selected from stripping, simple distillation, flash distillation, rectification, or a combination thereof, and correspondingly, the precipitation treatment device used can be selected from a stripping pot, a stripping column, a fractionating column, a flash column, a rectification column, or a combination thereof.

[0075] More preferably, the precipitation treatment is a stripping-distillation-coupled process, in which the stripping agent is water. For example, in some embodiments, after the chlorine-containing solution is passed through the first solvent recovery device and contacted with the stripping agent water, the dissolved plastic (e.g., PVC and / or PS) precipitates as solid particles, and the remaining liquid portion becomes the first organic solvent containing water; the first organic solvent containing water is distilled to obtain water and the recovered first organic solvent, which can then be reused.

[0076] In some further preferred embodiments, the back-extracted effluent solution is separated by filtration to obtain a wastewater containing plastic (PVC and / or PS) particles and organic solvent, and the filtration device used is selected from one or more stages connected in series or parallel of a filter press, a plate and frame filter, a centrifuge, a screw desolventizer, or combinations thereof.

[0077] In a preferred embodiment, the plastic waste pretreatment system further includes an extraction device, a pretreatment agent recovery device, and a second solvent recovery device; the extraction device comprises an insoluble material inlet, a second organic solvent inlet, a solid material outlet, and a liquid material outlet, and the insoluble material outlet of the solid-liquid separation device is in communication with the insoluble material inlet of the extraction device; the pretreatment agent recovery device has a solid material inlet and a circulating pretreatment agent outlet, the solid material outlet of the extraction device is connected to the solid material inlet of the pretreatment agent recovery device, and the circulating pretreatment agent outlet of the pretreatment agent recovery device is connected to the pretreatment agent inlet of the plastic waste pretreatment device; The second solvent recovery device has a liquid material inlet, a solid plastic particle outlet, and a recovered second organic solvent outlet, and the liquid material outlet of the extraction device is connected to the liquid material inlet of the second solvent recovery device.

[0078] In this preferred embodiment, one or more of a solvent extraction tower and a static mixing extractor can be provided in the extraction device, and the operating conditions of the extraction device are consistent with the second organic solvent used, and the purpose of the extraction is to remove the solvent oil adhering to the discharged solid material, reduce the total amount of the discharged solid material, and ultimately achieve the purpose of emission reduction.

[0079] In this preferred embodiment, the solid material obtained from the extractor is treated in a pretreatment agent recovery device, and then a portion or all of it is returned to the plastic waste pretreatment device as a recycled pretreatment agent. The treatment performed in the pretreatment agent recovery device can be selected from screening, regeneration, or a combination thereof. The pretreatment agent recovery device can be in the form of a vibrating screen, a rotary screen, a single-section or multi-section fluidized bed regenerator, a rotary kiln regenerator, an infrared heating furnace, etc.

[0080] In this preferred embodiment, the liquid material obtained from the extraction device is subjected to precipitation treatment and separation in the second solvent recovery device to obtain solid plastic particles and a recovered second organic solvent, the precipitation treatment can be selected from back extraction, simple distillation, flash evaporation, rectification or a combination thereof, and the operating temperature can be flexibly controlled according to the type and amount of solvent used. The types of equipment that can be used in the second solvent recovery device are the same as those described above for the first solvent recovery device and will not be described in detail here.

[0081] Figure 1 is a schematic diagram of a preferred embodiment of a method and system for pretreating plastic waste according to the present application. As shown in Figure 1, dried and crushed plastic waste 25 is introduced into a plastic waste dissolution-dechlorination device 1 and completely dissolved in a first organic solvent 8. The dissolved effluent is subjected to solid-liquid separation in a dechlorination-separation device to obtain a chlorine-containing solution 10 and chlorine-removed plastic waste 9. The obtained chlorine-containing solution 10 is passed through a first solvent recovery device 2, and after precipitation and separation, plastic (PVC and / or PS, etc.) particles 12 and a recovered first organic solvent 11 are obtained. The recovered first organic solvent 11 is recycled.

[0082] The dried and crushed plastic waste 13 and any chlorine-removed plastic waste 9 are passed through a plastic waste pre-treatment device 3, where they are contacted with a solvent oil 14 and a pre-treatment agent 15 to perform an impurity removal treatment, and the treated effluent 16 passes through a solid-liquid separator 4 and is separated into insoluble materials 17 and an impurity-removed plastic-containing solution 24.

[0083] The obtained insoluble material 17 is passed through the extraction device 5 and contacted with a second organic solvent 18 for solvent extraction, and the obtained product is subjected to solid-liquid separation to obtain a solid material 21 and a liquid material 19. The obtained solid material 21 is treated in the pretreatment agent recovery device 7, and then at least a portion of the solid material is returned to the plastic waste pretreatment device 3 as a circulating pretreatment agent 22, and the remaining solid material 23 is discharged outside the device. The obtained liquid material 19 is subjected to precipitation treatment and separation in the second solvent recovery device 6 to obtain solid plastic particles 26 and a recovered second organic solvent 20, which is recycled.

[0084] In a third aspect, the present application provides a method for producing motor fuel from plastic waste, comprising the steps of: Step I) obtaining an impurity-removed plastic-containing solution using the plastic waste pretreatment method or the plastic waste pretreatment system described in the present application; Step II) contacting the impurity-removed plastic-containing solution and any catalytic cracking feedstock with a catalytic cracking catalyst for reaction; and Step III) Separating the reaction product of step II) to obtain a gasoline fraction and / or a diesel fraction.

[0085] According to the present application, the optional catalytic cracking feedstock can be any conventional catalytic cracking feedstock, such as VGO, atmospheric residue (AR), deasphalted oil (DAO), etc.

[0086] According to the present application, the catalytic cracking catalyst used in step II) can be any conventional catalytic cracking catalyst. In a preferred embodiment, the catalytic cracking catalyst comprises a zeolite, an inorganic oxide binder, and optionally a clay; preferably, based on the total weight of the catalyst, The zeolite is present in an amount of 5% to 50% by weight, the inorganic oxide is present in an amount of 5% to 90% by weight, and the clay is present in an amount of 0% to 70% by weight.

[0087] More preferably, the zeolite is selected from the group consisting of rare earth-containing or rare earth-free Y or HY zeolites, rare earth-containing or rare earth-free ultrastable Y zeolites, zeolites with MFI structure, or combinations thereof.

[0088] In a preferred embodiment, the catalytic cracking conditions used in step II) include the following: a reaction temperature of 460°C to 530°C, a reaction pressure of 0.1 MPa to 0.4 MPa, a catalyst to oil ratio of 3 to 10, and a reaction time of 2 seconds to 4 seconds. When the catalytic cracking reaction is carried out in a riser reactor, the catalyst to oil ratio refers to the weight ratio of the catalyst circulation amount to the total feed amount, and the reaction time refers to the average residence time of the reaction stream in the riser reactor before entering the inlet of a cyclone.

[0089] In a preferred embodiment, the catalytic cracking product obtained in step II) is separated in step III) to obtain at least a gas, a gasoline fraction, and a diesel fraction. Both the obtained gasoline fraction and diesel fraction are high-quality automobile fuel components and may be subjected to further processing. For example, the gasoline fraction can be processed using Sinopec's S-Zorb technology, Sinopec Research Institute of Petroleum Processing Co., Ltd.'s RSDS technology, etc. to produce clean gasoline that meets China's national V or national VI standards. The diesel fraction can be processed together with a straight-run diesel fraction using RTS technology or Sinopec Research Institute of Petroleum Processing Co., Ltd.'s diesel hydrotreatment ultra-deep desulfurization technology, etc. to produce clean diesel that meets China's national V or national VI standards.

[0090] In some preferred embodiments, the method for producing motor fuel from plastic waste of the present application comprises the steps of: Step A) mixing plastic waste with a first organic solvent (herein also referred to as solvent I) and completely dissolving the mixed solvent in a plastic waste dissolving-dechlorination apparatus (herein also referred to as a first plastic waste impurity removal apparatus) at a temperature of 25°C to 120°C; Step B) subjecting the dissolved effluent of step A) to solid-liquid separation in a dechlorination-separation device (also referred to herein as solid-liquid separation device I or separation device I) to obtain a chlorine-containing solution (also referred to herein as a first solution) and a chlorine-removed plastic waste (also referred to herein as a first solid mixture); Step C) contacting the chlorine-removed plastic waste obtained in Step B) and optionally additional plastic waste with a pretreatment agent (also referred to herein as an impurity removal additive) and a solvent oil (also referred to herein as solvent II), and carrying out an impurity removal treatment at a temperature of 200°C to 450°C in a plastic waste pretreatment device (also referred to herein as a second plastic waste impurity removal device); Step D) separating the effluent of step C) in a solid-liquid separator (also referred to herein as separator II) to obtain an insoluble material (also referred to herein as a second solid mixture) and an impurity-removed plastic-containing solution (also referred to herein as a second solution), having a chlorine content of less than 3 μg / g and a silicon content of less than 3 μg / g; Step E) contacting the impurity-removed plastic-containing solution obtained in step D) and any catalytic cracking feedstock with a catalytic cracking catalyst in a catalytic cracking unit for reaction; and Step F) Separating the reaction products of step E) to obtain gas, gasoline fraction and diesel fraction.

