Multi-zone coordinated control riser reactor system

Abstract

The utility model provides a multi-zone coordinated control riser reactor system, belongs to the technical field of catalytic cracking risers, and solves the problem that the scheme switching of high yields of ethylene, propylene and butylene gas and high yields of gasoline and diesel oil cannot be flexibly carried out in the prior art. The device comprises a regenerator and a reaction settler, the reaction settler is communicated with a lifting pipe, the reaction settler is connected with a regeneration inclined pipe communicated with the regenerator, the regenerator is connected with a leading-in inclined pipe, the leading-in inclined pipe is connected with a stripper, and a stripping gas distribution pipe located below a pipe opening of the leading-in inclined pipe is arranged in the stripper. A stripping gas return pipe communicated with the regenerator is arranged at the top of the stripper, and a regeneration inclined pipe communicated with the bottom of the lifting pipe is arranged at the bottom of the stripper. The stripper is arranged on the regeneration inclined tube, so that the temperature of a regenerated catalyst entering the reactor can be effectively adjusted while non-hydrocarbon gas entering the riser is reduced, and the ratio of the catalyst to oil can be conveniently adjusted according to a production scheme to obtain required product distribution.

Description

Technical Field

[0001] This invention belongs to the field of catalytic cracking riser technology, specifically to a riser reactor system with multi-zone coordinated control. Background Technology

[0002] The riser reactor system is a widely used equipment system in catalytic cracking processes. It mainly consists of two core parts: the reactor and the regenerator. The reactor consists of a riser and a settling chamber. The catalyst first enters the riser and reacts under the influence of feedstock oil and steam. After the reaction, the catalyst activity decreases, and it then enters the settling chamber for preliminary separation before finally entering the regenerator for regeneration.

[0003] The prior art is disclosed in patent publication number CN113583702B, which discloses a catalytic cracking method for producing ethylene and propylene. This catalytic cracking method includes: (1) subjecting heavy feedstock oil to heavy catalytic cracking; and preheating light feedstock oil rich in low-carbon alkanes to 200-800°C before subjecting it to light catalytic cracking. The catalytic cracking method further includes one of the following: (2) feeding the oil material after heavy catalytic cracking into a fluidized bed reactor for fluidized bed catalytic cracking; and (3) feeding the oil material after heavy catalytic cracking and the oil material after light catalytic cracking into a fluidized bed reactor for fluidized bed catalytic cracking. This invention also provides a catalytic cracking system for the catalytic cracking method described above. Through the above technical solution, the yields of ethylene and propylene are significantly improved.

[0004] However, when the fluidized bed reactor described above is used for fluidized bed catalytic cracking, it cannot effectively adjust the reaction time and reaction depth according to the amount of feedstock, nor can it flexibly switch between producing more ethylene, propylene, and butene gas and producing more gasoline and diesel. As a result, the products of the catalytic cracking or catalytic pyrolysis unit cannot meet market needs. Utility Model Content

[0005] To address the aforementioned problems, the purpose of this invention is to provide a multi-zone coordinated control riser reactor system. A stripper is installed on the regeneration inclined tube used to transport the regenerated catalyst, which reduces the entry of non-hydrocarbon gases into the riser while effectively regulating the temperature of the regenerated catalyst entering the reactor. This allows for convenient adjustment of the catalyst-to-oil ratio according to the production plan to obtain the desired product distribution.

[0006] The technical solution adopted in this utility model is as follows:

[0007] A multi-zone coordinated control riser reactor system includes a regenerator and a reaction settling tank. The reaction settling tank is connected to a riser and a pre-regeneration inclined tube that communicates with the regenerator. The regenerator is connected to an inlet inclined tube, which is connected to a stripper. The stripper has a stripping gas distribution pipe located below the inlet of the inlet inclined tube. The top of the stripper has a stripping gas return pipe that communicates with the regenerator, and the bottom of the stripper has a regeneration inclined tube that communicates with the bottom of the riser.

[0008] Preferably, the stripper is provided with a heat extraction coil.

[0009] Preferably, the riser is provided with a rising medium inlet, a recycle liquefied gas inlet, and a raw material oil nozzle from bottom to top, and the connection between the regeneration inclined pipe and the riser is located between the rising medium inlet and the recycle liquefied gas inlet.

[0010] Preferably, the riser pipe is provided with a lower expansion section located above the feed oil nozzle, and the side wall of the lower expansion section is provided with a dilution steam inlet and a recycle oil or slurry inlet from bottom to top.

