Process for producing chemicals by graded gas phase dehydrogenation cracking of mixed feed of waste plastics and crude oil

Abstract

The process for producing chemicals by mixed feeding of waste plastics and crude oil with graded gas phase dehydrogenation cracking comprises a waste plastic self-thermal melting dechlorination pretreatment process, a waste plastic melt and crude oil selective vaporization dehydrogenation cracking process, a high-temperature cracking oil and gas gas-phase catalytic cracking process, and a cracking oil and gas fractionation and refining process. The recycled oil and cracking dry gas from the cracking oil and gas fractionation and refining process are respectively recycled to the waste plastic self-thermal melting dechlorination pretreatment process for high-temperature melting and liquefaction and carrying feed addition. The waste plastic melt from the waste plastic self-thermal melting dechlorination pretreatment process is sent out to be mixed with crude oil and used as the raw material for the waste plastic melt and crude oil selective vaporization dehydrogenation cracking process. Atomizing nozzles are used for efficient feeding, and selective vaporization dehydrogenation cracking and gas-phase catalytic cracking are completed in sequence and graded. Then, the cracking oil and gas fractionation and refining subsystem produces triolefins and triphenyls, high-temperature recycled oil and cracking dry gas.

Description

1. Technical Field

[0001] The invention provides a process for producing chemicals by graded gas phase dehydrogenation and cracking of mixed feed of waste plastics and crude oil, belonging to the field of energy chemical industry. 2. Background Technology

[0002] While the widespread use of plastics has brought significant convenience to people's lives, it has also led to significant levels of white pollution. Plastics have a very short lifespan. A large number of plastic products, especially packaging, are discarded after approximately 6-12 months, and 40% of plastic is discarded after only 1-2 years. Globally, the annual production of plastic waste has reached 50 million tons. For decades, waste plastics have been included as part of municipal solid waste (MSW). According to surveys, waste plastics account for 4%-10% (wt%) or 10%-20% (v%) of MSW in industrialized countries, primarily from packaging waste, automobile waste, and processing waste. The percentages of various types of waste plastics are as follows: low-density polyethylene (LDPE) 27%; high-density polyethylene (HDPE) 21%; polypropylene (PP) 18%; polystyrene (PS) 16%; and polyvinyl chloride (PVC) 7%. Due to the lack of efficient, clean, and scalable technologies, waste plastics have become a pressing environmental challenge worldwide.

[0003] Landfill, incineration, and recycling are the three primary methods used to treat urban plastic solid waste. These methods vary from country to country due to varying circumstances, with landfill being the primary method in the United States, and incineration being the primary method in Europe and Japan. Currently, rapid pyrolysis / catalytic pyrolysis of waste plastics to liquefy or produce chemicals has become a hot topic both domestically and internationally, and is considered the most promising waste plastics treatment technology for industrialization.

[0004] Rapid pyrolysis / catalytic pyrolysis of waste plastics is an effective recycling method that involves heating waste plastics at high temperatures in the absence of oxygen or low oxygen conditions to decompose them and produce valuable products. This includes 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 being bulky and light, difficult to compress, airtight, easily expandable, easily melted and bonded, and having poor thermal conductivity, it is difficult to solve the problems of continuous feeding and rapid heating. Currently, most waste plastic pyrolysis and liquefaction methods use reactor-type batch reactions and horizontal rotary kiln reactions, which have slow heating rates, severe feed adhesion and coking, low liquid product yields and added value, difficulty in increasing processing capacity, difficulty in scaling up pyrolysis equipment, and difficulty in subsequent processing of chlorine-containing liquid products. These factors restrict the efficient, clean, and large-scale utilization of waste plastics. Currently, there are no large-scale commercial waste plastic pyrolysis equipment.

