CN115364775B - Device for controlling reaction temperature in olefin preparation by crude oil catalytic pyrolysis - Google Patents

Device for controlling reaction temperature in olefin preparation by crude oil catalytic pyrolysis Download PDF

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Publication number
CN115364775B
CN115364775B CN202210985465.1A CN202210985465A CN115364775B CN 115364775 B CN115364775 B CN 115364775B CN 202210985465 A CN202210985465 A CN 202210985465A CN 115364775 B CN115364775 B CN 115364775B
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pipe
section
cyclone separator
riser
settler
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CN115364775A (en
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李治
丁书兵
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Shandong High End Chemical Research Institute Co ltd
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Shandong High End Chemical Research Institute Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/0055—Separating solid material from the gas/liquid stream using cyclones
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/007—Separating solid material from the gas/liquid stream by sedimentation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/065—Feeding reactive fluids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
    • C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
    • C07C4/06—Catalytic processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B01J2208/00902—Nozzle-type feeding elements
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/584—Recycling of catalysts

Abstract

The invention belongs to the field of petrochemical industry, and relates to a device for controlling reaction temperature in olefin preparation by catalytic cracking of crude oil, which comprises a riser reactor, wherein the riser reactor comprises a riser, a conveying bed reactor and a pre-riser, the bottom of the riser is provided with the conveying bed reactor, the bottom of the conveying bed reactor is provided with the pre-riser, the upper part of the conveying bed reactor is connected with a regenerator through an upper regeneration inclined tube, the pre-riser is connected with the regenerator through a lower regeneration inclined tube, the upper part of the riser is connected with a first settler, the bottom of the first settler is connected with the regenerator through a stand pipe, a first coarse cyclone separator and a first top cyclone separator are arranged in parallel in the first settler, and the outlet of the first coarse cyclone separator corresponds to the inlet of the first top cyclone separator.

Description

Device for controlling reaction temperature in olefin preparation by crude oil catalytic pyrolysis
Technical Field
The invention belongs to the field of petrochemical industry, and relates to a device for controlling reaction temperature in the process of preparing olefin by catalytic cracking of crude oil.
Background
The popularization of the technology for preparing olefin by catalytic cracking of crude oil has profound significance for the industries of oil refining and petrochemical industry, and the successful popularization of the technology breaks through the traditional oil refining and petrochemical process and has great propulsion effects on further reducing energy consumption, improving diene yield and saving investment. Riser is an important device for catalytic cracking in crude catalytic cracking units. The length of the riser reactor is about 10-30 m, the reaction residence time is controlled within 2s, and the riser reactor is a vertically installed tubular reactor. In the production process, raw materials are continuously sent into the riser reactor to be mixed with the catalyst, the regenerated catalyst is conveyed into the riser reactor through an independent single pipeline, and after the single-path high-temperature regenerated catalyst is contacted with the raw materials, the reaction temperature is reduced, the activity is reduced, and the side reaction is increased. To promote adequate conversion of the feedstock requires an increase in the temperature of the regenerated catalyst, but excessive temperatures can exacerbate the formation of methane by-products.
Based on the method, the novel device for controlling the reaction temperature of preparing olefin by catalytic cracking of crude oil is designed by introducing two paths of high-temperature regenerated catalysts at different positions in the dense bed reactor.
Disclosure of Invention
The invention aims to provide a device for controlling the reaction temperature of olefin prepared by catalytic cracking of crude oil, which introduces two paths of high-temperature regenerated catalysts at different positions in a dense bed reactor, wherein the temperature of each path of catalyst can be properly controlled to be slightly lower, and the temperature is kept more uniform in a longer interval in the reactor, so that the rapid reduction of local high temperature and temperature is avoided, the generation of methane is inhibited, and the generation of ethylene and propylene is improved. The quality of the high-temperature catalyst entering the reactor is controlled by two paths of regeneration inclined pipes, so that the regulation is more flexible and the operation is easier.
The utility model provides a device of crude catalytic cracking system olefin control reaction temperature, includes the riser reactor, the riser reactor includes riser, transport bed reactor and pre-riser, the bottom of riser is equipped with the transport bed reactor, the bottom of transport bed reactor is equipped with pre-riser, the upper portion of transport bed reactor links to each other with the regenerator through last regeneration inclined tube, pre-riser links to each other with the regenerator through lower regeneration inclined tube, the upper portion of riser links to each other with first settler, the bottom of first settler links to each other with the regenerator through waiting for the riser, be equipped with in the first settler and install first coarse cyclone and first top cyclone in parallel, the export of first coarse cyclone corresponds with first top cyclone separator entry.
