A catalytic conversion process for the production of low carbon olefins and light aromatics from crude oil

Abstract

The present application provides a catalytic conversion method for producing low-carbon olefins and light aromatics from crude oil, which comprises: S1, contacting the whole fraction of crude oil with a first catalyst in a countercurrent bed reactor to perform a first catalytic conversion reaction, and separating the material after the first catalytic conversion reaction through a first oil agent separator to obtain a first spent catalyst and a first oil and gas product; S2, making the first oil and gas product enter an upflow bed reactor to contact with a second catalyst in the upflow bed reactor to perform a second catalytic conversion reaction, thereby generating a second oil and gas product and a second spent catalyst. Through the above technical solution, the present application uses a reactor type combining a countercurrent bed reactor and an upflow bed reactor, can realize relay of the primary cracking and secondary cracking reactions of the whole fraction of crude oil, and can realize independent and flexible regulation of the reaction environments of the two reaction zones, thereby improving the yield of chemicals such as ethylene, propylene and light aromatics.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of petroleum chemical industry, in particular to a catalytic conversion method for producing low-carbon olefins and light aromatics from crude oil. BACKGROUND

[0002] Crude oil is a complex mixture of various hydrocarbons. At present, oil refineries mainly convert crude oil into fuels such as gasoline, kerosene and diesel, while producing by-products such as ethylene, propylene and BTX (benzene, toluene and xylene, referred to as BTX). With the rapid development of new energy vehicles, the annual growth rate of demand for vehicle fuels is gradually declining, and fuels such as gasoline, kerosene and diesel are facing the trend of overcapacity, which has a certain impact on the expansion and reconstruction of oil refineries. However, petroleum chemical products such as ethylene, propylene and BTX have very wide applications, and the annual growth rate of demand has been greater than the annual growth rate of production in recent years, resulting in a shortage of supply in the market. Therefore, some technical solutions for increasing the production of ethylene, propylene and BTX have emerged.

[0003] For example, CN106029610A discloses an integrated method and facility for converting crude oil into petrochemical products. The integrated method in the method includes crude oil distillation, hydrocracking, aromatization and olefin synthesis, and the facility in the method includes a crude oil distillation unit, a hydrocracking unit, an aromatization unit and an olefin synthesis unit.

[0004] However, it is necessary to further improve the conversion rate and the yield of target products in the catalytic conversion of crude oil to produce low-carbon olefins and light aromatics. SUMMARY

[0005] The present application aims to further improve the conversion rate and the yield of target products in the catalytic conversion of crude oil to produce low-carbon olefins and light aromatics.

[0006] To achieve the above-mentioned purpose, the present application provides a catalytic conversion method for producing low-carbon olefins and light aromatics from crude oil, which comprises: S1, contacting a full distillation fraction of crude oil with a first catalyst in a countercurrent bed reactor to perform a first catalytic conversion reaction, and separating the material after the first catalytic conversion reaction through a first oil agent separator to obtain a first spent catalyst and a first oil and gas product; leading the first spent catalyst out of the countercurrent bed reactor; S2, contacting the first oil and gas product with a second catalyst in an upflow bed reactor to perform a second catalytic conversion reaction in the upflow bed reactor to generate a second oil and gas product and a second spent catalyst.

[0007] Through the above technical solution, the present invention uses a reactor type that combines a reverse-flowing bed reactor and an ascending bed reactor, which can realize the relay of primary cracking and secondary cracking reactions of the entire crude oil fraction, and can realize independent and flexible regulation of the reaction environment of the two reaction zones, thereby improving the yield of chemicals such as ethylene, propylene and light aromatics.

[0008] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0009] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the following detailed description, they are used to explain the present invention but do not constitute a limitation of the present invention. In the accompanying drawings:

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

[0011] Description of Reference Numerals

[0012] Figure 1 In the figure, the reference numerals are described as follows:

[0013] 1-Reverse bed reactor 2-First stripper 3-Upward bed reactor

[0014] 4-settler 5-second stripper 6-first regeneration zone

[0015] 7-Second regeneration zone

[0016] 11-Full crude oil fraction 12, 15-First spent catalyst delivery pipe 13, 21-Stripping gas

[0017] 14, 22-stripping baffle 16-oil and gas 17-catalyst distributor

[0018] 18-First oil separator 19-Auxiliary feed

[0019] 20-Second reaction oil delivery pipe

[0020] 23- Second spent agent delivery pipe 24- Second oil agent separator 25- Gas collecting chamber

[0021] 26-reaction oil and gas 27-main air 28-fuel gas

[0022] 29-first regeneration agent delivery pipe 30-second regeneration agent delivery pipe 31-regeneration baffle

[0023] 32- cyclone separator 33- gas collecting chamber 34- regeneration flue gas

[0024] 35-Raw material distributor DETAILED DESCRIPTION

[0025] The following is a detailed description of the specific embodiments of the present invention. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present invention and are not intended to limit the present invention.

