CN115364775A - Device for controlling reaction temperature in olefin preparation through crude oil catalytic cracking - Google Patents

Device for controlling reaction temperature in olefin preparation through crude oil catalytic cracking Download PDF

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Publication number
CN115364775A
CN115364775A CN202210985465.1A CN202210985465A CN115364775A CN 115364775 A CN115364775 A CN 115364775A CN 202210985465 A CN202210985465 A CN 202210985465A CN 115364775 A CN115364775 A CN 115364775A
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pipe
section
riser
cyclone separator
settler
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CN202210985465.1A
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CN115364775B (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

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention belongs to the field of petrochemical industry, and relates to a device for controlling reaction temperature in olefin preparation through crude oil catalytic cracking, 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 pipe, the pre-riser is connected with the regenerator through a lower regeneration inclined pipe, 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 to-be-regenerated riser, the first settler is internally provided with a first coarse cyclone separator and a first top cyclone separator which are arranged in parallel, 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 through crude oil catalytic cracking
Technical Field
The invention belongs to the field of petrochemical industry, and relates to a device for controlling reaction temperature in the preparation of 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 oil refining and petrochemical industry, the successful popularization of the technology breaks through the traditional oil refining and petrochemical process, and the technology has great promotion effects on further reducing energy consumption, improving diene yield and saving investment. Risers are important equipment for performing catalytic cracking in crude oil catalytic cracking units. The riser reactor is a vertically installed tubular reactor with the length of about 10-30 m and the reaction residence time controlled within 2 s. In the production process, raw materials are continuously fed 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 of 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 increased temperatures for regeneration of the catalyst, but too high temperatures can exacerbate the formation of methane by-product.
Based on the above, the invention designs a novel device for controlling the reaction temperature of olefin preparation by catalytic cracking of crude oil by introducing two paths of high-temperature regenerated catalysts at different upper and lower positions in a dense-phase bed reactor.
Disclosure of Invention
The invention aims to provide a device for controlling reaction temperature in olefin preparation through crude oil catalytic cracking, which introduces two paths of high-temperature regenerated catalysts at different positions in a dense-phase bed reactor, wherein the temperature of each path of catalyst can be properly controlled to be slightly lower, and a longer interval is arranged in the reactor to keep the temperature more uniform, thereby avoiding the rapid reduction of local high temperature and temperature, inhibiting the generation of methane and improving the generation of ethylene and propylene. The quality of the high-temperature catalyst entering the reactor is controlled by two paths of regeneration inclined pipes, so that the adjustment is more flexible and the operation is easier.
A device for controlling reaction temperature in olefin preparation through crude oil catalytic cracking comprises a riser reactor, wherein the riser reactor comprises a riser, a transport bed reactor and a pre-riser, the bottom of the riser is provided with the transport bed reactor, the bottom of the transport bed reactor is provided with the pre-riser, the upper part of the transport bed reactor is connected with a regenerator through an upper regeneration inclined pipe, the pre-riser is connected with the regenerator through a lower regeneration inclined pipe, 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 to-be-regenerated vertical pipe, a first rough cyclone separator and a first top cyclone separator are arranged in the first settler in parallel, and an outlet of the first rough cyclone separator corresponds to an inlet of the first top cyclone separator.
Further, the outlet of the first coarse cyclone separator corresponds to the inlet of the first top cyclone separator, and a gap of 8cm is formed between the outlet of the first coarse cyclone separator and the inlet of the first top cyclone separator.
Further, the distance between the joint of the upper regeneration inclined pipe and the conveying bed reactor and the distance between the lower regeneration inclined pipe and the pre-lifting pipe is 0.1-50m, and preferably 1-10 m.
Furthermore, a pre-lifting medium conveying pipe is arranged in the pre-lifting pipe, and the outlet end of the pre-lifting pipe is positioned above the upper edge of the outlet section of the lower regeneration inclined pipe and is not more than 0.2m.
Furthermore, a raw material nozzle and a dilution gas ring pipe are arranged at the upper part of the pre-lifting 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.
Furthermore, the upper regeneration inclined pipe and the lower regeneration inclined pipe are provided with regeneration slide valves.
Furthermore, 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 rough cyclone separator and a second top cyclone separator are arranged in the second settler, an outlet of the second rough cyclone separator is connected with an inlet of the second top cyclone separator, and the stand pipe to be generated is arranged in an inclined manner.
