Process for processing waste plastics

Abstract

The present application relates to the technical field of waste plastic chemical conversion, and discloses a waste plastic processing technology, which comprises the following steps: (1) contacting waste plastic, solvent I and a decontaminating agent, and performing heat treatment to obtain a product, and then performing solid-liquid separation to obtain liquid-phase material and solid-phase material; wherein the waste plastic comprises mechanical impurities, PVC and PS, and further comprises at least one of PE and PP; the decontaminating agent comprises an adsorption component and an acid-removing component; (2) performing catalytic hydrogenation on the liquid-phase material to obtain catalytic hydrogenation tail oil; (3) contacting the solid-phase material with solvent II to perform extraction and obtain extraction liquid; (4) recycling the extraction liquid to obtain recycled solvent II and PS; wherein the recycled solvent II is recycled to the extraction process. The waste plastic processing technology provided by the present application has mild reaction conditions, can solve the corrosion problem of HCl, reduce the content of Si in the hydrogenation tail oil, is beneficial to improving the yield of the hydrogenation tail oil, and can obtain high-quality hydrogenation tail oil.

Description

Technical Field

[0001] This invention relates to the field of chemical conversion technology for waste plastics, and more specifically to a waste plastics processing technology. Background Technology

[0002] The plastics industry has made a significant contribution to social development. Currently, my country's annual plastic production has reached approximately 120 million tons, the vast majority of which is discarded after a single use. Statistics show that my country's waste plastic production is approximately 2.4-4.8 million tons per year, and by 2035, approximately 8 billion tons of waste plastic will exist in the natural environment globally. Since plastic takes 200-500 years to fully degrade, the continuous accumulation of waste plastic not only causes serious environmental pollution but also affects the ecological balance of the natural environment. On the other hand, my country's dependence on imported crude oil and petroleum has both exceeded 70%, and the large amount of waste plastic left in the natural environment represents a serious waste of petrochemical resources.

[0003] Existing waste plastic treatment technologies mainly include landfill and incineration. Landfill cannot fundamentally solve the problem. Currently, there are only about 400 waste-to-energy plants in China capable of processing waste plastics, and the rate of waste plastic incineration for power generation is far slower than the growth rate of waste plastics.

[0004] Chemical conversion of waste plastics is a process that can achieve sustainable development. Among them, pyrolysis has attracted the attention of researchers and enterprises around the world due to its environmental friendliness and high yield. At present, the main problems of waste plastic pyrolysis are as follows: 1) A large number of organic or inorganic additives are often added during the plastic production process to improve the performance of plastics; therefore, the composition of waste plastics is complex and contains a large number of heteroatoms, resulting in a high content of Cl and Si in the pyrolysis oil. Cl can easily cause equipment corrosion problems in the subsequent processing of waste plastic pyrolysis oil, while Si can easily cause complete deactivation of the catalyst in the refinery hydrogenation process; 2) Plastics are prone to adhering to a large number of impurities during disposal, resulting in a high content of mechanical impurities in waste plastics; 3) Waste plastics contain various types of plastics, and direct pyrolysis results in low yield and poor quality of pyrolysis oil. Summary of the Invention

[0005] The purpose of this invention is to address the shortcomings of high impurity content in pyrolysis oil and high catalyst cost in subsequent hydrogenation processes in waste plastic pyrolysis, and to provide a waste plastic processing technology.

[0006] To achieve the above objectives, the present invention provides a waste plastic processing technology, wherein the technology includes:

[0007] (1) Waste plastic, solvent I and impurity removal agent are brought into contact and subjected to heat treatment to obtain a product. After solid-liquid separation, liquid phase material and solid phase material are obtained. The waste plastic includes mechanical impurities, PVC and PS, and also includes at least one of PE and PP. The impurity removal agent includes an adsorption component and an acid removal component.

[0008] (2) The liquid phase material is subjected to catalytic hydrogenation to obtain catalytically hydrogenated tail oil;

[0009] (3) The solid material is contacted with solvent II for extraction to obtain an extract;

[0010] (4) The extract is recovered to obtain recovered solvent II and PS; wherein the recovered solvent II is recycled back to the extract.