[0026] refer to Figure 1 The present invention provides a catalytic conversion method for producing light olefins and light aromatics from crude oil. The catalytic conversion method comprises: S1, allowing the whole crude oil fraction to be countercurrently contacted with a first catalyst in a retrograde bed reactor to perform a first catalytic conversion reaction, and separating the material after the first catalytic conversion reaction through a first oil-agent separator to obtain a first spent catalyst and a first oil and gas product; leading the first spent catalyst out of the retrograde bed reactor; S2, allowing the first oil and gas product to enter an upper bed reactor and contact with a second catalyst in the upper bed reactor to perform a second catalytic conversion reaction to generate a second oil and gas product and a second spent catalyst.

[0027] Wherein, optionally, the initial distillation point of the crude oil full fraction is any value between 30 and 60°C, and the final distillation point is any value between 650 and 730°C.

[0028] Optionally, the whole crude oil fraction is introduced into the bottom of the retrograde bed reactor through a raw material distributor and dispersed and atomized.

[0029] Optionally, the first catalyst is introduced into the upper part of the retrograde bed reactor through a catalyst distributor, the catalyst distributor has a perforated disc structure, and the perforated disc has a porosity of 50% to 90%, preferably 60% to 80%.

[0030] Wherein, optionally, the first catalyst comprises unmodified Y-type molecular sieve or modified Y-type molecular sieve, clay and a binder. Based on the total weight of the catalyst, the content of the unmodified Y-type molecular sieve or modified Y-type molecular sieve is 10 to 80%, preferably 30 to 60%, the content of the clay is 10 to 80%, preferably 15 to 60%, and the content of the binder is 10 to 30%, preferably 10 to 20%.

[0031] Optionally, the second catalyst comprises unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve, a contacting agent, clay, and a binder. The contacting agent is selected from one or more of SiO2, MgO, CaO, BaO, and MnO2. Based on the total weight of the catalyst, the content of the unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve is 10-60%, preferably 20-50%, the content of the contacting agent is 5-40%, preferably 10-30%, the content of the clay is 10-80%, preferably 20-70%, and the content of the binder is 10-30%, preferably 10-20%. The contacting agent can play a role in thermal cracking, which helps increase ethylene production. The clay can be selected from one or more of kaolin, montmorillonite, and bentonite, and the binder can be selected from one or more of silica sol, alumina sol, and pseudo-boehmite.

[0032] Among them, optionally, the conditions of the first catalytic conversion reaction include: reaction temperature of 520-620°C, preferably 540-600°C, mass space velocity of 2-20h -1 , preferably 5 to 15 hours -1 , the catalyst bed density is 100~500kg / m 3 , preferably 150~300kg / m 3 , the reaction pressure is 0-0.4 MPa, preferably 0.05-0.3 MPa.

[0033] Among them, optionally, the conditions of the second catalytic conversion reaction include: reaction temperature of 620-700°C, preferably 640-680°C, agent-oil ratio of 2-30, preferably 5-20, reaction time of 1-15s, preferably 2-10s, and pressure in the reactor of 0-0.4MPa, preferably 0-0.2MPa.

[0034] Optionally, the method further includes: performing a first stripping and a first regeneration on the first spent catalyst to obtain a first regenerated catalyst, and returning the first regenerated catalyst to step S1 to participate in the first catalytic conversion reaction.

[0035] Optionally, the method further includes: performing a second stripping and a second regeneration on the second spent catalyst to obtain a second regenerated catalyst, and returning the second regenerated catalyst to step S2 to participate in the second catalytic conversion reaction.

[0036] Among them, optionally, the first regeneration is carried out in the first regeneration zone, and the second regeneration is carried out in the second regeneration zone; the first regeneration zone and the second regeneration zone are arranged in series, and the regenerated flue gas obtained in the first regeneration zone is introduced into the second regeneration zone to continue to participate in the second regeneration.

[0037] wherein, optionally, the conditions of the first regeneration comprise: a regeneration temperature of 660-720°C, preferably 680-700°C, a catalyst density of 30-350 kg / m 3 , preferably 80-250 kg / m 3 , a primary air residence time of 0.5-15 s, preferably 2-10 s.

