A catalytic conversion system

Abstract

This invention provides a catalytic conversion system comprising a first ascending bed reactor, a second ascending bed reactor, a settling tank, and a regenerator. The first ascending bed reactor has a first catalyst inlet and a first oil-catalyst mixture outlet. The second ascending bed reactor has a second catalyst inlet and a second oil-catalyst mixture outlet. The first oil-catalyst mixture outlet is connected to the lower part of the second ascending bed reactor. The settling tank is equipped with a settling zone baffle and a catalyst separator. Through this technical solution, this invention can construct different reaction environments using multiple reaction zones, separate the catalyst to achieve the use of suitable catalysts for different reactions, and regenerate the catalyst using different regeneration zones, thereby improving the yield of the target product. More specifically, this invention further improves the yield of ethylene and propylene from the catalytic cracking of heavy feedstock oil.

Description

Technical Field

[0001] This invention relates to the field of petrochemicals, specifically to a catalytic conversion system with catalyst gradation and zone control. Background Technology

[0002] In petrochemical production, different reaction environments can be constructed by using multiple reactors or multiple reaction zones. At the same time, different catalysts can be separated to allow different reactions to use appropriate catalysts, or different regeneration zones can be used to regenerate the catalysts, thereby improving the yield of the target product.

[0003] For example, CN110317628A discloses a catalyst partitioning integrated catalytic cracking method and apparatus. The apparatus includes a main reactor, a secondary reactor, a regenerator, and catalyst A and catalyst B storage tanks. Catalyst A and catalyst B initial swirl separators are installed above each of the two tanks. The regenerator is connected to the catalyst A initial swirl separator, the catalyst A initial swirl separator is connected to the catalyst B initial swirl separator, and the catalyst B initial swirl separator is connected to the regenerator. The bottom of the catalyst A storage tank is connected to the main reactor, and the bottom of the catalyst B storage tank is connected to the secondary reactor.

[0004] However, when existing catalytic cracking conversion systems are used to catalytically crack heavy feedstock oil to produce ethylene and propylene, it is still necessary to further increase the yield of ethylene and propylene. Summary of the Invention

[0005] The purpose of this invention is to further improve the yield of ethylene and propylene produced by catalytic cracking of heavy feedstock oil.

[0006] To achieve the above objectives, the present invention provides a catalytic conversion system comprising a first ascending bed reactor, a second ascending bed reactor, a settling tank, and a regenerator; the first ascending bed reactor has a first catalyst inlet and a first oil-electrolyte mixture outlet; the second ascending bed reactor has a second catalyst inlet and a second oil-electrolyte mixture outlet; the first oil-electrolyte mixture outlet is connected to the lower part of the second ascending bed reactor; the settling tank is provided with a settling partition and a catalyst separator, the settling partition dividing the settling zone into a first settling zone and a second settling zone; the catalyst separator is connected to the second oil-electrolyte mixture outlet. The regenerator has a material inlet, a first material outlet located in the first settling zone, and a second material outlet located in the second settling zone; the regenerator is provided with a regenerator baffle, which divides the regenerator into a first regeneration zone and a second regeneration zone in parallel; the first settling zone and the first regeneration zone are connected by a first catalyst transport connection; the second settling zone and the second regeneration zone are connected by a second catalyst transport connection; the first regeneration zone and the first ascending bed reactor are connected by a first regeneration catalyst transport connection; and the second regeneration zone and the second ascending bed reactor are connected by a second regeneration catalyst transport connection.

[0007] Through the above technical solution, this invention can construct different reaction environments using multiple reaction zones, separate catalysts to achieve different reactions using suitable catalysts, and regenerate the catalysts using different regeneration zones, thereby improving the yield of the target product. More specifically, this invention further improves the yield of ethylene and propylene from the catalytic cracking of heavy feedstock oil.

[0008] Other features and advantages of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0009] The accompanying drawings are provided to further illustrate the invention and form part of the specification. They are used together with the following detailed description to explain the invention, but do not constitute a limitation thereof. In the drawings:

[0010] Figure 1 This is a schematic diagram of the structure of a catalytic conversion system according to one embodiment of the present invention.

[0011] Figure 2 This is a schematic diagram of one embodiment of the reaction unit in this invention.

[0012] Figure 3 This is a schematic diagram of one embodiment of the reaction unit in this invention.

[0013] Figure 4This is a schematic diagram of one embodiment of the reaction unit in this invention.