[0091] In a fourth aspect, there is provided a system for carrying out the method for producing automotive fuel from plastic waste of the present application, comprising the plastic waste pretreatment system described herein and a catalytic cracking apparatus; the catalytic cracking apparatus is provided with an impurity-removed plastic-containing solution inlet, an optional catalytic cracking feedstock inlet, and at least one outlet, and the impurity-removed plastic-containing solution outlet of the solid-liquid separation apparatus of the plastic waste pretreatment system is connected to the impurity-removed plastic-containing solution inlet of the catalytic cracking apparatus.

[0092] In the system for producing automotive fuel from plastic waste of the present application, the catalytic cracker may be any of various reactors suitable for carrying out a catalytic cracking reaction, for example, a fixed-bed catalytic cracker, a moving-bed catalytic cracker, a fluidized-bed catalytic cracker, a riser reactor catalytic cracker, or a combination thereof. In particular, the catalytic cracker may be selected from a TSRFCC, MIP, MIP-CGP, FDF-CC, MGG, MIO, ARGG catalytic cracker, or a combination thereof, allowing for flexible selection according to the existing facilities of the refinery.

[0093] In some preferred embodiments, the system for producing motor fuel from plastic waste comprises a plastic waste dissolution-dechlorination unit, a dechlorination-separation unit, a plastic waste pretreatment unit, a solid-liquid separation unit, and a catalytic cracking unit; The plastic waste dissolution-dechlorination apparatus comprises a plastic waste inlet, a first organic solvent inlet, a stirring device, a heating device, and a dissolution effluent outlet; the dechlorination-separation device comprises an inlet, a chlorine-containing solution outlet, and a chlorine-removed plastic waste outlet; The plastic waste pre-treatment device comprises a plastic waste inlet, a chlorine-removed plastic waste inlet, a pre-treatment agent inlet, a solvent oil inlet, a stirring device, a heating device, and a pre-treated effluent outlet; The solid-liquid separation device has an inlet, an insoluble material outlet, and an impurity-removed plastic-containing solution outlet; the catalytic cracking unit comprises an impurity-removed plastic-containing solution inlet, an optional catalytic cracking feedstock inlet, a gas outlet, a gasoline fraction outlet, and a diesel fraction outlet; The dissolution effluent outlet of the plastic waste dissolution-dechlorination device is connected to the inlet of the dechlorination-separation device, the chlorine-removed plastic waste outlet of the dechlorination-separation device is connected to the chlorine-removed plastic waste inlet of the plastic waste pretreatment device, the pretreatment effluent outlet of the plastic waste pretreatment device is connected to the inlet of the solid-liquid separation device, and the impurity-removed plastic-containing solution outlet of the solid-liquid separation device is connected to the impurity-removed plastic-containing solution inlet of the catalytic cracking device.

[0094] In a further preferred embodiment, the system for producing motor fuel from plastic waste further comprises a first solvent recovery device having a chlorine-containing solution inlet, a plastic particle outlet (also referred to herein as a chlorine-containing plastic particle outlet), and a recovered first organic solvent outlet, wherein the chlorine-containing solution outlet of the dechlorination-separation device is in communication with the chlorine-containing solution inlet of the first solvent recovery device, and optionally, the recovered first organic solvent outlet of the first solvent recovery device is in communication with the first organic solvent inlet of the plastic waste dissolution-dechlorination device.

[0095] FIG. 2 is a schematic diagram of a preferred embodiment of a method and system for producing automotive fuel from plastic waste according to the present invention. As shown in FIG. 2, plastic waste is sequentially processed in a drying device 201 and a crushing device 202. The dried and crushed plastic waste particles and a first organic solvent are introduced into a plastic waste dissolution-dechlorination device 203, where they are thoroughly mixed and dissolved. The dissolved effluent is separated into a chlorine-containing solution and chlorine-removed plastic waste in a dechlorination-separation device 204. The resulting chlorine-containing solution is treated in a first solvent recovery device 209 to obtain the first organic solvent and plastic particles (e.g., PVC and / or PS). The resulting chlorine-removed plastic waste is passed through a plastic waste pretreatment device 205 and subjected to impurity removal treatment in the presence of a solvent oil and a pretreatment agent. The treated material is separated into an impurity-removed plastic-containing solution and insoluble materials via a solid-liquid separation section 206. The resulting impurity-removed plastic-containing solution is passed through a fluid transport device 207 to a catalytic cracking device 208, where it contacts a catalytic cracking catalyst, optionally together with a catalytic cracking feedstock, to carry out a catalytic cracking reaction. The reaction products are separated to obtain gas, a gasoline fraction, a diesel fraction, a heavy cycle oil fraction, and a slurry oil. The gasoline fraction and the diesel fraction are used as automobile fuel. The resulting insoluble material and the second organic solvent are mixed and passed to an extraction device 210 to separate into solid and liquid materials. The resulting solid material is passed to a pretreatment agent recovery device 211, where a portion of the recovered pretreatment agent is recycled and the remainder is discharged as a waste pretreatment agent. The resulting liquid material is passed to a second solvent recovery device 212, where it is treated to obtain a recovered second organic solvent and solid plastic particles.

[0096] In some particularly preferred embodiments, the present application provides the following technical solutions: [Item A1] A method for pre-treating plastic waste, comprising the following steps: Step (1) optionally passing plastic waste through a plastic waste dissolution-dechlorination device to completely dissolve it in a first organic solvent, and subjecting the dissolution effluent to solid-liquid separation to obtain a chlorine-containing solution and chlorine-removed plastic waste, wherein the first organic solvent is selected from tetrahydrofuran, a ketone solvent, a chlorinated aliphatic hydrocarbon, or a combination thereof; Step (2) passing plastic waste, optionally together with the chlorine-removed plastic waste obtained in step (1), through a plastic waste pre-treatment device, contacting it with a pre-treatment agent and a solvent oil for impurity removal, and passing the effluent through a solid-liquid separator to obtain insoluble materials and an impurity-removed plastic-containing solution having a metal content of less than 5 μg / g, a chlorine content of less than 20 μg / g, and a silicon content of less than 3 μg / g; The pretreatment agent is one or more selected from humus soil, red mud, waste catalyst from petroleum refineries, kaolin, semi-coke, activated carbon, gasification ash and gasification slag, and optionally, alkaline oxides.

[0097] [Item A2] The method according to Item A1, wherein the plastic waste is selected from plastic waste in fresh household waste, plastic waste from industrial and agricultural production, plastic waste in mature waste, or a combination thereof, and the type of the plastic waste is one or more of PE, PP, PS, and PVC.

[0098] [Item A3] The method according to Item A1, wherein the plastic waste is washed, dried and crushed before passing through the optional plastic waste dissolving-dechlorination device, and the crushed plastic waste has a particle size of 1 mm to 200 mm, preferably 1 mm to 50 mm.

[0099] [Item A4] The first organic solvent is a mixed solvent of tetrahydrofuran and a ketone solvent in any weight ratio, the ketone solvent is selected from methyl ethyl ketone, methyl isobutyl ketone, cyclohexanone, isophorone, or a combination thereof; The method according to Item A1, wherein the weight ratio of the first organic solvent to the plastic waste is 1:10 to 10:1.

[0100] [Item A5] The ketone solvent is one or more selected from methyl ethyl ketone and cyclohexanone; preferably methyl ethyl ketone; the first organic solvent is a mixed solvent of tetrahydrofuran and a ketone solvent in a weight ratio of 1:3 to 3:1; Preferably, the first organic solvent is a mixed solvent of tetrahydrofuran and a ketone solvent in a weight ratio of 1:2 to 2:1.

[0101] [Item A6] The method according to Item A1, wherein in step (1), the plastic waste is completely dissolved in the first organic solvent in the plastic waste dissolving-dechlorination apparatus at a temperature of 50°C to 100°C for a residence time of the plastic waste of 30 minutes to 60 minutes.

[0102] [Item A7] A process comprising: providing a first solvent recovery device; passing the chlorine-containing solution obtained in step (1) through the first solvent recovery device and subjecting it to precipitation treatment and separation to obtain PVC and / or PS particles and a recovered first organic solvent; The method according to item A1, wherein the precipitation treatment is selected from back-extraction, simple distillation, flash evaporation, rectification, or a combination thereof.

