A catalytic conversion system with a series reactor and a catalyst separator

Abstract

This invention provides a catalytic conversion system with a series reactor and catalyst separator. The system includes a first rising bed reactor, a second rising bed reactor, a settling tank, a catalyst separator, and a regenerator. Through this technical solution, the invention can construct different reaction environments using multiple reaction zones, separate the catalyst to allow for 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 dehydrogenation cracking of low-carbon alkanes.

Description

Technical Field

[0001] This invention relates to the field of petrochemicals, and more specifically to a catalytic conversion system having a series reactor and a catalyst separator. Background Technology

[0002] To improve economic efficiency, petrochemical plants need to have the ability to process products further. However, a single reactor is often insufficient to meet this requirement. Therefore, it is necessary to connect and combine single reactors of the same or different types and sizes in series.

[0003] For example, CN104560149A discloses a catalytic conversion method for producing butene. This method uses four reactors. In addition to a double-riseer plus fluidized bed reactor configuration, a fluidized bed reactor is installed outside the settling tank for cracking the gasoline fraction. The reaction products enter the riser reactor for further cracking. The catalyst after the reaction is regenerated by coke burning and then returned to the reactor for recycling. This method uses a mixture containing γ-zeolite and β-zeolite as a catalyst and can achieve high yields of propylene and butene.

[0004] However, when existing catalytic cracking conversion systems are used to dehydrogenate and crack low-carbon alkanes 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 dehydrogenation cracking of low-carbon alkanes.

[0006] To achieve the above objectives, the present invention provides a catalytic conversion system with a series reactor and a catalyst separator. The catalytic conversion system includes a first rising bed reactor, a second rising bed reactor, a settling tank, a catalyst separator, and a regenerator. The first rising bed reactor has a first catalyst inlet and a first oil-catalyst mixture outlet. The second rising 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 rising bed reactor. The settling tank has an oil-catalyst mixture inlet and a mixed catalyst outlet, the oil-catalyst mixture inlet being connected to the second oil-catalyst mixture outlet. The catalyst separator... The separator has a material inlet connected to the outlet of the mixed spent catalyst, a first spent catalyst outlet, and a second spent catalyst outlet; the regenerator is provided with a regenerator baffle, which divides the regenerator into a first regeneration zone and a second regeneration zone; the first spent catalyst outlet is connected to the first regeneration zone by a first spent catalyst conveying connection; the second spent catalyst outlet is connected to the second regeneration zone by a second spent catalyst conveying connection; the first regeneration zone is connected to the first ascending bed reactor by a first regenerated catalyst conveying connection; and the second regeneration zone is connected to the second ascending bed reactor by a second regenerated catalyst conveying connection.

[0007] Through the above technical solution, the present invention can construct different reaction environments using multiple reaction zones, separate catalysts to achieve different reactions using suitable catalysts, and regenerate catalysts using different regeneration zones, thereby improving the yield of the target product. More specifically, the present invention further improves the yield of ethylene and propylene from the dehydrogenation cracking of low-carbon alkanes.

[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 stripper, 2-2 is the settling device, 21 is the stripping gas, 22 is the gas baffle, 23 is the mixed regenerated agent conveying pipe, 24 is the primary catalyst separator, 25 is the catalyst conveying pipe, 26 is the secondary catalyst separator, 27 is the residual reaction oil and gas, 28 is the gas-solid separation device, 29 is the gas collecting chamber, and 30 is the reaction oil and gas; 3-1 is the first regeneration zone, 3-2 is the second regeneration zone, 31 is the main air, 32 is the first regenerated agent conveying pipe, 33 is the second regenerated agent conveying pipe, 34 is the regeneration baffle, 35 is the cyclone separator, 36 is the gas collecting chamber, 37 is the regenerated flue gas, 38 is the first regenerated agent conveying pipe, and 39 is the second regenerated agent conveying pipe. 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 with a series reactor and a catalyst separator. The catalytic conversion system includes a first rising bed reactor, a second rising bed reactor, a settling tank, a catalyst separator, and a regenerator. The first rising bed reactor has a first catalyst inlet and a first oil-catalyst mixture outlet. The second rising 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 rising bed reactor. The settling tank has an oil-catalyst mixture inlet and a mixed catalyst outlet, the oil-catalyst mixture inlet being connected to the second oil-catalyst mixture outlet. The catalyst separator has… The regenerator includes a material inlet, a first catalyst outlet, and a second catalyst outlet connected to the outlet of the mixed catalyst; a regenerator baffle is provided in the regenerator, which divides the regenerator into a first regeneration zone and a second regeneration zone; a first catalyst conveying connection is established between the first catalyst outlet and the first regeneration zone; a second catalyst conveying connection is established between the second catalyst outlet and the second regeneration zone; a first regeneration catalyst conveying connection is established between the first regeneration zone and the first ascending bed reactor; and a second regeneration catalyst conveying connection is established between the second regeneration zone and the second ascending bed reactor.