[0014] Figure 5 This is a schematic diagram of one embodiment of the catalyst separation unit in this invention.

[0015] Figure 6 This is a schematic diagram of one embodiment of the catalyst separator in this invention.

[0016] Figure 7 This is a schematic diagram of one embodiment of the catalyst separator in this invention.

[0017] Figure 8 This is a schematic diagram of one embodiment of the catalyst separator in this invention.

[0018] Figure 9 This is a schematic diagram of one embodiment of the catalyst separator in this invention.

[0019] Figure 10 This is a schematic diagram of one embodiment of the regenerator in this invention.

[0020] Explanation of reference numerals in the attached figures

[0021] Figure 1-10 In the diagram, 1-1 is the first reaction zone, 1-2 is the second reaction zone, 11 is the first raw material, 12 is the pre-lifting gas, 13 is the second raw material, and 16 is the reaction oil-agent mixture; 2-1 is the first stripping zone, 2-2 is the first settling zone, 2-3 is the second settling zone, 2-4 is the second stripping zone, 21 is the stripping gas, 22 is the gas baffle, 23 is the first regenerator delivery pipe, 24 is the catalyst separator, 25 is the settling zone baffle, 26 is the second catalyst delivery pipe, 27 is the cyclone separator, 28 is the gas collection chamber, and 29 is the reaction oil-gas; 3-1 is the first regeneration zone, 3-2 is the second regeneration zone, 31 is the main air, 32 is the first regenerator delivery pipe, 33 is the second regenerator delivery pipe, 34 is the regeneration baffle, 35A and 35B are cyclone separators, 36 is the gas collection chamber, 37 is the regeneration flue gas, 38 is the second regenerator delivery pipe, and 30 and 39 are the stripping products. Detailed Implementation

[0022] The following provides a detailed description of specific embodiments of the present invention. It should be understood that the specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit the scope of the invention.

[0023] refer to Figure 1This invention provides a catalytic conversion system comprising a first rising bed reactor, a second rising bed reactor, a settling tank, and a regenerator. The first rising bed reactor has a first catalyst inlet and a first oil-electrolyte mixture outlet. The second rising bed reactor has a second catalyst inlet and a second oil-electrolyte mixture outlet. The first oil-electrolyte mixture outlet is connected to the lower part of the second rising bed reactor. The settling tank is provided with a settling partition and a catalyst separator, the settling partition dividing the settling zone into a first settling zone and a second settling zone. The catalyst separator has a material outlet connected to the second oil-electrolyte mixture outlet. The regenerator comprises an inlet, a first material outlet located in the first settling zone, and a second material outlet located in the second settling zone; the regenerator is provided with a regenerator baffle, which divides the regenerator into a first regeneration zone and a second regeneration zone in parallel; a first catalyst transport connection is provided between the first settling zone and the first regeneration zone; a second catalyst transport connection is provided between the second settling zone and the second regeneration zone; a first regeneration catalyst transport connection is provided between the first regeneration zone and the first ascending bed reactor; and a second regeneration catalyst transport connection is provided between the second regeneration zone and the second ascending bed reactor.

[0024] In this invention, the outlet of the first oil-agent mixture is connected to the lower part of the second ascending bed reactor, meaning the first and second ascending bed reactors are connected in series. This allows the materials undergoing the first catalytic conversion in the first ascending bed reactor (including the first catalyst, reaction oil and gas, and fluidizing medium) to enter the second ascending bed reactor without separation, contacting the second catalyst for the second catalytic conversion reaction. This enables the relay of the first and second catalytic conversion reactions. The catalyst separator separates the materials undergoing the second catalytic conversion in the second ascending bed reactor (including the first catalyst, second catalyst, reaction oil and gas, and fluidizing medium), allowing the catalyst with the larger particle size and density to enter the first settling zone, while the catalyst with the smaller particle size and density enters the second settling zone with the reaction oil and gas and fluidizing medium. Subsequently, the catalyst with the larger density is regenerated in the first regeneration zone, and the catalyst with the smaller density is regenerated in the second regeneration zone, thus achieving independent regeneration of the first and second catalysts. The independently regenerated first and second catalysts are then returned to the first and second ascending bed reactors, respectively, to participate in the reaction again. This invention provides a catalytic conversion system with catalyst gradation and zone control, creating a suitable reaction environment for the relay reaction of single or multiple feedstocks, thereby improving the yield of target products, especially the yield of ethylene and propylene produced by catalytic cracking of heavy feedstock oil.