[0011] The beneficial technical effects achieved by the present invention through the above technical solution are as follows:

[0012] 1) The present invention provides a waste plastic processing technology that uses solvent I and impurity remover to remove HCl and high molecular weight organic Si, thereby reducing the content of impurities in hydrogenated tail oil;

[0013] 2) The waste plastic processing technology provided by the present invention uses heat treatment to remove mechanical impurities, which can greatly reduce water consumption compared with conventional water washing to remove impurities;

[0014] 3) The waste plastic processing technology provided by this invention utilizes solvent I to remove PS, which can reduce hydrogen consumption in the catalytic hydrogenation process and help reduce costs;

[0015] 4) The waste plastic processing technology provided by this invention has mild process conditions, is easy to couple with refinery processes, will not have a negative impact on existing refinery equipment, has a high yield of hydrogenated tail oil, and is suitable for industrial promotion. Attached Figure Description

[0016] Figure 1 This is a flow chart of a preferred embodiment of the waste plastic processing technology provided in this invention. Detailed Implementation

[0017] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0018] This invention provides a waste plastic processing technology, the process comprising:

[0019] (1) Waste plastic, solvent I and impurity removal agent are brought into contact and subjected to heat treatment to obtain a product. After solid-liquid separation, liquid phase material and solid phase material are obtained. The waste plastic includes mechanical impurities, PVC and PS, and also includes at least one of PE and PP. The impurity removal agent includes an adsorption component and an acid removal component.

[0020] (2) The liquid phase material is subjected to catalytic hydrogenation to obtain catalytically hydrogenated tail oil;

[0021] (3) The solid material is contacted with solvent II for extraction to obtain an extract;

[0022] (4) The extract is recovered to obtain recovered solvent II and PS; wherein the recovered solvent II is recycled back to the extract.

[0023] In step (1):

[0024] In this invention, during the heat treatment of waste plastics, solvent I, and the impurity remover, PE and PP can dissolve in solvent I, but PS agglomerates and cannot dissolve in solvent I. PVC undergoes pyrolysis, releasing HCl and generating semi-coke and a small amount of pyrolysis products soluble in solvent I. The adsorption component in the impurity remover can adsorb impurities such as high-molecular-weight organosilicon dissolved in solvent I, and the deacidifying component in the impurity remover can neutralize the generated HCl, thereby achieving the removal of HCl and Si, and separating PS and mechanical impurities to improve the quality of the hydrotreated tail oil.

[0025] In one embodiment of the present invention, the source of waste plastics is not specifically limited, and waste plastics from daily life, aged garbage or industrial and agricultural production can be used in the present invention.

[0026] In one embodiment of the present invention, the waste plastic is pretreated before being brought into contact with solvent I and the impurity removal agent; wherein, the pretreatment includes drying, wastewater treatment and crushing.

[0027] In one embodiment of the present invention, the drying operating conditions include: a drying temperature of 90-150°C, preferably 100-120°C; and a drying time of 0.1-4 hours, preferably 0.5-1 hour.

[0028] In this invention, the drying process is used to dehydrate waste plastics, thereby improving the dissolution efficiency of waste plastics in solvent I during the pyrolysis reaction and reducing the operating pressure of the heat treatment process. This invention does not impose any particular limitation on the drying method; any drying method that can remove water from the waste plastics can be used. For example, the drying method in this invention can be either single-stage drying or multi-stage drying; the heating method for the drying temperature can be electric heating, flue gas heating, or steam heating; and the heat exchange method can be direct contact heat exchange drying or indirect contact heat exchange drying.

[0029] In one embodiment of the present invention, the wastewater separated from the drying process is subjected to the wastewater treatment, which is used to purify the wastewater. The purified water meets the discharge standards and can be directly discharged or recycled.

[0030] The wastewater treatment methods in this invention are selected from one or more of the following: oxidation ditch process, A2 / O process (anaerobic-anoxic-aerobic biological nitrogen and phosphorus removal process), A / O process (anoxic-aerobic biological nitrogen and phosphorus removal process), traditional activated sludge process, biofilm process, SBR process (intermittent activated sludge process), continuous circulation aeration technology, SPR high turbidity wastewater treatment technology, and BIOLAK wastewater treatment technology. To improve wastewater treatment efficiency, different wastewater treatment methods can be combined. The specific implementation of the wastewater treatment in this invention can preferably utilize existing refinery wastewater treatment systems, or it can be adjusted according to actual needs.

