A system and method for the regeneration of a catalyst for the catalytic conversion of light hydrocarbon oils

Abstract

The present disclosure relates to a system and method for regenerating a light hydrocarbon oil catalytic conversion catalyst, which adopts a coking drum, a dilute phase pipe and a two-bed coupled system for catalyst regeneration treatment, does not need to additionally add a regenerated catalyst degassing drum, can reduce device energy consumption and operating costs, and further reduces the investment of the equipment. Moreover, a heat supplement device is arranged in the system, which can increase the coke content of the regenerated catalyst returned to the coking drum, can not only ensure the heat balance of the light hydrocarbon oil catalytic conversion reaction and the regeneration system, but also can avoid the problem of catalyst crushing and deactivation caused by directly spraying fuel into the regenerator. In addition, the system can be independently arranged, which improves the safety and applicability of the system.

Description

TECHNICAL FIELD

[0001] The present disclosure relates to the field of petroleum chemical industry, in particular, to a system and method for regeneration of a catalyst for catalytic conversion of light hydrocarbon oil. BACKGROUND

[0002] In the production technology of low-carbon olefins by cracking of hydrocarbons, the tubular furnace thermal cracking method is one of the main methods for production of ethylene and propylene in the world. With the increasing demand for propylene derivatives, the production of propylene obtained by the thermal cracking method has been unable to meet the demand, therefore, improving the propylene / ethylene yield has become a hot issue. In recent years, more and more attention has been paid to other new technologies for production of low-carbon olefins and low-carbon aromatic hydrocarbons. The technology for production of low-carbon olefins and low-carbon aromatic hydrocarbons by catalytic cracking of light gas oil is one of the most widely used technologies. However, the method for converting light gas oil into low-carbon olefins has a series of problems such as insufficient heat of the reaction-regeneration system, safety hazards caused by reactor wear, and high-temperature crushing and deactivation of the catalyst due to low coke formation during the catalytic conversion of light hydrocarbon oil. SUMMARY

[0003] The purpose of the present disclosure is to provide a system and method for regeneration of a catalyst for catalytic conversion of light hydrocarbon oil, which has solved the problems of insufficient heat of the reaction-regeneration system, safety hazards caused by reactor wear, and high-temperature crushing and deactivation of the catalyst due to low coke formation in the prior art.

[0004] To achieve the above object, the first aspect of the present disclosure provides a system for regenerating a catalyst for catalytic conversion of light hydrocarbon oil, which comprises a coking drum, a dilute phase pipe, a double bed and a heat supplement device; the coking drum, the dilute phase pipe and the double bed are coaxially arranged; the coking drum is integrally arranged below the double bed; the dilute phase pipe is arranged above the coking drum and inside the double bed; the inlet of the dilute phase pipe is in communication with the outlet of the coking drum; the coking drum comprises a main air inlet, a spent catalyst inlet, a heat supplement catalyst inlet and a third regenerated catalyst inlet; the shell of the double bed is provided with a first regenerated catalyst outlet, a second regenerated catalyst outlet, a third regenerated catalyst outlet and a heat supplement flue gas inlet; the upper part of the heat supplement device is provided with a second regenerated catalyst inlet, the lower part is provided with a heat supplement catalyst outlet and the top is provided with a heat supplement flue gas outlet; the main air inlet of the coking drum is used in communication with a main air source, the spent catalyst inlet of the coking drum is used in communication with a spent catalyst source through a spent catalyst inclined pipe; the first regenerated catalyst outlet of the double bed is used in communication with a light hydrocarbon oil catalytic conversion reactor through a regenerated catalyst inclined pipe; the second regenerated catalyst outlet of the double bed is in communication with the second regenerated catalyst inlet of the heat supplement device through an upper heat supplement device inclined pipe; the heat supplement catalyst outlet of the heat supplement device is in communication with the heat supplement catalyst inlet of the coking drum through a lower heat supplement device inclined pipe; the heat supplement flue gas outlet of the heat supplement device is in communication with the heat supplement flue gas inlet of the double bed through a heat supplement flue gas return pipe; the third regenerated catalyst outlet of the double bed is in communication with the third regenerated catalyst inlet of the coking drum through a regenerated catalyst circulation inclined pipe.