[0103] [Item A8] The method according to Item A7, wherein in the first solvent recovery device, the precipitation treatment is stripping-distillation combined, the stripping solvent is water, the stripping temperature is 70°C to 100°C, and the distillation temperature is 80°C to 100°C.

[0104] [Item A9] The method according to Item A1, wherein the treatment conditions of the plastic waste pretreatment device include a temperature of 250°C to 410°C, a pressure of 0.1 MPa to 5 MPa, and a residence time of the plastic waste of 10 minutes to 60 minutes.

[0105] [Item A10] The method according to Item A9, wherein the treatment conditions of the plastic waste pretreatment device include a temperature of 320°C to 390°C, a pressure of 0.5 MPa to 4.0 MPa, and a residence time of the plastic waste of 15 minutes to 45 minutes.

[0106] [Item A11] The method according to Item A1, wherein the distillation range of the solvent oil is 80°C to 550°C, the solvent oil has a total aromatic compound content of more than 50% by mass and a monocyclic aromatic compound content of more than 20% by mass, and the weight ratio of the solvent oil to the plastic waste is 1:10 to 10:1.

[0107] [Item A12] The method according to Item A11, wherein the content of monocyclic aromatic compounds in the solvent oil exceeds 40% by mass; and the weight ratio of the solvent oil to the plastic waste is 1:1 to 7:1.

[0108] [Item A13] The particle size of the pretreatment agent is in the range of 75 μm to 150 μm; The method according to Item A1, wherein the weight ratio of the pretreatment agent to the plastic waste is 1:10 to 2:1, preferably 1:7 to 1:5.

[0109] [Item A14] The method according to Item A1 or A13, wherein the pretreatment agent is one or more of a waste catalytic cracking catalyst, humus, red mud, activated carbon, and optionally an alkaline oxide.

[0110] [Item A15] The method according to Item A1, wherein the operating temperature of the solid-liquid separation device is 250°C to 410°C; and the impurity-removed plastic-containing solution has a metal content of less than 3 μg / g, a chlorine content of less than 1 μg / g, and a silicon content of less than 1 μg / g.

[0111] [Item A16] The method according to Item A1, further comprising the following steps: Step (3) passing the insoluble material obtained in step (2) through an extractor, contacting it with a second organic solvent for solvent extraction, and subjecting the resulting product to solid-liquid separation to obtain a solid material and a liquid material, The obtained solid material is treated in a pretreatment agent recovery device, and at least a part of the solid material is recycled as a circulating pretreatment agent in the plastic waste pretreatment device in step (2); subjecting the obtained liquid material to precipitation and separation in a second solvent recovery device to obtain solid plastic particles and a recovered second organic solvent; The second organic solvent is selected from benzene, toluene, trichloromethane, cyclohexanone, ethyl acetate, butyl acetate, carbon disulfide, tetrahydrofuran, gasoline, or a combination thereof.

[0112] [Item A17] The method according to Item A16, wherein the processing in the pretreatment agent recovery device includes one or more of screening and regeneration.

[0113] [Item A18] The method according to Item A16, wherein in the second solvent recovery device, the precipitation treatment is selected from back extraction, simple distillation, flash evaporation, rectification, or a combination thereof.

[0114] [Item A19] A system useful in the method according to any one of Items A1 to A18, comprising an optional plastic waste dissolution-dechlorination device, a plastic waste pretreatment device, and a solid-liquid separation device; The plastic waste dissolution-dechlorination apparatus comprises a plastic waste inlet, a first organic solvent inlet, a chlorine-containing solution outlet, and a chlorine-removed plastic waste outlet; the plastic waste pretreatment device comprises a plastic waste inlet, an optional chlorine-removed plastic waste inlet, a pretreatment agent inlet, a solvent oil inlet, and a pretreatment effluent outlet, the pretreatment effluent outlet being in communication with the inlet of the solid-liquid separation device; The solid-liquid separation device includes an insoluble material outlet and an impurity-removed plastic-containing solution outlet.

[0115] [Item A20] The system described in Item A19, further comprising a first solvent recovery device having a chlorine-containing solution inlet, a PVC and / or PS particle outlet, and a recovered first organic solvent outlet; the chlorine-containing solution outlet of the plastic waste dissolution-dechlorination device is connected to the chlorine-containing solution inlet of the first solvent recovery device.

[0116] [Item A21] The system according to Item A19, further comprising an extraction device, a pretreatment agent recovery device, and a second solvent recovery device; the extraction device comprises an insoluble material inlet, a second organic solvent inlet, a solid material outlet, and a liquid material outlet, and the insoluble material outlet of the solid-liquid separation device is in communication with the insoluble material inlet of the extraction device; the pretreatment agent recovery device includes a solid material inlet and a circulating pretreatment agent outlet, and the solid material outlet of the extraction device is in communication with the solid material inlet of the pretreatment agent recovery device; The circulating pretreatment agent outlet of the pretreatment agent recovery device is connected to the pretreatment agent inlet of the plastic waste pretreatment device; The second solvent recovery device has a liquid material inlet, a solid plastic particle outlet, and a recovered second organic solvent outlet, and the liquid material outlet of the extraction device is in communication with the liquid material inlet of the second solvent recovery device.

[0117] [Item B1] A method for producing automotive fuel from plastic waste, comprising the following steps: Step (1) passing plastic waste and a first organic solvent through a plastic waste dissolving-dechlorinating device to thoroughly mix and dissolve at a temperature of 25°C to 120°C, and separating the dissolving effluent into a chlorine-containing solution and chlorine-removed plastic waste in a dechlorinating-separating device, wherein the first organic solvent is selected from tetrahydrofuran, a ketone solvent, a chlorinated aliphatic hydrocarbon, or a combination thereof; Step (2) passing the chlorine-removed plastic waste through a plastic waste pretreatment device and subjecting it to treatment at a temperature of 200°C to 450°C in the presence of a solvent oil for removing impurities and a pretreatment agent for removing impurities, and separating the treated material in a solid-liquid separator to obtain an impurity-removed plastic-containing solution having a chlorine content of less than 3 μg / g and a silicon content of less than 3 μg / g, and an insoluble material; Step (3) Passing the impurity-removed plastic-containing solution, optionally together with a catalytic cracking feedstock, through a catalytic cracking device to contact it with a catalytic cracking catalyst for a catalytic cracking reaction, and separating to obtain at least a gas, a gasoline fraction, and a diesel fraction.

[0118] [Item B2] The first organic solvent is a mixed solvent of tetrahydrofuran and a ketone solvent in any weight ratio, and the ketone solvent is selected from methyl ethyl ketone, methyl isobutyl ketone, cyclohexanone, isophorone, or a combination thereof; The method according to Item B1, wherein the weight ratio of the first organic solvent to the plastic waste is 1:10 to 10:1.

[0119] [Item B3] The ketone solvent is one or more selected from methyl ethyl ketone and cyclohexanone, preferably methyl ethyl ketone; The method according to item B2, wherein the first organic solvent is a mixed solvent of tetrahydrofuran and a ketone solvent in a weight ratio of 1:3 to 3:1.

[0120] [Item B4] The method according to any one of Items B1 to B3, wherein the first organic solvent is a mixed solvent of tetrahydrofuran and a ketone solvent in a weight ratio of 1:2 to 2:1.

[0121] [Item B5] The method according to Item B1, wherein in step (1), the plastic waste is thoroughly mixed and dissolved in the first organic solvent at a temperature of 50°C to 100°C in the plastic waste dissolving-dechlorination apparatus; and the residence time of the plastic waste is preferably 30 minutes to 60 minutes.

[0122] [Item B6] The method according to Item B1, wherein the chlorine content of the chlorine-removed plastic waste is less than 20 μg / g.

[0123] [Item B7] In step (2), the solvent oil is an aromatic-rich distillate having a distillation range of 80°C to 540°C; the solvent oil has a total aromatic compound content of more than 50% by mass and a monocyclic aromatic compound content of more than 20% by mass; Preferably, the solvent oil has a monocyclic aromatic compound content of more than 40% by weight.

[0124] [Item B8] The method according to Item B1, wherein in step (2), the pretreatment agent is one or more selected from the group consisting of humus soil, red mud, waste catalyst from an oil refinery, kaolin, activated carbon, semi-coke, gasification ash, and gasification slag; and the particle size of the pretreatment agent is within the range of 75 μm to 150 μm.

[0125] [Item B9] The method according to Item B8, wherein in step (2), the pretreatment agent is one or more selected from the group consisting of waste catalytic cracking catalyst from a catalytic cracking unit, humus soil, and activated carbon.

[0126] [Item B10] In step (2), the weight ratio of the solvent oil to the plastic waste is 1:10 to 10:1; The method according to Item B1, wherein the pretreatment agent is used in an amount of 1% by weight to 10% by weight based on the total weight of the material in the plastic waste pretreatment device. [Item B11] The method according to Item B1, wherein in step (2), the conditions for the impurity removal treatment include the following: a temperature of 280°C to 390°C, a pressure of 0.1 MPa to 5 MPa, and a residence time of the chlorine-containing solution of 10 minutes to 30 minutes.