[0005] Crude oil graded gas-phase dehydrogenation and cracking to produce chemicals bypasses traditional crude oil processing technologies such as atmospheric and vacuum distillation, catalytic cracking, hydrocracking, and delayed coking, directly producing basic chemical raw materials such as triolefins and triphenyls through catalytic dehydrogenation and cracking. This technology features a short process, simple operation, low cost and energy consumption, and minimal investment. It is the most promising oil-to-oil refining technology for industrialization, adapting to the energy transition brought about by the electrification of automobiles. Combining rapid pyrolysis / catalytic pyrolysis of waste plastics with graded gas-phase dehydrogenation and cracking of crude oil to produce chemicals is an effective means to improve the clean and efficient raw material utilization of waste plastics, reduce petroleum resource consumption, solve the feed problem of waste plastics pyrolysis, and improve chemical yields and the economic benefits of the equipment. Therefore, it is urgently necessary to develop processes and equipment for graded gas-phase dehydrogenation and cracking of chemicals using a mixed feed of waste plastics and crude oil. 3. Summary of the Invention

[0006] 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 chemicals by graded gas-phase dehydrogenation cracking of mixed feed of waste plastic and crude oil. The process utilizes pyrolysis dry gas and high-temperature recycled oil circulation to carry out hot-melt dechlorination and sulfur removal pretreatment of waste plastic and liquid-phase atomization feeding, thereby solving the problems of difficult pyrolysis feeding and difficult removal of chlorine and sulfur heteroatoms. The process adopts graded gas-phase catalytic cracking in a downer reactor, and the cracking characteristics of the mixed feed of waste plastic and crude oil complement each other, eliminating the liquid phase cage wall effect, regulating the breakage of CC and CH bonds, inhibiting condensation coking, eliminating the amplification effect, realizing controllable cracking of waste plastic, and maximizing the production of triolefins and triphenyls. The process solves the five common problems in the industry, namely, adhesion and coking of waste plastic feed, difficulty in mixing with heat carriers, low yield and added value of liquid products, difficulty in removing chlorine and sulfur heteroatoms of liquid products, thereby affecting subsequent processing, and difficulty in scaling up pyrolysis equipment, thereby realizing efficient, clean, and high-value large-scale utilization of waste plastics and crude oil.

[0007] The technical solution of the present invention:

[0008] Waste plastics and crude oil are mixed and fed into a graded gas phase dehydrogenation cracking process to produce chemicals. The clean PE and PP waste plastics are sorted through a waste plastic crusher and the waste plastic fragments are added to a 20-95℃ water-cooled feed pipe through a controllable feeder. The waste plastic fragments are carried by the cracking dry gas and fall into the 240-320℃ oil slurry melt in a hot melt dechlorination reactor with stirring. The melt dechlorination and desulfurization pretreatment is carried out by stirring and mixing. The molten plastic liquid extracted from the bottom of the hot melt dechlorination reactor is pressurized and transported by a delivery pump. A part of it is heated to a temperature higher than that of the oil slurry melt through a high-speed circulation pipe with external heating. The liquid temperature is 20-60℃ higher and then returns to the upper part of the hot melt dechlorination reactor. The other part is sent to the upper part of the downward cracking reactor together with crude oil as raw material through the atomizing feed nozzle. The gas extracted from the top of the hot melt dechlorination reactor is treated by the desulfurization and dechlorination reactor and then enters the refinery gas network as fuel gas. The flow rate of the high-speed circulation pipe is 2-30m / s, the circulation ratio of the molten plastic liquid to the raw material is 1-10:1, and the steam consumption of the atomizing feed nozzle is 4%-12% of the raw material amount. The atomized particle feed of the mixture of the molten plastic liquid and crude oil is the same as that of the mixture from the downward cracking reactor. The cracking regeneration catalyst falling from the top of the reactor undergoes rapid mixing, vaporization and controllable cracking reaction. The steam dosage of the atomizing feed nozzle is 4% to 12% of the raw material amount, the cracking reaction temperature is 500 to 550 ° C, the pressure is 0-0.3 MPa, and the reaction time is 600 milliseconds to 2 seconds. The oil and gas-solid separation is carried out at the bottom of the descending cracking reactor; the separated catalyst to be regenerated flows through the return device to the bottom of the cracking riser regenerator for air fluidization and coking regeneration at 500-750 ° C. The cracking riser regenerator is provided with a regeneration air inlet at the bottom and a regeneration air inlet at the top in sequence. The system is equipped with a gas-solid separator, a heat exchanger, and a regenerated flue gas outlet. The regenerated catalyst separated by the gas-solid separator at the top of the cracking riser regenerator is circulated back to the top of the descending cracking reactor through a return controller to catalytically crack the mixture of molten plastic liquid and crude oil. The high-temperature cracked oil and gas are directly injected from the gas phase feed hole in the upper part of the descending cracking reactor without condensation, and rapidly mixed with the cracking regenerated catalyst falling from the top and undergoing a controllable cracking reaction. The oil and gas are then separated from the solids at the bottom of the descending cracking reactor. The cracking reaction temperature is 570-650℃ and the pressure is 0-0.3MPa, reaction time 200 milliseconds to 1 second; the separated cracking catalyst flows through a return feeder to the bottom of the cracking riser regenerator for regeneration by charring at 600-750°C air fluidization. The cracking riser regenerator is equipped with an air inlet at the bottom and a gas-solid separator, heat exchanger, and regeneration flue gas outlet at the top. The regenerated catalyst separated by the gas-solid separator at the top of the cracking riser regenerator is recycled through the return feeder to the top of the descending cracking reactor to catalytically crack the high-temperature cracking oil and gas. The high-temperature cracking oil and gas enter the fractionating tower for separation. The cracked dry gas at the top of the fractionating tower is recycled back to the water-cooled feed pipe at the top of the hot melt dechlorination reactor as feed carrier gas on one route and to the cracking gas refining system to produce triolefins on another route. The fractionating tower refining oil is recycled back to the top of the hot melt dechlorination reactor as high-temperature molten oil on one route and to the product after waste heat recovery on another route. Other side streams from the fractionating tower produce crude benzene and diesel fractions.