Further, the outlet of the first coarse cyclone corresponds to the inlet of the first top cyclone, and a gap of 8cm is reserved between the outlet of the first coarse cyclone and the inlet of the first top cyclone.
Further, the distance between the junction of the upper regeneration chute and the transport bed reactor and between the lower regeneration chute and the pre-riser is 0.1-50m, preferably 1-10 m.
Further, a pre-lifting medium conveying pipe is arranged in the pre-lifting pipe, and the outlet end of the pre-lifting medium conveying pipe is positioned above the upper edge of the outlet section of the lower regeneration inclined pipe and is not more than 0.2m.
Further, the upper part of the pre-lifting pipe is provided with a raw material nozzle and a dilution gas ring pipe, the dilution gas distribution pipe is arranged below, the raw material nozzle is arranged above, and the distance between the dilution gas distribution pipe and the raw material nozzle is 0.1-50m, preferably 0.2-20m.
Further, the upper regeneration inclined pipe and the lower regeneration inclined pipe are provided with regeneration slide valves.
Further, the regenerator and the first settler are arranged in parallel in height, a second settler is arranged at the top of the regenerator, a second coarse cyclone separator and a second top cyclone separator are arranged in the second settler, an outlet of the second coarse cyclone separator is connected with an inlet of the second top cyclone separator, and the stand pipe to be regenerated is obliquely arranged.
Further, the regenerator and the first settler are arranged coaxially, a stripping section is arranged at the bottom of the first settler, a stand pipe to be regenerated is arranged at the lower part of the stripping section, the stand pipe to be regenerated stretches into the regenerator, a sleeve distributor to be regenerated is sleeved on the periphery of the bottom of the stand pipe to be regenerated, the sleeve distributor to be regenerated is positioned at the bottom of the regenerator, a catalyst pre-separation structure is arranged between the coarse cyclone separator and the lifting pipe, the catalyst pre-separation structure comprises a pre-separation pipe and a pre-separation blanking pipe, and the pre-separation blanking pipe is connected with the pre-separation pipe.
Further, the pre-separation tube includes: the cyclone separator comprises an upper horizontal section connected with the cyclone separator and a lower horizontal section connected with the upper end of the lifting pipe, wherein the upper horizontal section and the lower horizontal section are connected through a vertical section, the lower end of the pre-separation discharging pipe stretches into the settler and then is connected with the stripping section, the vertical section and the lower horizontal section are in smooth transition through an arc section, the upper horizontal section and the vertical section are in smooth transition through an arc section, and the upper end of the pre-separation discharging pipe is connected with the tangent line of the arc section between the vertical section and the lower horizontal section.
Further, the upper regeneration inclined tube is an inclined section and an arc section, the diameter of the inclined section is designed to be variable from top to bottom, the upper diameter is 300mm, the lower diameter is 272.85mm, the bottom of the arc section is obliquely provided with a medium conveying tube, the medium conveying tube is positioned in the tangential direction of the arc section, and the diameter of the medium conveying tube is 80mm.
Further, the lower regeneration inclined pipe is divided into a vertical section and an inclined section, a regeneration slide valve is arranged on the inclined section, and the included angle between the inclined section and the vertical section is 32 degrees.
The beneficial effects of the invention are as follows:
(1) The catalyst enters the riser reactor from different heights through the upper regeneration inclined tube and the lower regeneration inclined tube, the axial temperature distribution in the conveying bed reactor can be regulated and controlled by adjusting the opening of the upper regeneration slide valve and the lower regeneration slide valve to control the proportion of the catalyst entering the reactor, so that a high-temperature dense bed reaction zone with uniform temperature is formed, excessive thermal cracking reaction caused by overhigh temperature when the raw materials are contacted with a high-temperature regenerant is avoided when a single-strand catalyst is adopted, the yield of methane is reduced, and the selectivity of low-carbon olefins such as ethylene, propylene and the like is improved.