[0127] [Item B12] In step (3), the catalytic cracking catalyst comprises a zeolite, an inorganic oxide binder, and optionally a clay; The zeolite is present in an amount of 5 wt% to 50 wt%, the inorganic oxide is present in an amount of 5 wt% to 90 wt%, and the clay is present in an amount of 0 wt% to 70 wt%, based on the total weight of the catalyst; The method according to item B1, wherein the zeolite is selected from the group consisting of rare earth-containing or rare earth-free Y or HY zeolite, rare earth-containing or rare earth-free ultrastable Y zeolite, zeolite with MFI structure, or a combination thereof.

[0128] [Item B13] The method according to item B1, wherein in step (3), the catalytic cracking conditions include a reaction temperature of 460°C to 530°C, a catalyst to oil ratio of 5 to 10, and a reaction time of 2 to 4 seconds.

[0129] [Item B14] The method according to Item B1, wherein the plastic waste is selected from plastic waste in fresh household waste, plastic waste from industrial and agricultural production, plastic waste in mature waste, or a combination thereof, and the type of the plastic waste is one or more of PE, PP, PS, and PVC.

[0130] [Item B15] The method according to Item B1, wherein the plastic waste is washed, dried and crushed before passing through the plastic waste dissolving-dechlorination device, and the crushed plastic waste has a particle size of 1 mm to 200 mm, preferably 1 mm to 50 mm.

[0131] [Item B16] The method according to any one of Items B1 to B15, wherein a solvent recovery device is provided in step (1), and the chlorine-containing solution is passed through the solvent recovery device and subjected to a treatment selected from back-extraction, simple distillation, flash evaporation, rectification, or a combination thereof to obtain a recovered first organic solvent and chlorine-containing plastic particles.

[0132] [Item B17] The method according to Item B16, wherein in step (1), the treatment in the solvent recovery apparatus is stripping-distillation combined, the stripping solvent is water, the stripping temperature is 70°C to 100°C, and the distillation temperature is 80°C to 100°C.

[0133] [Item B18] A system for producing motor fuel from plastic waste useful in the method according to any one of items B1 to B15, comprising a plastic waste dissolution-dechlorination unit, a plastic waste pretreatment unit, and a catalytic cracking unit; the plastic waste dissolving-dechlorinating device comprises a plastic waste inlet, a first organic solvent inlet, a material outlet, a stirring device and a heating device, the material outlet of the plastic waste dissolving-dechlorinating device is connected to the dechlorination-separation device, and the dechlorination-separation device comprises a chlorine-containing solution outlet and a chlorine-removed plastic waste outlet; The plastic waste pre-treatment device comprises a chlorine-removed plastic waste inlet, a solvent oil inlet, a pre-treatment agent inlet, a material outlet, a stirring device, and a heating device, the chlorine-removed plastic waste outlet of the dechlorination-separation device is connected to the chlorine-removed plastic waste inlet of the plastic waste pre-treatment device; the material outlet of the plastic waste pre-treatment device is connected to a solid-liquid separation device, the solid-liquid separation device is equipped with an impurity-removed plastic-containing solution outlet and an insoluble material outlet; The catalytic cracking device comprises an impurity-removed plastic-containing solution inlet, an optional catalytic cracking feedstock inlet, a gas outlet, a gasoline fraction outlet, and a diesel fraction outlet, and the solid-liquid separation device comprises an impurity-removed plastic-containing solution outlet that is in communication with the impurity-removed plastic-containing solution inlet of the catalytic cracking device.

[0134] [Item B19] A system for producing motor fuel from plastic waste useful in the method described in Item B16, comprising a plastic waste dissolving-dechlorination unit, a solvent recovery unit, a plastic waste pretreatment unit and a catalytic cracking unit; The plastic waste dissolution-dechlorination apparatus comprises a plastic waste inlet, a first organic solvent inlet, a material outlet, a stirring device, and a heating device; The material outlet of the plastic waste dissolution-dechlorination device is connected to the dechlorination-separation device; The dechlorination-separation device comprises a chlorine-containing solution outlet and a chlorine-removed plastic waste outlet; The solvent recovery device includes an inlet for a chlorine-containing solution, an outlet for a recovered first organic solvent, and an outlet for a chlorine-containing plastic particle; the chlorine-containing solution outlet of the dechlorination-separation device is in communication with the chlorine-containing solution inlet of the solvent recovery device; The recovered first organic solvent outlet of the solvent recovery device is connected to the first organic solvent inlet of the plastic waste dissolution-dechlorination device; The plastic waste pre-treatment device includes a chlorine-removed plastic waste inlet, a solvent oil inlet, a pre-treatment agent inlet, a material outlet, a stirring device, and a heating device; The chlorine-removed plastic waste discharge outlet of the dechlorination-separation device is connected to the chlorine-removed plastic waste inlet of the plastic waste pre-treatment device; the material outlet of the plastic waste pre-treatment device is connected to a solid-liquid separation device, and the material discharge outlet of the plastic waste pre-treatment device is connected to the solid-liquid separation device, and the solid-liquid separation device has an impurity-removed plastic-containing solution discharge outlet and an insoluble material discharge outlet; The catalytic cracking device comprises an impurity-removed plastic-containing solution inlet, an optional catalytic cracking feedstock inlet, a gas outlet, a gasoline fraction outlet, and a diesel fraction outlet, and the solid-liquid separation device comprises an impurity-removed plastic-containing solution outlet that is in communication with the impurity-removed plastic-containing solution inlet of the catalytic cracking device.

[0135] [Example] The present application is further illustrated by, but not limited to, the following examples.

[0136] In the following examples, the chlorine content in the solid material was measured by coulometry in accordance with the standard method of RIPP 64-90 (see "Determination of Total Chlorine in Crude Oil by Coulometric Method" in "Petrochemical Analysis Methods (RIPP Test Methods)," edited by Cuiding YANG et al., Science Press, 1990, pp. 164-167). The instrument used was a Thermo Fisher ECS300 microcoulomb analyzer, and the sample was a frozen and crushed powdered sample of plastic waste.

[0137] In the following examples, the chlorine content of the liquid materials was also measured by the RIPP 64-90 method, except that the samples were liquid mixtures.

[0138] In the following examples, the silicon content and metal content of the liquid materials were measured in accordance with GB17476-1998 "Standard Test Method for Determination of Additive Elements, Wear Metals, and Contaminants in Used Lubricating Oils and for Determination of Selected Elements in Base Oils by Inductively Coupled Plasma Atomic Emission Spectroscopy (ICP-AES)."

[0139] In the following examples, unless otherwise specified, the plastic waste was crushed using a shear crusher with a mesh size of 50 mm.

[0140] The plastic waste feedstocks used in Examples Series I and Comparative Examples Series I were as follows: Plastic waste A1 is greenhouse film, mulching film, etc. from a location in Shandong Province, which is cleaned, dried, and then crushed. The obtained plastic waste A1 contains 4.3% ash and 0.5% water, and contains PE as the main plastic component, a small amount of EVA, and trace amounts of other inseparable materials such as PP and PS, with an average total chlorine content of about 850 ppm; Plastic waste B1 is plastic waste separated from the refuse of a paper mill in Jiangsu Province. It is washed, strongly dried, and then crushed. The obtained plastic waste B1 contains 9.5% ash and 0% water, and contains PE and PP as the main plastic components, as well as small amounts of PVC, PET, PS, etc., with an average chlorine content of 2.2%; Plastic waste C is plastic waste from mature garbage excavated from a landfill in Guangdong Province. It is washed, strongly dried, and then crushed. The obtained plastic waste C contains 7.3% ash and 0% water, and is a mixed plastic waste containing PE, PP, PS, PET, and PVC, with an average chlorine content of 1.9%; Plastic waste D was excavated from a landfill in Ganzhou, Jiangxi Province, washed, thoroughly dried, and then crushed. The resulting plastic waste D contained 11.9% ash, 0.5% water, and 2.2% chlorine, and its main components were mixed plastic waste containing PE, PP, PS, PET, and PVC.

