Process for preparing oil products through waste plastic double-carrier circulation rapid pyrolysis

Abstract

The invention provides a process for preparing an oil product through waste plastic double-carrier circulation rapid pyrolysis. The process comprises the following steps: adding waste plastic fragments into a double-heat-carrier downward pyrolysis reactor; high-temperature pyrolysis dry gas is sprayed out from a perforated plate with the aperture ratio of 0.1%-15%, and the plastic fragments are prevented from being adhered and coked while being heated; the thermal plastic fragments are collided and mixed with the first-stage solid thermal carrier; after being subjected to enhanced mixing and pyrolytic reaction for multiple times through a mixing inner component of the double-heat-carrier downward pyrolysis reactor, the heat carriers flow into a moving bed reactor, the heat carriers containing the waste plastic melt are further subjected to pyrolytic reaction in a moving bed, and pyrolytic oil gas flows into a fractionating tower and is separated into wax oil, diesel oil, gasoline and pyrolysis dry gas; the coke-containing heat carrier at the bottom of the moving bed reactor is fluidized and combusted at the bottom of the riser heating regenerator; large and medium particle heat carriers separated by the first-stage gas-solid separator at the top of the lifting pipe heating regenerator participate in rapid pyrolysis of waste plastics, and fine ash separated by the second-stage gas-solid separator is circulated back to the bottom of the lifting pipe heating regenerator.

Description

1. Technical Field

[0001] The invention provides a process for preparing oil products by dual-carrier cyclic rapid pyrolysis of waste plastics, and belongs to the field of environmental engineering. 2. Background technology

[0002] The increasing use of plastic resins has brought great convenience to people's lives, but also brought a lot of white pollution. The use cycle of plastics is very short. A large number of plastic products, especially packaging materials, are discarded after about 6-12 months. 40% of plastics are discarded after 1-2 years. The total annual output of plastic waste in the world has reached 50 million tons. In the past few decades, waste plastics have been regarded as part of municipal solid waste (MSW). According to surveys, waste plastics account for 4%-10% (wt) or 10%-20% (v%) in MSW in industrialized countries, mainly from packaging waste, automobile garbage and processing waste. The percentages of various types of waste plastics are: low-density polyethylene (LDPE) 27%; high-density polyethylene (HDPE) 21%; polypropylene (PP) 18%; polystyrene (PS) 16%; polyvinyl chloride (PVC) 7%. Due to the lack of efficient, clean and large-scale technology, waste plastics have become an environmental problem that needs to be solved in the world.

[0003] In the treatment of urban plastic solid waste, landfill, incineration and recycling are the three main methods currently used. Due to different national conditions, each country has its own differences. The United States mainly uses landfill, while Europe and Japan mainly use incineration.

[0004] (1) Landfill treatment is adopted because plastic products are large and light (65kg / m 3 ), difficult to compress, airtight, easy to expand and not easy to rot, which will cause the landfill to become a soft foundation, causing water pollution, occupying land, sewer blockage, etc. Therefore, most developed countries strictly prohibit the disposal of large amounts of plastic waste by landfill.

[0005] (2) Incineration for heating or power generation. Plastic waste is a chemical substance with a high calorific value extracted from petroleum. It has the highest average calorific value among all household waste. In order to make plastic waste energy-efficient and economical, sending plastic waste to incinerators for combustion can provide heat for heating or power generation. However, considering that plastic waste incineration produces dioxin and fly ash pollution and the strong corrosive and destructive power of chlorine gas released during combustion, many environmental groups oppose the incineration of plastics. At present, Germany has 200,000 tons of PVC waste each year, of which 30% is burned in incinerators, causing panic among the people. The law has to formulate countermeasures for this. The German Federal Environment Agency has stipulated that all incinerators must meet the limit of less than 0.1ng (nanogram) per cubic meter of exhaust gas. Although Germany's incinerator air pollution standards are already recognized as high standards in the world, it still dares not to say that the combustion method will not release harmful substances due to mechanical failure. Therefore, it can be predicted that environmental groups in various countries will still strongly oppose the incineration method to recover heat energy.

[0006] (3) Recycling and reuse methods. Due to the labor-intensive, high recycling costs and lack of corresponding recycling channels, recycling and reuse currently only accounts for about 15% of the total plastic consumption in the world. However, due to the limited oil resources in the world, from the perspective of saving earth resources, the recycling and reuse of plastics is of great significance. To this end, countries around the world are currently investing a lot of manpower and material resources to develop various key technologies for recycling and reuse of waste plastics, and are committed to reducing the cost of recycling and reuse of plastics and developing suitable application areas.