[0025] Optionally, in operation, the first rising bed reactor contains an upward-moving first catalyst; the second rising bed reactor contains an upward-moving second catalyst and an upward-moving first catalyst; the particle size and density of the first catalyst are different from those of the second catalyst, and the density of the first catalyst is greater than that of the second catalyst. The catalyst separator separates the first catalyst from the second catalyst based on the density difference between the two catalysts. The first settling zone is located below the settling zone partition, and the second settling zone is located above the settling zone partition.

[0026] Optionally, the lower part of the first rising bed reactor is further provided with a first feedstock inlet and a fluidizing medium inlet; the lower part of the second rising bed reactor is further provided with a second feedstock inlet. The first feedstock inlet can be used to introduce heavy feedstock. The second feedstock inlet can be used to introduce light feedstock. As an embodiment where the first regeneration zone and the first rising bed reactor have a first regenerated catalyst transport connection, the lower part of the first rising bed reactor is further provided with a first catalyst inlet, which can be used to introduce fresh first catalyst or regenerated first catalyst. As an embodiment where the second regeneration zone and the second rising bed reactor have a second regenerated catalyst transport connection, the lower part of the second rising bed reactor is further provided with a second catalyst inlet, which can be used to introduce fresh second catalyst or regenerated second catalyst.

[0027] Optionally, the first and second rising bed reactors are each independently a riser reactor, a fast bed reactor, or a fluidized bed reactor. In one embodiment, the diameters of the first and second rising bed reactors can be adjusted so that the material in the first rising bed reactor enters the second rising bed reactor, and the material in the second rising bed reactor enters the catalyst separator.

[0028] In one implementation, reference Figure 2Both the first and second ascending bed reactors are equal-diameter riser reactors. The first regeneration catalyst from the first regeneration zone 3-1 is introduced into the bottom of the first ascending bed reactor (riser reactor) 1-1 via the first regenerator delivery pipe 32. It is then introduced into the first ascending bed reactor (riser reactor) 1-1 via pre-lift gas 12, where it reacts with the first feedstock 11 from the first ascending bed reactor (riser reactor) 1-1. The resulting first oil-based mixture is introduced into the bottom of the second ascending bed reactor (riser reactor) 1-2. The second regeneration catalyst from the second regeneration zone 3-2 is introduced into the bottom of the second ascending bed reactor (riser reactor) 1-2 via the second regenerator delivery pipe 33. It reacts with the first reaction oil-based mixture from the bottom of the second ascending bed reactor (riser reactor) 1-2 and the second feedstock 13. The resulting reaction oil-based mixture is then introduced into a catalyst separator for separation.

[0029] In one implementation, reference Figure 3 The first rising bed reactor is a constant diameter riser reactor, and the second rising bed reactor is a rapid bed reactor.

[0030] In one implementation, reference Figure 4 The first rising bed reactor is a riser reactor with equal diameter, and the second rising bed reactor is a fluidized bed reactor.

[0031] Optionally, refer to Figure 5 The catalyst separator 24 is fixed on the settling zone partition 25.

[0032] Optionally, part or all of the second rising bed reactor may be located within the first settling zone or the second settling zone. For example, the horizontal tube 16 of the second rising bed reactor may be located within the second settling zone.

[0033] Optionally, the catalyst separator is one or more of the following combinations: cyclone rapid separator, three-lobe rapid separator, catapult rapid separator, U-shaped tube separator, and wall-mounted cutting rapid separator, preferably a cyclone rapid separator; the number of catalyst separators in each settling tank is one or more; the multiple catalyst separators are connected in series and / or in parallel.

[0034] In one implementation, reference Figure 6 In the catalyst separator, the material inlet is located on the side of the catalyst separator, the first material outlet is located at the bottom of the catalyst separator, and the second material outlet is located at the top of the catalyst separator.

[0035] In one implementation, reference Figure 7In the catalyst separator, the material inlet is located at the bottom of the catalyst separator, the first material outlet is located on the side of the catalyst separator, and the second material outlet is located at the top of the catalyst separator.

[0036] In one implementation, reference Figure 8 and Figure 9 In the catalyst separator, the material inlet is located at the top, the first material outlet is located at the bottom, and the second material outlet is located on the side. The second material outlet can be configured as a type of movable louvers, the number and angle of which can be adjusted to control its flow rate.