[0141] (Example I-1) The crushed plastic waste A1 was sent through a screw feeder to a plastic waste pre-treatment device. The plastic waste was mixed with a pre-treatment agent and solvent oil, and then subjected to impurity removal treatment at 350°C and 1.5 MPa, with a residence time of 30 minutes. The treated material was separated into insoluble material and an impurity-removed plastic-containing solution in a solid-liquid separator. The plastic components in the resulting impurity-removed plastic-containing solution were mainly PE and PP (EVA was decomposed and mixed into the solvent oil). The plastic component concentration of the solution was 14.4%, the silicon content was less than 1 μg / g, the chlorine content was 6 μg / g, and the total metal content was 5.5 μg / g. The insoluble material was sent to an extraction device and contacted with tetrahydrofuran for solvent extraction, the resulting product was separated to obtain solid and liquid materials, the resulting solid material was treated in a pretreatment agent recovery device, and a portion of the solid material was recycled to the plastic waste pretreatment device as a circulating pretreatment agent. The liquid material was contacted with a stripping agent in a second solvent recovery device for stripping, the resulting solid-liquid mixture was filtered to obtain solid plastic particles and a mixed solution, and the resulting mixed solution was rectified to recover and reuse tetrahydrofuran and the stripping agent, respectively.

[0142] The solvent oil used was a catalytic cracking light cycle oil with a distillation range of 195°C to 355°C, a total aromatic compound content of 73% by mass, and a monocyclic aromatic compound content of 52% by mass, and the weight ratio of the solvent oil to the plastic waste was 5:1.

[0143] The pretreatment agent used was a waste FCC equilibrium catalyst provided by a refinery. Its particle size was 75 μm to 150 μm, its SiO2 content was 38.1%, and the contents of the main metal components were as follows: Al2O3 50.5%, Fe2O3 1.31%, NiO 1.8%, La2O3 3.3%, and CeO2 1.4%. The weight ratio of the pretreatment agent to the plastic waste was 1:9.

[0144] The back-extraction agent was water, which was used in an amount three times the amount of the liquid material, and the back-extraction temperature was room temperature.

[0145] (Example I-2) The crushed plastic waste B1 was sent through a screw feeder to a plastic waste pretreatment device. The plastic waste was mixed with a pretreatment agent and solvent oil and then subjected to impurity removal treatment at 300°C and 1.2 MPa. The residence time of the plastic waste B1 was 40 minutes. The treated material was separated into insoluble material and an impurity-removed plastic-containing solution in a solid-liquid separator. The resulting impurity-removed plastic-containing solution contained PE and PP. The plastic component concentration of the solution was 14.2%, the silicon content was less than 1 μg / g, the chlorine content was 18 μg / g, and the total metal content was 7.9 μg / g. The insoluble material was sent to an extractor and contacted with tetrahydrofuran for solvent extraction. The resulting product was separated to obtain solid and liquid materials. The resulting solid material was treated in a pretreatment agent recovery device, and a portion of the solid material was recycled as a circulating pretreatment agent in the plastic waste pretreatment device. The liquid material was contacted with stripping agent water in a solvent recovery device for stripping, and the resulting solid-liquid mixture was filtered to obtain solid plastic particles and a mixed solution, which was then rectified to recover and reuse tetrahydrofuran and the stripping agent, respectively.

[0146] The solvent oil used was a catalytic cracking light cycle oil with a distillation range of 195°C to 355°C, a total aromatic compound content of 73% by mass, and a monocyclic aromatic compound content of 52% by mass, and the weight ratio of the solvent oil to the plastic waste was 5:1.

[0147] The pretreatment agent used was a mixture of sieved humus and CaO. The humus was sieved to remove any organic matter present, and a portion of the humus with particle sizes of 75 μm to 150 μm was used as the pretreatment agent. Lumped calcium oxide was crushed and sieved, and samples of the same particle size were mixed with humus in a mass ratio of 8:2, so the weight ratio of the pretreatment agent to the plastic waste was 1:7.

[0148] (Example I-3) The crushed plastic waste B1 was sent to a plastic waste pre-treatment device via a screw feeder. The plastic waste was mixed with a pre-treatment agent and solvent oil and then subjected to impurity removal treatment at 350°C and 1.8 MPa, with a residence time of 45 minutes. The treated material was separated into insoluble material and an impurity-removed plastic-containing solution in a solid-liquid separator. The plastic components in the resulting impurity-removed plastic-containing solution were PE and PP, with a plastic component concentration of 14.2%, a silicon content of less than 1 μg / g, a chlorine content of 10 μg / g, and a total metal content of 3.8 μg / g.

[0149] The solvent oil used was VGO from an oil refinery, with a distillation range of 275°C to 581°C, a total aromatics content of 45.1% by mass, and a monocyclic aromatics content of 21% by mass; the weight ratio of the solvent oil to the plastic waste was 5:1.

[0150] The pretreatment agent used was a mixture of coal-based activated carbon and Fe2O3 in a mass ratio of 9:1, with particle sizes ranging from 75 μm to 150 μm. The weight ratio of the pretreatment agent to the plastic waste was 1:8.

[0151] (Example I-4) The crushed plastic waste B1 was sent via a screw feeder to a plastic waste pretreatment device. The plastic waste was mixed with a pretreatment agent and solvent oil and then subjected to impurity removal treatment at 350°C and 1.8 MPa, with a residence time of 30 minutes. The treated material was separated into insoluble material and an impurity-removed plastic-containing solution in a solid-liquid separator. The plastic components in the resulting impurity-removed plastic-containing solution were PE and PP. The plastic component concentration of the solution was 14.2%, with a silicon content of less than 1 μg / g, a chlorine content of 11 μg / g, and a total metal content of 4.1 μg / g.

[0152] The solvent oil used was a catalytic cracking light cycle oil with a distillation range of 156°C to 338°C, a total aromatic compound content of 76.8% by mass, and a monocyclic aromatic compound content of 63.8% by mass; the weight ratio of the solvent oil to the plastic waste was 5:1.

[0153] The pretreatment agent used was a mixture of coal-based activated carbon and Fe2O3 in a mass ratio of 9:1, with particle sizes ranging from 75 μm to 150 μm. The weight ratio of the pretreatment agent to the plastic waste was 1:8.

[0154] (Comparative example I-1) This comparative example was carried out using the same plastic waste raw material, solvent oil, and impurity removal treatment conditions as those described in Example I-4, except that no pretreatment agent was used. The treated material was separated into insoluble material and an impurity-removed plastic-containing solution in a solid-liquid separator. The plastic components in the obtained impurity-removed plastic-containing solution were PE and PP, and the solution had a plastic component concentration of 14.2%, a silicon content of 42 μg / g, a chlorine content of 207 μg / g, and a total metal content of 13 μg / g.

[0155] The impurity content in the impurity-removed plastic-containing solution obtained in this comparative example was too high to be directly used as a feed material for the subsequent processing equipment.

[0156] (Examples I-5 to I-9) The crushed plastic waste C was preheated to 60°C and fed into a plastic waste dissolving-dechlorination device, which is a plastic waste dissolving-dechlorination device, where it was dissolved in a first organic solvent at 60°C. The residence time of the plastic waste C in the plastic waste dissolving-dechlorination device was 30 minutes, and the dissolved eluate was separated into a chlorine-containing solution and chlorine-removed plastic waste using a screw squeezing desolventizer. The chlorine-removed plastic waste was further dried at a temperature slightly higher than the boiling point of the first organic solvent to recover the solvent.

[0157] The first organic solvent used in Example I-5 was tetrahydrofuran, and the weight ratio of the organic solvent to the plastic waste C was 10:1; the chlorine content in the chlorine-removed plastic waste was 23 μg / g.

[0158] The first organic solvent used in Example I-6 was methyl ethyl ketone, and the weight ratio of the organic solvent to the plastic waste C was 10:1; the chlorine content in the chlorine-removed plastic waste was 20 μg / g.

[0159] The first organic solvent used in Example I-7 was cyclohexanone, and the weight ratio of the organic solvent to the plastic waste C was 10:1; the chlorine content in the chlorine-removed plastic waste was 25 μg / g.

[0160] The first organic solvent used in Example I-8 was a mixture of tetrahydrofuran and methyl ethyl ketone in a weight ratio of 1:1, and the weight ratio of the organic solvent to the plastic waste C was 10:1; the chlorine content in the chlorine-removed plastic waste was 17 μg / g.

[0161] The first organic solvent used in Example I-9 was a mixture of tetrahydrofuran and methyl ethyl ketone in a weight ratio of 1:2, and the weight ratio of the organic solvent to the plastic waste C was 10:1; the chlorine content in the chlorine-removed plastic waste was 19 μg / g.

[0162] (Example I-10) The experiment was carried out as described in Example I-5, except that the first organic solvent was chlorobenzene, the dissolving temperature was 80° C., and the drying temperature of the chlorine-removed plastic waste was 140° C. The chlorine content in the chlorine-removed plastic waste was 32 μg / g.

[0163] (Example I-11) The crushed plastic waste D was sent to a continuous plastic waste dissolving and dechlorination device at a flow rate of 10 kg / h; a first organic solvent, THF / MEK=1:1, was preheated to 60°C and supplied to the continuous plastic waste dissolving and dechlorination device at a flow rate of 100 kg / h, and the propeller rotation speed of the plastic waste dissolving and dechlorination device was adjusted to obtain a residence time of 60 minutes. The mixed solution was sent to a screw squeeze desolventization device and separated into chlorine-removed plastic waste and a chlorine-containing solution at 60°C.