(2) The inclined tube of the upper regeneration inclined tube adopts a variable diameter design, the diameter of the upper surface is large, the diameter of the lower surface is small, the arrangement is favorable for controlling the total circulation quantity of the catalyst, the rapid degassing of the flue gas in the catalyst is favorable, the bottom of the upper regeneration inclined tube is an arc section, the design is favorable for preventing reaction oil gas from flowing backwards towards the regenerator, the arc section of the upper regeneration inclined tube is provided with a medium conveying tube for conveying a medium, the catalyst can be prevented from accumulating at a turning position, and the direction of the medium conveying tube is along the tangential direction of the arc section of the upper regeneration inclined tube, so that the catalyst can move along the direction of a riser reactor.
(3) The invention is provided with the pre-separation pipe, the height difference is formed between the upper horizontal section and the lower horizontal section through the vertical section, after crude oil passes through the riser reactor, catalyst and oil gas go upward along the pre-separation pipe, in the upward process, solid catalyst passes through the pre-separation blanking pipe, part of the catalyst enters the stripping section through the pre-separation blanking pipe under the action of gravity, and only part of the catalyst continuously enters the crude cyclone separator along the vertical section and the upper horizontal section, so that the operation load of the crude cyclone separator is greatly reduced, the operation stability of the crude cyclone separator is ensured, the catalyst running agent is effectively prevented, the operation stability of an olefin preparation device by crude oil catalytic cracking is ensured, and meanwhile, the pre-separation system is arranged, the length of the riser reactor is effectively reduced, the reaction time of reaction oil gas is reduced, the occurrence of side reaction is reduced, and the yield of a target product is improved.
(4) The pre-separation blanking pipe is provided with the inclined angle, and the phenomenon that the catalyst is accumulated above the pipe wall of the pre-separation blanking pipe in the settler can be well avoided due to the arrangement of the inclined angle; and secondly, the arrangement of the inclined angle has the degassing effect, and can separate part of oil gas carried in the sliding process of the catalyst. During actual operation, the catalyst more or less carries part of the reaction oil gas during the downward sliding process. The arrangement of the inclined angle makes full use of the gravity effect of the catalyst, so that the catalyst slides down near the lower part of the blanking pipe at the inclined section of the blanking pipe, and even if reaction oil is carried in, the catalyst can also return to the pre-separation system through the upper part of the inclined section of the blanking pipe, thereby achieving the effect of catalyst degassing. Meanwhile, after the inclined angle is arranged on the pre-separation blanking pipe, the problem that the catalyst carries oil gas to enter the stripping section in the pre-separation process can be greatly solved, the stripping load of the stripping section is reduced, the steam consumption is reduced, and the energy consumption of the device is further reduced.
Drawings
The invention is further described below with reference to the accompanying drawings:
FIG. 1 is a schematic view of the structure of the present invention when the regenerator and the first settler are arranged side by side;
FIG. 2 is a schematic view of the structure of the present invention with the regenerator and the first settler coaxially arranged;
FIG. 3 is an enlarged schematic view of a transport bed reactor and a pre-riser;
FIG. 4 is an enlarged schematic view of FIG. 2A;
FIG. 5 is an enlarged schematic view of the structure shown at B in FIG. 2;
in the figure, 1-riser, 2-transport bed reactor, 3-pre-riser, 4-upper regeneration chute, 5-regenerator, 6-lower regeneration chute, 7-first settler, 8-spent riser, 9-first coarse cyclone, 10-first top cyclone, 11-pre-riser medium transport pipe, 12-feed nozzle, 13-dilution gas loop, 14-regeneration slide valve, 15-second settler, 16-second coarse cyclone, 17-second top cyclone, 18-stripping section, 19-spent sleeve distributor, 20-pre-separation blanking pipe, 21-pre-separation pipe.
Detailed Description
Example 1
As shown in fig. 1, a device for controlling reaction temperature in olefin preparation by catalytic cracking of crude oil comprises a riser reactor, wherein the riser reactor comprises a riser 1, a conveying bed reactor 2 and a pre-riser 3, the bottom of the riser 1 is provided with the conveying bed reactor 2, the bottom of the conveying bed reactor 2 is provided with the pre-riser 3, the upper part of the conveying bed reactor 2 is connected with a regenerator 5 through an upper regeneration inclined tube 4, the pre-riser 3 is connected with the regenerator 5 through a lower regeneration inclined tube 6, the upper part of the riser 1 is connected with a first settler 7, the bottom of the first settler 7 is connected with the regenerator 5 through a waiting vertical tube 8, and regeneration slide valves 14 are arranged on the upper regeneration inclined tube 4 and the lower regeneration inclined tube 6. The first settler 7 is internally provided with a first coarse cyclone separator 9 and a first top cyclone separator 10 which are installed in parallel, the outlet of the first coarse cyclone separator 9 corresponds to the inlet of the first top cyclone separator 10, and a gap of 8cm is reserved between the outlet of the first coarse cyclone separator 9 and the inlet of the first top cyclone separator 10.