[0005] Optionally, the inside of the heat supplement device is provided with a heat supplement fuel distributor and a fluidizing medium distributor arranged below the heat supplement fuel distributor; the inlet of the heat supplement fuel distributor is used in communication with a heat supplement fuel source; the inlet of the fluidizing medium distributor is used in communication with a fluidizing medium source; the heat supplement fuel distributor is provided with a plurality of downwardly opening injection holes; the fluidizing medium distributor is provided with a plurality of upwardly opening injection holes.

[0006] Optionally, the bottom of the coking drum is provided with a coking drum main air distributor; the lower part of the double bed is provided with at least one set of double bed main air distributors; the coking drum main air distributor and the double bed main air distributor are each independently selected from one or more of a dendritic distribution pipe, a distribution ring and a distribution nozzle; the regenerated catalyst circulation inclined pipe is provided with a regenerated catalyst circulation slide valve; the lower heat supplement device inclined pipe is provided with a lower heat supplement device slide valve.

[0007] Optionally, the dilute phase pipe is provided with a dilute phase pipe quick separation head; the outlet of the dilute phase pipe is in communication with the inlet of the dilute phase pipe quick separation head; the dilute phase pipe quick separation head comprises one or more of an inverted L-shaped quick separation, a T-shaped quick separation, a multi-leaf quick separation, a cyclone quick separation and a coarse cyclone quick separation.

[0008] Optionally, the second dense bed is internally provided with a plenum chamber and a cyclone separator; the upper portion of the dilute phase pipe is located at the middle upper portion of the second dense bed; the plenum chamber is located above the dilute phase pipe, the separation portion of the cyclone separator is located above the dilute phase pipe, the bottom of the dipleg is located above and / or below the dilute phase pipe; the top of the second dense bed comprises a regenerated flue gas outlet, the plenum chamber comprises a regenerated flue gas inlet and a regenerated flue gas outlet; the cyclone separator comprises a gas outlet, a catalyst outlet and a gas inlet; the gas outlet of the cyclone separator is in communication with the regenerated flue gas inlet of the plenum chamber; the outlet of the plenum chamber is in communication with the regenerated flue gas outlet of the second dense bed; the catalyst outlet of the cyclone separator is located above and / or below the dense phase bed layer of the regenerated catalyst in the second dense bed.

[0009] The second aspect of the present disclosure provides a method for regenerating a catalyst for catalytic conversion of light hydrocarbon oil by using the system of the first aspect of the present disclosure, the method comprising: passing the spent catalyst through the spent inclined pipe into the decoking tank to contact with the decoking main air for regeneration treatment, to obtain a mixture of regenerated flue gas and regenerated catalyst; making the mixture flow upward into the dilute phase pipe to separate to obtain the regenerated flue gas entraining a small amount of catalyst and part of the regenerated catalyst; making the regenerated flue gas entraining the catalyst flow upward and further separate to obtain the regenerated flue gas and another part of the regenerated catalyst; making the part of the regenerated catalyst and the another part of the regenerated catalyst flow downward into the second dense bed as regenerated catalyst, and dividing the regenerated catalyst into first regenerated catalyst, second regenerated catalyst and third regenerated catalyst; making the first regenerated catalyst pass through the regenerated inclined pipe into the light hydrocarbon oil catalytic conversion reactor, and making the third regenerated catalyst pass through the regenerated circulating inclined pipe to return to the decoking tank; making the second regenerated catalyst pass through the upper inclined pipe of the heat compensator into the heat compensator to mix with the heat compensation fuel for heat compensation reaction to obtain heat compensation regenerated catalyst and heat compensation flue gas; and making the heat compensation regenerated catalyst pass through the lower inclined pipe of the heat compensator into the decoking tank, and making the heat compensation flue gas pass through the heat compensator flue gas return pipe into the second dense bed.