[0164] The chlorine-containing solution was sent to a stripping device at 80°C and stripped using hot water. The resulting product was passed through a plate and frame filter press to separate the PVC and PS, and the solvent was passed through a fractionation system to separate the first organic solvent and water, which were then recovered and recycled.

[0165] The chlorine-removed plastic waste was sent through a screw feeder to a stirrer-equipped kettle-type plastic waste pretreatment device. 80 kg / h of catalytic cracking light cycle oil preheated to 350°C, used as a solvent oil, was sent to the plastic waste pretreatment device together with 2 kg / h of FCC equilibrium catalyst, used as a pretreatment agent, and treated at 350°C and 1.5 MPa for 35 minutes. The resulting product was then passed through a screw squeeze desolventizer to obtain oil-containing insoluble materials and an impurity-removed plastic-containing solution. The plastic components in the obtained impurity-removed plastic-containing solution were mainly PE and PP, and the solution had a plastic component concentration of 9.7%, a silicon content of 2.3 μg / g, a chlorine content of 2.8 μg / g, and a total metal content of 1.8 μg / g.

[0166] The resulting oil-containing insoluble material was sent to an extraction device and contacted with toluene for solvent extraction. The resulting product was separated to obtain solid and liquid materials. The resulting solid material was treated in a pretreatment agent recovery device, and a portion of it was recycled as a circulating pretreatment agent in the plastic waste pretreatment device. The liquid material was then rectified in a solvent recovery device to obtain solid plastic particles (PS), recovered toluene, and a small amount of attached solvent oil.

[0167] The plastic waste feedstocks used in Example Series II and Comparative Example Series II were as follows: Plastic waste A2 was a mixture obtained by blending PE, PP, PS, and PVC in a weight ratio of 10:5:1:1.5, with a chlorine content of 0.88%, with PE, PP, and PVC existing as films and PS existing as foam.

[0168] Plastic waste B2 was a mixed plastic waste separated from matured waste excavated from a landfill in Guangdong Province, containing PE, PP, and small amounts of PS, PET, and PVC. The separated plastic waste was substantially free of moisture, had an ash content of approximately 9.9% by weight, and a total chlorine content of 1.18%.

[0169] (Examples II-1 to II-5) The plastic waste A2 pulverized into particles was sent to a plastic waste dissolution-dechlorination device together with a first organic solvent preheated to 65° C. and dissolved at 65° C. for 60 minutes, and the dissolved effluent was passed through a high-temperature filter and separated into a chlorine-containing solution and chlorine-removed plastic waste at 65° C. The plastic waste from which the chlorine had been removed was further dried to recover the solvent, and the chlorine content therein was analyzed.

[0170] The first organic solvent used in Example II-1 was tetrahydrofuran, and the weight ratio of the first organic solvent to the plastic waste A2 was 10:1; the chlorine content in the chlorine-removed plastic waste was 23 μg / g.

[0171] The first organic solvent used in Example II-2 was methyl ethyl ketone, and the weight ratio of the first organic solvent to the plastic waste A2 was 10:1; the chlorine content in the chlorine-removed plastic waste was 25 μg / g.

[0172] The first organic solvent used in Example II-3 was a mixture of tetrahydrofuran and cyclohexanone in a weight ratio of 1:1, and the weight ratio of the first organic solvent to the plastic waste A2 was 5:1; the chlorine content in the chlorine-removed plastic waste was 22 μg / g.

[0173] The first organic solvent used in Example II-4 was a mixture of tetrahydrofuran and methyl ethyl ketone in a weight ratio of 1:1, and the weight ratio of the first organic solvent to the plastic waste A2 was 10:1; the chlorine content in the chlorine-removed plastic waste was 13 μg / g.

[0174] The first organic solvent used in Example II-5 was a mixture of tetrahydrofuran and methyl ethyl ketone in a weight ratio of 1:2, the weight ratio of the first organic solvent to the plastic waste A2 was 10:1, and the chlorine content in the chlorine-removed plastic waste was 19 μg / g.

[0175] (Example II-6) The chlorine-removed plastic waste obtained in Example II-5 was sent to a plastic waste pretreatment device and dissolved in the presence of a solvent oil and a pretreatment agent for impurity removal at 350°C and 1.5 MPa for 30 minutes. The treated material was separated into an impurity-removed plastic-containing solution and insoluble materials using a high-temperature filter. The plastic components of the obtained impurity-removed plastic-containing solution were PE and PP, and the plastic component concentration of the solution was 16.1%, the chlorine content was 2.7 μg / g, the silicon content was 3.0 μg / g, and the total metal content was 2.1 μg / g.

[0176] The solvent oil used was a distilled oil rich in aromatic hydrocarbons, a mixed oil of wax oil fractions obtained in petroleum processing, with a distillation range of 220°C to 540°C, a total aromatic compound content of 59.6% by mass, and a monocyclic aromatic compound content of 21% by mass; the weight ratio of the solvent oil to the dechlorinated plastic waste was 5:1.

[0177] The pretreatment agent used was semi-coke with a particle size of 75 μm to 100 μm, and was used in an amount of 2.5 wt % based on the total weight of the materials in the plastic waste pretreatment device.

[0178] (Example II-7) The chlorine-removed plastic waste obtained in Example II-5 was sent to a plastic waste pretreatment device and dissolved in the presence of a solvent oil and a pretreatment agent for impurity removal at 350°C and 1.5 MPa for 30 minutes. The treated material was separated into an impurity-removed plastic-containing solution and insoluble materials using a high-temperature filter. The plastic components of the obtained impurity-removed plastic-containing solution were PE and PP, and the solution had a plastic component concentration of 16.1%, a chlorine content of 2.5 μg / g, a silicon content of 2.2 μg / g, and a total metal content of 1.2 μg / g.

[0179] The solvent oil used was a catalytic cracking distillate oil with a distillation range of 150°C to 338°C, a total aromatic compound content of 76.8% by mass, and a monocyclic aromatic compound content of 63.8% by mass; the weight ratio of the solvent oil to the chlorine-removed plastic waste was 5:1.

[0180] The pretreatment agent used was humus soil with a particle size of 75 μm to 100 μm, and was used in an amount of 2.5 wt % based on the total weight of the materials in the plastic waste pretreatment device.

[0181] (Example II-8) The chlorine-removed plastic waste obtained in Example II-5 was sent to a plastic waste pretreatment device and dissolved in the presence of a solvent oil and a pretreatment agent for impurity removal at 350°C and 1.5 MPa for 30 minutes. The treated material was separated into an impurity-removed plastic-containing solution and insoluble materials using a high-temperature filter. The plastic components of the obtained impurity-removed plastic-containing solution were PE and PP, and the solution had a plastic component concentration of 15.9%, a chlorine content of 2.5 μg / g, a silicon content of 2.5 μg / g, and a total metal content of 1.3 μg / g.

[0182] The solvent oil used was an aromatic hydrocarbon-rich distillate oil with a distillation range of 138°C to 362°C, a total aromatic compound content of 90.9% by mass, and a monocyclic aromatic compound content of 26.8% by mass; the weight ratio of the solvent oil to the dechlorinated plastic waste was 5:1.

[0183] The pretreatment agent used was a mixture of gasification ash and gasification slag with an FCC equilibrium catalyst in a weight ratio of 1:1, with a particle size of 75 μm to 100 μm. The pretreatment agent was used in an amount of 2.5 wt % based on the total weight of the materials in the plastic waste pretreatment device.

[0184] (Example II-9) The chlorine-removed plastic waste obtained in Example II-5 was sent to a plastic waste pretreatment device and dissolved in the presence of a solvent oil and a pretreatment agent for impurity removal at 350°C and 1.5 MPa for 30 minutes. The treated material was separated into an impurity-removed plastic-containing solution and insoluble materials using a high-temperature filter. The plastic components of the obtained impurity-removed plastic-containing solution were PE and PP, and the solution had a plastic component concentration of 16.1%, a chlorine content of 2.5 μg / g, a silicon content of 2.8 μg / g, and a total metal content of 1.9 μg / g.

[0185] The solvent oil used was an aromatic hydrocarbon-rich distillate oil with a distillation range of 138°C to 362°C, a total aromatic compound content of 90.9% by mass, and a monocyclic aromatic compound content of 26.8% by mass; the weight ratio of the solvent oil to the dechlorinated plastic waste was 5:1.

[0186] The pretreatment agent used was an FCC equilibrium catalyst having a particle size of 75 μm to 100 μm, and was used in an amount of 2.5 wt % based on the total weight of the materials in the plastic waste pretreatment device.