In this embodiment, the distance between the junction of the upper regeneration chute 4 and the transport bed reactor 2 and the lower regeneration chute 6 and the pre-riser 3 is 0.1-50m, preferably 1-10 m. The pre-lifting pipe 3 is internally provided with a pre-lifting medium conveying pipe 11, and the outlet end of the pre-lifting medium conveying pipe is positioned above the upper edge of the outlet section of the lower regeneration inclined pipe 6 and is not more than 0.2m. The upper part of the pre-lifting pipe 3 is provided with a raw material nozzle 12 and a dilution gas ring pipe 13, the dilution gas distribution pipe is arranged below, the raw material nozzle 12 is arranged above, and the distance between the dilution gas distribution pipe and the raw material nozzle 12 is 0.1-50m, preferably 0.2-20m.
In this embodiment, the regenerator 5 and the first settler 7 are arranged in parallel, a second settler 15 is arranged at the top of the regenerator 5, a second coarse cyclone separator 16 and a second top cyclone separator 17 are arranged in the second settler 15, an outlet of the second coarse cyclone separator 16 is connected with an inlet of the second top cyclone separator 17, and the stand pipe 8 to be regenerated is obliquely arranged.
The working principle of the invention is as follows: crude oil outside the boundary region enters a riser reactor through a raw material nozzle 12 after being desalted and dehydrated and heated by a second-stage electric desalting tank, reacts with regenerated catalyst in the riser reactor, the reacted oil gas and the spent catalyst enter the riser reactor through a first coarse cyclone 9 and a first top cyclone 10 at the outlet of the riser 1 after carrying catalyst fine powder is removed, enter a spent riser 8 to leave a first settler 7, then enter a second settler 15, enter a regenerator 5 after being subjected to secondary separation by a second coarse cyclone 16 and a second top cyclone 17, and complete burnt regeneration of the catalyst in the regenerator 5, and the regenerated catalyst enters the riser reactor through an upper regeneration inclined tube 4 and a lower regeneration inclined tube 6, so that the recycling of the catalyst is realized.
Example 2
As shown in fig. 2, a device for controlling reaction temperature in olefin preparation by catalytic cracking of crude oil comprises a riser reactor, wherein the riser reactor comprises a riser 1, a conveying bed reactor 2 and a pre-riser 3, the bottom of the riser 1 is provided with the conveying bed reactor 2, the bottom of the conveying bed reactor 2 is provided with the pre-riser 3, the upper part of the conveying bed reactor 2 is connected with a regenerator 5 through an upper regeneration inclined tube 4, the pre-riser 3 is connected with the regenerator 5 through a lower regeneration inclined tube 6, the upper part of the riser 1 is connected with a first settler 7, the bottom of the first settler 7 is connected with the regenerator 5 through a waiting vertical tube 8, and regeneration slide valves 14 are arranged on the upper regeneration inclined tube 4 and the lower regeneration inclined tube 6. The first settler 7 is internally provided with a first coarse cyclone separator 9 and a first top cyclone separator 10 which are installed in parallel, the outlet of the first coarse cyclone separator 9 corresponds to the inlet of the first top cyclone separator 10, and a gap of 8cm is reserved between the outlet of the first coarse cyclone separator 9 and the inlet of the first top cyclone separator 10.
In this embodiment, the distance between the junction of the upper regeneration chute 4 and the transport bed reactor 2 and the lower regeneration chute 6 and the pre-riser 3 is 0.1-50m, preferably 1-10 m. The pre-lifting pipe 3 is internally provided with a pre-lifting medium conveying pipe 11, and the outlet end of the pre-lifting medium conveying pipe is positioned above the upper edge of the outlet section of the lower regeneration inclined pipe 6 and is not more than 0.2m. The upper part of the pre-lifting pipe 3 is provided with a raw material nozzle 12 and a dilution gas ring pipe 13, the dilution gas distribution pipe is arranged below, the raw material nozzle 12 is arranged above, and the distance between the dilution gas distribution pipe and the raw material nozzle 12 is 0.1-50m, preferably 0.2-20m.