[0031] In one embodiment of the present invention, the dried waste plastic is crushed, and the particle size of the crushed waste plastic is 1-200 mm, preferably 1-50 mm. Crushing the waste plastic can further accelerate the heat treatment speed during heat treatment.

[0032] In this invention, the crushing is carried out in a crushing device, which is selected from one or more of compression, impact, grinding, and shearing crushing devices. To improve the crushing effect, different crushing devices can be selected to perform crushing together, or the crushing operation can be repeated until the particle size is between 1-200mm.

[0033] In one embodiment of the present invention, the solvent I is selected from one or more of VGO (reduced pressure diesel), hydrotreated CGO (coking wax oil), LCO (catalytic cracking light cycle oil), or hydrotreated LCO.

[0034] This invention does not specifically limit the types of vacuum diesel, hydrotreated coking wax oil, catalytic cracking light cycle oil, and hydrotreated catalytic cracking light cycle oil. Conventional vacuum diesel, hydrotreated coking wax oil, catalytic cracking light cycle oil, and hydrotreated catalytic cracking light cycle oil can all be used in this invention.

[0035] In one embodiment of the present invention, the mass ratio of solvent I to waste plastic is 0.1-10:1, preferably 5-10:1.

[0036] In one embodiment of the present invention, the adsorption component is selected from one or more of ZSM-5, Y-type molecular sieve, natural molecular sieve, and red mud, preferably ZSM-5 molecular sieve, wherein the molar ratio of silica to alumina in the ZSM-5 molecular sieve is preferably 20-50:1; the present invention does not specifically limit the source of ZSM-5 molecular sieve, which can be commercially purchased ZSM-5 molecular sieve or waste catalyst prepared using ZSM-5 molecular sieve as a carrier, such as waste FCC catalyst balancer. The acid removal component is selected from one or more of ferric oxide, magnesium oxide, calcium oxide, strontium oxide, and barium oxide, preferably calcium oxide.

[0037] In one embodiment of the present invention, the mass ratio of the adsorption component to the waste plastic is 1:1-40, preferably 1:10-20; the mass ratio of the acid removal component to the waste plastic is 1:1-40, preferably 1:10-20.

[0038] In one embodiment of the present invention, the operating conditions of the heat treatment include: a heat treatment temperature of 180-400℃, preferably 300-360℃; a heat treatment pressure of 0.1-3MPa, preferably 0.5-1MPa; a stirring rate of 30-300r / min, preferably 60-100r / min; and a heat treatment time of 10-60min, preferably 20-30min.

[0039] In one embodiment of the present invention, the heat treatment is carried out in a kettle-type melting device. The present invention does not impose any particular limitation on the kettle-type melting device, and it can be selected according to actual conditions. The present invention also does not impose any particular requirement on the number of kettle-type melting devices; it can be one or more, and multiple kettle-type melting devices can be connected in series or in parallel. The effective volume of the kettle-type melting device is preferably 0.1-100 m³. 3 .

[0040] In this invention, the kettle-type dissolving apparatus is equipped with a waste plastic inlet, a solvent I inlet, a fresh purifying agent inlet, a discharge port, a stirring device, and a heating device. The waste plastic inlet is connected to a waste plastic storage tank, the solvent I inlet is connected to a solvent I storage tank, and the fresh purifying agent inlet is connected to a purifying agent storage tank. The material outlet is located at the bottom of the kettle-type dissolving apparatus. The stirring device is located inside the kettle-type dissolving apparatus and can be electrically driven or magnetically driven. The stirring paddle is selected from one of the following: paddle type, anchor type, frame type, or screw type stirring paddle. The heating device can be located inside the kettle-type dissolving apparatus, for example, it can be a built-in steam-heated coil; or it can be located outside the kettle-type dissolving apparatus, for example, it can be a heating jacket with an electric heat source or a semi-circular coil with a steam heat source.

[0041] In one embodiment of the present invention, the operating conditions for solid-liquid separation include: a separation temperature of 150-250°C, preferably 160-210°C.