[0011] Preferably, the riser pipe is provided with a middle expansion section located above the lower expansion section, and the riser pipe is provided with a recycle light gasoline inlet located between the middle expansion section and the lower expansion section.

[0012] Preferably, the middle expansion section is connected to a first circulation inclined pipe that communicates with the bottom of the reaction sedimentation tank.

[0013] Preferably, the lower expansion section is connected to a second circulation inclined pipe that communicates with the bottom of the reaction sedimentation tank.

[0014] Preferably, the top of the riser is provided with a VQS quick separator, and the reaction settling tank is provided with a VQS sealing cover covering the outside of the VQS quick separator. The side wall of the VQS sealing cover is connected to a single-stage cyclone separator located outside the VQS sealing cover. The top of the reaction settling tank is provided with a reaction oil and gas outlet communicating with the top of the single-stage cyclone separator. The bottom of the reaction settling tank is provided with a stripping section, and the connection between the waiting inclined tube and the reaction settling tank is located below the stripping section.

[0015] Preferably, the regenerator includes a first regenerator connected to the regeneration inclined tube, a first main air distribution pipe is provided in the first regenerator, a second regenerator connected to the regeneration inclined tube is connected to the top of the first regenerator, a second main air distribution pipe is provided in the second regenerator, and a two-stage cyclone separator located above the second main air distribution pipe is provided in the second regenerator, and the two-stage cyclone separator is connected to an air collection chamber.

[0016] Preferably, an external heat exchanger is provided on the outside of the regenerator, and the external heat exchanger is connected to a feed pipe communicating with the second regenerator and a discharge pipe communicating with the first regenerator. The external heat exchanger is provided with a fluidizing air inlet.

[0017] In summary, due to the adoption of the above technical solution, the beneficial effects of this utility model are:

[0018] A stripper is installed on the regeneration inclined tube used to transport the regenerated catalyst. This reduces the amount of non-hydrocarbon gases entering the riser and effectively regulates the temperature of the regenerated catalyst entering the reactor. This allows for easy adjustment of the catalyst-to-oil ratio according to the production plan to obtain the desired product distribution. Attached Figure Description

[0019] To more clearly illustrate the technical solutions of the embodiments of this utility model, the drawings used in the embodiments will be briefly introduced below. It should be understood that the following drawings only show some embodiments of this utility model and should not be regarded as a limitation on the scope. For those skilled in the art, other related drawings can be obtained based on these drawings without creative effort.

[0020] Figure 1 A flowchart illustrating an embodiment of this utility model.

[0021] Attached reference numerals: 1-Lifting medium inlet; 2-Recycled liquefied gas inlet; 3-Feed oil nozzle; 4-Dilution steam inlet; 5-Recycled oil or slurry inlet; 6-Recycled light gasoline inlet; 7-Middle expansion section; 8-Lower stripping steam distributor; 9-Upper stripping steam distributor; 10-Reaction settling tank; 11-Single-stage cyclone separator; 12-Reaction oil and gas outlet; 13-VQS enclosure; 14-VQS quick separator; 15-Stripping baffle; 16-Stripping section; 17-Waiting inclined tube; 18-Waiting slide valve; 19-First circulation slide valve; 20-First circulation inclined tube; 21-Lower expansion section; 22-Regeneration inclined tube; 23-Regeneration slide valve; 24-Gas collection chamber; 25-First regenerator; 26-Two-stage cyclone separator; 27-Second regenerator; 28-Second main air distribution pipe; 29-Feed pipe; 30-External heat exchanger; 31-Fluidizing air inlet; 32-External heat exchanger slide valve; 33-Discharge pipe; 34-First main air distribution pipe; 35-Stripper; 36-Heat exchange coil; 37-Stripper gas return pipe; 38-Introduction inclined tube; 39-Stripper gas distribution pipe; 40-Second circulation slide valve; 41-Second circulation inclined tube; 42-Lifting pipe. Detailed Implementation

[0022] To make the objectives, technical solutions, and advantages of the embodiments of this utility model clearer, the technical solutions of the embodiments of this utility model will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of this utility model, and not all embodiments. The components of the embodiments of this utility model described and shown in the accompanying drawings can generally be arranged and designed in various different configurations.

[0023] Therefore, the following detailed description of the embodiments of the present invention provided in the accompanying drawings is not intended to limit the scope of the claimed invention, but merely to illustrate selected embodiments of the invention. All other embodiments obtained by those skilled in the art based on the embodiments of the present invention without inventive effort are within the scope of protection of the present invention.