[0038] wherein, optionally, the conditions of the second regeneration comprise: a regeneration temperature of 680-740°C, preferably 700-720°C, a catalyst density of 30-350 kg / m 3 , preferably 80-250 kg / m 3 , a primary air residence time of 0.5-15 s, preferably 2-10 s.

[0039] wherein, optionally, the method further comprises: introducing an auxiliary feedstock into the upflow bed reactor, the auxiliary feedstock being selected from the group consisting of one or more of a mixture of carbon four fraction, light gasoline fraction, and a mixture of C4-C8 hydrocarbons.

[0040] wherein, optionally, the first oil agent separator is located at the top of the downflow bed reactor, and the first reaction oil gas is led out of the downflow bed reactor through the first oil agent separator.

[0041] wherein, optionally, the first oil agent separator is selected from the group consisting of one or more of a combination of a filter, a filter plate, a porous partition, and a fast separation device, preferably a filter plate; the filter plate has a pore size of 5-40 μm, preferably 10-30 μm.

[0042] wherein, optionally, the downflow bed reactor is selected from the group consisting of one or more of a combination of an equal-diameter downflow bed reactor and a variable-diameter downflow bed reactor, the ratio of the diameter to the height of the downflow bed reactor being 1:1-5, preferably 1:1.5-3; the upflow bed reactor is selected from the group consisting of one or more of a combination of a bubbling bed reactor, a turbulent bed reactor, a fast bed reactor, and a transport bed reactor, preferably a fast bed reactor.

[0043] According to a particularly preferred embodiment of the present invention, the preheated crude oil full fraction is sprayed into the bottom of the retrograde bed reactor 1 through the feed pipeline 11 via the raw material distributor 35, and contacts with the first catalyst from the first regeneration zone 6 and introduced into the upper part of the retrograde bed reactor 1 through the first catalyst distributor 17 to carry out a first catalytic conversion reaction. The obtained first oil-agent mixture is separated by the first oil-agent separator 18 at the top of the retrograde bed reactor 1, wherein the first catalyst to be regenerated is introduced into the first stripper 2 for stripping to remove a small amount of reaction oil and gas carried on the catalyst. The obtained stripped first catalyst to be regenerated is introduced into the first regeneration zone 6 through the first regenerated agent delivery pipe 15 for regeneration, and the regenerated first catalyst is introduced into the retrograde bed reactor 1 through the first regeneration agent delivery pipe 29 for recycling. The first reaction oil and gas separated by the first oil separator 18 is introduced into the upper bed reactor 3 for contact reaction with the second catalyst from the second regeneration zone 7. Optionally, an auxiliary raw material can be introduced into the upper bed reactor 3 through the auxiliary feed line 19. Then, a second catalytic conversion reaction is carried out in the upper bed reactor 3. The second reaction oil after the reaction is introduced into the second oil separator 24 in the settler 4 through the second reaction oil delivery pipe 20. The separated second regenerated catalyst is introduced into the second stripper 5 for stripping to remove a small amount of reaction oil and gas carried on the catalyst. The stripped second regenerated catalyst is introduced into the second regeneration zone 6 through the second regenerated agent delivery pipe 23 for regeneration. The regenerated second catalyst is introduced into the upper bed reactor 3 through the second regeneration agent delivery pipe 30 for recycling. The reaction oil and gas separated by the second oil separator 24 is discharged to the device.

[0044] The present invention is described in detail below with reference to the embodiments, but the scope of the present invention is not limited thereby.

[0045] Example

[0046] Unless otherwise specified, all reagents used below are chemically pure.

[0047] The catalysts used in the Examples and Comparative Examples were GOR-II, RAG-6, and DMMC-2, all commercially available catalysts produced by the Qilu Branch of Sinopec Catalyst Company. Specific properties of the three catalysts are shown in Table 1. Prior to testing, the catalysts were aged for 17 hours at 800°C and 100% steam. The feedstock oil used in the Examples and Comparative Examples was Yangzhou crude oil, with specific properties shown in Table 2. A C4 fraction and a light gasoline fraction were also used as auxiliary feeds in the Examples and Comparative Examples. Their compositions and properties are shown in Tables 3 and 4, respectively.

