Method and system for processing chlorine-containing waste plastics by multiphase flow hydrocracking unit

Abstract

The invention discloses a method and a system for processing chlorine-containing waste plastics by a multiphase flow hydrocracking device. The method comprises the following steps: S1, preparing the chlorine-containing waste plastics, a dechlorinating agent, a solid catalyst and heavy oil in a raw material tank to form uniform mixed slurry; s2, the mixed slurry is pumped to a multiphase flow hydrocracking reactor through a high-pressure feeding pump, chlorine elements in the plastic react with a dechlorinating agent to generate chlorate under the high-temperature hydrogen condition, and the chlorate is adsorbed on the surface of a catalyst and enters a thermal high-pressure separator together with a reaction product; s3, separating the reaction product by a thermal high-pressure separator to obtain light distillate oil and solid-containing heavy distillate oil; s4, the solid-containing heavy distillate oil passes through a vacuum tower and a hot melting extraction device, vacuum wax oil, vacuum residual oil and a solid waste catalyst are obtained, and the vacuum residual oil can be returned to a raw material tank to be used as a raw material. According to the method, deep removal of chlorine in the chlorine-containing waste plastic is realized, and meanwhile, through synergistic conversion of various substances, the reaction severity is reduced, the resource utilization efficiency is improved, and a high-added-value product is obtained.

Description

Technical Field

[0001] The invention relates to the technical field of waste plastic resource recycling, and in particular to a method and system for processing chlorine-containing waste plastics in a multiphase flow hydrocracking device. Background Art

[0002] High-value utilization of waste plastics is one of the effective ways to reduce environmental pollution and improve resource utilization efficiency. Chemical fuel recovery is regarded as an "upgraded" method of waste plastic utilization that can achieve closed-loop recycling, mainly through thermal cracking, thermal cracking, catalytic cracking, catalytic cracking and other technologies to achieve waste plastic conversion.

[0003] In the prior art, CN10461030B discloses a coking method for producing fuel oil from waste plastics, in which high aromatic components and waste plastics or plastic oil are preheated in a raw material buffer tank, then heated in a tubular heating furnace, and then sprayed into a delayed coking tower for coking reaction. The waste plastics mentioned in the patent are one or more of polyethylene, polypropylene and polystyrene, and do not contain polyvinyl chloride, so it is impossible to process waste plastic raw materials mixed with polyvinyl chloride.

[0004] CN108410490B discloses a pyrolysis treatment process and system for chlorine-containing waste plastics, which is subjected to low-temperature pyrolysis treatment of chlorine-containing waste plastics to generate a mixed gas consisting of tar, hydrogen chloride and combustible gas. The mixed gas after tar is removed by tar reforming reacts with a dechlorinating agent to remove hydrogen chloride in the mixed gas. This patent converts chlorine-containing waste plastics into hydrogen chloride by low-temperature pyrolysis treatment, and then removes hydrogen chloride in the mixed gas by tar reforming and reacting with a dechlorinating agent. There is a problem of equipment corrosion in the whole process.

[0005] In summary, when the existing waste plastic pyrolysis process technology is used to treat high-chlorine-containing waste plastics, there are problems such as the inability to process chlorine-containing waste plastics, difficulty in removing chlorine pollutants, poor quality of liquid products, and severe equipment corrosion. Summary of the invention

[0006] In order to overcome the deficiencies of the above-mentioned prior art, the purpose of the present invention is to provide a method and system for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit, which can not only achieve the deep removal of chlorine in chlorine-containing waste plastics, but also avoid equipment corrosion and environmental pollution problems caused by the processing of chlorine-containing waste plastics from the source, but also reduce the severity of the reaction through the synergistic conversion of multiple substances, obtain higher quality liquid products, improve resource utilization efficiency, and obtain high value-added products.