[0024] In the description of this utility model, it should be noted that if terms such as "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer" appear to indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings, or the orientation or positional relationship commonly used when the product is in use, they are only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation, and therefore should not be construed as a limitation of this utility model.

[0025] The following is combined Figure 1 This utility model will be described in detail.

[0026] Example

[0027] A multi-zone coordinated control riser reactor system includes a regenerator and a reaction settling tank 10. The reaction settling tank 10 is connected to a riser 42 and a regenerating inclined tube 17 connected to the regenerator. The regenerator is connected to an inlet inclined tube 38 and a stripper 35. A stripping gas distribution pipe 39 is provided in the stripper 35 below the inlet of the inlet inclined tube 38. A stripping gas return pipe 37 connected to the regenerator is provided at the top of the stripper 35, and a regeneration inclined tube 22 connected to the bottom of the riser 42 is provided at the bottom of the stripper 35.

[0028] After the catalyst is mixed with the raw material in the riser 42, the raw material reacts. The catalyst that has participated in the reaction enters the regenerator from the regenerated inclined tube 17 for regeneration. The regenerated catalyst then enters the stripper 35 from the inlet inclined tube 38. The stripper gas distribution pipe 39 in the stripper 35 uses nitrogen to strip out any non-hydrocarbon gases that may be entrained in the regenerated catalyst, preventing excessive non-hydrocarbon gases from entering the riser 42. The stripper 35 can also adjust the temperature of the regenerated catalyst, making it easier to control the temperature of the riser 42 to process different raw materials.

[0029] The stripper 35 is equipped with a heat exchange coil 36. Boiler water or low-pressure saturated steam is introduced into the heat exchange coil 36 to adjust the temperature of the regenerated catalyst.

[0030] The riser 42 is provided with a rising medium inlet 1, a recycle liquefied gas inlet 2, and a feedstock oil nozzle 3 from bottom to top. The connection between the regeneration inclined pipe 22 and the riser 42 is located between the rising medium inlet 1 and the recycle liquefied gas inlet 2. The regenerated catalyst delivered by the regeneration inclined pipe 22 is lifted by the medium at the pre-lifting medium inlet 1 and moves upward. It first comes into contact with the liquefied gas coming from the recycle liquefied gas inlet 2, causing the liquefied gas to undergo a cracking reaction; then it comes into contact with the catalytic cracking or cracking feedstock injected through the feedstock oil nozzle inlet 3, and a rapid catalytic cracking or cracking reaction occurs.

[0031] The riser 42 is equipped with a lower expansion section 21 located above the feedstock nozzle 3. From bottom to top, the sidewall of the lower expansion section 21 has a dilution steam inlet 4 and a recycle oil or slurry inlet 5. The dilution steam inlet 4 in the lower expansion section 21 allows for adjustment of the dilution steam flow rate according to changes in feedstock quantity or production plan, thereby adjusting the catalytic cracking or catalytic pyrolysis reaction time or depth. The recycle oil or slurry inlet 5, located on the lower expansion section 21, allows for the transfer of incompletely converted oil to the riser 42 for further conversion. This allows for flexible adjustment of reaction time and depth requirements to achieve high yields of ethylene, propylene, and butene.

[0032] The main feedstocks are atmospheric and vacuum distillate oil, atmospheric distillate oil, vacuum distillate oil, hydrogenated wax oil, and hydrogenated residue oil. They also include recycled oil from riser 42, oil slurry from riser 42, and liquefied petroleum gas or gasoline from riser 42.

[0033] The riser pipe 42 is provided with a middle expansion section 7 located above the lower expansion section 21, and the riser pipe 42 is provided with a recycle light gasoline inlet 6 located between the middle expansion section 7 and the lower expansion section 21.

[0034] By setting a liquefied petroleum gas inlet 2 at the lower part of the riser 42 and a light gasoline inlet 6 in the middle of the riser 42, the requirements of catalytic cracking or catalytic pyrolysis units for increasing the yield of ethylene, propylene, and butene can be met.

[0035] The middle expansion section 7 is connected to a first circulation inclined pipe 20, which communicates with the bottom of the reaction settling tank 10. The lower expansion section 21 is connected to a second circulation inclined pipe 41, which also communicates with the bottom of the reaction settling tank 10. The first circulation inclined pipe 20 introduces the catalyst to be produced into the middle expansion section 7, and the second circulation inclined pipe 41 introduces the catalyst to be produced into the lower expansion section 21. This promotes the bimolecular reaction of the catalytic reaction, increases hydrogen transfer and isomerization reactions, reduces the olefin content in gasoline, and produces high-quality gasoline.