[0024] In this invention, the reaction unit may include a first ascending bed reactor and a second ascending bed reactor. The outlet of the first oil-catalyst 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 that have undergone the first catalytic conversion in the first ascending bed reactor (including the first catalyst, reacting oil and gas, and fluidizing medium) to enter the second ascending bed reactor without separation and contact the second catalyst for a second catalytic conversion reaction. This enables the relay of the first and second catalytic conversion reactions. The catalyst separation unit may include the settling tank and the catalyst separator. The settling tank can perform gas-solid separation and stripping on the materials that have undergone the second catalytic conversion in the second ascending bed reactor (including the first catalyst, the second catalyst, reacting oil and gas, and fluidizing medium) to obtain oil and gas products and a mixed catalyst to be recycled. The catalyst separator can separate the mixed catalyst to be recycled, allowing the catalyst with the larger particle size and density to enter the first regeneration zone, while the catalyst with the smaller particle size and density enters the second regeneration zone. Subsequently, the catalyst with the larger particle size and density from the first and second catalysts is regenerated in the first regeneration zone, while the catalyst with the smaller particle size and 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 rising 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 the target product, particularly increasing the yield of ethylene and propylene from the dehydrogenation cracking of low-carbon alkanes.

[0025] Optionally, in operation, the first upward-flowing bed reactor contains an upward-flowing first catalyst; the second upward-flowing bed reactor contains an upward-flowing second catalyst and an upward-flowing first catalyst; the particle size and density of the first catalyst are different from those of the second catalyst, and the particle size and density of the first catalyst are greater than those of the second catalyst. The catalyst separator separates the first catalyst from the second catalyst based on the difference in particle size and density between the first catalyst and the second catalyst. In the catalyst separator, the outlet of the first spent catalyst is located below the outlet of the second spent catalyst.

[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 low-carbon alkanes. The second feedstock inlet can be used to introduce olefins. 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 moving 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 moving bed reactors can be adjusted so that material in the first moving bed reactor enters the second moving bed reactor, and material in the second moving bed reactor enters the settling tank.

[0028] In one implementation, reference Figure 2 Both 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-lifting 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 settling tank 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 4The 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 is located outside the settler.

[0032] Optionally, part or all of the second rising bed reactor is disposed within the settling tank. For example, the horizontal tube 16 of the second rising bed reactor is disposed within the settling tank.

[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 connected to the outside of 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 7 In 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] In one implementation, reference Figure 5 The settling device is externally connected to a primary catalyst separator. The lower part of the primary catalyst separator has a first outlet for the spent catalyst, and the upper part of the primary catalyst separator has a light material outlet. The light material outlet is connected to the material inlet of the secondary catalyst separator. The upper part of the secondary catalyst separator is provided with a residual reaction oil and gas outlet, and the lower part of the secondary catalyst separator is provided with a second outlet for the spent catalyst.

[0038] In one implementation, reference Figure 5The lower part of the settling device 2-2 is provided with a stripper 2-1; the upper part of the settling device 2-2 is provided with an oil and gas product outlet; and the interior of the settling device is also provided with a gas-solid separation device.

[0039] In one implementation, reference Figure 5 The reaction oil mixture 16 from the second ascending bed reactor is introduced into the rapid separation device 28 of the settling tank 2-2. The resulting reaction oil gas 30 is introduced into the subsequent product separation unit (not shown in the figure) through the gas collecting chamber 29. The resulting mixed spent catalyst is introduced into the stripper 2-1 for stripping. The stripped mixed spent catalyst is introduced into the catalyst separator 24. According to the particle size distribution and particle density of the catalyst, the spent catalyst is divided into a first spent catalyst with a larger particle size distribution and a larger particle density, and a second spent catalyst with a smaller particle size distribution and a smaller particle density. The first spent catalyst is introduced into the first regeneration zone 3-1 for regeneration through the first spent catalyst delivery pipe 38, and the second spent catalyst is introduced into the second regeneration zone 3-2 for regeneration through the second spent catalyst delivery pipe 39. The gas remaining in the catalyst separator is introduced into the gas collecting chamber 29 and led out of the system together with the reaction oil gas 30.