[0007] In order to achieve the above object, the technical solution adopted by the present invention is:

[0008] A method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit comprises the following steps:

[0009] S1: preparing chlorine-containing waste plastics, dechlorination agent, solid catalyst and heavy oil in a raw material tank 5 to form a uniform mixed slurry;

[0010] S2: The mixed slurry is pumped to the multiphase flow hydrocracking reactor 10 by the high-pressure feed pump 7. Under high-temperature hydrogen conditions, the chlorine element in the plastic reacts with the dechlorinating agent to generate chloride salt, which is adsorbed on the catalyst surface and enters the hot high-pressure separator 11 together with the reaction products;

[0011] S3: The reaction product is separated by a hot high-pressure separator 11 to obtain a light distillate oil and a solid-containing heavy distillate oil;

[0012] S4: The solid-containing heavy distillate oil passes through a vacuum tower 16 and a hot-melt extraction device 18 to obtain vacuum wax oil, vacuum residue oil and solid waste catalyst respectively. The vacuum residue oil can be returned to the raw material tank for use as a raw material.

[0013] The chlorine-containing waste plastics described in S1 are mixed plastics containing PVC, and the mixed plastics are one or more of PP, PE, PS, and PET.

[0014] The chlorine-containing waste plastics described in S1 are in granular form, with a maximum particle size not exceeding 150 μm, and the addition amount is 0-50% based on the mass fraction of the total feed amount;

[0015] The chlorine-containing waste plastics described in S1 are calculated based on the total feed mass fraction, and the proportion of PVC shall not exceed 10%.

[0016] The dechlorinating agent in S1 is in powder form and is one or more of sodium sulfide, sodium thiosulfate, sodium carbonate, sodium bicarbonate, calcium oxide, and calcium carbonate;

[0017] The dechlorinating agent in S1 is calculated based on the total feed mass fraction, and the added amount is 0-5%.

[0018] The solid catalyst active group described in S1 comprises one or more of iron oxide hydroxide, nickel oxide, cobalt oxide, tungsten oxide and molybdenum oxide. The carrier is a porous carbon-based material, and the porous carbon-based material is activated carbon, coal powder and coke. The catalyst is calculated based on the total feed mass fraction, and the addition amount is 0.5-2.0%.

[0019] The solid catalyst is calculated by weight, and the iron oxyhydroxide is 15-49%, and the nickel oxide, cobalt oxide, molybdenum oxide or tungsten oxide is 1-20% (the active component can load a variety of metal active components, and the content range of each active component is given here), and the catalyst bulk density is 0.6-0.8g / cm 3 , average particle size 65-75μm, specific surface area 400-600m 2 / g.

[0020] The heavy oil in S1 is one or more of atmospheric residue oil, vacuum residue oil, coal tar, catalytic oil slurry, steam cracking tar or other secondary processed distillate oil, or is oil-coal slurry containing coal powder.

[0021] The ratio of the chlorine-containing waste plastic, the dechlorinating agent, the solid catalyst and the heavy oil in S1 is (0-50):(0-5):(0.5-2.0):(50-100).

[0022] The reaction conditions of the multiphase flow hydrocracking reactor in S2 are: reaction temperature 370-470°C, reaction pressure 4-15MPa, liquid space velocity 0.3-2.0h -1 , hydrogen-oil ratio 800-1500NL / kg. Waste plastics, heavy oil or coal powder and other materials react in the multiphase flow hydrocracking reactor, and the setting conditions are to ensure that both waste plastics and heavy oil can be converted.

[0023] The multiphase flow hydrogenation reactor in S2 is composed of 1 to 3 reactors in a series or parallel combination mode, and the reactor type is one or a combination of suspended bed, boiling bed, and bubbling bed.

[0024] The reaction product in S3 is separated by a hot high fraction separator to obtain a light distillate oil and a solid-containing heavy distillate oil, wherein the final distillation point of the light distillate oil is not higher than 450°C.

[0025] The solid-containing heavy fraction oil in S4 is subjected to vacuum distillation in a vacuum tower to obtain vacuum wax oil and solid-containing oil residue, wherein the vacuum wax oil can be used as a catalytic cracking or hydrocracking raw material; the distillation range is 350-500°C.

[0026] The solid oil residue in S4 is separated by a hot-melt extraction device to obtain vacuum residue oil and solid waste catalyst. The vacuum residue oil is used in whole or in part as circulating oil, and the waste catalyst adsorbed with chloride salt and coke is treated as solid waste or recycled for secondary utilization.

[0027] The extraction solvent of the hot melt extraction device in S4 is one or a mixture of several hydrocarbons such as n-heptane, benzene, toluene and xylene, also known as coal liquefaction light oil.