[0042] The solid-liquid separation is carried out in a separation device, which is selected from a filter and / or a centrifuge. When the separation device is a filter, the filter screen pore size is less than 1 mm, preferably 1-10 μm; the filtration pressure is 0.1-1.5 MPa, preferably 0.5-1 MPa.

[0043] In a preferred embodiment, the separation device is a filter and / or centrifuge with automatic slag discharge function. In a further preferred embodiment, the separation device is a filter and / or centrifuge with a heating device and / or a heat preservation device. The heating device can be externally heated or internally heated; externally heated devices are selected from jacketed or semi-circular coil types, while internally heated devices are selected from coil types. The heat source for the heating device can be one of electricity, thermal oil, steam, or open flame.

[0044] In step (2):

[0045] In one embodiment of the present invention, the catalytic hydrogenation catalyst in the catalytic hydrogenation comprises 10-40 parts by weight, preferably 15-35 parts by weight, of an active component and 60-90 parts by weight, preferably 65-85 parts by weight, of a support.

[0046] The active component is selected from one or more of W, Mo, Zn, Cr, Fe, Co, Ni, Pt, Pd, and Cu; preferably selected from one or more of Fe, Mo, Co, Ni, and Cu; the support is selected from at least one of alumina, silicon dioxide, magnesium aluminum hydrotalcite, and activated carbon, preferably alumina.

[0047] The catalyst used in this invention can be a commercially available product, such as an industrial RL-1 catalyst, a DHC-type catalyst, an HC-type catalyst, or an ICR series catalyst. Alternatively, it can be prepared using conventional methods in the field of catalysts; the specific preparation methods will not be detailed here.

[0048] In one embodiment of the present invention, the conditions for catalytic hydrogenation include: a catalytic hydrogenation temperature of 300-450°C, preferably 340-420°C; a catalytic hydrogenation pressure of 5-20 MPa, preferably 6-15 MPa; and a volume hourly space velocity (VHSV) of 0.5-2 h⁻¹ for the liquid phase material. -1 Preferably 1-1.5h -1 The hydrogen-to-oil volume ratio is 100-2000:1, preferably 500-1000:1.

[0049] In one embodiment of the present invention, the reactor for hydrogenation catalysis is selected from at least one of a fixed-bed reactor, a moving-bed reactor, and a fluidized-bed reactor, wherein the fluidized-bed reactor may be a riser.

[0050] The processing methods after catalytic hydrotreating can be carried out according to conventional practices in the field, and will not be described in detail here. The catalytic hydrotreating tail oil obtained after catalytic hydrotreating can be stored in a catalytic hydrotreating tail oil storage tank.

[0051] In one embodiment of the present invention, the liquid material is transported to the catalytic hydrogenation at a temperature of 150-360°C, preferably 160-180°C.

[0052] In one embodiment of the present invention, the conveying equipment for conveying liquid phase materials is selected from one or more of plunger pumps, rotor pumps, single screw pumps, twin screw pumps, and gear pumps. Multiple conveying equipment can be configured, and multiple fluid conveying equipment can be connected in parallel or in series.

[0053] In one embodiment of the present invention, the yield of the catalytic hydrotreating tail oil is 50-65%, preferably 57-62%.

[0054] In this invention, liquid-phase materials undergo catalytic hydrogenation to obtain catalytic hydrogenation tail oil, with unconverted oil and hydrogenated gas mixture remaining. This invention utilizes solvent I to first dissolve waste plastics before catalytically hydrogenating them, which not only increases the yield of catalytic hydrogenation tail oil but also reduces the Cl and Si content in the tail oil, resulting in high-quality catalytic hydrogenation tail oil.

[0055] In step (3):

[0056] In one embodiment of the present invention, solvent II is selected from one or more of benzene, toluene, chloroform, cyclohexanone, ethyl acetate, butyl acetate, carbon disulfide, tetrahydrofuran, and gasoline, preferably one or more of cyclohexanone, ethyl acetate, butyl acetate, and gasoline. In this invention, solvent II is used to dissolve PS, separating PS from the solid phase material.

[0057] In one embodiment of the present invention, the ratio of the solid material to solvent II is 1-1000g:1L, preferably 50-200g:1L.