[0036] The riser reactor system of this application utilizes a multi-zone coordinated control system via a stripper 35, a first circulating inclined tube 20, a second circulating inclined tube 41, a lower expansion section 21 of the riser 42, and a middle expansion section 7. Depending on the production requirements of the catalytic converter, a portion of the spent catalyst can enter the lower and middle sections of the riser 42 to promote hydrogen transfer and isomerization reactions in catalytic cracking or catalytic pyrolysis, thereby reducing the olefin content in gasoline and producing high-quality gasoline. By combining the two expansion sections, the lower expansion section 21 meets the depth requirements of the cracking or pyrolysis reaction, while the middle expansion section 7 and the lower expansion section 21 adjust the amount of spent catalyst to meet the olefin reduction quality requirements of gasoline. By adjusting the dilution steam volume, the regenerated catalyst circulation volume, the amount of spent catalyst entering the middle expansion section 7, and the reaction temperature and time, a DCC process production scheme or an RFCC / FCC production scheme can be flexibly implemented.

[0037] The DCC reactor uses light hydrotreated wax oil or atmospheric heavy oil as feedstock, equipped with a proprietary catalyst, and produces high-value-added products such as ethylene, propylene, and butene. The RFCC and FCC reactors use hydrotreated heavy oil or atmospheric and vacuum residue as feedstock, equipped with proprietary catalysts, and primarily produce low-olefin, high-quality gasoline and diesel. The essence and characteristic of DCC (catalytic cracking), RFCC (heavy oil catalytic cracking), and FCC (fluidized catalytic cracking) units is to produce corresponding products needed by the market at different times by adjusting the reaction depth of the riser reactor.

[0038] The temperature of the regenerated catalyst can be flexibly adjusted between 600 and 700℃; the temperature of the feedstock oil in the lower expansion section 21 is 500–650℃, the pressure is 0.1–0.5 MPa, and the reaction time is 0.5–5 s; the temperature of the feedstock oil in the middle expansion section 7 is 490–580℃, the pressure is 0.1–0.45 MPa, and the reaction time is 4–8 s; preferably, the temperature of the lower expansion section 21 is 520–580℃, the pressure is 0.2–0.4 MPa, and the reaction time is 1.2–3 s. The temperature of the central expansion section 7 is 510–560℃, the pressure is 0.2–0.4MPa, and the reaction time is 4–6s. The microsphere catalyst composed of rare earth oxides, alkali metal oxides, ZSM-5 and ZRP molecular sieves, and AL2O3 support can carry out the reaction of feedstock oil catalytic cracking or catalytic decomposition to produce liquefied petroleum gas containing ethylene, propylene, and butene, as well as gasoline, diesel and other oil products, under the conditions of a catalyst-to-oil ratio of 6–20, preferably 6–18. The reaction can be completed rapidly.

[0039] This application allows for flexible switching between DCC (Digital Crack) technology and RFCC / FCC (Radio-Release Crack) technology based on market conditions for each product; to produce gaseous products such as ethylene, propylene, and butene, or fuel products such as high-quality gasoline and diesel. ① When the unit adopts DCC technology to maximize the production of ethylene, propylene, and butene, the steam generator in stripper 35 reduces steam output, appropriately increases the temperature of the regenerated catalyst to 660–700℃, and increases the dilution steam and regenerated catalyst circulation in the lower expansion section 21. This reduces the residence time of the feedstock in the main riser, maintaining a total reaction time of 2–5 seconds. The temperature in the middle of the lower expansion section 21 is maintained at 550–580℃, and the temperature in the upper part at 530–560℃, making the catalytic cracking reaction predominantly a single-molecule reaction, maximizing the production of ethylene, propylene, and butene; ② When the unit adopts DCC technology to maximize the production of gasoline and diesel... When using RFCC and FCC processes with oil as the target product, the steam generator in stripper 35 increases steam output, appropriately lowers the temperature of the regenerated catalyst to 600–650°C, reduces the dilution steam and regenerated catalyst circulation in the lower expansion section 21, increases the residence time of the feedstock in the main riser, maintains the total reaction time at 4–8 seconds, keeps the middle temperature of the lower expansion section 21 at 510–530°C, and the upper temperature at 490–510°C. Under the action of the regenerated catalyst, the catalytic cracking reaction tends to be dominated by bimolecular reactions, thus increasing gasoline and diesel production and reducing gasoline olefin content, producing as much high-quality gasoline as possible. This precise multi-zone coordinated riser reactor system, combined with catalysts specifically designed for DCC, RFCC, and FCC processes, allows for flexible implementation of DCC, RFCC, and FCC processes on a single riser reactor, effectively adapting to various market needs and maximizing the efficiency of the catalytic cracking unit.