In this embodiment, the regenerator 5 and the first settler 7 are coaxially arranged, a stripping section 18 is arranged at the bottom of the first settler 7, a stand pipe 8 to be regenerated is arranged at the lower part of the stripping section 18, the stand pipe 8 to be regenerated stretches into the regenerator 5, a sleeve distributor 19 to be regenerated is sleeved at the periphery of the bottom of the stand pipe 8 to be regenerated, the sleeve distributor to be regenerated is positioned at the bottom of the regenerator 5, a catalyst pre-separation structure is arranged between the coarse cyclone separator and the riser 1, the catalyst pre-separation structure comprises a pre-separation pipe 21 and a pre-separation blanking pipe 20, and the pre-separation blanking pipe 20 is connected with the pre-separation pipe 21.
In this embodiment, the pre-separation pipe 21 includes: the upper horizontal section connected with the coarse cyclone separator and the lower horizontal section connected with the upper end of the lifting pipe 1 are connected through a vertical section, the lower end of the pre-separation blanking pipe 20 stretches into the settler and then is connected with the stripping section 18, the vertical section and the lower horizontal section are in smooth transition through an arc section, the upper horizontal section and the vertical section are in smooth transition through an arc section, and the upper end of the pre-separation blanking pipe 20 is connected to the tangent line of the arc section between the vertical section and the lower horizontal section.
In this embodiment, the upper regeneration inclined tube 4 is an inclined section and an arc section, the diameter of the inclined section is designed to be variable from top to bottom, the upper diameter is 300mm, the lower diameter is 272.85mm, the bottom of the arc section is obliquely provided with a medium conveying tube, the medium conveying tube is located in the tangential direction of the arc section, and the diameter of the medium conveying tube is 80mm.
In this embodiment, the lower regeneration chute 6 is divided into a vertical section and an inclined section, on which a regeneration slide valve 14 is arranged, the angle of which is 32 ° to the vertical section.
The working principle of the invention is as follows: crude oil outside the boundary region enters the boundary region from the raw oil buffer tank, is subjected to electric desalting, heat exchange and temperature rise, and then enters the riser reactor from the raw material nozzle 12, and is contacted with a catalyst for temperature rise, vaporization and reaction. The reacted oil gas and spent catalyst enter a lower horizontal section at an outlet at the upper end of the riser reactor, then reach the circular arc section, part of the catalyst falls into a stripping section 18 through a pre-separation blanking pipe 20 under the action of self gravity, the rest of the spent catalyst enters a first coarse cyclone separator 9 along with the oil gas through a pre-separation vertical section and an upper horizontal section, then leaves a first settler 7 after the carried catalyst fine powder is removed through a first top cyclone separator 10, heat is recovered through a reaction oil gas waste heat boiler, medium-pressure steam with pressure of 4.0MPa enters a fractionating tower, and the rest of the spent catalyst enters the stripping section 18. The spent catalyst entering the stripping section 18 through the blanking pipe and the pre-separation blanking pipe 20 of the first coarse cyclone 9 and the first top cyclone 10 enters the regenerator 5 through the spent sleeve distributor 19, the burnt regeneration of the catalyst is completed in the regenerator 5, and then enters the riser 1 generator through the regeneration slide valve 14 for recycling.
The technical features are known to those skilled in the art except the technical features described in the specification.