[0058] In one embodiment of the present invention, the extraction operating conditions include: the extraction temperature is 30-60°C lower than the boiling point of solvent II at normal pressure, preferably 40-50°C lower; and the extraction time is 0.1-3h, preferably 0.5-1.5h.

[0059] In one embodiment of the invention, the extraction is carried out in a solvent extraction tower or a static mixing extractor.

[0060] In one embodiment of the present invention, the solid material is contacted with solvent II for extraction to obtain an extracted solid phase. The extracted solid phase mainly comprises a purifying agent used for impurity removal, mechanical impurities, and semi-coke. Preferably, the mechanical impurities can be separated from the extracted solid phase, and the remaining portion can be returned to heat treatment as a purifying agent; alternatively, the extracted solid phase can be sent to an off-site facility for waste disposal.

[0061] In step (4):

[0062] In one embodiment of the present invention, the recovery method is selected from distillation and / or flash evaporation. The present invention does not impose specific limitations on the specific operating conditions for recovery, which can be selected according to the solvent II actually used.

[0063] The present invention will be described in detail below through embodiments.

[0064] The chlorine content was determined by coulometric method. The specific method can be referred to the standard method of RIPP 64-90 (see "Analytical Methods for Petrochemical Products" (RIPP Test Methods), edited by Yang Cuiding et al., Science Press, 1990, pp. 164-167, "Determination of Total Chlorine Content in Crude Oil by Coulometric Method").

[0065] The silicon content was determined using the method described in GB17476-1998, "Determination of Additive Elements, Wear Metals and Contaminants in Used Lubricating Oils and Certain Elements in Base Oils (Inductively Coupled Plasma Spectrometry)".

[0066] Mechanical impurities and moisture content in waste plastics were determined using the "Industrial Analysis Methods for Coal" (GB212-91).

[0067] The mass content of different plastic components in waste plastics was measured using the flotation method based on the density of different plastics. Ten samples were randomly selected, and the average value was taken as the test result. The densities of PP and PE were 0.85-1 g / ml; PS density was 1-1.15 g / ml; and PVC density was >1.35 g / ml. In this invention, PP and PE have similar densities and similar pyrolysis effects, so there is no need to distinguish between PP and PE.

[0068] Example 1

[0069] The process flow in Example 1 is as follows: Figure 1 As shown:

[0070] (1) Waste plastics (PVC: 2wt%, PS: 2wt%, PE+PP: 74wt%, mechanical impurities: 12wt%, moisture: 10wt%) excavated and sorted from the landfill are fed into an intermittent heat exchange dryer via a conveyor belt and dried at 105℃ for 0.5h; the wastewater discharged from the intermittent heat exchange dryer is condensed and sent to the wastewater treatment system for treatment using continuous circulation aeration technology, and is directly discharged after meeting the standards; the dried waste plastics are sent to a shear crusher via a conveyor belt, and the particle size of the crushed waste plastics is 1-50mm;

[0071] Crushed waste plastics are fed into an externally heated autoclave via a screw feeder. Iranian VGO (purchased from Sinopec Shijiazhuang Refinery) and a filtration agent (ZSM-5 molecular sieve with a silica-alumina molar ratio of 40 and calcium oxide) are fed into the autoclave via a metering pump. The waste plastics, Iranian VGO, and filtration agent are in contact within the autoclave for heat treatment. The mass ratio of waste plastics to Iranian VGO is 1:7, the mass ratio of ZSM-5 to waste plastics is 1:15, and the mass ratio of calcium oxide to waste plastics is 1:15. The heat treatment temperature is 350℃, the heat treatment pressure is 0.5MPa, the agitator speed is 60r / min, and the heat treatment time is 30min. After heat treatment, the material in the autoclave is discharged through the bottom outlet to a high-temperature filter, where it is filtered at 180℃ to obtain liquid and solid phase materials.