[0007] The pyrolysis of waste plastics is an effective recycling method that heats waste plastics at high temperatures under oxygen-free or low-oxygen conditions to decompose them and reproduce valuable products, such as the pyrolysis and liquefaction of waste plastics to produce gasoline, diesel, petroleum wax and other chemical raw materials. However, due to the characteristics of waste plastics such as large size and light weight, difficulty in compression, airtightness, easy expansion, easy melting and bonding, and poor thermal conductivity, it is difficult to solve the problem of continuous feeding and rapid heating. At present, most of the pyrolysis and liquefaction of waste plastics adopt reactor-type intermittent reactions and horizontal rotary kiln reactions. The heating rate is slow, the feed sticks and cokes seriously, the liquid product yield is low, the processing capacity is difficult to improve, and the pyrolysis device is difficult to scale up, which restricts the efficient and clean large-scale utilization of waste plastics. At present, there is no large-scale pyrolysis device in commercial operation, and it is urgent to develop continuous and rapid pyrolysis and liquefaction processes and equipment technologies for waste plastics. 3. Summary of the invention

[0008] The purpose of the present invention is to overcome the shortcomings of the existing waste plastic pyrolysis liquefaction technology and provide a process for producing oil products by dual-carrier circulation rapid pyrolysis of waste plastics. The pyrolysis dry gas is graded and reasonably utilized according to different temperatures, and the two-stage combination of gas and solid heat carriers is used to improve the pyrolysis heating rate, and solve the four common problems in the industry: adhesion and coking of waste plastic feed, difficulty in mixing with heat carriers, low yield of liquid products, and difficulty in scaling up pyrolysis equipment.

[0009] The technical solution of the present invention:

[0010] The process for preparing oil products by dual-carrier circulation rapid pyrolysis of waste plastics comprises the following steps: the waste plastics are first crushed by a waste plastic crusher, and then the waste plastic fragments of 0 to 30 mm are added to a water-cooled feed pipe with a water-cooled jacket on the top of a dual-heat carrier descending pyrolysis reactor by a controllable feeder, and flow downward into the high-temperature gas hot melting section of the dual-heat carrier descending pyrolysis reactor under the influence of pyrolysis dry gas; 300°C-600°C pyrolysis dry gas pressurized by a pressurized fan and a pyrolysis dry gas heat exchanger is injected into the high-temperature pyrolysis dry gas inner jacket, and uniformly sprayed out from a porous plate with an opening rate of 0.1%-15%, heating and melting the waste plastic fragments while preventing the plastic fragments from adhering to the dual-heat carrier descending pyrolysis reactor. The inner wall of the reactor forms coke; the mixed pyrolysis dry gas carries the waste plastic melt and flows downward to the high-temperature gas hot melting section at the top of the dual heat carrier descending pyrolysis reactor, collides and mixes with the primary solid heat carrier that enters obliquely from the side, and a pyrolysis reaction occurs; the downward-flowing pyrolysis gas, heat carrier and waste plastic melt pass through the mixing internal components composed of the guide plates in the inner cavity of the dual heat carrier descending pyrolysis reactor for multiple enhanced mixing and pyrolysis reactions, and then flow into the moving bed reactor from one side of the top of the moving bed reactor for preliminary gas-solid separation; the separated heat carrier containing the waste plastic melt further undergoes a pyrolysis reaction in the moving bed, and the pyrolysis oil vapor is further separated and purified through the oil-gas separator The pyrolysis oil vapor is separated into wax oil, diesel, gasoline and pyrolysis dry gas in the distillation tower. An induced draft fan is arranged at the pyrolysis dry gas outlet at the top of the distillation tower. One path of dry gas is connected to the water-cooled feed pipe as the carrying air, and the other path of dry gas is pressurized and heated by the booster fan and the pyrolysis dry gas heat exchanger and then returns to the high-temperature pyrolysis dry gas inner jacket of the high-temperature gas hot melt section at the upper part of the double heat carrier descending pyrolysis reactor. The remaining dry gas is sent out as the product. The char-containing heat carrier at the bottom of the moving bed reactor is added to the turbulent bed at the bottom of the riser heating regenerator through the return feeder of the heat carrier to be generated, and is fluidized and burned by the air added through the air inlet pipe and the gas distributor. The generated flue gas and the carried heat carrier to be generated are passed through the The entrained bed at the top of the riser heating regenerator is further burned and heated. The large and medium-particle heat carriers are separated by the first-stage gas-solid separator at the top of the riser heating regenerator, and then the fine ash is separated by the second-stage gas-solid separator. After the flue gas recovers heat through the pyrolysis dry gas heat exchanger and the waste heat boiler, the flue gas is discharged; the large and medium-particle heat carriers separated by the first-stage gas-solid separator are circulated back to the solid heat carrier inlet at the top of the dual heat carrier descending pyrolysis reactor through the first-stage solid heat carrier return feeder to participate in the rapid pyrolysis of waste plastics; the fine ash separated by the second-stage gas-solid separator is circulated back to the turbulent bed at the bottom of the riser heating regenerator through the hot ash circulation pipe and the hot ash circulation return feeder to maintain fluidized combustion.