[0009] The outer wall of the water-cooled feed pipe is provided with a water-cooling jacket, which has a shape of a forward cone, a straight tube or an inverted cone, preferably a forward cone.

[0010] The controllable feeder is a rotary feeder, a double-shaft screw feeder or a single-shaft screw feeder.

[0011] The high-speed circulation tube is heated by electromagnetic induction heating, thermal oil heating, steam heating or resistance heating, preferably electromagnetic induction heating.

[0012] The cracking catalyst is a mixture of one or more of semi-coke microspheres, alumina microspheres, calcium aluminate porous microspheres, magnesium aluminum spinel porous microspheres, aluminum silicate porous microspheres, calcium silicate porous microspheres, magnesium silicate porous microspheres, and porous microsphere carriers loaded with alkali metals and / or alkaline earth metals.

[0013] The cracking catalyst is a mixture of one or more of an FCC molecular sieve catalyst, a ZSM-5 type selective molecular sieve catalyst, and an alkaline solid porous catalyst.

[0014] The riser regenerator is composed of a turbulent fluidized bed at the bottom and an entrained reactor at the top. The turbulent fluidized bed has a larger equivalent diameter, while the entrained reactor has a smaller equivalent diameter, with a diameter ratio of 2 to 3:1. The entrained 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, with a diameter ratio of 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 present invention will be described in detail with reference to embodiments. 4. Description of the Figures

[0016] Attachment Figure 1 The figure is a schematic diagram of the process flow of producing chemicals by graded gas phase dehydrogenation cracking of mixed feed of waste plastics and crude oil according to the present invention.

[0017] Attachment Figure 1 The drawing settings are as follows:

[0018] 1. Gas-solid separator, 2. Return controller, 3. Atomizing feed nozzle, 4. Downward cracking reactor, 5. Gas-solid rapid separator, 6. Pyrolysis oil and gas outlet, 7. Return feeder, 8. Downward cracking reactor, 9. Regeneration agent inlet, 10. Cracking riser regeneration reactor, 11. Heat exchanger, 12. Regeneration flue gas outlet, 13. Cracking riser regeneration reactor, 14. Air inlet, 15. Flue gas outlet, 16. Fractionator, 17. Crude benzene fraction, 18. Diesel fraction, 19. Recycled oil pump, 20. Hot melt dechlorination reactor, 21. Waste plastic pulverizer, 22. Controllable feeder, 23. Water-cooled feed pipe, 24. Desulfurization and dechlorination reactor, 25. Transfer pump, 26. High-speed circulation pipe, 27. Refinery dry gas network