[0072] (2) The obtained liquid material is pumped to a catalytic hydrogenation fixed-bed reactor at a conveying temperature of 180°C using a screw pump, and then contacted with the industrial RL-1 catalyst for catalytic hydrogenation. The catalytic hydrogenation conditions are: catalytic hydrogenation temperature of 370°C, catalytic hydrogenation pressure of 8 MPa, and liquid material space velocity of 1.0 h⁻¹. -1The hydrogen-to-oil volume ratio was 1000:1, and catalytic hydrotreating tail oil was obtained. The impurity content of the catalytic hydrotreating tail oil was analyzed, and the results are shown in Table 1.

[0073] (3) The above solid material is contacted with solvent II cyclohexanone in a solvent extraction tower and extracted at 145°C for 1 hour to obtain an extract and an extracted solid phase; wherein, the ratio of solid material to solvent II cyclohexanone is 100g:1L and the extracted solid phase is sent to the outside for waste solid treatment.

[0074] (4) The above extract is flash evaporated to obtain recovered solvent II cyclohexanone and PS; wherein the recovered solvent II is recycled back to the extract.

[0075] Example 2

[0076] Same as Example 1, except that the waste plastics are different and the amount of acid removal component is different.

[0077] Example 2: The waste plastic contained PVC: 3wt%, PS: 3wt%, PE+PP: 70wt%, mechanical impurities: 7wt%, moisture: 17wt%, and the mass ratio of calcium oxide to waste plastic was 1:20.

[0078] The impurity content of the obtained catalytic hydrotreating tail oil was analyzed, and the results are shown in Table 1.

[0079] Comparative Example 1

[0080] Using Iranian VGO as feedstock, catalytic hydrotreating was performed under the same conditions as in Example 1. The impurity content of the resulting catalytic hydrotreating tail oil was analyzed, and the results are shown in Table 1.

[0081] Comparative Example 2

[0082] Waste plastic (same as in Example 1 and in the same amount) was placed in a reactor and pyrolyzed at 500°C for 50 min. The impurity content of the obtained pyrolysis oil was analyzed, and the results are shown in Table 1.

[0083] Table 1

[0084]

[0085] *: The yields of catalytic hydrotreating tail oil in Examples 1 and 2 are calculated based on the amount of waste plastics added, excluding the added solvent I. The hydrotreating tail oil yields of the solvent in Examples 1 and 2 are calculated with reference to Comparative Example 1.

[0086] As shown in Table 1, the content of impurities such as Cl, Si, S, and N in the catalytic hydrogenation tail oil produced by the waste plastic processing technology provided in this invention is significantly reduced, resulting in high yield and high quality hydrogenation tail oil.

[0087] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A waste plastic processing technology, characterized in that, The process includes: (1) Waste plastic, solvent I and impurity removal agent are contacted and heat-treated to obtain a product. After solid-liquid separation, liquid phase material and solid phase material are obtained. The waste plastic includes mechanical impurities, PVC and PS, and also includes at least one of PE and PP. The impurity removal agent includes an adsorption component and an acid removal component. (2) The liquid phase material is subjected to catalytic hydrogenation to obtain catalytically hydrogenated tail oil; (3) The solid material is contacted with solvent II for extraction to obtain an extract; (4) The extract is recovered to obtain recovered solvent II and PS; wherein the recovered solvent II is recycled back to the extract; The adsorption component is selected from one or more of ZSM-5, Y-type molecular sieve, natural molecular sieve, and red mud, and the acid removal component is selected from one or more of ferric oxide, magnesium oxide, calcium oxide, strontium oxide, and barium oxide. The operating conditions for the heat treatment include a heat treatment temperature of 300-400℃.

2. The processing technology according to claim 1, wherein, Before contacting the waste plastics with solvent I and the impurity removal agent, the waste plastics are pretreated; wherein, the pretreatment includes drying, wastewater treatment and crushing.

3. The processing technology according to claim 2, wherein, The drying operating conditions include: a drying temperature of 90-150℃ and a drying time of 0.1-4h.

4. The processing technology according to claim 3, wherein, The drying operating conditions include: a drying temperature of 100-120℃ and a drying time of 0.5-1h.

5. The processing technology according to claim 2, wherein, The wastewater treatment method in the wastewater treatment process is selected from one or more of the following: oxidation ditch process, A2 / O process, A / O process, traditional activated sludge process, biofilm process, SBR process, continuous circulation aeration technology, SPR high turbidity wastewater treatment technology, and BIOLAK wastewater treatment technology.