[0048] Table 1 Composition and properties of catalysts

[0049] catalyst GOR-II RAG-6 DMMC-2 Chemical composition, % (w) <![CDATA[Al2O3]]> 57.5 51.2 48.1 SiO2 36.1 43.1 46.0 BET Full Analysis BET total area / (m 2 ·g -1 )]]> 181.000 197.000 102.491 <![CDATA[微孔面积 / (m 2 ·g -1 )]]> 104.000 98.000 49.601 <![CDATA[总孔体积 / (cm 3 ·g -1 )]]> 0.224 0.150 0.1057 <![CDATA[微孔体积 / (cm 3 ·g -1 )]]> 0.034 0.045 0.0259 Particle size distribution, %(w) 0-20μm 0.1 0.5 0.1 0-40μm 5.1 32.6 17 0-80μm 20.3 87.3 70.9 0-105μm 50.6 98.5 87.8 >105μm 49.4 1.5 12.2

[0050] Table 2 Composition and properties of Yangzhou crude oil

[0051]

[0052]

[0053] Table 3 Chemical composition of C4 fraction

[0054] project C4 fraction Mass composition, wt% n-butane 6.77 Isobutane 16.5 Alkane content 23.27 n-Butene 15.1 Isobutylene 30.3 Trans-butene 17.1 Cis-butene 13.8 1,3-Butadiene 0.43 total 100

[0055] Table 4 Chemical composition and properties of light gasoline fractions

[0056] project Light gasoline <![CDATA[密度(20℃) / (kg / m 3 )]]> 635.1 Element mass composition / % carbon 84.76 hydrogen 15.24 Sulfur / (μg / g) 46.29 Nitrogen / (μg / g) 32 Distillation range / ℃ Initial distillation point 12 10v％ 18 30v％ 30 50v％ 35 70v％ 57 90v％ 59 Final distillation point 60 Mass group composition / % Alkanes 37.19 Olefins 62.49 Cycloalkanes 0.32 Aromatics 0

[0057] Example 1

[0058] The test Figure 1 The experiment was conducted on the apparatus shown in the figure. The diameter of the retrograde bed reactor was 150 mm and the length was 300 mm, while the diameter of the ascending bed reactor was 30 mm and the height was 480 mm. GOR-II catalyst was used in the retrograde bed reactor, and RAG-6 catalyst was used in the ascending bed reactor. Before the experiment began, the reactor was heated to a predetermined temperature. Yangzhou crude oil was introduced into the bottom of the retrograde bed reactor under water vapor dilution, and reacted after contact with the GOR-II catalyst. The resulting first reaction oil was separated by a filter. The first reaction oil gas was introduced into the ascending bed reactor, contacted with the RAG-6 catalyst and reacted. The resulting oil mixture was separated by a filter, and the reaction oil gas was condensed and analyzed to obtain the yields of different products. The used catalyst was regenerated and reused. The reaction conditions and results are shown in Table 5.

[0059] Example 2

[0060] The method of Example 1 was followed, except that the C4 fraction was introduced as an auxiliary feedstock into the bottom of the ascending bed reactor. The mass ratio of the C4 fraction to Yangzhou crude oil was 0.05:1. The reaction conditions and results are shown in Table 5.

[0061] Comparative Example 1

[0062] The experiment was conducted in a single ascending bed reactor with a diameter of 30 mm and a height of 480 mm, loaded with GOR-II catalyst. Before the experiment began, the reactor was heated to a predetermined temperature. Preheated Yangzhou crude oil was introduced into the reaction zone, diluted with steam, where it came into contact with the GOR-II catalyst and reacted. The resulting oil-solvent mixture was separated by a filter, and the reaction oil and gas were condensed and analyzed to determine the yields of various products. The used catalyst was regenerated and reused. The reaction conditions and results are shown in Table 5.

[0063] Comparative Example 2

[0064] The method of Example 1 was followed, except that the catalyst used in both the reverse-flowing bed reactor and the ascending bed reactor was RAG-6 catalyst. The reaction conditions and results are shown in Table 5.