[0019] The process characteristics of the present invention are described in detail below with reference to the accompanying drawings and embodiments. 5. Specific implementation methods

[0020] The present invention provides a process for producing chemicals by mixing waste plastics and crude oil into a graded gas phase dehydrogenation cracking process. The clean PE and PP waste plastics separated are fed into a waste plastic crusher (21). The waste plastic fragments are fed into a water-cooled feed pipe (23) at 20-95°C through a controllable feeder (22). The waste plastic fragments are carried by cracking dry gas and fall into a 240-320°C oil slurry melt in a hot melt dechlorination reactor (20) with stirring. The melt dechlorination and desulfurization pretreatment is carried out by stirring and mixing. The molten plastic liquid extracted from the bottom of the hot melt dechlorination reactor (20) is fed into a delivery pump (25). The gas is conveyed under pressure, and a part of it is heated to 20-60°C higher than the temperature of the slurry melt through a high-speed circulation pipe (26) with external heating and then returned to the upper part of the hot melt dechlorination reactor (20). The other part is sent to the upper part of the downward cracking reactor (4) together with the crude oil as raw material through the atomizing feed nozzle (3). The gas extracted from the top of the hot melt dechlorination reactor (20) is processed by the desulfurization and dechlorination reactor (24) and then enters the refinery gas network as fuel gas. The flow rate of the high-speed circulation pipe (25) is 2-30m / s, and the circulation ratio of the molten plastic liquid to the raw material is 1 ~10:1, the steam dosage of the atomizing feed nozzle (3) is 4% to 12% of the raw material amount; the atomized particle feed of the mixture of the molten plastic liquid and the crude oil is rapidly mixed, vaporized and subjected to a controllable cracking reaction with the cracking regeneration catalyst falling from the top of the descending cracking reactor (4), the steam dosage of the atomizing feed nozzle (3) is 4% to 12% of the raw material amount, the cracking reaction temperature is 500 to 550°C, the pressure is 0-0.3 MPa, the reaction time is 600 milliseconds to 2 seconds, and oil-gas-solid separation (5) is carried out at the bottom of the descending cracking reactor (4) The separated catalyst to be regenerated flows through the return device (7) into the bottom of the cracking riser regenerator (10) and is regenerated by air fluidization burning at 500-750°C. The bottom of the cracking riser regenerator (10) is provided with a regeneration air inlet (9), and the top is provided with a gas-solid separator (1), a heat exchanger (11) and a regeneration flue gas outlet (12) in sequence. The regenerated catalyst is separated by the gas-solid separator (1) at the top of the cracking riser regenerator (10) and circulated back to the top of the descending cracking reactor (4) through the return controller (2) to catalytically crack the mixture of molten plastic liquid and crude oil.The high-temperature cracking oil and gas are directly sprayed into the gas phase feed hole in the upper part of the descending cracking reactor (8) without being condensed, and are rapidly mixed with the cracking regeneration catalyst falling from the top and undergo a controllable cracking reaction. The oil and gas gas-solid separation (5) is carried out at the bottom of the descending cracking reactor (8). The cracking reaction temperature is 570-650°C, the pressure is 0-0.3MPa, and the reaction time is 200 milliseconds to 1 second. The separated cracking catalyst to be regenerated flows into the bottom of the cracking riser regenerator (113) through a return device (7) and is regenerated by air fluidization at 600-750°C. The cracking riser regenerator (10) is provided with an air inlet (14) at the bottom and a gas-solid separator (1), a heat exchanger (11) and a regeneration flue gas outlet (15) at the top. The cracking regeneration catalyst separated by the gas-solid separator (1) at the top of the cracking riser regenerator (13) is circulated back to the top of the descending cracking reactor (13) through the return device (7) to catalytically crack the high-temperature cracking oil and gas. The high-temperature cracking oil and gas enter the fractionation tower (3) for separation. One line of the cracking dry gas pipeline at the top of the fractionation tower (3) is connected to the feed carrying gas inlet of the water-cooled feed pipe (23) at the top of the hot melt dechlorination reactor (20), and the other line is connected to the cracking gas refining system for producing triolefins. One line of the fractionation tower (16) refining pipeline is connected to the high-temperature molten oil inlet at the top of the hot melt dechlorination reactor (20), and the other line recovers the waste heat and is sent out as a product. Other side lines of the fractionation tower (16) are crude benzene fraction and diesel fraction.