[0010] Optionally, the reaction conditions of the heat compensation reaction comprise: the reaction temperature is 450℃-850℃, the reaction pressure is 0.01-1.0 MPa(g), the average gas superficial linear velocity is 0.01-10 m / s, the flow ratio of the heat compensation fuel to the second regenerated catalyst is (0.001-0.5):1, and the average catalyst residence time of the heat compensator is 0.1-30 min; the oxygen volume content in the heat compensation flue gas is 0-5 Vol%; the heat compensation fuel is selected from heavy oil products with a combustion point lower than 380℃; preferably one or more of diesel, slurry oil, wax oil, hydrocracked heavy oil and residual oil; and the fluidization medium comprises one or more of water vapor, nitrogen, air, oxygen, carbon dioxide and regenerated flue gas.

[0011] Optionally, the two-bed operation conditions include: a temperature of 450-850℃, a pressure of 0.01-1.0 MPa(g), an average gas superficial linear velocity of the dense phase bed of the two-bed of 0.01-0.2 m / s, an average catalyst residence time of 0.5-20 min, and an average gas superficial linear velocity of the dilute phase section of the two-bed of 0.1-1.5 m / s.

[0012] Optionally, the regeneration conditions include: a temperature of 450-850℃, a pressure of 0.01-1.0 MPa(g), a superficial linear velocity of the coking main air of 0.5-3.5 m / s, an average catalyst residence time of 0.01-5.0 min, an oxygen volume content of 0-10 Vol% in the mixture, and the coking main air including one or more of a mixture of air, oxygen and nitrogen, a mixture of air and flue gas, a mixture of oxygen and flue gas, and a mixture of oxygen and carbon dioxide.

[0013] Optionally, the regenerated catalyst includes zeolite, inorganic oxide and clay, the content of the zeolite is 0.5-90 wt% based on the total weight of the regenerated catalyst, the content of the inorganic oxide is 1-99 wt% based on the total weight of the regenerated catalyst, and the content of the clay is 0-80 wt% based on the total weight of the regenerated catalyst; the zeolite includes mesoporous zeolite, mesoporous zeolite and optional macroporous zeolite, the content of the mesoporous zeolite is 10-90 wt% based on the total weight of the zeolite, the content of the mesoporous zeolite is 10-90 wt% based on the total weight of the zeolite, and the content of the macroporous zeolite is 0-50 wt% based on the total weight of the zeolite.

[0014] By the above technical solution, the system coupling a coking tank, a dilute phase pipe and a two-bed is used for catalyst regeneration, the coke burning of the spent catalyst is completed in the coking tank and the dilute phase pipe, the two-bed functions as a buffer for the regenerated catalyst, and the low superficial gas velocity of the two-bed can ensure that the flue gas entrainment in the regenerated catalyst is less than 1 Nm 3 , so that a nitrogen or steam degassing tank for the regenerated catalyst is not needed, thereby reducing the large amount of nitrogen or steam needed for the degassing tank, reducing the energy consumption and operation cost of the device, and reducing the investment in the equipment. On the other hand, compared with the conventional coking tank and bed regeneration mode, the outlet pressure of the main air blower can be reduced by 10-30 kPa in the coking tank and dilute phase pipe regeneration mode, so that the power consumption of the main air blower and the energy consumption of the device can be reduced, thereby reducing the investment in the equipment. In addition, the heat exchanger provided in the system can increase the coke content of the regenerated catalyst returned to the coking tank, which can not only ensure the heat balance of the light hydrocarbon oil catalytic conversion reaction and the regeneration system, but also avoid the problem of catalyst breakage and deactivation caused by direct fuel injection into the regenerator. In addition, the system can be independently set up, thereby improving the safety and applicability of the system.