[0037] Optionally, a stripping device may be installed downstream of the first settling zone and the second settling zone (either inside or outside the first catalyst delivery connection or the second catalyst delivery connection) to extract the oil and gas products attached to the catalyst.

[0038] In one implementation, reference Figure 5 A first stripper 2-1 is provided at the lower part of the first settling zone 2-2; a first stripping material outlet is provided at the upper part of the first settling zone 2-2; the first stripping material outlet is connected to the pipeline 30.

[0039] In one implementation, reference Figure 5 The second catalyst delivery connection 26 is provided with a second stripper 2-4; the upper part of the second stripper 2-4 is also provided with a second stripping material outlet; the second stripping material outlet is connected to the pipeline 39.

[0040] In one implementation, reference Figure 5 The settling device includes a first stripping zone 2-1, a first settling zone 2-2, a second settling zone 2-3, a second stripping zone 2-4, and a catalyst separator 24. A second oil-catalyst mixture 16 from the second ascending bed reactor is introduced into the catalyst separator 24. Based on the particle size distribution and density of the catalyst, the second oil-catalyst mixture 16 is divided into a first catalyst with a larger particle size distribution and higher particle density, a second catalyst with a smaller particle size distribution and lower particle density, and reaction oil and gas. The first catalyst is introduced into the first stripping zone via the first settling zone 2-2. After stripping in step 2-1, the first catalyst to be recycled is obtained. The first catalyst to be recycled is introduced into the first regeneration zone 3-1 for regeneration through the first catalyst delivery pipe 23. The second catalyst is introduced into the second stripping zone 2-4 through the second settling zone 2-3 for stripping to obtain the second catalyst to be recycled. The second catalyst to be recycled is introduced into the second regeneration zone 3-2 for regeneration through the second catalyst delivery pipe 38. The stripping gas 30 in the first stripping zone 2-1 and the stripping gas 39 in the second stripping zone 2-4 are both introduced into the gas collecting chamber 28 and led out of the system together with the reaction oil and gas 29.

[0041] Optionally, refer to Figure 10 The first regeneration zone 3-1 and the second regeneration zone 3-2 are arranged side by side.

[0042] Optionally, refer to Figure 10 The upper parts of the first regeneration zone 3-1 and the second regeneration zone 3-2 are connected; the first regeneration zone 3-1 and the second regeneration zone 3-2 are respectively provided with gas-solid separators 35A and 35B; the upper edge of the regenerator partition 34 is higher than the solid outlet of the gas-solid separators 35A and 35B.

[0043] refer to Figure 10 In one embodiment, the regenerator 3 includes a first regeneration zone 3-1, a second regeneration zone 3-2, and a regeneration baffle 34. A first spent catalyst from the first stripping zone 2-1 is introduced into the first regeneration zone 3-1 through a first spent catalyst delivery pipe 23, where it contacts the main air from the bottom of the first regeneration zone 3-1 and undergoes a regeneration reaction. The resulting first regeneration catalyst is introduced into the first reaction zone 1-1 for recycling through a first regenerator delivery pipe 32. The regenerated flue gas 37 is led out of the regeneration unit 3 through a gas collection chamber 36. A second spent catalyst from the second stripping zone 2-4 is introduced into the second regeneration zone 3-2 through a second spent catalyst delivery pipe 38, where it contacts the main air from the bottom of the second regeneration zone 3-2 and undergoes a regeneration reaction. The resulting second regeneration catalyst is introduced into the second reaction zone 1-2 for recycling through a second regeneration delivery pipe 33. The regenerated flue gas 37 is led out of the regenerator 3 through a gas collection chamber 36.

[0044] The present invention will be further described in detail below through embodiments. Unless otherwise specified, the raw materials used in the embodiments are all commercially available.

[0045] In the embodiments and comparative examples of this invention, the gaseous products were tested using the RIPP 77-90 method for petrochemical analysis, the coke content was determined using the RIPP 107-90 method for petrochemical analysis, the composition of the organic liquid products was determined using the SH / T0558-1993 method, the fraction cut-off points of gasoline and diesel were 221℃ and 343℃, respectively, and the light aromatics in gasoline were determined using the RIPP 82-90 method for petrochemical analysis.

[0046] The conversion rate is calculated as follows:

[0047] Conversion rate = (weight of dry gas + weight of liquefied gas + weight of gasoline + weight of coke) / weight of fresh feedstock × 100%;

[0048] The yield is calculated as follows:

[0049] Yield = Weight of product separated from reaction products / Weight of fresh feedstock oil × 100%;

[0050] The RIPP petrochemical analysis method used in this invention is selected from "Petrochemical Analysis Methods (RIPP Test Methods)", edited by Yang Cuiding et al., Science Press, 1990.