[0187] (Example II-10) The impurity-removed plastic-containing solution obtained in Example II-6 was fed to a riser reactor catalytic cracker and contacted with a catalytic cracking catalyst for catalytic cracking reaction. The reaction products were separated to obtain gas, gasoline fraction, diesel fraction, heavy cycle oil and oil slurry, and the obtained heavy cycle oil was recycled to the catalytic cracker.

[0188] The catalytic cracking catalyst was available from Sinopec Catalyst Co., Ltd. under the trade name GOR-Q, and its equilibrium catalytic properties were as follows: specific surface area ≥ 240 m 2 / g; bulk density > 0.68 g / ml; pore volume > 0.34 ml / g; attrition resistance ≦ 2.8% / h; microactivity ≧ 76% (measured at 800 °C for 4 h); average particle size 70 μm ~ 75 μm; Al2O3 ≧ 46%; and Re2O3 ≧ 3%.

[0189] The catalytic cracking conditions included a temperature of 500° C., a pressure of 0.15 MPa, a catalyst to oil ratio of 4, and a reaction time of 2.02 seconds.

[0190] The product yields obtained are shown in Table 1. The decomposition products of organosilicon compounds are mainly octamethylcyclotetrasiloxane and decamethylcyclopentasiloxane, which are mainly concentrated in the gasoline fraction, so the content of impurities in the gasoline fraction is the main focus of analysis.

[0191] (Example II-11) The impurity-removed plastic-containing solution obtained in Example II-7 was sent to a riser reactor catalytic cracking unit together with the catalytic cracking feedstock VGO in a weight ratio of 1:1 of the impurity-removed plastic-containing solution to the VGO, and contacted with a catalytic cracking catalyst for catalytic cracking reaction. The reaction products were separated to obtain gas, gasoline fraction, diesel fraction, heavy cycle oil and slurry oil, and the obtained heavy cycle oil was circulated in the catalytic cracking unit.

[0192] The catalytic cracking catalyst used was GOR-Q, and the catalytic cracking conditions included a temperature of 500° C., a pressure of 0.15 MPa, a catalyst to oil ratio of 4, and a reaction time of 2.02 seconds.

[0193] The product yields obtained are shown in Table 1.

[0194] [Table 1]

[0195] (Example II-12) Plastic waste B2 was sent to an intermittent heat exchange dryer via a conveyor belt. The heat source used was low-grade steam. The temperature of the dryer was 105°C, and the residence time of the plastic waste in the dryer was 30 minutes. The dried plastic waste was sent to a shear-type shredder with a 10 mm mesh diameter via a conveyor belt. The shredded plastic waste was passed through an externally heated kettle-type dissolver of the plastic waste dissolution and dechlorination device via a screw feeder. Meanwhile, a 2:1 mixed solvent of methyl ethyl ketone and tetrahydrofuran was also passed through the externally heated kettle-type dissolver via a metering pump at a weight ratio of 1:5 to the solvent. In the dissolver, the dissolution temperature was 65°C, the operating pressure was atmospheric, and the rotation speed of the stirring paddle was 60 rpm. After dissolving plastic waste B2 in the dissolver for 30 minutes, the solvent was replaced with new solvent for the next dissolution three times, until the total usage time was 90 minutes. The dissolution vessel includes two vessels connected in parallel, and the mixture is passed through a high-temperature filter through an outlet at the bottom of the dissolution vessel, and the mixture is separated into a chlorine-removed plastic waste and a chlorine-containing solution at 65° C. The chlorine-containing solution is subjected to flash evaporation to recover the first organic solvent and the chlorine-containing plastic waste.

[0196] The chlorine-removed plastic waste was dried at 80°C, and the first organic solvent was further recovered. The dried mixture was then sent to an externally heated kettle-type dissolver of a plastic waste pretreatment device via a screw feeder. The solvent oil was sent to the externally heated kettle-type dissolver via a metering pump at a weight ratio of 1:10 for the plastic waste to the solvent oil. The waste FCC equilibrium catalyst was also sent to the externally heated kettle-type dissolver via a metering pump at a weight ratio of 1:10 for the plastic waste to the pretreatment agent. The impurity removal treatment temperature was 390°C, the operating pressure was 0.5 MPa, the stirring paddle rotation speed was 60 rpm, and the residence time of the chlorine-removed plastic waste in the dissolver was 30 minutes. The dissolver included two dissolvers connected in parallel; the treated mixture was passed through a high-temperature filter at the bottom of the dissolver and filtered at 350°C to remove insoluble impurities, yielding an impurity-removed plastic-containing solution. The plastic components in the impurity-removed plastic-containing solution were mainly PE and PP, and the solution had a plastic component concentration of approximately 8.7%, a chlorine content of 2.2 μg / g, a silicon content of 1.7 μg / g, and a total metal content of 3.6 μg / g.

[0197] The impurity-removed plastic-containing solution was sent to a riser reactor catalytic cracking unit using a single-screw pump, where it was brought into contact with a catalytic cracking catalyst for a catalytic cracking reaction, and the reaction products were separated to obtain gas, a gasoline fraction, a diesel fraction, a slurry oil, and a semi-coke.

[0198] The solvent oil was a catalytically cracked distillate oil having a distillation range of 150°C to 338°C, a total aromatic compound content of 76.8 mass%, and a monocyclic aromatic compound content of 63.8 mass%.

[0199] The catalytic cracking catalyst was GOR-Q, and the catalytic cracking conditions included a temperature of 500° C., a pressure of 0.15 MPa, a catalyst to oil ratio of 4, and a reaction time of 2.02 seconds.

[0200] The product yield and the contents of some impurities are shown in Table 2.

[0201] (Example II-13) The experiments were carried out using the same plastic waste B2 feedstock, first organic solvent and treatment conditions for the plastic waste dissolution-dechlorination device, solvent oil, pretreatment agent and treatment conditions for the plastic waste pretreatment device, and catalyst and reaction conditions for the catalytic cracker as in Example II-12, except that the feedstock supplied to the catalytic cracker was a mixed feedstock of the impurity-removed plastic-containing solution and the catalytic cracking feedstock, i.e., VGO from the Shengli oilfield (Shengli VGO), in a weight ratio of 1:1, and the catalytic cracker was a conventional circulating fluidized bed device.

[0202] In this example, the replacement amount of catalytic cracking catalyst in this example was set to 1.2 kg / ton by using the replacement amount of catalyst required to process 1 ton of feedstock oil as an index while regenerating the deactivated catalyst in the regenerator and maintaining steady operation of the equipment.

[0203] The product yield and the contents of some impurities are shown in Table 2.

[0204] (Comparative Example II-1) Using the same catalyst and reaction conditions as in Example II-12, Shengli VGO was reacted in a catalytic cracking unit. The product yield and the contents of some impurities are shown in Table 2.

[0205] (Comparative Example II-2) An experiment was carried out using the same plastic waste B2 raw material, first organic solvent and treatment conditions for the plastic waste dissolving-dechlorination device, the same solvent oil and treatment conditions for the plastic waste pretreatment device, and the same raw material, catalyst and reaction conditions for the catalytic cracking device as in Example II-13, except that no pretreatment agent was used in the plastic waste pretreatment device.

[0206] The replacement amount of catalytic cracking catalyst in this comparative example was 1.22 kg / ton.

[0207] The product yield and the contents of some impurities are shown in Table 2.

[0208] [Table 2]

[0209] The results shown in Table 2 show that the method and system of the present invention can significantly reduce the relative content of harmful elements in the resulting oil product and produce a qualified product oil. It should be noted that because some plastics are added to the VGO, the yields of dry gas, liquefied gas, and coke in the FCC unit increase slightly, while the yields of gasoline and diesel oil decrease slightly.

[0210] Although the present application has been described in detail above with reference to preferred embodiments, it is not intended to be limited to these embodiments. Various modifications can be made in accordance with the inventive concept of the present application, and these modifications must be made within the scope of the present application.

[0211] It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, the present application will not describe the various possible combinations.

[0212] Furthermore, the embodiments of the present application can be combined in any manner without departing from the spirit of the present application, and the combined embodiments should be considered as the disclosure of the present application. [Brief explanation of the drawings]

[0213] [Figure 1] 1 is a schematic diagram of a preferred embodiment of a method and system for pre-treating plastic waste according to the present application; FIG. [Figure 2]1 is a schematic diagram of a preferred embodiment of a method and system for producing motor fuel from plastic waste according to the present application.

Claims

1. A method for pre-treatment of plastic waste, comprising the steps of: Step 1) contacting plastic waste with a pretreatment agent and a solvent oil for impurity removal, The pretreatment agent is selected from humus soil, red mud, waste catalyst from an oil refinery, kaolin, semi-coke, activated carbon, gasification ash and gasification slag, or a combination thereof; Optionally, a step including an alkaline oxide; and Step 2) A step of subjecting the effluent of step 1) to solid-liquid separation to obtain insoluble materials and a solution containing impurities-removed plastics, the impurity-removed plastic-containing solution having a metal content of less than 5 μg / g, a chlorine content of less than 20 μg / g, and a silicon content of less than 3 μg / g; The solvent oil used in step 1) has a distillation range of 80°C to 550°C, a total aromatics content of more than 50% by weight, and a monocyclic aromatics content of more than 20% by weight; The conditions for step 1) include a treatment temperature of 250° C. to 410° C.; a pressure of 0.1 MPa to 5 MPa; and a treatment time of 10 minutes to 60 minutes.