[0015] Other features and advantages of the present disclosure will be described in detail in the following detailed description. BRIEF DESCRIPTION OF DRAWINGS

[0016] The accompanying drawings are included to provide a further understanding of the present disclosure and constitute a part of the specification, illustrate embodiments of the present disclosure and, together with the specific description below, serve to explain the present disclosure but do not limit the present disclosure. In the drawings:

[0017] Figure 1 is a schematic diagram of a system for regeneration of a catalyst for catalytic conversion of light hydrocarbon oil according to the present disclosure.

[0018] Explanation of reference signs

[0019] 1, coking drum; 2, dilute phase pipe; 3, dual dense bed; 4, heat supplement device; 5, regeneration inclined pipe; 6, regeneration inclined pipe; 7, upper inclined pipe of heat supplement device; 8, lower inclined pipe of heat supplement device; 9, lower slide valve of heat supplement device; 10, flue gas return pipe of heat supplement device; 11, regeneration circulation inclined pipe; 12, regeneration circulation slide valve; 13, main air distributor of coking drum; 14, main air distributor of dual dense bed; 15, quick separation head of dilute phase pipe; 16, cyclone separator; 17, gas collecting chamber; 18, fuel distributor of heat supplement device; 19, fluidizing medium distributor; 101, main air of coking drum; 102, main air of dual dense bed; 103, regeneration flue gas; 104, fuel source of heat supplement device; 105, fluidizing medium source. DETAILED DESCRIPTION

[0020] The specific embodiments of the present disclosure will be described below in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are merely intended to illustrate and explain the present disclosure, and are not intended to limit the present disclosure.

[0021] In the present disclosure, the orientation words such as "upper" and "lower" used herein generally refer to the upper and lower of the device in the normal use state, for example, with reference to the drawing surface direction of Figure 1 , "inner" and "outer" refer to relative to the outline of the device. In addition, the terms "first", "second", "third" are only for descriptive purposes, and cannot be understood as indicating or implying relative importance or implicitly indicating the number of the indicated technical features. Therefore, the features defined with "first", "second", "third" can explicitly or implicitly include one or more of the features. In the description of the present disclosure, the meaning of "a plurality of" is two or more, unless otherwise specifically limited.

[0022] The first aspect of the present disclosure provides a system for regenerating a light hydrocarbon oil catalytic conversion catalyst, which comprises a coking drum 1, a dilute phase pipe 2, a double dense bed 3 and a heat supplement device 4; the coking drum 1, the dilute phase pipe 2 and the double dense bed 3 are coaxially arranged; the coking drum 1 is integrally arranged below the double dense bed 3; the dilute phase pipe 2 is arranged above the coking drum 1 and inside the double dense bed 3; the inlet of the dilute phase pipe 2 is in communication with the outlet of the coking drum 1; the coking drum 1 comprises a main air inlet, a spent catalyst inlet, a heat supplement catalyst inlet and a third regenerated catalyst inlet; the shell of the double dense bed 3 is provided with a first regenerated catalyst outlet, a second regenerated catalyst outlet, a third regenerated catalyst outlet and a heat supplement flue gas inlet; the upper part of the heat supplement device 4 is provided with a second regenerated catalyst inlet, the lower part is provided with a heat supplement catalyst outlet and the top is provided with a heat supplement flue gas outlet; the main air inlet of the coking drum 1 is used to communicate with a main air source so that the main air can enter the coking drum 1 for regeneration treatment; the spent catalyst inlet of the coking drum 1 is communicated with a spent catalyst source through a spent catalyst inclined pipe 6 so that the spent catalyst can enter the coking drum 1; the first regenerated catalyst outlet of the double dense bed 3 is communicated with a light hydrocarbon oil catalytic conversion reactor through a regenerated catalyst inclined pipe 5 so that the first regenerated catalyst can enter the subsequent light hydrocarbon oil catalytic conversion reactor; the second regenerated catalyst outlet of the double dense bed 3 is communicated with the second regenerated catalyst inlet of the heat supplement device 4 through a heat supplement device upper inclined pipe 7 so that the second regenerated catalyst can enter the heat supplement device 4; the heat supplement catalyst outlet of the heat supplement device 4 is communicated with the heat supplement catalyst inlet of the coking drum 1 through a heat supplement device lower inclined pipe 8 so that the heat supplement catalyst can return to the coking drum 1; the heat supplement flue gas outlet of the heat supplement device 4 is communicated with the heat supplement flue gas inlet of the double dense bed 3 through a heat supplement device flue gas return pipe 10 so that the heat supplement flue gas can enter the double dense bed 3; the third regenerated catalyst outlet of the double dense bed 3 is communicated with the third regenerated catalyst inlet of the coking drum 1 through a regenerated catalyst circulation inclined pipe 11 so that the third regenerated catalyst can return to the coking drum 1 to increase the inlet temperature of the coking drum 1 and thus improve the coking capacity.