6. The processing technology according to claim 2, wherein, The particle size of the crushed waste plastic is 1-200mm.

7. The processing technology according to claim 6, wherein, The particle size of the crushed waste plastic is 1-50mm.

8. The processing method according to any one of claims 1-7, wherein, Solvent I is selected from one or more of vacuum diesel, hydrotreated coking wax oil, catalytic cracking light cycle oil, or hydrotreated catalytic cracking light cycle oil.

9. The processing method according to any one of claims 1-7, wherein, The mass ratio of solvent I to waste plastic is 0.1-10:

1.

10. The processing technology according to claim 9, wherein, The mass ratio of solvent I to waste plastic is 5-10:

1.

11. The processing method according to any one of claims 1-7, wherein, The mass ratio of the adsorption component to the waste plastic is 1:1-40; the mass ratio of the acid removal component to the waste plastic is 1:1-40.

12. The processing technology according to claim 11, wherein, The mass ratio of the adsorption component to the waste plastic is 1:10-20; the mass ratio of the acid removal component to the waste plastic is 1:10-20.

13. The processing method according to any one of claims 1-7, wherein, In step (1), the operating conditions for the heat treatment include: heat treatment temperature of 300-360℃; heat treatment pressure of 0.1-3MPa; stirring rate of 30-300r / min; and treatment time of 10-60min.

14. The processing technology according to claim 13, wherein, The heat treatment pressure is 0.5-1 MPa; the stirring rate is 60-100 r / min; and the treatment time is 20-30 min.

15. The processing method according to any one of claims 1-7, wherein, In step (2), the catalytic hydrogenation catalyst in the catalytic hydrogenation comprises 10-40 parts by weight of active component and 60-90 parts by weight of support; The active component is selected from one or more of W, Mo, Zn, Cr, Fe, Co, Ni, Pt, Pd, and Cu; the support is selected from at least one of alumina, silicon dioxide, magnesium aluminum hydrotalcite, and activated carbon.

16. The processing method according to claim 15, wherein, In step (2), the catalytic hydrogenation catalyst in the catalytic hydrogenation comprises 15-35 parts by weight of active component and 65-85 parts by weight of support; The active component is selected from one or more of Fe, Mo, Co, Ni, and Cu; the support is alumina.

17. The processing method according to any one of claims 1-7, wherein, In step (2), the conditions for catalytic hydrogenation include: a catalytic hydrogenation temperature of 300-450℃; a catalytic hydrogenation pressure of 5-20 MPa; and a volume hourly space velocity (VHSV) of 0.5-2 h⁻¹ for the liquid phase material. -1 The hydrogen-to-oil volume ratio is 100-2000:

1.

18. The processing method according to claim 17, wherein, In step (2), the conditions for catalytic hydrogenation include: a catalytic hydrogenation temperature of 340-420℃; a catalytic hydrogenation pressure of 6-15 MPa; and a volume hourly space velocity (VHSV) of 1-1.5 h⁻¹ for the liquid phase material. -1 The hydrogen-to-oil volume ratio is 500-1000:

1.

19. The processing method according to any one of claims 1-7, wherein, In step (3), solvent II is selected from one or more of benzene, toluene, chloroform, cyclohexanone, ethyl acetate, butyl acetate, carbon disulfide, tetrahydrofuran, and gasoline.

20. The processing technology according to claim 19, wherein, Solvent II is one or more of cyclohexanone, ethyl acetate, butyl acetate, and gasoline.

21. The processing method according to any one of claims 1-7, wherein, The ratio of the solid material to solvent II is 1-1000g:1L.

22. The processing technology according to claim 21, wherein, The ratio of the solid material to solvent II is 50-200 g: 1 L.

23. The processing method according to any one of claims 1-7, wherein, In step (3), the extraction conditions include: the extraction temperature is 30-60°C lower than the boiling point of solvent II at normal pressure; and the extraction time is 0.1-3h.

24. The processing technology according to claim 23, wherein, In step (3), the extraction conditions include: the extraction temperature is 10-20°C lower than the boiling point of solvent II at normal pressure; and the extraction time is 0.5-1.5h.

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