[0011] A feed pipe with a water-cooling jacket is arranged on the top of a double heat carrier descending pyrolysis reactor, and the size is 0-100mm smaller than the reactor inner cavity; a high-temperature pyrolysis dry gas inner jacket with a thickness of 10mm-100mm is formed by the inner cavity and a porous plate with an opening rate of 0.1%-15% at the upper part of the reactor, and the jacket height is 0.5-4 times the equivalent diameter of the inner cavity; an inclined solid heat carrier inlet is arranged on the side of the upper part of the reactor, which is located 100-1500mm downward from the top of the reactor and has a horizontal downward angle of 0-85°; a mixed internal component composed of 1-10 guide plates with a horizontal downward inclination of 25°-85° is arranged in the reactor inner cavity, and adjacent guide plates are staggered at 180°, and the distance between the bottom end of the guide plate and the opposite inner cavity wall is 100-400mm.

[0012] The controllable feeder is a rotary feeder, a double-shaft screw feeder or a single-shaft screw feeder.

[0013] The equivalent diameter of the upper part of the moving bed reactor is 1.2-4.0 times larger than that of the dual heat carrier descending pyrolysis reactor. The outlet and the oil and gas outlet of the dual heat carrier descending pyrolysis reactor are respectively installed on both sides of the top of the moving bed reactor; the bottom of the moving bed reactor is conical and directly connected to the return feeder of the heat carrier to be generated with a crushing function.

[0014] The riser heating regenerator is composed of a turbulent fluidized bed at the bottom and a carrying reactor at the top. The turbulent fluidized bed has a larger equivalent diameter, while the carrying reactor has a smaller equivalent diameter, and the diameter ratio is 2 to 3:1. The carrying reactor can be a straight tube reactor with a uniform equivalent diameter, or it can be composed of large and small straight tubes with diameters of different multiples of the equivalent diameter connected by large and small head pipe fittings, and the diameter ratio of the large and small straight tubes is 1.2 to 2:1. The equivalent diameter of the fluidized bed is only 10%-50% of the equivalent diameter of the turbulent fluidized bed.

[0015] The outlet temperature of the dual heat carrier descending pyrolysis reactor is 400-600°C, the reaction temperature at the bottom of the riser heating regenerator is 600-1000°C, and the reaction temperature at the top outlet is 650-1200°C.

[0016] The present invention will be described in detail with reference to embodiments. 4. Description of the drawings

[0017] Attached Figure 1 The present invention is a schematic diagram of the process of producing oil products by dual-carrier cyclic rapid pyrolysis of waste plastics.

[0018] Attached Figure 1 The drawing settings are as follows:

[0019] 1. Waste plastic crusher 2. Controllable feeder 3. Water-cooled feed pipe 4. High-temperature gas hot melt section 5. Dual heat carrier descending pyrolysis reactor 6. Moving bed reactor 7. Oil-gas separator 8. Fractionation tower 9. Wax oil outlet 10. Diesel outlet 11. Gasoline outlet 12. Induced draft fan 13. Pyrolysis dry gas outlet 14. Pyrolysis dry gas heat exchanger 15. Waste heat boiler 16. Flue gas outlet 17. Return feeder for heat carrier to be generated 18. Riser heating regenerator 19. Gas distributor 20. Inlet pipe 21. Ash discharge port 22. First-stage gas-solid separator 23. First-stage solid heat carrier return feeder 24. Second-stage gas-solid separator 25. Hot ash circulation return feeder 26. Pressurized fan

[0020] The process characteristics of the present invention are described in detail below in conjunction with the accompanying drawings and embodiments. 5. Specific implementation methods