[0023] By the above technical solution, the system coupling the coking drum 1, the dilute phase pipe 2 and the double dense bed 3 is used for catalyst regeneration treatment; since the spent catalyst completes the whole coking process in the coking drum 1 and the dilute phase pipe 2, the double dense bed 3 plays a role in buffering the regenerated catalyst, and the apparent gas velocity of the double dense bed 3 is low, which can ensure that the flue gas entrainment in the regenerated catalyst is less than 1 Nm 3Therefore, there is no need to add a regenerative catalyst degassing tank, thereby reducing the large amount of nitrogen or water vapor required for the regenerative catalyst degassing tank, reducing the energy consumption and operating cost of the device; on the other hand, compared with the conventional coking tank 1 and bed regeneration method, the coking tank 1 and the dilute phase pipe 2 regeneration method can reduce the outlet pressure of the main fan by 10-30 kPa, so as to reduce the power consumption of the main fan and the energy consumption of the device, and further reduce the investment of the equipment. And, the heat exchanger 4 is arranged in the system, which can increase the coke content of the regenerated catalyst returned to the coking tank 1, not only can ensure the heat balance of the light hydrocarbon oil catalytic conversion reaction and the regeneration system, but also can avoid the problem of catalyst crushing and deactivation caused by directly spraying fuel into the regenerator. In addition, the system can be independently arranged, which improves the safety and applicability of the system.

[0024] In an embodiment, the coking tank 1 is provided with a coking tank main air distributor 13 at the bottom, wherein the coking tank main air distributor 13 is arranged at the tangent position below the coking tank 1; the coking tank main air distributor 13 is selected from one or more of a dendritic distribution pipe, a distribution ring and a distribution nozzle, wherein the coking tank main air distributor 13 is provided with a plurality of injection holes, which can be oriented upward along the axial direction or obliquely upward; the heat recovery catalyst inlet of the coking tank 1 is arranged above the coking tank main air distributor 13; the regenerated catalyst inlet is arranged above the heat recovery catalyst inlet; and the spent catalyst inlet of the coking tank 1 is arranged above the heat recovery catalyst inlet and the regenerated catalyst inlet.

[0025] In an embodiment, the heat exchanger 4 is arranged in parallel with the coking tank 1 and the two dense beds 3, and is communicated with the two dense beds 3 and the coking tank 1 through the upper inclined pipe 7 and the lower inclined pipe 8 of the heat exchanger to form a loop, wherein the lower inclined pipe 8 of the heat exchanger is provided with a lower sliding valve 9 of the heat exchanger to control the flow of the heat recovery catalyst.

[0026] In an embodiment, the two dense beds 3 and the coking tank 1 are communicated through the regeneration circulation inclined pipe 11 to form a loop, wherein the regeneration circulation inclined pipe 11 is provided with a regeneration circulation sliding valve 12 to control the flow of the third regenerated catalyst circulating from the two dense beds 3 to the coking tank 1.