[0065] Table 5 Reaction conditions and results of Examples 1-2 and Comparative Examples 1-2

[0066]

[0067]

[0068] Example 3

[0069] The test Figure 1 The system shown in the figure is used. The reverse-flow bed reactor has a diameter of 300 mm and a length of 600 mm, while the ascending bed reactor has a diameter of 40 mm and a height of 1000 mm. The catalyst used in the reverse-flow bed reactor is GOR-II, while the catalyst used in the ascending bed reactor is RAG-6. Yangzhou crude oil is preheated to 250°C and introduced into the bottom of the reverse-flow bed reactor, where it reacts with the GOR-II catalyst in a reverse-flow manner. The resulting first reaction oil is separated in a first oil separator. The first spent catalyst is stripped in the first spent catalyst stripper and then regenerated in the first catalyst regeneration zone. The regenerated first catalyst is then returned to the reverse-flow bed reactor for recycling. The first reaction oil gas generated in the first oil separator is introduced into the ascending bed reactor for further reaction with the RAG-6 catalyst. The resulting second reaction oil is then separated in a second oil separator in the settler. The second spent catalyst is stripped in the second spent catalyst stripper and then regenerated in the second catalyst regeneration zone. The regenerated second catalyst is then returned to the ascending bed reactor for recycling. The reaction oil gas exits the system. The reaction conditions and results are shown in Table 6.

[0070] Example 4

[0071] The method of Example 3 was followed, except that a light gasoline fraction was introduced as an auxiliary feedstock into the ascending bed reactor for the reaction, and the mass ratio of the light gasoline fraction to the Yangzhou crude oil was 0.1:1. The reaction conditions and results are shown in Table 6.

[0072] Comparative Example 3

[0073] The experiment was conducted in a single ascending bed reactor with a diameter of 40 mm and a height of 1000 mm. RAG-6 catalyst was used. Yangzhou crude oil was preheated to 250°C and introduced into the bottom of the ascending bed reactor. It then ascended in contact with the RAG-6 catalyst and reacted. The resulting reaction oil was separated in an oil separator within the settler. The spent catalyst was stripped in a spent catalyst stripper and then regenerated in the catalyst regeneration zone. The regenerated catalyst was returned to the ascending bed reactor for recycling. A reaction oil and gas extraction system was installed. Reaction conditions and results are shown in Table 6.

[0074] Comparative Example 4

[0075] The method of Example 3 was followed, except that the catalyst used in both the retrograde bed reactor and the ascending bed reactor was DMMC-2. The reaction conditions and results are shown in Table 6.

[0076] Table 6 Reaction conditions and results of Examples 3 to 4 and Comparative Examples 3 to 4

[0077]

[0078]

[0079] As shown in Tables 5 and 6, the conversion rate of the reactants and the yield of the target product are greatly improved by adopting the method provided by the present invention.

[0080] The preferred embodiments of the present invention are described in detail above. However, the present invention is not limited to the specific details in the above embodiments. Within 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 scope of protection of the present invention.

[0081] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any appropriate manner without contradiction. To avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0082] In addition, the various embodiments of the present invention may be arbitrarily combined, and as long as they do not violate the concept of the present invention, they should also be regarded as the contents disclosed by the present invention.

Claims

1. A catalytic conversion method for producing light olefins and light aromatics from crude oil, characterized in that: The catalytic conversion method comprises: S1. Allowing the crude oil fraction to contact the first catalyst in a countercurrent bed reactor to perform a first catalytic conversion reaction, and separating the materials after the first catalytic conversion reaction by a first oil-agent separator to obtain a first spent catalyst and a first oil and gas product; and removing the first spent catalyst from the countercurrent bed reactor. S2, allowing the first oil and gas product to enter the upward bed reactor and contact with the second catalyst in the upward bed reactor to perform a second catalytic conversion reaction to generate a second oil and gas product and a second spent catalyst; The initial boiling point of the crude oil fraction is any value between 30°C and 60°C, and the final boiling point is any value between 650°C and 730°C; the crude oil fraction is introduced into the bottom of the retrograde bed reactor through a raw material distributor and dispersed and atomized; The first catalyst comprises an unmodified Y-type molecular sieve or a modified Y-type molecular sieve, clay, and a binder. Based on the total weight of the first catalyst, the content of the unmodified Y-type molecular sieve or the modified Y-type molecular sieve is 10-80%, the content of the clay is 10-80%, and the content of the binder is 10-30%. The second catalyst comprises unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve, a contact agent, clay and a binder, wherein the contact agent is selected from one or more of SiO2, MgO, CaO, BaO and MnO2. Based on the total weight of the second catalyst, the content of the unmodified ZSM-5 molecular sieve or modified ZSM-5 molecular sieve is 10 to 60%, the content of the contact agent is 5 to 40%, the content of the clay is 10 to 80%, and the content of the binder is 10 to 30%. The sum of the weights of the components in the second catalyst is 100%.

2. The method according to claim 1, wherein The first catalyst is introduced into the upper part of the retrograde bed reactor through a catalyst distributor, wherein the catalyst distributor has a perforated disc structure, and the perforated disc has an opening rate of 50% to 90%.