[0040] Optionally, refer to Figure 10 The first regeneration zone 3-1 and the second regeneration zone 3-2 are connected in series, with the first regeneration zone 3-1 located below the second regeneration zone 3-2.

[0041] Optionally, refer to Figure 10 The regenerator partition is provided with a first regenerated flue gas outlet.

[0042] In one implementation, reference Figure 10The regenerator includes a first regeneration zone 3-1, a second regeneration zone 3-2, and a regeneration baffle 34. A first regenerated catalyst from the catalyst separator is introduced into the first regeneration zone 3-1 through a first regenerated catalyst delivery pipe 38, where it contacts the main air from the bottom of the first regeneration zone 3-1 and undergoes a first regeneration reaction to generate a first regeneration catalyst and first regeneration flue gas. The generated first regeneration catalyst is introduced into the first reaction zone 1-1 for recycling through a first regeneration catalyst delivery pipe 32, and the first regeneration flue gas is introduced into the second regeneration zone 3-2 through the regeneration baffle 34. A second regenerated catalyst from the catalyst separator 24 is introduced into the second regeneration zone 3-2 through a second regenerated catalyst delivery pipe 39, where it contacts the first regeneration flue gas from the first regeneration zone 3-1 and undergoes a second regeneration reaction to generate a second regeneration catalyst and second regeneration flue gas. The generated second regeneration catalyst is introduced into the second reaction zone 1-2 for recycling through a second regeneration catalyst delivery pipe 33, and the second regeneration flue gas 37 is led out of the regenerator 3 through a gas collection chamber 36. The first regeneration is an incomplete regeneration, and the second regeneration is a complete regeneration. That is, the first regenerated flue gas obtained in the first regeneration zone 3-1 is introduced into the second regeneration zone 3-2 to undergo a regeneration reaction with the second catalyst.

[0043] The system with a series reactor and catalyst separator provided by the present invention can be operated in the following manner, which includes: a first feedstock oil 11 is preheated to 100-150°C and then sprayed into the bottom of the first riser reaction zone 1-1 through a nozzle. Under the conditions of a reaction temperature of 520-720°C, preferably 560-660°C, an oil-to-catalyst ratio of 2-25, preferably 3-20, and a reaction time of 1-15 seconds, preferably 2-10 seconds, the feedstock oil comes into contact with and reacts with a first catalyst introduced into the bottom of the first riser reaction zone 1-1 through a first regenerator delivery pipe 32. The resulting first oil-to-catalyst mixture is then introduced into the second riser reaction zone 1-2. After the second feedstock oil 13 is preheated to 100-150°C, it is sprayed into the bottom of the reaction zone 1-2 of the second riser through a nozzle. Under the conditions of a reaction temperature of 500-700°C, preferably 540-640°C, an oil-to-catalyst ratio of 2-25, preferably 3-20, and a reaction time of 1-15 seconds, preferably 2-10 seconds, it comes into contact with and reacts with the second catalyst introduced into the bottom of the reaction zone 1-2 of the second riser through the second regenerator conveying pipe 33, and the first oil-to-catalyst mixture from the reaction zone 1-1 of the first riser. The resulting oil-to-catalyst mixture is introduced into the rapid separation device 28 of the settling tank 2-2. The resulting reaction oil gas 30 is led out through the gas collecting chamber 29. The resulting mixed spent catalyst is introduced into the stripper 2-1 for stripping. The stripped mixed spent catalyst is introduced into the catalyst separator 24. The first spent catalyst obtained is introduced into the first regeneration zone 3-1 for regeneration through the first spent catalyst conveying pipe 38, and the second spent catalyst is introduced into the second regeneration zone 3-2 for regeneration through the second spent catalyst conveying pipe 39. The regenerated first and second regenerated catalysts are introduced into the bottom of the first riser reaction zone 1-1 and the second riser reaction zone 1-2 through the first regenerator delivery pipe 32 and the second regenerator delivery pipe 33, respectively, for recycling.