[0027] In an embodiment, the internal part of the heat supplementing device 4 is provided with a heat supplementing fuel distributor 18 and a fluidizing medium distributor 19 arranged below the heat supplementing fuel distributor 18; the inlet of the heat supplementing fuel distributor 18 is used to communicate with a heat supplementing fuel source 104 to enable the heat supplementing fuel to participate in the heat supplementing process; the inlet of the fluidizing medium distributor 19 is used to communicate with a fluidizing medium source 105 to enable the fluidizing medium to enter the heat supplementing device 4 to participate in the heat supplementing process; the heat supplementing fuel distributor 18 is provided with a plurality of downwardly opening injection holes; the fluidizing medium distributor 19 is provided with a plurality of upwardly opening injection holes; wherein the heat supplementing fuel distributor 18 and the fluidizing medium distributor 19 are arranged in a horizontal direction, the heat supplementing fuel distributor 18 can be arranged below the inlet of the catalyst to be heated in the heat supplementing device 4; the fluidizing medium distributor 19 can be arranged above the outlet of the heat supplementing catalyst in the heat supplementing device 4.

[0028] In a preferred embodiment, the inlet of the heat supplementing catalyst in the coking drum 1 is arranged above the main air distributor 13 of the coking drum; the inlet of the third regenerated catalyst is arranged at the same height and / or above the inlet of the heat supplementing catalyst; the inlet of the spent catalyst in the coking drum 1 is arranged above the inlet of the heat supplementing catalyst and the inlet of the third regenerated catalyst.

[0029] In an embodiment, the top of the dilute phase pipe 2 is sealed, only the side surface of the upper part of the dilute phase pipe 2 is provided with a plurality of outlets, and a dilute phase pipe quick separation head 15 is arranged at the outlets; the outlet of the dilute phase pipe 2 communicates with the inlet of the dilute phase pipe quick separation head 15 to enable the stream after the regeneration process to be preliminarily separated.

[0030] In an embodiment, the top of the dilute phase pipe 2 is sealed, only the side surface of the upper part of the dilute phase pipe 2 is provided with a plurality of outlets, and a dilute phase pipe quick separation head 15 is arranged at the outlets; the outlet of the dilute phase pipe 2 communicates with the inlet of the dilute phase pipe quick separation head 15 to enable the stream after the regeneration process to be preliminarily separated.

[0031] In one embodiment, the inner part of the second dense bed 3 is provided with a gas collecting chamber 17 and a cyclone separator 16; the upper part of the dilute phase pipe 2 is located in the upper middle part of the second dense bed 3; the gas collecting chamber 17 is located above the dilute phase pipe 2, the separation part of the cyclone separator 16 is located above the dilute phase pipe 2, the bottom of the leg is located above and / or below the dilute phase pipe 2; the top of the second dense bed 3 comprises a regenerated flue gas outlet, the gas collecting chamber 17 comprises a regenerated flue gas inlet and a regenerated flue gas outlet; the cyclone separator 16 comprises a gas outlet, a catalyst outlet and a gas inlet; the gas outlet of the cyclone separator 16 communicates with the regenerated flue gas inlet of the gas collecting chamber 17, the outlet of the gas collecting chamber 17 communicates with the regenerated flue gas outlet of the second dense bed 3, so that the separated regenerated flue gas can be discharged from the system through the gas collecting chamber 17; the catalyst outlet of the cyclone separator 16 is located above and / or below the dense phase bed layer of the regenerated catalyst in the second dense bed 3.

[0032] In order to further enhance the separation effect of the regenerated flue gas and the regenerated catalyst fine powder, the number of the cyclone separators 16 is at least two, the gas phase inlet of the first cyclone separator is used to receive the gas phase in the second dense bed 3, the gas phase outlet of the first cyclone separator communicates with the gas phase inlet of the second cyclone separator, which is used to perform secondary separation on the preliminarily separated flue gas, and the gas phase outlet of the second cyclone separator communicates with the regenerated flue gas inlet of the gas collecting chamber 17; the bottoms of the legs of the first and second cyclone separators can be located above and / or below the dense phase bed layer of the regenerated catalyst in the second dense bed 3 at the same time, or one is located above the dense phase bed layer of the regenerated catalyst in the second dense bed 3 and the other is located below the dense phase bed layer of the regenerated catalyst in the second dense bed 3. After the entrained catalyst fine powder is separated by the cyclone separator 16, it enters the subsequent treatment unit, further recovers the heat energy and pressure energy in the high-temperature regenerated flue gas, and removes SO X , NO X and dust and other pollutants.