Furthermore, the regenerator and the first settler are arranged in a coaxial manner, a stripping section is arranged at the bottom of the first settler, a to-be-regenerated vertical pipe is arranged at the lower part of the stripping section and extends into the regenerator, a to-be-regenerated sleeve distributor is sleeved on the periphery of the bottom of the to-be-regenerated vertical pipe and is positioned at the bottom of the regenerator, a catalyst pre-separation structure is arranged between the coarse cyclone separator and the riser, 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 comprises: the device comprises an upper horizontal section and a lower horizontal section, wherein the upper horizontal section is connected with a rough cyclone separator, the lower horizontal section is connected with the upper end of a lifting pipe, the upper horizontal section is connected with the lower horizontal section through a vertical section, the lower end of a pre-separation blanking pipe extends into a settler and then is connected with a 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 blanking pipe is connected with a tangent line of the arc section between the vertical section and the lower horizontal section.
Furthermore, go up regeneration pipe chute for slope section and circular arc section, the diameter from the top down of slope section is the reducing design, and the diameter of higher authority is 300mm, and the diameter is 272.85mm below, the bottom slope of circular arc section is equipped with the medium conveyer pipe, the medium conveyer pipe is located the tangential direction of circular arc section, the diameter of medium conveyer pipe is 80mm.
Furthermore, 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:
(1) The catalyst enters the riser reactor from different heights through the upper regeneration inclined pipe and the lower regeneration inclined pipe, the axial temperature distribution in the conveying bed reactor can be regulated and controlled by controlling the proportion of the catalyst entering the reactor through adjusting the opening degrees of the upper regeneration slide valve and the lower regeneration slide valve so as to form a high-temperature dense bed reaction interval with uniform temperature, and excessive thermal cracking reaction caused by overhigh temperature when raw materials are contacted with a high-temperature regenerant when single-strand catalysts are adopted is avoided, so that 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 reducing design, the upper diameter is large, the lower diameter is small, the arrangement is favorable for controlling the total circulation quantity of the catalyst and controlling the rapid degassing of flue gas in the catalyst, the bottom of the upper regeneration inclined tube is an arc section, the design is favorable for preventing reaction oil gas from flowing backwards to a regenerator, the arc section of the upper regeneration inclined tube is provided with a medium conveying pipe for conveying a medium, the accumulation of the catalyst at a corner can be prevented, the direction of the medium conveying pipe is along the tangential direction of the arc section of the upper regeneration inclined tube, and the movement of the catalyst along the direction of a riser reactor is favorable.
(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, the catalyst and oil gas go upwards along the pre-separation pipe, in the ascending process, the solid catalyst passes through the pre-separation blanking pipe, one part of the solid catalyst enters the stripping section through the pre-separation blanking pipe under the action of gravity, and only one part of the solid catalyst continues to enter the coarse cyclone separator along the vertical section and the upper horizontal section, so that the operation load of the coarse cyclone separator is greatly reduced, the operation stability of the coarse cyclone separator is ensured, the catalyst is effectively prevented from leaking, the operation stability of the crude oil catalytic cracking olefin preparation device is ensured, and meanwhile, the length of the riser reactor can be effectively reduced, the reaction time of the reacted oil gas is shortened, the occurrence of side reactions is reduced, and the yield of target products is improved.
(4) The pre-separation blanking pipe is provided with the inclination angle, and the inclination angle can well avoid the phenomenon that the catalyst is accumulated above the pipe wall of the pre-separation blanking pipe in the settler; and the arrangement of the inclination angle has a degassing function, so that part of oil gas carried in the sliding process of the catalyst can be separated. In actual operation, the catalyst carries more or less part of the reaction oil gas in the downward sliding process. The inclined angle makes full use of the action of the gravity of the catalyst, so that the catalyst slides down at the inclined section of the blanking pipe close to the lower part of the blanking pipe, and even if reaction oil is brought in, the catalyst can return to the pre-separation system through the upper part of the inclined section of the blanking pipe, and the degassing effect of the catalyst is achieved. Meanwhile, after the pre-separation blanking pipe is provided with the inclination angle, 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 with reference to the accompanying drawings in which:
FIG. 1 is a schematic structural view of the present invention in which a regenerator and a first settler are arranged in parallel in high and low directions;
FIG. 2 is a schematic structural view of the present invention with the regenerator and the first settler arranged coaxially;
FIG. 3 is an enlarged schematic view of a transport bed reactor and a pre-riser;
FIG. 4 is an enlarged schematic view of the structure at A in FIG. 2;
FIG. 5 is an enlarged view of the structure at B in FIG. 2;
in the figure, 1-lifting pipe, 2-conveying bed reactor, 3-pre-lifting pipe, 4-upper regeneration inclined pipe, 5-regenerator, 6-lower regeneration inclined pipe, 7-first settler, 8-waiting vertical pipe, 9-first coarse cyclone separator, 10-first top cyclone separator, 11-pre-lifting medium conveying pipe, 12-raw material nozzle, 13-dilution gas ring pipe, 14-regeneration slide valve, 15-second settler, 16-second coarse cyclone separator, 17-second top cyclone separator, 18-stripping section, 19-waiting sleeve distributor, 20-pre-separation discharging pipe, 21-pre-separation pipe and 22-medium conveying pipe.