[0021] The outer wall of the water-cooling feed pipe (23) is provided with a water-cooling jacket, which has a shape of a forward cone, a straight pipe or an inverted cone, preferably a forward cone.

[0022] The controllable feeder (22) is a rotary feeder, a double-shaft screw feeder or a single-shaft screw feeder.

[0023] The high-speed circulation pipe (26) is heated by electromagnetic induction heating, thermal oil heating, steam heating or resistance heating, preferably electromagnetic induction heating.

[0024] The cracking catalyst used in the descending cracking reaction tube (4) is a mixture of one or more of semi-coke microspheres, alumina microspheres, calcium aluminate porous microspheres, magnesium aluminum spinel porous microspheres, aluminum silicate porous microspheres, calcium silicate porous microspheres, magnesium silicate porous microspheres, and porous microsphere carriers loaded with alkali metals and / or alkaline earth metals.

[0025] The cracking catalyst used in the downlink cracking reactor (8) is a mixture of one or more of an FCC molecular sieve catalyst, a ZSM-5 type selective molecular sieve catalyst, and an alkaline solid porous catalyst.

[0026] The riser regenerator is composed of a turbulent fluidized bed at the bottom and an entrained reactor at the top. The turbulent fluidized bed has a larger equivalent diameter, while the entrained reactor has a smaller equivalent diameter, with a diameter ratio of 2 to 3:1. The entrained 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, with a diameter ratio of 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.

[0027] The process of producing chemicals by graded gas-phase dehydrogenation cracking of mixed feed of waste plastics and crude oil can continuously, efficiently and cleanly produce high-value-added chemicals such as trienes and triphenyls from waste plastics and crude oil on a large scale. It solves five common industry problems: adhesion and coking of waste plastic feed, difficulty in mixing with high-temperature catalysts, low yield and added value of liquid products, difficulty in scaling up pyrolysis equipment, and difficulty in subsequent processing of chlorine-containing liquid products. The triene yield is ≥50%, the triphenyl yield is ≥15%, the diesel yield is ≥20%, and the total liquid product yield is above 93% (including liquefied gas), which is more than 25 percentage points higher than the traditional waste plastic pyrolysis technology, ensuring safe, stable, full and excellent operation of the equipment.