[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] The catalysts used in the examples and comparative examples were dehydrogenation catalyst DH-1 and cracking catalyst RAG-6. The chemical composition and properties of the two catalysts are shown in Table 1. The raw materials used included n-octane with a purity of 99.5%; C5-C8 alkanes, the composition of which is shown in Table 2; and C5-C8 olefins, the composition of which is shown in Table 3.

[0046] Table 1. Composition and properties of catalysts

[0047] project DH-1 RAG-6 Chemical composition / % <![CDATA[Al2O3]]> 93.4 51.2 <![CDATA[SiO2]]> 1.2 43.1 <![CDATA[K2O]]> 0.375 0.253 <![CDATA[P2O5]]> 1.34 <![CDATA[Fe2O3]]> 0.106 0.80 <![CDATA[Cr2O3]]> <![CDATA[Re2O3]]> 0.29 <![CDATA[Ga2O3]]> 3.06 BET Full Analysis <![CDATA[ BET total surface area / (m 2 ·g -1 )]]> 136.752 197.000 <![CDATA[Total pore volume / (cm 3 ·g -1 )]]> 0.4680 0.150 <![CDATA[Particle density / (kg / m 3 )]]> 1218 965 Particle size distribution, % (w) 0-20μm 0.1 0.5 0-40μm 4.2 32.6 0-80μm 18.5 87.3 0-105μm 45.7 98.5 >105μm 54.3 1.5

[0048] Table 2 Composition of C5-C8 alkanes

[0049] project mass fraction / % n-Pentane 15.68 isopentane 21.25 n-Hexane 9.25 isohexane 3.64 n-Heptane 8.12 Isoheptane 12.89 n-Octane 19.33 Isooctane 9.84 total 100.00

[0050] Table 3 Composition of C5-C8 olefins

[0051] project mass fraction / % n-pentene 21.08 Isoprene 12.96 n-Hexene 11.25 Isohexene 4.33 n-Heptene 6.44 Isoheptene 11.42 n-Octene 20.85 Isooctene 11.67 total 100.00

[0052] Example 1

[0053] The device 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 outside the settling tank and can separate the catalyst into two fractions with different particle sizes and densities. Preheated n-octane and the first catalyst are introduced to the bottom of the riser reactor, where they react in contact. The resulting oil-catalyst mixture is introduced into the fluidized bed reactor, where it contacts the second catalyst and continues to react. The resulting oil-catalyst mixture is then separated by a cyclone separator. The catalyst is stripped in the settling tank and stripper before being introduced into the catalyst separator, where it is separated into a first catalyst rich in DH-1 catalyst and a second catalyst rich in RAG-6 catalyst. The two catalysts are then introduced into the first and second regeneration zones of the regenerator, respectively. The regenerated catalyst is returned to the riser reactor and the fluidized bed reactor for recycling. The oil and gas are introduced into a fractionation system for separation. The reaction conditions and results are shown in Table 4.

[0054] Comparative Example 1

[0055] The method described in Example 1 was followed, except that RAG-6 catalyst was used in both the riser reactor and the fluidized bed reactor. The reaction conditions and results are shown in Table 4.

[0056] Table 4. Reaction conditions and results of Example 1 and Comparative Example 1

[0057] project Example 1 Comparative Example 1 riser Raw material 1 n-Octane n-Octane catalyst First catalyst First catalyst DH-1 content in catalyst / weight % 96 0 RAG-6 content in catalyst / weight % 4 100 Outlet temperature / °C 650 650 Agent-to-oil ratio 13 11 reaction time / s 4 4 fluidized bed catalyst Second catalyst Second catalyst DH-1 content in catalyst / weight % 8 0 RAG-6 content in catalyst / weight % 92 100 Outlet temperature / °C 600 600 Agent-to-oil ratio 13 11 <![CDATA[airspeed / h -1 > 8 9 Regeneration temperature / °C 680 680 Ethylene yield / wt% 13.12 5.71 propylene yield / wt% 16.74 10.98

[0058] Example 2

[0059] The device comprises two riser reactors, each with an inner diameter of 16 mm and a length of 3200 mm. A catalyst separator, located outside the settler, separates the catalyst into two fractions with different particle sizes and densities. Preheated C5-C8 alkanes and the first catalyst are introduced to the bottom of the first riser reactor, where they react in contact. The resulting oil-catalyst mixture is introduced into the second riser reactor, where it reacts with the second catalyst. The oil-catalyst mixture is then separated by a cyclone separator. The catalyst is stripped in the settler and stripper before being introduced into the catalyst separator, where it is separated into a first catalyst rich in DH-1 catalyst and a second catalyst rich in RAG-6 catalyst. These two catalysts are then introduced into the first and second regeneration zones of the regenerator, respectively. The regenerated catalyst is returned to the first and second riser reactors for recycling. The oil and gas are introduced into a fractionation system for separation. The reaction conditions and results are shown in Table 5.