[0040] A VQS fast separator 14 is installed at the top of the riser 42. A VQS sealing cover 13 is installed in the reaction settling tank 10, covering the outside of the VQS fast separator 14. The side wall of the VQS sealing cover 13 is connected to a single-stage cyclone separator 11 located outside the VQS sealing cover 13. A reaction oil and gas outlet 12 connected to the top of the single-stage cyclone separator 11 is installed at the top of the reaction settling tank 10. A stripping section 16 is installed at the bottom of the reaction settling tank 10. The connection between the waiting inclined tube 17 and the reaction settling tank 10 is located below the stripping section 16. The mixed catalyst and cracked oil and gas are thrown out from the VQS fast separator 14. Under the action of centrifugal force, the catalyst particles are thrown towards the inner wall of the VQS sealing cover 13, thereby realizing gas-solid separation. The separated oil and gas are separated again by the single-stage cyclone separator 11 and finally enter the reaction oil and gas outlet 12. The stripping section 16 strips the separated catalyst. Steam is used in the stripping section 16 to replace the entrained reaction gas within the catalyst, preventing raw material waste. The cleaned catalyst enters the regenerator through the inclined tube 17 for coke burn-off regeneration. The connection points of the first circulating inclined tube 20 and the second circulating inclined tube 41 with the reaction settling tank 10 are located below the stripping section 16, allowing the catalyst to be stripped before re-entering the first circulating inclined tube 20 and the second circulating inclined tube 41. The stripping section 16 is equipped with a lower stripping steam distributor 8, an upper stripping steam distributor 9, and a stripping baffle 15. The stripping section 16 also features annular and disc-shaped grids, which break up air bubbles, increasing the steam-solid contact probability and improving the stripping effect.

[0041] In the VQS fast separator 14, larger catalyst particles are captured, achieving an efficiency of over 90%. The outlet gas phase enters the single-stage cyclone separator 11 along the riser pipe, where the single-stage cyclone separation efficiency is also over 90%. The total efficiency after separation by the VQS fast separator 14 and the single-stage cyclone separator 11 is over 99.99%. The single-stage cyclone separators 11 are arranged in groups of 4 to 12. The VQS fast separator 14 and VQS enclosure 13 reduce the gas-solid contact time between the reaction oil / gas and the catalyst, reducing side reactions such as olefin condensation and coking, resulting in higher catalyst conversion and selectivity, and reducing coke formation in the reaction settling tank 10, thus extending the production cycle. The gas-solid separation device in this application uses a VQS fast separator, which can also be replaced by a coarse cyclone separator.

[0042] The regenerator includes a first regenerator 25 connected to the pre-regeneration inclined tube 17, a first main air distribution pipe 34 disposed in the first regenerator 25, and a second regenerator 27 connected to the top of the first regenerator 25 and the regeneration inclined tube 22. The second regenerator 27 is equipped with a second main air distribution pipe 28, and a two-stage cyclone separator 26 located above the second main air distribution pipe 28 is disposed in the second regenerator 27. The two-stage cyclone separator 26 is connected to a gas collection chamber 24. After preliminary coking and regeneration in the first regenerator 25, the pre-regeneration catalyst enters the second regenerator 27 for further coking to restore its good activity. The two-stage cyclone separator 26 separates the catalyst from the gas, preventing the catalyst from escaping from the regenerator.

[0043] An external heat exchanger 30 is installed on the outside of the regenerator. The external heat exchanger 30 is connected to a feed pipe 29 communicating with the second regenerator 27 and a discharge pipe 33 communicating with the first regenerator 25. A fluidizing air inlet 31 is also provided on the external heat exchanger 30. The external heat exchanger 30 can recover heat from the regenerated catalyst, improving heat utilization. A slide valve 32 is installed in the discharge pipe 33 to control the amount of regenerated catalyst discharged into the regenerator.

[0044] A waiting slide valve 18 is provided on the waiting inclined tube 17, a waiting slide valve 23 is provided on the regeneration inclined tube 22, an external heat exchanger slide valve 32 is provided on the feed pipe 33, a first circulation slide valve 19 is provided on the first circulation inclined tube 20, and a second circulation slide valve 40 is provided on the second circulation inclined tube 41. The above slide valves are used to control the catalyst circulation amount or cut off the catalyst circulation.