2. 10. The method of claim 1, having one or more of the following features: The solvent oil used in step 1) has a monocyclic aromatic compound content of more than 40% by weight; The conditions for step 1) include a treatment temperature of 320°C to 390°C; a pressure of 0.5 MPa to 4.0 MPa; and a treatment time of 15 minutes to 45 minutes; The weight ratio of the solvent oil to the plastic waste used in step 1) is 1:10 to 10:1; The pretreatment agent used in step 1) has a particle size in the range of 75 μm to 150 μm; The weight ratio of the pretreatment agent to the plastic waste used in step 1) is 1:10 to 2:1; and The plastic waste used in step 1) is washed, dried and crushed in advance, and the crushed plastic waste has a particle size of 1 mm to 200 mm.

3. The operating temperature of the solid-liquid separation in step 2) is 250°C to 410°C; 3. The method of claim 1 or 2, wherein the impurity-removed plastic-containing solution has a metal content of less than 3 μg / g, a chlorine content of less than 1 μg / g, and a silicon content of less than 1 μg / g.

4. The method according to any one of claims 1 to 3, wherein at least a part of the plastic waste used in step 1) has been subjected to a dechlorination treatment comprising the steps of: step i) dissolving the plastic waste in a first organic solvent selected from tetrahydrofuran, a ketone solvent, a chlorinated aliphatic hydrocarbon, or a combination thereof; and Step ii) A step of subjecting the mixture obtained in step i) to solid-liquid separation to obtain a chlorine-containing solution and chlorine-removed plastic waste.

5. 5. The method of claim 4, having one or more of the following features: In step i), dissolving the plastic waste in the first organic solvent at 50°C to 100°C for 30 minutes to 60 minutes; The first organic solvent used in step i) is a mixed solvent of tetrahydrofuran and a ketone solvent in a weight ratio of 1:3 to 3:1, and the ketone solvent is selected from methyl ethyl ketone, methyl isobutyl ketone, cyclohexanone, isophorone, or a combination thereof; and The weight ratio of the first organic solvent to the plastic waste used in step i) is 1:10 to 10:

1.

6. 6. The method according to claim 4 or 5, wherein the dechlorination treatment further comprises the following steps: Step iii) subjecting the chlorine-containing solution obtained in step ii) to precipitation and separation to obtain plastic particles and a recovered first organic solvent, wherein the precipitation is selected from the group consisting of back-extraction, simple distillation, flash evaporation, rectification, or a combination thereof.

7. The method described in claim 6, wherein the precipitation treatment is back-extraction combined distillation, the back-extraction solvent is water, the back-extraction temperature is 70°C to 100°C, and the distillation temperature is 80°C to 100°C.

8. The method of any one of claims 1 to 7, further comprising the steps of: Step 3) contacting the insoluble material obtained in step 2) with a second organic solvent for solvent extraction, and subjecting the resulting product to solid-liquid separation to obtain a solid material and a liquid material, wherein the second organic solvent is selected from benzene, toluene, trichloromethane, cyclohexanone, ethyl acetate, butyl acetate, carbon disulfide, tetrahydrofuran, gasoline, or a combination thereof; step 4) treating the solid material obtained in step 3) to recover the pretreatment agent, and recycling at least a portion of the recovered pretreatment agent to step 1), wherein the treatment is selected from screening, recycling, or a combination thereof; and Step 5) subjecting the liquid material obtained in step 3) to a precipitation treatment and separation to obtain solid plastic particles and a recovered second organic solvent, wherein the precipitation treatment is selected from back-extraction, simple distillation, flash evaporation, rectification or a combination thereof.

9. The plastic waste is selected from plastic waste in fresh household waste, plastic waste from industrial and agricultural production, plastic waste in mature waste, or a combination thereof; 9. The method of any one of claims 1 to 8, wherein the plastic waste comprises one or more selected from polyethylene (PE), polypropylene (PP), polystyrene (PS) and polyvinyl chloride (PVC) plastics, or combinations thereof.

10. The waste plastics pretreatment device and the solid-liquid separation device are included. the plastic waste pretreatment device comprises a plastic waste inlet, an optional chlorine-removed plastic waste inlet, a pretreatment agent inlet, a solvent oil inlet, and a pretreatment effluent outlet; The solid-liquid separation device includes an inlet, an insoluble material outlet, and an impurity-removed plastic-containing solution outlet; A plastic waste pretreatment system for carrying out the plastic waste pretreatment method according to any one of claims 1 to 9, wherein the pretreated effluent outlet of the plastic waste pretreatment device is in communication with the inlet of the solid-liquid separation device.

11. Further comprising a plastic waste dissolution-dechlorination unit and a dechlorination-separation unit; the plastic waste dissolution-dechlorination apparatus comprises a plastic waste inlet, a first organic solvent inlet, and a dissolution effluent outlet; the dechlorination-separation device comprises an inlet, a chlorine-containing solution outlet, and a chlorine-removed plastic waste outlet; 11. The system according to claim 10, wherein the dissolution effluent outlet of the plastic waste dissolution-dechlorination device is in communication with the inlet of the dechlorination-separation device, and the chlorine-removed plastic waste outlet of the dechlorination-separation device is in communication with the chlorine-removed plastic waste inlet of the plastic waste pretreatment device.

12. further comprising a first solvent recovery device having a chlorine-containing solution inlet, a plastic particle outlet, and a recovered first organic solvent outlet; 12. The system of claim 11, wherein the chlorine-containing solution outlet of the dechlorination-separation device is in communication with the chlorine-containing solution inlet of the first solvent recovery device.

13. The system of any one of claims 10 to 12, further comprising an extraction device, a pretreatment agent recovery device, and a second solvent recovery device; the extraction device comprises an insoluble material inlet, a second organic solvent inlet, a solid material outlet, and a liquid material outlet; the insoluble material outlet of the solid-liquid separation device is in communication with the insoluble material inlet of the extraction device; the pretreatment agent recovery device includes a solid material inlet and a circulating pretreatment agent outlet; the solid material outlet of the extraction device is in communication with the solid material inlet of the pretreatment agent recovery device; The circulating pretreatment agent discharge port of the pretreatment agent recovery device is connected to the pretreatment agent inlet of the plastic waste pretreatment device; The second solvent recovery device has a liquid material inlet, a solid plastic particle outlet, and a recovered second organic solvent outlet, and the liquid material outlet of the extraction device is in communication with the liquid material inlet of the second solvent recovery device.

14. A method for producing motor fuel from plastic waste, comprising the steps of: Step I) A step of obtaining an impurity-removed plastic-containing solution by pretreating plastic waste with the method according to any one of claims 1 to 9 or by using the plastic waste pretreatment system according to any one of claims 10 to 13; Step II) contacting the impurity-removed plastic-containing solution and any catalytic cracking feedstock with a catalytic cracking catalyst for reaction; and Step III) Separating the reaction product of step II) to obtain a gasoline fraction and / or a diesel fraction.

15. The catalytic cracking catalyst used in step II) comprises a zeolite, an inorganic oxide binder, and optionally a clay; Based on the total weight of the catalytic cracking catalyst, the zeolite is present in an amount of 5% to 50% by weight; the inorganic oxide is present in an amount of 5% to 90% by weight; the clay is present in an amount of 0% to 70% by weight; 15. The method of claim 14, wherein the zeolite is selected from the group consisting of rare earth-containing or rare earth-free Y or HY zeolites, rare earth-containing or rare earth-free ultrastable Y zeolites, zeolites with MFI structure, or combinations thereof.

16. The conditions for step II) are:

16. The method according to claim 14 or 15, comprising a reaction temperature of 460°C to 530°C, a reaction pressure of 0.1MPa to 0.4MPa, a catalyst to oil ratio of 5 to 10, and a reaction time of 2 seconds to 4 seconds.

17. A system for carrying out the method for producing motor fuel from plastic waste according to any one of claims 14 to 16, comprising the plastic waste pretreatment system according to any one of claims 10 to 13 and a catalytic cracking unit; The catalytic cracking apparatus comprises an impurity-removed plastic-containing solution inlet, an optional catalytic cracking feedstock inlet, and at least one outlet; The plastic waste pretreatment system has a solid-liquid separation device in which an outlet for the impurity-removed plastic-containing solution is connected to an inlet for the impurity-removed plastic-containing solution of the catalytic cracking device.

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