[0033] The gas collecting chamber 17 can be arranged inside or outside the second dense bed 3; if the gas collecting chamber 17 is arranged inside the second dense bed 3, a certain gap can be left between the top of the gas collecting chamber 17 and the top of the second dense bed 3, or a part of the top of the second dense bed 3 can be tightly combined with the side wall of the gas collecting chamber 17, and a cavity can be formed through the tight connection between the bottom and the side wall, and the regenerated flue gas outlet of the second dense bed 3 can be used as the regenerated flue gas outlet of the gas collecting chamber 17; if the gas collecting chamber 17 is arranged outside the second dense bed 3, the gas phase outlet of the cyclone separator 16 communicates with the regenerated flue gas inlet of the gas collecting chamber 17 through the regenerated flue gas outlet of the second dense bed 3.

[0034] The lower part of the second dense bed 3 is provided with at least one set of second dense bed main air distributors 14, wherein the second dense bed main air distributors 14 are arranged above the horizontal position of the first regenerated catalyst outlet of the second dense bed 3; the coke burning tank main air distributors 13 and the second dense bed main air distributors 14 are each selected from one or more of a dendritic distribution pipe, a distribution ring and a distribution nozzle, wherein the main air distributors 13 are provided with a plurality of injection holes, and the injection holes can be oriented upward along the axial direction or obliquely upward.

[0035] The second aspect of the present disclosure provides a method for regenerating a light hydrocarbon oil catalytic conversion catalyst using the system of the first aspect of the present disclosure, which comprises: making the spent catalyst pass through the spent inclined pipe 6 to contact the coke burning main air in the coke burning tank 1 for regeneration treatment, to obtain a mixture of regenerated flue gas and regenerated catalyst; making the mixture flow upward into the dilute phase pipe 2 to separate to obtain regenerated flue gas entraining a small amount of catalyst and part of the regenerated catalyst; the regenerated flue gas entraining a small amount of catalyst fine powder flows upward and is further separated to obtain regenerated flue gas with a trace amount of catalyst fine powder and another part of the regenerated catalyst; the part of the regenerated catalyst and the another part of the regenerated catalyst flow downward into the second dense bed 3 as regenerated catalyst, and the regenerated catalyst is divided into first regenerated catalyst, second regenerated catalyst and third regenerated catalyst; making the first regenerated catalyst pass through the regeneration inclined pipe 5 to enter the catalytic conversion reactor, and making the third regenerated catalyst pass through the regeneration circulating inclined pipe 11 to return to the coke burning tank 1; making the second regenerated catalyst pass through the upper heat compensator inclined pipe 7 to enter the heat compensator 4 to mix with the heat compensation fuel for heat compensation reaction to obtain heat compensation regenerated catalyst and heat compensation flue gas; making the heat compensation regenerated catalyst pass through the lower heat compensator inclined pipe 8 to enter the coke burning tank 1, and making the heat compensation flue gas pass through the heat compensator flue gas return pipe 10 to enter the second dense bed 3.

[0036] Through the above technical solution, the second regenerated catalyst is sent into the heat compensator 4 to mix with the coke converted from the heat compensation fuel, and then is sent into the coke burning tank 1 to mix with the spent catalyst and the third regenerated catalyst, which can increase the coke content of the catalyst in the coke burning tank 1, and thus can ensure the heat balance of the light hydrocarbon oil catalytic conversion reaction and regeneration system; at the same time, the problem of catalyst breakage and deactivation caused by directly spraying heat compensation fuel into the regenerator during the regeneration process can be avoided.