Detailed Description
Example 1
As shown in fig. 1, a device for controlling reaction temperature in olefin production by crude oil catalytic cracking comprises a riser reactor, wherein the riser reactor comprises a riser 1, a transport bed reactor 2 and a pre-riser 3, the transport bed reactor 2 is arranged at the bottom of the riser 1, the pre-riser 3 is arranged at the bottom of the transport bed reactor 2, the upper part of the transport 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 to-be-regenerated vertical tube 8, and regeneration slide valves 14 are arranged on the upper regeneration inclined tube 4 and the lower regeneration inclined tube 6. A first rough cyclone separator 9 and a first top cyclone separator 10 are arranged in the first settler 7 in parallel, the outlet of the first rough cyclone separator 9 corresponds to the inlet of the first top cyclone separator 10, and a gap of 8cm is formed between the outlet of the first rough cyclone separator 9 and the inlet of the first top cyclone separator 10.
In this embodiment, the distance between the connection of the upper regeneration chute 4 to the transport bed reactor 2 and the lower regeneration chute 6 to the pre-riser 3 is 0.1 to 50m, preferably 1 to 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 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 in a high-low manner, the top of the regenerator 5 is provided with a second settler 15, the second settler 15 is internally provided with a second rough cyclone 16 and a second top cyclone 17, an outlet of the second rough cyclone 16 is connected with an inlet of the second top cyclone 17, and the spent riser 8 is arranged in an inclined manner.
The working principle of the invention is as follows: crude oil outside a boundary area is desalted, dehydrated and heated by a secondary electric desalting tank, enters a riser reactor through a raw material nozzle 12, reacts with a regenerated catalyst in the riser reactor, oil gas after reaction and the spent catalyst enter a spent riser 8 after carried fine catalyst powder is removed at the outlet of the riser 1 through a first coarse cyclone separator 9 and a first top cyclone separator 10, leave a first settler 7, then enter a second settler 15, enter a regenerator 5 after secondary separation is carried out through a second coarse cyclone separator 16 and a second top cyclone separator 17, and complete the scorching 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 cyclic utilization of the catalyst is realized.
Example 2
As shown in fig. 2, a device for controlling reaction temperature in olefin production by crude oil catalytic cracking comprises a riser reactor, wherein the riser reactor comprises a riser 1, a transport bed reactor 2 and a pre-riser 3, the transport bed reactor 2 is arranged at the bottom of the riser 1, the pre-riser 3 is arranged at the bottom of the transport bed reactor 2, the upper part of the transport 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 to-be-regenerated vertical tube 8, and regeneration slide valves 14 are arranged on the upper regeneration inclined tube 4 and the lower regeneration inclined tube 6. 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 formed 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 connection of the upper regenerating chute 4 to the transport bed reactor 2 and the lower regenerating chute 6 to the pre-riser 3 is 0.1 to 50m, preferably 1 to 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 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 coaxially, the bottom of the first settler 7 is provided with a stripping section 18, the lower part of the stripping section 18 is provided with a spent riser 8, the spent riser 8 extends into the regenerator 5, the periphery of the bottom of the spent riser 8 is sleeved with a spent sleeve distributor 19, the spent sleeve distributor 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 discharge pipe 20, and the pre-separation discharge pipe 20 is connected with the pre-separation pipe 21.
In the present embodiment, the preseparation tube 21 includes: the device comprises an upper horizontal section connected with a rough cyclone separator and a lower horizontal section connected with the upper end of a riser 1, wherein the upper horizontal section is connected with the lower horizontal section through a vertical section, the lower end of a pre-separation blanking pipe 20 extends into a settler and then is connected with a 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 with the tangent 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 a variable diameter design from top to bottom, the diameter of the upper surface is 300mm, the diameter of the lower surface is 272.85mm, the bottom of the arc section is obliquely provided with a medium conveying pipe 22, the medium conveying pipe 22 is located in the tangential direction of the arc section, and the diameter of the medium conveying pipe 22 is 80mm.
In this embodiment, the lower regeneration down tube 6 is divided into a vertical section and an inclined section, the inclined section is provided with a regeneration slide valve 14, and the included angle between the inclined section and the vertical section is 32 °.