[0045] The above are merely preferred embodiments of this utility model and are not intended to limit the scope of this utility model. Various modifications and variations can be made to this utility model by those skilled in the art. Any modifications, equivalent substitutions, or improvements made within the spirit and principles of this utility model should be included within the protection scope of this utility model.

Claims

1. A multi-zone coordinated control riser reactor system comprising a regenerator and a reaction settler (10), the reaction settler (10) being communicated with a riser (42), the reaction settler (10) being connected with a spent catalyst slanted pipe (17) communicated with the regenerator, characterized in that, The regenerator is connected with an introduction inclined pipe (38), the introduction inclined pipe (38) is connected with a stripper (35), the stripper (35) is provided with a stripping gas distribution pipe (39) located below the pipe opening of the introduction inclined pipe (38), the top of the stripper (35) is provided with a stripping gas return pipe (37) in communication with the regenerator, and the bottom of the stripper (35) is provided with a regenerated inclined pipe (22) in communication with the bottom of the lifting pipe (42).

2. A multi-zone coordinated control riser reactor system as claimed in claim 1, wherein, The stripper (35) is provided with a heat-removing coil (36).

3. A multi-zone coordinated control riser reactor system as claimed in claim 1, wherein, The lifting pipe (42) is sequentially provided with a lifting medium inlet (1), a back-refining liquefied gas inlet (2) and a raw oil nozzle (3) from bottom to top, and the connection position of the regenerated inclined pipe (22) and the lifting pipe (42) is located between the lifting medium inlet (1) and the back-refining liquefied gas inlet (2).

4. A multi-zone coordinated control riser reactor system as claimed in claim 3, wherein, The lifting pipe (42) is provided with a lower diameter expansion section (21) located above the raw oil nozzle (3), and the side wall of the lower diameter expansion section (21) is sequentially provided with a dilution steam inlet (4) and a back-refining oil or oil slurry inlet (5) from bottom to top.

5. A multi-zone coordinated control riser reactor system as claimed in claim 4, wherein, The lifting pipe (42) is provided with a middle diameter expansion section (7) located above the lower diameter expansion section (21), and the lifting pipe (42) is provided with a back-refining light gasoline inlet (6) located between the middle diameter expansion section (7) and the lower diameter expansion section (21).

6. A multi-zone coordinated control riser reactor system as claimed in claim 5, wherein, The middle diameter expansion section (7) is connected with a first circulating inclined pipe (20) in communication with the bottom of the reaction settler (10).

7. A multi-zone coordinated control riser reactor system as claimed in claim 4, wherein, The lower diameter expansion section (21) is connected with a second circulating inclined pipe (41) in communication with the bottom of the reaction settler (10).

8. A multi-zone coordinated control riser reactor system as claimed in claim 1, wherein, The top of the lifting pipe (42) is provided with a VQS quick separation head (14), the reaction settler (10) is provided with a VQS closed cover (13) covering the outside of the VQS quick separation head (14), the side wall of the VQS closed cover (13) is in communication with a single-stage cyclone separator (11) located outside the VQS closed cover (13), the top of the reaction settler (10) is provided with a reaction oil gas outlet (12) in communication with the top of the single-stage cyclone separator (11), and the bottom of the reaction settler (10) is provided with a stripping section (16), and the connection position of the standby inclined pipe (17) and the reaction settler (10) is located below the stripping section (16).

9. A multi-zone coordinated control riser reactor system as claimed in claim 1, wherein, The regenerator comprises a first regenerator (25) connected with the standby inclined pipe (17), the first regenerator (25) is provided with a first main air distribution pipe (34), the top of the first regenerator (25) is in communication with a second regenerator (27) connected with the regenerated inclined pipe (22), the second regenerator (27) is provided with a second main air distribution pipe (28), the second regenerator (27) is provided with a two-stage cyclone separator (26) located above the second main air distribution pipe (28), and the two-stage cyclone separator (26) is connected with a gas collecting chamber (24).

10. A multi-zone coordinated control riser reactor system as claimed in claim 1, wherein, The outside of the regenerator is provided with an external heat-removing device (30), the external heat-removing device (30) is connected with a feeding pipe (29) in communication with the second regenerator (27) and a discharging pipe (33) in communication with the first regenerator (25), and the external heat-removing device (30) is provided with a fluidizing air inlet (31).

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