[0021] The invention discloses a process for preparing oil products by dual-carrier cycle rapid pyrolysis of waste plastics. The waste plastics are firstly crushed by a waste plastic crusher (1), and then the waste plastic fragments with a diameter of 0 to 30 mm are added to a water-cooled feed pipe with a water-cooled jacket on the top of a dual-heat carrier descending pyrolysis reactor (5) by a controllable feeder (2). The waste plastic fragments flow downward into a high-temperature gas hot melting section (4) of the dual-heat carrier descending pyrolysis reactor (5) under the influence of pyrolysis dry gas. The high-temperature pyrolysis dry gas with a temperature of 300 to 600°C pressurized by a pressurized fan (26) and a pyrolysis dry gas heat exchanger (14) is injected into the inner jacket of the high-temperature pyrolysis dry gas, and the opening rate is 0.1%-15% of the waste plastic fragments are uniformly sprayed out from the porous plate, heating and melting the waste plastic fragments while preventing the plastic fragments from adhering to the inner wall of the dual heat carrier descending pyrolysis reactor (5) to form coke; the mixed pyrolysis dry gas carries the waste plastic melt liquid and flows downward to the high-temperature gas hot melting section (4) at the upper part of the dual heat carrier descending pyrolysis reactor (5), collides and mixes with the primary solid heat carrier that enters obliquely from the side, and a pyrolysis reaction occurs; the downward-flowing pyrolysis gas, heat carrier and waste plastic melt pass through the mixing internal component composed of the inner cavity guide plate of the dual heat carrier descending pyrolysis reactor (5) for multiple intensified mixing and pyrolysis reactions, and then flows out from the moving bed reactor (6 ) flows into the moving bed reactor (6) from one side of the top, and the vapor and solid are initially separated; the separated heat carrier containing the waste plastic melt further undergoes a pyrolysis reaction in the moving bed, and the pyrolysis oil vapor is further separated and purified through the oil-gas separator (7) and then flows into the fractionation tower (8); the pyrolysis oil vapor is separated into wax oil, diesel, gasoline and pyrolysis dry gas in the fractionation tower (8); an induced draft fan (12) is provided at the pyrolysis dry gas outlet at the top of the fractionation tower (8), one path of dry gas is connected to the water-cooled feed pipe (3) as a carrying wind, and the other path of dry gas is pressurized and heated by the pressurized fan (26) and the pyrolysis dry gas heat exchanger (14) and then returns to the dual heat carrier downward heat exchanger (14). The high-temperature pyrolysis dry gas inner jacket and the remaining dry gas of the high-temperature gas hot melting section (4) at the top of the decomposition reactor (5) are sent out as products; the coke-containing heat carrier at the bottom of the moving bed reactor (6) is added to the turbulent bed at the bottom of the riser heating regenerator (18) through the heat carrier return device (17) to be generated, and is fluidized and burned by the air added through the air inlet pipe (20) and the gas distributor (19); the generated flue gas and the carried heat carrier to be generated are further burned and heated through the carrying bed at the top of the riser heating regenerator (18), and are separated into large and medium particles by the first-stage gas-solid separator (22) at the top of the riser heating regenerator (18). The heat carrier is then separated into fine ash by the second-stage gas-solid separator (24). After the flue gas recovers heat through the pyrolysis dry gas heat exchanger (14) and the waste heat boiler (15), the flue gas is discharged; the large and medium-sized particle heat carrier separated by the first-stage gas-solid separator (22) is circulated back to the solid heat carrier inlet at the top of the double heat carrier descending pyrolysis reactor (5) through the first-stage solid heat carrier return device (23) to participate in the rapid pyrolysis of waste plastics; the fine ash separated by the second-stage gas-solid separator (24) is circulated back to the turbulent bed at the bottom of the riser heating regenerator (18) through the hot ash circulation pipe and the hot ash circulation return device (25) to maintain fluidized combustion.

[0022] The top of the dual heat carrier descending pyrolysis reactor (5) is provided with a feed pipe with a water cooling jacket, the size of which is 0-100 mm smaller than the reactor inner cavity; the upper part of the reactor is provided with a high-temperature pyrolysis dry gas inner jacket with a thickness of 10 mm-100 mm formed by the inner cavity and a porous plate with an opening rate of 0.1%-15%, and the jacket height is 0.5-4 times the equivalent diameter of the inner cavity; an inclined solid heat carrier inlet is provided on the side of the upper part of the reactor, located 100-1500 mm downward from the top of the reactor, with a horizontal angle of 45°-85°; the inner cavity of the reactor is provided with a mixed internal component consisting of 1-10 guide plates with a horizontal inclination of 25°-85°, the adjacent guide plates are staggered at 180°, and the bottom of the guide plate is 100-400 mm away from the inner cavity wall.