[0051] Unless otherwise specified, all reagents used below are chemically pure.

[0052] Two catalysts, GOR-II and RAG-6, were used in the examples and comparative examples. Both were commercial catalysts produced by Sinopec Catalyst Company, Qilu Branch. The specific properties of the two catalysts are shown in Table 1. GOR-II is a catalyst containing 40% by weight of Y molecular sieve, and RAG-6 is a catalyst containing 35% by weight of ZSM-5 molecular sieve. The catalysts were aged at 800°C and 100% steam for 17 hours prior to the experiment.

[0053] Table 1 Composition and properties of catalysts

[0054] catalyst GOR-II RAG-6 Chemical composition, % (w) <![CDATA[Al2O3]]> 57.5 51.2 <![CDATA[SiO2]]> 36.1 43.1 BET Full Analysis <![CDATA[ BET total surface area / (m 2 ·g -1 )]]> 181.000 197.000 <![CDATA[Micropore area / (m 2 ·g -1 )]]> 104.000 98.000 <![CDATA[Total pore volume / (cm 3 ·g -1 )]]> 0.224 0.150 <![CDATA[Micropore volume / (cm 3 ·g -1 )]]> 0.034 0.045 <![CDATA[Particle density / (kg / m 3 )]]> 1352 965 Particle size distribution, % (w) 0-20μm 0.1 0.5 0-40μm 5.1 32.6 0-80μm 20.3 87.3 0-105μm 50.6 98.5 >105μm 49.4 1.5

[0055] The raw materials used in Examples 1-2 and Comparative Examples 1-2 were wax oil and light gasoline, and their specific properties are shown in Tables 2 and 3.

[0056] Table 2 Composition and Properties of Wax Oils

[0057]

[0058]

[0059] Table 3 Composition and properties of light gasoline

[0060] project Light gasoline <![CDATA[Density (20 °C) / (kg / m 3 )]]> 635.1 Elemental mass composition / % carbon 84.76 hydrogen 15.24 Sulfur / (μg / g) 46.29 Nitrogen (μg / g) 32 Distillation range / ℃ Initial boiling point 12 10v％ 18 30v％ 30 50v％ 35 70v％ 57 90v％ 59 Final boiling point 60 Mass family composition / % Alkanes 37.19 Olefins 62.49 Cycloalkanes 0.32 Aromatics 0

[0061] Example 1

[0062] refer to Figure 1 , 3Unit 10 comprises a riser reactor and a fluidized bed reactor. The riser reactor has an inner diameter of 16 mm and a length of 3200 mm, while the fluidized bed reactor has an inner diameter of 64 mm and a height of 500 mm. A catalyst separator is located inside the settler and can separate the catalyst into two parts with different particle densities. Preheated wax oil and the first catalyst (GOR-II catalyst) were both introduced into the bottom of the riser reactor, where they reacted. The resulting oil-catalyst mixture was then introduced into a fluidized bed reactor, where it reacted with the second catalyst (RAG-6 catalyst). The reacted oil-catalyst mixture then entered a catalyst separator. The first catalyst (GOR-II catalyst), with its higher density, was separated into the first settling zone, while the second catalyst (RAG-6 catalyst), with its lower density, was separated into the second settling zone along with the reacted oil and gas. The mixture was then separated by a cyclone separator. The first catalyst (GOR-II catalyst) and the second catalyst (RAG-6 catalyst) were stripped and introduced into the first and second regeneration zones of the regenerator, respectively. The regenerated catalysts were returned to the riser reactor and the fluidized bed reactor for recycling. The oil and gas were introduced into a fractionation system for separation. The reaction conditions and results are shown in Table 4.

[0063] Comparative Example 1

[0064] The method is the same as in Example 1, except that the catalysts used in both the first and second reaction zones are mixed catalysts obtained by mixing GOR-II and RAG-6 catalysts in a mass ratio of 1:1. The mixed catalyst is added to the second reaction zone. The two catalysts are not separated or independently regenerated in the catalytic conversion system. The reaction conditions and results are shown in Table 4.

[0065] Example 2

[0066] The method was the same as in Example 1, except that preheated light gasoline was introduced into the second reaction zone. The reaction conditions and results are shown in Table 4.