[0028] The control process parameters of the hot extraction separation device in S4 are pressure 0.1-0.5MPa, extraction temperature 90-150°C, agent-oil ratio (1-20):1, and extraction time 0.5-2 hours.

[0029] A system for processing chlorine-containing waste plastics by a multiphase flow hydrocracking device, comprising a raw material tank 5, the input end of which is respectively connected to the input ends of a pipeline for conveying chlorine-containing waste plastics 1, a dechlorinating agent 2, a solid catalyst 3 and a heavy oil 4, and the chlorine-containing waste plastics 1, the dechlorinating agent 2, the solid catalyst 3 and the heavy oil 4 are prepared in the raw material tank 5 to form a uniform mixed slurry;

[0030] The mixed slurry output end enters the mixer 8 through the high-pressure feed pump 7 to mix with the hydrogen 6, and after being preheated by the heating furnace 9, enters the multiphase flow hydrocracking reactor 10;

[0031] The output end of the multiphase flow hydrocracking reactor 10 is connected to a hot high-pressure separator 11, and the gaseous phase product of the hot high-pressure separator 11 enters a hot low-pressure separator 12, and the gaseous hydrocarbons obtained by separation enter a circulating hydrogen compressor 13, and the liquid light distillate oil 14 exits the device. The solid-containing heavy distillate oil enters a vacuum tower 16 and a hot melt extraction device 18 after being cooled and reduced in pressure by a vacuum valve 15, and vacuum wax oil 17, vacuum residue oil 19 and solid waste catalyst 20 are obtained respectively. The vacuum residue oil 19 is returned to the raw material tank for use as a raw material, and the solid waste catalyst exits the device for solid waste treatment or secondary processing.

[0032] Beneficial effects of the present invention:

[0033] 1. The method provided by the present invention can not only promote the reaction between elemental chlorine and the dechlorinating agent through the multiphase flow hydrocracking reaction to achieve the purpose of deep dechlorination, but also can play a role in hydrogenation and modification of waste plastic liquid hydrocarbons to obtain high value-added chemical raw materials or chemicals.

[0034] 2. The method provided by the present invention makes full use of the metal active components loaded on the surface of the solid catalyst, which can not only promote the removal of elemental chlorine in waste plastics, but also the unique large specific surface area can adsorb particles such as chloride salts, coking precursors, and impurity elements formed during the reaction on the catalyst surface and carry them out of the reaction system, effectively avoiding equipment corrosion and blockage problems.

[0035] 3. The method provided by the present invention makes full use of the synergistic and complementary effect between waste plastics and heavy oil to achieve the synergistic transformation of the two materials. It not only provides a new technical path for the high-value utilization of waste plastics and reduces the environmental pollution of waste plastics, but also can reduce the severity of the reaction and improve the efficiency of resource utilization. BRIEF DESCRIPTION OF THE DRAWINGS

[0036] Figure 1 The present invention provides a schematic diagram of a process flow for processing chlorine-containing waste plastics using a multiphase flow hydrocracking unit.

[0037] 1- chlorine-containing waste plastics; 2- dechlorinating agent; 3- solid catalyst; 4- heavy oil; 5- raw material tank; 6- hydrogen; 7- high-pressure feed pump; 8- mixer; 9- heating furnace; 10- multiphase flow hydrocracking reactor; 11- hot high-pressure separator; 12- hot low-pressure separation tank; 13- circulating hydrogen compressor; 14- light distillate oil; 15- pressure reducing valve; 16- pressure reducing tower; 17- pressure reducing wax oil; 18- hot melt extraction device; 19- pressure reducing residue oil; 20- solid waste catalyst. DETAILED DESCRIPTION

[0038] The present invention will be further described below in conjunction with embodiments:

[0039] The present invention discloses a method for treating chlorine-containing waste plastics by multiphase flow hydrocracking. Figure 1 As shown, chlorine-containing waste plastic 1, dechlorinating agent 2, solid catalyst 3 and heavy oil 4 are prepared in a raw material tank 5 to form a uniform mixed slurry. The mixed slurry is mixed with hydrogen 6 in a mixer 8 through a high-pressure feed pump 7. After being preheated by a heating furnace 9, it enters a multiphase flow hydrocracking reactor 10. Under the conditions of a reaction temperature of 380-450°C, a reaction pressure of 8-15MPa, and a hydrogen-to-oil ratio of 800-1200NL / kg (the reaction involves multiple substances such as waste plastics, heavy oil or coal powder. The reaction is carried out in a multiphase flow hydrocracking reactor. The setting condition is to ensure that both waste plastics and heavy oil can be converted.), the chlorine element in the plastic reacts with the dechlorinating agent to generate chlorine The salt is adsorbed on the catalyst surface and enters the hot high-pressure separator 11 together with the reaction products. The reaction products are separated by the hot high-pressure separator 11 to obtain gaseous products and heavy distillate oil containing solids. The gaseous products enter the hot low-pressure separator 12, and the gaseous hydrocarbons are separated and enter the circulating hydrogen compressor 13. The liquid light distillate oil 14 exits the device. The heavy distillate oil containing solids enters the vacuum tower 16 and the hot melt extraction device 18 after being cooled and reduced in pressure by the vacuum valve 15 to obtain vacuum wax oil 17, vacuum residue oil 19 and solid waste catalyst 20 respectively. The vacuum residue oil 19 can be returned to the raw material tank for use as raw material, and the solid waste catalyst exits the device for solid waste treatment or secondary processing.

[0040] The technical scheme and technical effects of the present invention are further illustrated below in conjunction with embodiments, but are not limited to the following embodiments.

[0041] The properties of the raw oil slurry used are shown in Table 1, the physical and chemical properties of the catalyst are shown in Table 2, and the multiphase flow hydrogenation reaction conditions and the chlorine content of the liquid product are shown in Table 3.

[0042] Example 1

[0043] In this embodiment, PVC and preheated oil slurry are mixed uniformly according to a mass percentage of 2:98, 2% of dechlorinating agent and 1% of carbon-based catalyst are added to form a uniform slurry, and the multiphase flow hydrocracking reaction conditions are: reaction temperature 430°C, reaction pressure 8MPa, space velocity 0.5h -1 , hydrogen-to-oil ratio 1000NL / kg.

[0044] Example 2

[0045] In this embodiment, PVC and preheated oil slurry are mixed uniformly according to a mass percentage of 2:98, 2% of dechlorinating agent and 1% of carbon-based catalyst are added to form a uniform slurry, and the multiphase flow hydrocracking reaction conditions are: reaction temperature 430°C, reaction pressure 8MPa, space velocity 0.5h -1 , hydrogen-to-oil ratio 1000NL / kg.

[0046] Example 3

[0047] In this embodiment, PVC and preheated oil slurry are mixed uniformly according to a mass percentage of 5:95, 4% of dechlorinating agent and 2% of carbon-based catalyst are added to form a uniform slurry, and the multiphase flow hydrocracking reaction conditions are: reaction temperature 450°C, reaction pressure 10MPa, space velocity 0.5h -1 , hydrogen-to-oil ratio 1000NL / kg.

[0048] Example 4

[0049] In this embodiment, PVC and preheated oil slurry are mixed uniformly according to a mass percentage of 5:95, 4% of dechlorinating agent and 2% of carbon-based catalyst are added to form a uniform slurry, and the multiphase flow hydrocracking reaction conditions are: reaction temperature 450°C, reaction pressure 12MPa, space velocity 0.5h -1 , hydrogen-to-oil ratio 1000NL / kg.

[0050] Example 5

[0051] In this embodiment, PVC and preheated oil slurry are mixed uniformly according to a mass percentage of 5:95, 4% of dechlorinating agent and 2% of carbon-based catalyst are added to form a uniform slurry, and the multiphase flow hydrocracking reaction conditions are: reaction temperature 450°C, reaction pressure 14MPa, space velocity 0.5h -1 , hydrogen-to-oil ratio 1000NL / kg.

[0052] Comparative Example 6

[0053] In this embodiment, PP, PE, PS and PVC are selected to form a mixed waste plastic containing 20% ​​PVC, which is evenly mixed with the preheated oil slurry at a mass percentage of 30:70, and 4% of the dechlorinating agent and 2% of the carbon-based catalyst are added to form a uniform slurry. The multiphase flow hydrocracking reaction conditions are: reaction temperature 450°C, reaction pressure 12MPa, space velocity 0.5h -1 , hydrogen-to-oil ratio: 1200NL / kg.