Claims

1. The process for producing chemicals by graded gas phase dehydrogenation cracking of waste plastics and crude oil mixed feed, the technical characteristics of which are The clean PE and PP waste plastics that have been sorted are fed into a 20-95℃ water-cooled feed pipe through a waste plastic crusher and the waste plastic fragments are fed into the 240-320℃ oil slurry melt in a hot melt dechlorination reactor with stirring under the influence of cracking dry gas. The melt dechlorination and desulfurization pretreatment is carried out by stirring and mixing. The molten plastic liquid extracted from the bottom of the hot melt dechlorination reactor is pressurized and transported by a delivery pump. A part of the molten plastic liquid is heated to 20-60℃ higher than the oil slurry melt temperature through a high-speed circulation pipe with external heating and then returned to the upper part of the hot melt dechlorination reactor. The other part is sent to the upper part of the downward cracking reactor together with the crude oil as raw material through the atomizing feed nozzle. The gas extracted from the top of the hot melt dechlorination reactor is treated in the desulfurization and dechlorination reactor and then enters the refinery gas network as fuel gas. The flow rate of the high-speed circulation pipe is 2-30 m / s, the circulation ratio of the molten plastic liquid to the raw material is 1-10:1, and the steam dosage of the atomizing feed nozzle is 4wt%-12wt% of the raw material amount. The atomized particle feed of the mixture of the molten plastic liquid and crude oil is rapidly mixed, vaporized and controllably cracked by the cracking regeneration catalyst falling from the top of the descending cracking reactor. The steam dosage of the atomizing feed nozzle is 4wt%-12wt% of the raw material amount, the cracking reaction temperature is 500-550℃, the pressure is 0-0.3MPa, and the reaction time is 600 milliseconds to 2 seconds, and oil and gas-solid separation is carried out at the bottom of the descending cracking reactor; the separated catalyst to be regenerated flows into the bottom of the cracking riser regenerator through the return device and is regenerated by air fluidization at 500-750℃. The bottom of the cracking riser regenerator is provided with a regeneration air inlet, and the top is provided with a gas-solid separator, a heat exchanger and a regeneration flue gas outlet in sequence. The regenerated catalyst separated by the gas-solid separator at the top of the cracking riser regenerator is circulated back to the top of the descending cracking reactor through the return controller to catalytically crack the mixture of molten plastic liquid and crude oil; the high-temperature cracking oil and gas are not condensed and are directly sprayed into the gas phase feed hole in the upper part of the descending cracking reactor and mixed with the cracking regeneration catalyst falling from the top. The catalyst undergoes rapid mixing and controllable cracking reaction, and oil and gas are separated by gas-solid separation at the bottom of the descending cracking reactor. The cracking reaction temperature is 570-650°C, the pressure is 0-0.3MPa, and the reaction time is 200 milliseconds to 1 second. The separated cracking catalyst flows through a return device to the bottom of the cracking riser regenerator and is regenerated by air fluidization at 600-750°C. The bottom of the cracking riser regenerator is provided with an air inlet, and the top is provided with a gas-solid separator, a heat exchanger and a regenerated flue gas outlet in sequence. The cracking regenerated catalyst separated by the gas-solid separator at the top of the cracking riser regenerator is circulated back to the top of the descending cracking reactor through a return device to catalytically crack the high-temperature cracked oil and gas. The high-temperature cracking oil and gas enter the distillation tower for separation. The cracking dry gas at the top of the distillation tower is circulated back to the water-cooled feed pipe at the top of the hot-melt dechlorination reactor as feed carrier gas, and the other route is connected to the cracking gas refining system to produce trienes. The refining oil from the distillation tower is circulated back to the top of the hot-melt dechlorination reactor as high-temperature melting oil, and the other route is used to recover the waste heat and then be sent out as a product. The other side lines of the distillation tower are crude benzene fraction and diesel fraction.

2. The process for producing chemicals by gas phase dehydrogenation cracking of mixed feed of waste plastics and crude oil according to claim 1, characterized in that The outer wall of the water-cooled feed pipe is provided with a water-cooling jacket, which has a shape of a positive cone, a straight pipe or an inverted cone.

3. The process for producing chemicals by gas phase dehydrogenation cracking of mixed feed of waste plastics and crude oil according to claim 1, 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 producing chemicals by gas phase dehydrogenation cracking of mixed feed of waste plastics and crude oil according to claim 1, characterized in that The high-speed circulation tube is heated by electromagnetic induction heating, thermal oil heating, steam heating or resistance heating.

5. The process for producing chemicals by gas phase dehydrogenation cracking of mixed feed of waste plastics and crude oil according to claim 1, characterized in that The cracking catalyst is a mixture of one or more of semi-coke microspheres, alumina microspheres, calcium aluminate porous microspheres, magnesium aluminum spinel porous microspheres, aluminum silicate porous microspheres, calcium silicate porous microspheres, magnesium silicate porous microspheres, and porous microsphere carriers loaded with alkali metals and / or alkaline earth metals.

6. The process for producing chemicals by mixed feed of waste plastics and crude oil by graded gas phase dehydrogenation cracking according to claim 1, characterized in that The cracking catalyst is a mixture of one or more of an FCC molecular sieve catalyst, a ZSM-5 type selective molecular sieve catalyst, and an alkaline solid porous catalyst.

7. The process for producing chemicals by gas phase dehydrogenation cracking of mixed feed of waste plastics and crude oil according to claim 1, characterized in that The riser regenerator is composed of a turbulent fluidized bed at the bottom and an entrained reactor at the top. The ratio of the equivalent diameter of the turbulent fluidized bed to the equivalent diameter of the entrained reactor is 2 to 3:

1. The entrained 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. 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% to 50% of the equivalent diameter of the turbulent fluidized bed.

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