[0067] Comparative Example 2

[0068] The method was the same as in Comparative Example 2, except that preheated light gasoline was introduced into the middle of the reactor. The reaction conditions and results are shown in Table 4.

[0069] Table 4. Reaction conditions and results of Examples 1-2 and Comparative Examples 1-2

[0070]

[0071]

[0072] As shown in Table 4, compared with the comparative example, the catalytic conversion system provided by the present invention can improve the yield of low-carbon olefins such as ethylene and propylene.

[0073] The preferred embodiments of the present invention have been described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within the scope of the technical concept of the present invention, various simple modifications can be made to the technical solution of the present invention, and these simple modifications all fall within the protection scope of the present invention.

[0074] It should also be noted that the various specific technical features described in the above embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the present invention will not describe the various possible combinations separately.

[0075] Furthermore, various different embodiments of the present invention can be combined in any way, as long as they do not violate the spirit of the present invention, they should also be regarded as the content disclosed by the present invention.

Claims

1. A catalytic conversion system, characterized in that, The catalytic conversion system includes a first rising bed reactor, a second rising bed reactor, a settling tank, and a regenerator; the first rising bed reactor has a first catalyst inlet and a first oil-electrolyte mixture outlet; the second rising bed reactor has a second catalyst inlet and a second oil-electrolyte mixture outlet; the first oil-electrolyte mixture outlet is connected to the lower part of the second rising bed reactor; The settling device is provided with a settling zone partition and a catalyst separator. The settling zone partition divides the settling zone into a first settling zone and a second settling zone. The catalyst separator has a material inlet communicating with the outlet of the second oil-agent mixture, a first material outlet opened in the first settling zone, and a second material outlet opened in the second settling zone. The regenerator is equipped with a regenerator partition, which divides the regenerator into a first regeneration zone and a second regeneration zone in parallel; the first settling zone and the first regeneration zone are connected by a first catalyst supply connection; the second settling zone and the second regeneration zone are connected by a second catalyst supply connection; the first regeneration zone and the first rising bed reactor are connected by a first regeneration catalyst supply connection; the second regeneration zone and the second rising bed reactor are connected by a second regeneration catalyst supply connection. In operation, the first upward bed reactor contains an upward-moving first catalyst; The second upward bed reactor has an upward-moving second catalyst and an upward-moving first catalyst; the particle size and density of the first catalyst are both greater than those of the second catalyst.

2. The catalytic conversion system according to claim 1, wherein, The first settling zone is located below the settling zone partition, and the second settling zone is located above the settling zone partition.

3. The catalytic conversion system according to claim 1 or 2, wherein, The lower part of the first rising bed reactor is also provided with a first feed oil inlet and a fluidizing medium inlet; the lower part of the second rising bed reactor is also provided with a second feed oil inlet.

4. The catalytic conversion system according to claim 1 or 2, wherein, The first rising bed reactor and the second rising bed reactor are each independently a riser reactor, a fast bed reactor, or a fluidized bed reactor.

5. The catalytic conversion system according to claim 1 or 2, wherein, The catalyst separator is fixed to the settling zone partition plate; The second ascending bed reactor is partially or entirely located in the first settling zone or the second settling zone.

6. The catalytic conversion system according to claim 1 or 2, wherein, The catalyst separator is one or more of the following combinations: cyclone rapid separator, three-lobe rapid separator, catapult rapid separator, U-shaped tube separator, and wall-mounted cutting rapid separator; The number of catalyst separators in each settling tank is one or more; the multiple catalyst separators are connected in series and / or in parallel.

7. The catalytic conversion system according to claim 6, wherein, The catalyst separator is a cyclone rapid separator.

8. The catalytic conversion system according to claim 1 or 2, wherein, A second stripper is provided at the lower part of the second settling zone; a second stripping material outlet is provided at the upper part of the second settling zone.

9. The catalytic conversion system according to claim 8, wherein, The first catalyst delivery connection is equipped with a first stripper; the first stripper is also equipped with a first stripped material outlet at its upper part.

10. The catalytic conversion system according to claim 1 or 2, wherein, The first regeneration zone and the second regeneration zone are arranged side by side.

11. The catalytic conversion system according to claim 10, wherein, The upper parts of the first regeneration zone and the second regeneration zone are connected; the first regeneration zone and the second regeneration zone are respectively provided with gas-solid separators; the upper edge of the regenerator partition is higher than the solid outlet of the gas-solid separator.

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