[0023] The controllable feeder (2) is a rotary feeder, a double-shaft screw feeder or a single-shaft screw feeder.

[0024] The equivalent diameter of the upper portion of the moving bed reactor (6) is 1.2-4.0 times greater than that of the dual heat carrier descending pyrolysis reactor (5); the outlet and the oil and gas outlet of the dual heat carrier descending pyrolysis reactor (5) are respectively installed on both sides of the top of the moving bed reactor (6); the bottom of the moving bed reactor (6) is conical and directly connected to the return feeder (17) of the heat carrier to be generated with a crushing function.

[0025] The riser heating regenerator (18) is composed of a turbulent fluidized bed at the bottom and a carrying reactor at the top. The turbulent fluidized bed has a larger equivalent diameter, while the carrying reactor has a smaller equivalent diameter, and the diameter ratio is 2 to 3:1. The carrying reactor can be a straight tube reactor with a uniform equivalent diameter, or can be composed of large and small straight tubes with diameters of different multiples of the equivalent diameter connected by large and small head pipe fittings, and the diameter ratio of the large and small straight tubes is 1.2 to 2:1. The equivalent diameter of the fluidized bed is only 10% to 50% of the equivalent diameter of the turbulent fluidized bed.

[0026] The outlet temperature of the dual heat carrier descending pyrolysis reactor (5) is 400-600°C; the reaction temperature at the bottom of the riser heating regenerator (18) is 600-1000°C, and the reaction temperature at the top outlet is 650-1200°C.

[0027] The process of producing oil-based products by rapid pyrolysis of waste plastics with dual carriers in a cycle is capable of continuously, efficiently and cleanly pyrolyzing waste plastics on a large scale, solving four common industry problems: adhesion and coking of waste plastic feed, difficulty in mixing with heat carriers, low yield of liquid products, and difficulty in scaling up pyrolysis equipment. The liquid yield is over 88% (including liquefied gas), which is more than 15 percentage points higher than that of traditional waste plastic pyrolysis technology. It has high pyrolysis intensity, small equipment size, low steel consumption, greatly reduced fixed investment, and a simple ash removal process, ensuring safe, long-term and optimal operation of the device.

Claims

1. A process for preparing oil products by dual-carrier cycle rapid pyrolysis of waste plastics, the technical feature of which is that the waste plastics are first crushed by a waste plastic crusher, and then the waste plastic fragments of 0 to 30 mm are added to the water-cooled feed pipe with a water-cooled jacket on the top of the dual-heat carrier descending pyrolysis reactor by a controllable feeder, and flow downward into the high-temperature gas hot melting section of the dual-heat carrier descending pyrolysis reactor under the influence of pyrolysis dry gas; 300°C-600°C pyrolysis dry gas pressurized by a pressurized fan and a pyrolysis dry gas heat exchanger is injected into the high-temperature pyrolysis dry gas inner jacket, and is uniformly sprayed out from a porous plate with an opening rate of 0.1%-15%, heating and melting the waste plastic fragments while preventing the plastic fragments from adhering to the dual heat carrier Coke forms on the inner wall of the descending pyrolysis reactor; the mixed pyrolysis dry gas carries the waste plastic melt and flows downward to the high-temperature gas hot melting section at the top of the dual heat carrier descending pyrolysis reactor, where it collides and mixes with the primary solid heat carrier that enters obliquely from the side, and a pyrolysis reaction occurs; the downward-flowing pyrolysis gas, heat carrier and waste plastic melt undergo multiple enhanced mixing and pyrolysis reactions through the mixing internal components composed of the guide plates in the inner cavity of the dual heat carrier descending pyrolysis reactor, and then flows into the moving bed reactor from one side of the top of the moving bed reactor for preliminary gas-solid separation; the separated heat carrier containing the waste plastic melt further undergoes a pyrolysis reaction in the moving bed, and the pyrolysis oil vapor is further separated through the oil-gas separator After purification, it flows into the distillation tower; the pyrolysis oil vapor is separated into wax oil, diesel, gasoline and pyrolysis dry gas in the distillation tower; an induced draft fan is set at the pyrolysis dry gas outlet on the top of the distillation tower, one dry gas is connected to the water-cooled feed pipe as the carrying air, and the other dry gas is pressurized and heated by the booster fan and the pyrolysis dry gas heat exchanger and then returns to the high-temperature pyrolysis dry gas inner jacket of the high-temperature gas hot melt section at the upper part of the double heat carrier descending pyrolysis reactor, and the remaining dry gas is sent out as the product; the coke-containing heat carrier at the bottom of the moving bed reactor is added to the turbulent bed at the bottom of the riser heating regenerator through the return device of the heat carrier to be generated, and is fluidized and burned by the air added through the air inlet pipe and the gas distributor; the generated flue gas and the carried heat carrier to be generated The entrained bed at the top of the riser heating regenerator is further burned and heated. The large and medium-particle heat carriers are separated by the first-stage gas-solid separator at the top of the riser heating regenerator, and then the fine ash is separated by the second-stage gas-solid separator. The flue gas is discharged after the heat is recovered by the pyrolysis dry gas heat exchanger and the waste heat boiler; the large and medium-particle heat carriers separated by the first-stage gas-solid separator are circulated back to the solid heat carrier inlet at the top of the dual heat carrier descending pyrolysis reactor through the first-stage solid heat carrier return feeder to participate in the rapid pyrolysis of waste plastics; the fine ash separated by the second-stage gas-solid separator is circulated back to the turbulent bed at the bottom of the riser heating regenerator through the hot ash circulation pipe and the hot ash circulation return feeder to maintain fluidized combustion.