The working principle of the invention is as follows: the crude oil outside the boundary region enters the boundary region from the raw oil buffer tank, enters the riser reactor from the raw material nozzle 12 after electric desalting and heat exchange temperature rise, and contacts with the 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 a riser reactor and then reach an 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 9 along with the oil gas through a pre-separation vertical section and an upper horizontal section, then the fine powder of the carried catalyst is removed through a first top cyclone 10 and then leaves a first settler 7, the heat is recovered through a reaction oil gas waste heat boiler, the oil gas waste heat boiler generates 4.0MPa medium pressure steam and then 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 feeding pipes of the first rough cyclone 9 and the first top cyclone 10 and the pre-separation feeding pipe 20 enters the regenerator 5 through a spent sleeve distributor 19, completes the coke burning regeneration of the catalyst in the regenerator 5, and then enters the riser 1 generator through the regeneration slide valve 14 for recycling.
Other technical features than those described in the specification are known to those skilled in the art.

Claims (9)

1. A device for controlling reaction temperature in olefin preparation through crude oil catalytic cracking is characterized in that: the device comprises a riser reactor, wherein the riser reactor comprises a riser (1), a transport bed reactor (2) and a pre-riser (3), the transport bed reactor (2) is arranged at the bottom of the riser (1), the pre-riser (3) is arranged at the bottom of the transport bed reactor (2), the upper part of the transport 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) extends into a first settler (7), the bottom of the first settler (7) is connected with a regenerator (5) through a stand pipe (8) to be regenerated, a first rough cyclone separator (9) and a first top cyclone separator (10) are arranged in the first settler (7) in parallel, the outlet of the first rough cyclone separator (9) corresponds to the inlet of the first top cyclone separator (10), and a gap of 8cm is arranged between the outlet of the first rough cyclone separator (9) and the inlet of the first top cyclone separator (10).
2. The apparatus for controlling reaction temperature in the production of olefins by catalytic cracking of crude oil according to claim 1, wherein: the distance between the joint of the upper regeneration inclined pipe (4) and the conveying bed reactor (2) and the distance between the lower regeneration inclined pipe (6) and the pre-lifting pipe (3) is 0.1-50m, preferably 1-10 m.
3. The apparatus for controlling reaction temperature in the production of olefins by catalytic cracking of crude oil according to claim 1, wherein: a pre-lifting medium conveying pipe (11) is arranged in the pre-lifting pipe (3), and the outlet end of the pre-lifting 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 production 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 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.
5. The apparatus for controlling reaction temperature in the production of olefins by catalytic cracking of crude oil according to claim 1, wherein: regenerator (5) and first settler (7) adopt the coaxial-type setting, the bottom of first settler (7) is equipped with strip section (18), the lower part of strip section (18) is equipped with waits to give birth to riser (8), wait to give birth to in riser (8) stretches into regenerator (5), the bottom periphery cover of waiting to give birth to riser (8) is equipped with and waits to give birth to sleeve distributor (19), it is located regenerator (5) bottom to wait to give birth to sleeve distributor, be equipped with catalyst preseparation structure between thick cyclone and riser (1), catalyst preseparation structure includes preseparation pipe (21) and preseparation unloading pipe (20), preseparation unloading pipe (20) are connected with preseparation pipe (21).
6. The apparatus for controlling reaction temperature in the production of olefins by catalytic cracking of crude oil according to claim 5, wherein: the pre-separation duct (21) comprises: the device comprises an upper horizontal section connected with a rough cyclone separator and a lower horizontal section connected with the upper end of a lifting pipe (1), wherein the upper horizontal section is connected with the lower horizontal section through a vertical section, the lower end of a pre-separation blanking pipe (20) extends into a settler and then is connected with a stripping section (18), the vertical section is in smooth transition with the lower horizontal section through an arc section, the upper horizontal section is in smooth transition with the vertical section through an arc section, and the upper end of the pre-separation blanking pipe (20) is connected with the tangent of the arc section between the vertical section and the lower horizontal section.
7. The apparatus for controlling reaction temperature in the production of olefins by catalytic cracking of crude oil according to claim 6, wherein: go up regeneration pipe chute (4) for slope section and circular arc section, the diameter from the top down of slope section is the reducing design, and the diameter of going up is 300mm, and the diameter is 272.85mm below, the bottom slope of circular arc section is equipped with medium conveyer pipe (22), medium conveyer pipe (22) are located the tangential direction of circular arc section, the diameter of medium conveyer pipe (22) is 80mm.
8. The apparatus for controlling reaction temperature in the production of olefins by catalytic cracking of crude oil according to claim 6, wherein: the lower regeneration inclined pipe (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.
9. The apparatus for controlling reaction temperature in the production 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 a high-low mode, a second settler (15) is arranged at the top of the regenerator (5), a second rough cyclone separator (16) and a second top cyclone separator (17) are arranged in the second settler (15), an outlet of the second rough cyclone separator (16) is connected with an inlet of the second top cyclone separator (17), and the stand pipe (8) to be grown is obliquely arranged.
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