[0060] Comparative Example 2

[0061] The method of Example 2 was followed, except that the catalysts used in both the first and second reaction zones were composite catalysts obtained by mixing DH-1 and RAG-6 catalysts in a mass ratio of 1:1. The mixed catalyst was added to the second reaction zone, and the two catalysts were not separated or independently regenerated in the catalytic conversion system. The reaction conditions and results are shown in Table 5.

[0062] Example 3

[0063] The method was the same as in Example 2, except that the preheated C5-C8 olefin was introduced into the second reaction zone. The reaction conditions and results are shown in Table 5.

[0064] Comparative Example 3

[0065] The method was the same as in Comparative Example 2, except that the preheated C5-C8 olefins were introduced into the middle of the reactor. The reaction conditions and results are shown in Table 5.

[0066] Table 5. Reaction conditions and results of Examples 2-3 and Comparative Examples 2-3

[0067]

[0068]

[0069] As shown in Tables 4 and 5, the system provided by this invention can improve the yield of low-carbon olefins such as ethylene and propylene.

[0070] 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.

[0071] 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.

[0072] 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 having a series reactor and a catalyst separator, characterized in that, The catalytic conversion system includes a first rising bed reactor, a second rising bed reactor, a settler, a catalyst separator, and a regenerator; The first upward bed reactor has a first catalyst inlet and a first oil-agent mixture outlet; The second upward bed reactor has a second catalyst inlet and a second oil-liquid mixture outlet; the first oil-liquid mixture outlet is connected to the lower part of the second upward bed reactor; The settler has an oil mixture inlet and a mixed catalyst outlet, the oil mixture inlet being connected to the second oil mixture outlet; The catalyst separator has a material inlet connected to the outlet of the mixed catalyst, a first catalyst outlet, and a second catalyst outlet. The regenerator is equipped with a regenerator partition, which divides the regenerator into a first regeneration zone and a second regeneration zone; the first outlet of the spent catalyst is connected to the first regeneration zone via a first spent catalyst transport connection; the second outlet of the spent catalyst is connected to the second regeneration zone via a second spent catalyst transport connection; the first regeneration zone is connected to the first ascending bed reactor via a first regeneration catalyst transport connection; and the second regeneration zone is connected to the second ascending bed reactor via a second regeneration catalyst transport 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. The first outlet of the spent catalyst is located below the outlet of the second spent catalyst.

2. The catalytic conversion system according to claim 1, 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.

3. The catalytic conversion system according to claim 1, 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.

4. The catalytic conversion system according to claim 1, wherein, The catalyst separator is located outside the settler; part or all of the second ascending bed reactor is located inside the settler.

5. The catalytic conversion system according to claim 1, 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 connected to each of the settling tanks is one or more; the multiple catalyst separators are connected in series and / or in parallel.

6. The catalytic conversion system according to claim 5, wherein, The catalyst separator is a cyclone rapid separator.

7. The catalytic conversion system according to claim 5, wherein, The settling device is externally connected to a primary catalyst separator. The lower part of the primary catalyst separator has a first outlet for the catalyst to be generated, and the upper part of the primary catalyst separator has a light material outlet. The light material outlet is connected to the material inlet of the secondary catalyst separator. The upper part of the secondary catalyst separator is provided with a residual reaction oil and gas outlet, and the lower part of the secondary catalyst separator is provided with a second outlet for the catalyst to be generated.

8. The catalytic conversion system according to claim 1, wherein, The lower part of the settling tank is equipped with a stripper; the upper part of the settling tank is equipped with an oil and gas product outlet; and the interior of the settling tank is also equipped with a gas-solid separation device.

9. The catalytic conversion system according to claim 1, wherein, The first regeneration zone and the second regeneration zone are connected in series, with the first regeneration zone located below the second regeneration zone.

10. The catalytic conversion system according to claim 9, wherein, The regenerator partition is provided with a first regenerated flue gas outlet.

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