Claims (7)

1. A device for controlling the reaction temperature of olefin prepared by catalytic cracking of crude oil is characterized in that: the device comprises a riser reactor, wherein the riser reactor comprises a riser (1), a conveying bed reactor (2) and a pre-riser (3), the bottom of the riser (1) is provided with the conveying bed reactor (2), the bottom of the conveying bed reactor (2) is provided with the pre-riser (3), the upper part of the conveying bed reactor (2) is connected with a regenerator (5) through an upper regeneration inclined pipe (4), the pre-riser (3) is connected with the regenerator (5) through a lower regeneration inclined pipe (6), and regeneration slide valves (14) are arranged on the upper regeneration inclined pipe (4) and the lower regeneration inclined pipe (6);
the upper part of the lifting pipe (1) is connected with a first settler (7), the bottom of the first settler (7) is connected with a regenerator (5) through a stand pipe (8), a first coarse cyclone separator (9) and a first top cyclone separator (10) are arranged in the first settler (7) in parallel, the outlet of the first coarse cyclone separator (9) corresponds to the inlet of the first top cyclone separator (10), and a gap of 8cm is reserved between the outlet of the first coarse cyclone separator (9) and the inlet of the first top cyclone separator (10);
the novel catalyst pre-separation device is characterized in that the regenerator (5) and the first settler (7) are coaxially arranged, a stripping section (18) is arranged at the bottom of the first settler (7), a to-be-generated vertical pipe (8) is arranged at the lower part of the stripping section (18), the to-be-generated vertical pipe (8) stretches into the regenerator (5), a to-be-generated sleeve distributor (19) is sleeved on the periphery of the bottom of the to-be-generated vertical pipe (8), the to-be-generated sleeve distributor (19) is positioned at the bottom of the regenerator (5), a catalyst pre-separation structure is arranged between the coarse cyclone separator and the lifting pipe (1), the catalyst pre-separation structure comprises a pre-separation pipe (21) and a pre-separation blanking pipe (20), and the pre-separation blanking pipe (20) is connected with the pre-separation pipe (21);
the preseparation pipe (21) comprises: the cyclone separator comprises an upper horizontal section connected with the cyclone separator and a lower horizontal section connected with the upper end of the lifting pipe (1), wherein the upper horizontal section and the lower horizontal section are connected through a vertical section, the lower end of the pre-separation blanking pipe (20) stretches into the settler and then is connected with the stripping section (18), the vertical section and the lower horizontal section are smoothly transited through an arc section, the upper horizontal section and the vertical section are smoothly transited through an arc section, and the upper end of the pre-separation blanking pipe (20) is connected to the tangent line of the arc section between the vertical section and the lower horizontal section.
2. The apparatus for controlling reaction temperature in the preparation of olefins by catalytic cracking of crude oil according to claim 1, wherein: the distance between the connection part of the upper regeneration inclined tube (4) and the conveying bed reactor (2) and the distance between the lower regeneration inclined tube (6) and the pre-lifting tube (3) are 0.1-50m.
3. The apparatus for controlling reaction temperature in the preparation of olefins by catalytic cracking of crude oil according to claim 1, wherein: the pre-lifting pipe (3) is internally provided with a pre-lifting medium conveying pipe (11), and the outlet end of the pre-lifting medium conveying pipe is positioned above the upper edge of the outlet section of the lower regeneration inclined pipe (6) and is not more than 0.2m.
4. The apparatus for controlling reaction temperature in the preparation of olefins by catalytic cracking of crude oil according to claim 1, wherein: the upper part of the pre-lifting pipe (3) is provided with a raw material nozzle (12) and a dilution air ring pipe (13), the dilution air ring pipe (13) is arranged below, the raw material nozzle (12) is arranged above, and the distance between the dilution air ring pipe (13) and the raw material nozzle (12) is 0.1-50m.
5. The apparatus for controlling reaction temperature in the preparation of olefins by catalytic cracking of crude oil according to claim 1, wherein: the upper regeneration inclined tube (4) is an inclined section and an arc section, the diameter of the inclined section is designed to be variable from top to bottom, the upper diameter is 300mm, the lower diameter is 272.85mm, the bottom of the arc section is obliquely provided with a medium conveying tube, the medium conveying tube is positioned in the tangential direction of the arc section, and the diameter of the medium conveying tube is 80mm.
6. The apparatus for controlling reaction temperature in the preparation of olefins by catalytic cracking of crude oil according to claim 1, wherein: the lower regeneration inclined tube (6) is divided into a vertical section and an inclined section, a regeneration slide valve (14) is arranged on the inclined section, and the included angle between the inclined section and the vertical section is 32 degrees.
7. The apparatus for controlling reaction temperature in the preparation of olefins by catalytic cracking of crude oil according to claim 1, wherein: the regenerator (5) and the first settler (7) are arranged in parallel in height, a second settler (15) is arranged at the top of the regenerator (5), a second coarse cyclone separator (16) and a second top cyclone separator (17) are arranged in the second settler (15), an outlet of the second coarse cyclone separator (16) is connected with an inlet of the second top cyclone separator (17), and the stand pipe (8) to be regenerated is obliquely arranged.
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