3. The method according to claim 2, wherein: The opening rate of the perforated disc is 60% to 80%.

4. The method according to claim 1, wherein Based on the total weight of the first catalyst, the content of the unmodified Y-type molecular sieve or the modified Y-type molecular sieve is 30-60%, the content of the clay is 15-60%, and the content of the binder is 10-20%; Based on the total weight of the second catalyst, the content of the unmodified ZSM-5 molecular sieve or the modified ZSM-5 molecular sieve is 20-50%, the content of the contact agent is 10-30%, the content of the clay is 20-70%, and the content of the binder is 10-20%, wherein the sum of the weights of the components in the second catalyst is 100%.

5. The method according to claim 1, wherein The conditions of the first catalytic conversion reaction include: reaction temperature of 520-620°C, mass space velocity of 2-20h -1 , the catalyst bed density is 100~500kg / m 3 , the reaction pressure is 0~0.4MPa.

6. The method according to claim 5, wherein: The conditions of the first catalytic conversion reaction include: reaction temperature of 540-600°C, mass space velocity of 5-15h -1 , the catalyst bed density is 150~300kg / m 3 , the reaction pressure is 0.05~0.3MPa.

7. The method according to claim 1 or 5, wherein: The conditions for the second catalytic conversion reaction include: a reaction temperature of 620-700° C., a catalyst-to-oil ratio of 2-30, a reaction time of 1-15 seconds, and a pressure in the reactor of 0-0.4 MPa.

8. The method according to claim 7, wherein: The conditions of the second catalytic conversion reaction include: reaction temperature of 640-680° C., catalyst-oil ratio of 5-20, reaction time of 2-10 s, and pressure in the reactor of 0-0.2 MPa.

9. The method according to claim 1, wherein The method further includes: performing a first stripping and a first regeneration on the first spent catalyst to obtain a first regenerated catalyst, and returning the first regenerated catalyst to step S1 to participate in the first catalytic conversion reaction; performing a second stripping and a second regeneration on the second spent catalyst to obtain a second regenerated catalyst, and returning the second regenerated catalyst to step S2 to participate in the second catalytic conversion reaction; The first regeneration is carried out in the first regeneration zone, and the second regeneration is carried out in the second regeneration zone; the first regeneration zone and the second regeneration zone are arranged in series, and the regenerated flue gas obtained in the first regeneration zone is introduced into the second regeneration zone to continue to participate in the second regeneration.

10. The method according to claim 9, wherein: The first regeneration conditions include: regeneration temperature of 660-720°C, catalyst density of 30-350 kg / m 3 , the main wind stay time is 0.5~15s; The second regeneration conditions include: regeneration temperature of 680-740°C, catalyst density of 30-350 kg / m 3 , the main wind stay time is 0.5~15s.

11. The method according to claim 10, wherein: The first regeneration conditions include: regeneration temperature of 680-700°C, catalyst density of 80-250 kg / m 3 , the main wind stay time is 2 to 10 seconds; The second regeneration conditions include: regeneration temperature of 700-720°C, catalyst density of 80-250 kg / m 3 , the main wind stay time is 2 to 10s.

12. The method according to claim 1, wherein The method further comprises: introducing an auxiliary raw material into the upward bed reactor, wherein the auxiliary raw material is selected from a mixture of one or more of a C4 fraction, a light gasoline fraction and a mixture of C4-C8 hydrocarbons.

13. The method according to claim 1, wherein The first oil-agent separator is located at the top of the retrograde bed reactor, and the material after the first catalytic conversion reaction is led out of the retrograde bed reactor through the first oil-agent separator; The first oil separator is selected from a combination of one or more of a filter, a filter plate, and a quick separation device; the pore size of the filter plate is 5 to 40 μm.

14. The method according to claim 13, wherein The first oil separator is a porous partition.

15. The method according to claim 13, wherein: The first oil separator is a filter plate; the pore size of the filter plate is 10 to 30 μm.

16. The method according to claim 1, wherein The retrograde bed reactor is selected from one or a combination of a constant diameter retrograde bed reactor and a variable diameter retrograde bed reactor, and the ratio of the diameter to the height of the retrograde bed reactor is 1:1 to 5; the ascending bed reactor is selected from one or more combinations of a bubbling bed reactor, a turbulent bed reactor, a fast bed reactor, and a transport bed reactor.

17. The method according to claim 16, wherein The ratio of the diameter to the height of the retrograde bed reactor is 1:1.5-3; the ascending bed reactor is a fast bed reactor.

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