2. The process for preparing oil products by dual-carrier cyclic rapid pyrolysis of waste plastics according to claim 1 is characterized in that A feed pipe with a water-cooling jacket is arranged on the top of a double heat carrier descending pyrolysis reactor, and the size is 0-100mm smaller than the reactor inner cavity; a high-temperature pyrolysis dry gas inner jacket with a thickness of 10mm-100mm is formed by the inner cavity and a porous plate with an opening rate of 0.1%-15% at the upper part of the reactor, and the jacket height is 0.5-4 times the equivalent diameter of the inner cavity; an inclined solid heat carrier inlet is arranged on the side of the upper part of the reactor, which is located 100-1500mm downward from the top of the reactor and has a horizontal downward angle of 0-85°; a mixed internal component composed of 1-10 guide plates with a horizontal downward inclination of 25°-85° is arranged in the reactor inner cavity, and adjacent guide plates are staggered at 180°, and the distance between the bottom end of the guide plate and the opposite inner cavity wall is 100-400mm.

3. The process for preparing oil products by dual-carrier cyclic rapid pyrolysis of waste plastics according to claim 1 is characterized in that The controllable feeder is a rotary feeder, a double-shaft screw feeder or a single-shaft screw feeder.

4. The process for preparing oil products by dual-carrier cycle rapid pyrolysis of waste plastics according to claim 1 is characterized in that The controllable feeder is the upper part of the moving bed reactor, and its equivalent diameter is 1.2-4.0 times greater than that of the dual heat carrier descending pyrolysis reactor. The outlet and the oil and gas outlet of the dual heat carrier descending pyrolysis reactor are respectively installed on both sides of the top of the moving bed reactor; the bottom of the moving bed reactor is conical and directly connected to the return feeder of the heat carrier to be generated with a crushing function.

5. The process for preparing oil products by dual-carrier cycle rapid pyrolysis of waste plastics according to claim 1 is characterized in that The riser heating regenerator is composed of a turbulent fluidized bed at the bottom and a carrying reactor at the top, the ratio of the equivalent diameter of the turbulent fluidized bed to the equivalent diameter of the carrying reactor is 2 to 3:1; the carrying reactor is a straight tube reactor with a uniform equivalent diameter, or is composed of large and small straight tubes with diameters of different multiples of the equivalent diameter connected by large and small head pipe fittings, and the diameter ratio of the large and small straight tubes is 1.2 to 2:1; the equivalent diameter of the fluidized bed is 10%-50% of the equivalent diameter of the turbulent fluidized bed.

6. The process for preparing oil products by dual-carrier cycle rapid pyrolysis of waste plastics according to claim 1 is characterized in that The outlet temperature of the dual heat carrier descending pyrolysis reactor (5) is 400-600°C; the reaction temperature at the bottom of the riser heating regenerator (18) is 600-1000°C, and the reaction temperature at the top outlet is 650-1200°C.

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