[0054] Comparative Example 7

[0055] In this embodiment, PP, PE, PS and PVC are selected to form a mixed waste plastic containing 20% ​​PVC, which is evenly mixed with the preheated oil slurry at a ratio of 30:70, and 2% of the carbon-based catalyst is added to form a uniform slurry. The multiphase flow hydrocracking reaction conditions are: reaction temperature 450°C, reaction pressure 12MPa, space velocity 0.5h -1 , hydrogen-to-oil ratio: 1200NL / kg.

[0056] Table 1 Catalytic slurry raw material properties

[0057] raw material Catalytic slurry <![CDATA[Density (20 °C), g / cm 3 > 0.952 Elemental analysis, wt% C 88.68 H 9.57 S 0.36 N 0.41 Carbon residue, wt% 13.69 Metal elements, ppm Ni 5.9 Fe 21.6 V 6.0 Four components, wt% Saturation 41.18 Aroma 51.0 Gel 4.31 Asphaltene 3.51

[0058] Table 2 Physicochemical properties of carbon-based catalysts

[0059] <![CDATA[Density, g / cm 3 > <![CDATA[Specific surface area, m 2 / g]]> Active ingredient content, wt% Average particle size, μm 0.65 450 11%Fe, 0.5%Ni 70

[0060] Table 3 Multiphase hydrocracking reaction conditions and product chlorine content

[0061]

[0062]

[0063] As can be seen from Table 3, no dechlorinating agent was added in the comparative example, and the chlorine content in the liquid oil was relatively high, which mainly affected the quality of light oil products and limited its scope of utilization. However, the method of the present invention adds a certain amount of dechlorinating agent to the chlorine-containing waste plastics, and after a multiphase flow hydrocracking reaction, it can not only achieve complete conversion of the chlorine-containing waste plastics and deep removal of chlorine, but also transfer the chlorine to the catalyst surface for removal, reducing the corrosion of chlorine to the equipment, and can obtain a liquid oil product with a low chlorine content, providing favorable conditions for the secondary processing and utilization of liquid oil.

[0064] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit it. Although the present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that the technical solutions described in the aforementioned embodiments may still be modified, or some or all of the technical features therein may be replaced by equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. A method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit, characterized in that: The steps include: S1: preparing chlorine-containing waste plastic (1), a dechlorinating agent (2), a solid catalyst (3) and heavy oil in a raw material tank (5) to form a uniform mixed slurry; S2: The mixed slurry is pumped to a multiphase flow hydrocracking reactor (10) via a high-pressure feed pump (7). Under high-temperature hydrogen conditions, the chlorine element in the plastic reacts with a dechlorinating agent to generate chloride salts, which are adsorbed on the catalyst surface and enter a hot high-pressure separator (11) together with the reaction products. S3: the reaction product is separated by a hot high-pressure separator (11) to obtain a light distillate oil and a solid-containing heavy distillate oil; S4: The solid-containing heavy distillate oil is passed through a vacuum tower (16) and a hot melt extraction device (18) to obtain vacuum wax oil (17), vacuum residue oil (19) and solid waste catalyst (20), respectively. The vacuum residue oil (19) can be returned to the raw material tank (5) for use as a raw material.

2. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 1, characterized in that: The chlorine-containing waste plastic (1) in S1 is a mixed plastic containing PVC, and the mixed plastic is one or more of PP, PE, PS, and PET.

3. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 2, characterized in that: The chlorine-containing waste plastic (1) in S1 is in granular form, with a maximum particle size of no more than 150 μm, and the addition amount is 0-50% based on the mass fraction of the total feed amount; The chlorine-containing waste plastic (1) is calculated based on the total feed mass fraction, and the proportion of PVC does not exceed 10%; The dechlorinating agent (2) is in powder form and is one or more of sodium sulfide, sodium thiosulfate, sodium carbonate, sodium bicarbonate, calcium oxide, and calcium carbonate; The dechlorinating agent (2) is calculated based on the total feed mass fraction, and the added amount is 0-5%. The active components of the solid catalyst (3) include one or more of ferric oxyhydroxide, nickel oxide, cobalt oxide, tungsten oxide and molybdenum oxide. The carrier is a porous carbon-based material, and the porous carbon-based material is activated carbon, coal powder and coke. The catalyst is calculated based on the total feed mass fraction and the added amount is 0.5-2.0%.

4. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 3, characterized in that: The solid catalyst (3) is calculated by weight, wherein the iron oxyhydroxide is 15-49%, the nickel oxide, cobalt oxide, molybdenum oxide or tungsten oxide is 1-20%, and the bulk density of the catalyst is 0.6-0.8 g / cm 3 , average particle size 65-75μm, specific surface area 400-600m 2 / g; The heavy oil (4) is one or more of atmospheric residue oil, vacuum residue oil, coal tar, catalytic oil slurry, steam cracking tar or other secondary processed distillate oil, or is oil-coal slurry containing coal powder.

5. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 1, characterized in that: The ratio of the chlorine-containing waste plastic (1), the dechlorinating agent (2), the solid catalyst (3) and the heavy oil (4) in S1 is (0-50):(0-5):(0.5-2.0):(50-100).

6. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 1, characterized in that: The reaction conditions of the multiphase flow hydrocracking reactor (10) in S2 are: reaction temperature 370-470°C, reaction pressure 4-15MPa, liquid space velocity 0.3-2.0h -1 , hydrogen-oil ratio 800-1500NL / kg; The multiphase flow hydrogenation reactor (10) is composed of 1 to 3 reactors in a series or parallel combination mode, and the reactor type is one or a combination of a suspension bed, an ebullating bed, and a bubbling bed.

7. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 1, characterized in that: The reaction product in S3 is separated by a hot high fraction separator (11) to obtain a light distillate oil and a solid-containing heavy distillate oil, wherein the final boiling point of the light distillate oil is not higher than 450°C.

8. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 1, characterized in that: The solid-containing heavy fraction oil in S4 is subjected to vacuum distillation in a vacuum tower (16) to obtain vacuum wax oil and solid-containing oil residue, wherein the vacuum wax oil can be used as a catalytic cracking or hydrocracking raw material; The solid oil residue is separated by a hot-melt extraction device (18) to obtain vacuum residue oil and solid waste catalyst, wherein all or part of the vacuum residue oil is used as circulating oil, and the waste catalyst adsorbed with chloride salt and coke is treated as solid waste or recycled for secondary use; The extraction solvent of the hot melt extraction device (18) is one or more hydrocarbon mixtures selected from n-heptane, benzene, toluene and xylene, or coal liquefaction light oil.

9. The method for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit according to claim 8, characterized in that: The control process parameters of the hot extraction separation device (18) are pressure 0.1-0.5 MPa, extraction temperature 90-150° C., agent-oil ratio (1-20):1, and extraction time 0.5-2 hours.

10. A system for processing chlorine-containing waste plastics in a multiphase flow hydrocracking unit for implementing the method according to any one of claims 1 to 9, characterized in that: The invention comprises a raw material tank (5), wherein the input end of the raw material tank (5) is respectively connected to the input ends of the chlorine-containing waste plastic (1), the dechlorination agent (2), the solid catalyst (3) and the heavy oil (4) conveying pipeline, and the chlorine-containing waste plastic (1), the dechlorination agent (2), the solid catalyst (3) and the heavy oil (4) are prepared in the raw material tank (5) to form a uniform mixed slurry; The mixed slurry output end enters the mixer (8) through the high-pressure feed pump (7) to be mixed with the hydrogen (6), and after being preheated by the heating furnace (9), enters the multiphase flow hydrocracking reactor (10); The output end of the multiphase flow hydrocracking reactor (10) is connected to a hot high-pressure separator (11), and the gaseous phase product of the hot high-pressure separator (11) enters a hot low-pressure separator (12), and the gaseous hydrocarbons are separated and enter a circulating hydrogen compressor (13). The liquid light distillate oil (14) exits the device, and the solid-containing heavy distillate oil enters a vacuum tower (16) and a hot melt extraction device (18) after being cooled and reduced in pressure by a vacuum valve (15), and vacuum wax oil (17), vacuum residue oil (19) and solid waste catalyst (20) are obtained respectively. The vacuum residue oil (19) is returned to the raw material tank for use as a raw material, and the solid waste catalyst exits the device for solid waste treatment or secondary processing.

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