[0037] In one embodiment, the conditions of the regeneration process in the coking drum 1 include: temperature of 450-850°C, preferably 600-800°C, more preferably 650-750°C; pressure of 0.01-1.0 MPa(g), preferably 0.1-0.4 MPa(g), more preferably 0.12-0.28 MPa(g); gas superficial linear velocity of 0.5-3.5 m / s, preferably 0.8-2.0 m / s, more preferably 1.2-1.6 m / s; catalyst average residence time of 0.01-5.0 min, preferably 0.1-1.0 min, more preferably 0.2-0.5 min; oxygen volume content in the mixture at the top outlet of the coking drum 1 of 0-10%, preferably 1-5%, more preferably 2-4%.

[0038] The main air 101 of the coking drum is selected from one or more of air, a mixture of oxygen and nitrogen, a mixture of air and flue gas, a mixture of oxygen and flue gas, and a mixture of oxygen and carbon dioxide.

[0039] In one embodiment, the method further comprises: flowing the mixture upward into the dilute phase pipe 2, and then separating the mixture through the dilute phase pipe quick separation head 15 arranged at the outlet of the dilute phase pipe 2 to obtain regenerated flue gas entraining catalyst and part of the regenerated catalyst; further separating the regenerated flue gas entraining catalyst through the regeneration cyclone 16 to obtain another part of the regenerated catalyst and regenerated flue gas; returning the other part of the regenerated catalyst to the two dense beds 3 through the leg of the regeneration cyclone 16, and the regenerated flue gas enters the gas collecting chamber 17.

[0040] The operating conditions of the two dense beds 3 are as follows: temperature of 450-850°C, preferably 600-800°C, more preferably 650-750°C; pressure of 0.01-1.0 MPa(g), preferably 0.1-0.4 MPa(g), more preferably 0.12-0.28 MPa(g); average gas superficial linear velocity of the dense phase bed layer of the two dense beds 3 of 0.01-0.2 m / s, preferably 0.02-0.1 m / s, more preferably 0.03-0.06 m / s; catalyst average residence time of the dense phase bed layer of the two dense beds 3 of 0.5-20 min, preferably 1.0-5.0 min, more preferably 1.5-3 min; average gas superficial linear velocity of the dilute phase section of the two dense beds 3 of 0.1-1.5 m / s, preferably 0.4-1.0 m / s, more preferably 0.5-0.8 m / s.

[0041] The method further comprises: making the two dense bed main air 102 enter the two dense beds 3 through the two dense bed main air distributor 14, so that the regenerated flue gas in the regenerated catalyst can be discharged as completely as possible. The two dense bed main air 102 is selected from one or more of air, a mixture of oxygen and nitrogen, a mixture of air and flue gas, a mixture of oxygen and flue gas, and a mixture of oxygen and carbon dioxide.

[0042] In one embodiment, the second regenerated catalyst passes from the second dense bed 3 to the reheater 4 through the reheater upper inclined pipe 7; the reheating fuel produced by the reheating fuel source 104 is uniformly distributed on the second regenerated catalyst through the reheating fuel distributor 18; the fluidizing medium produced by the fluidizing medium source 105 is introduced through the fluidizing medium distributor 19, and under the conditions of low oxygen content and low temperature, the reheating fuel attached to the second regenerated catalyst is pre-combusted to form reheating regenerated catalyst with coke attached; the reheating regenerated catalyst with coke attached passes through the reheater lower inclined pipe 8 to the coking drum 1, and under the oxidation reaction of the coking drum main air 101, the coke is burned to release heat, which supplements the heat required by the reaction-regeneration system.

[0043] The reaction conditions of the reheating reaction in the reheater 4 include: a temperature of 450-850°C, preferably 600-800°C, and more preferably 650-750°C; a pressure of 0.01-1.0 MPa(g), preferably 0.1-0.4 MPa(g), and more preferably 0.12-0.28 MPa(g); an average gas superficial linear velocity of the reheater 4 of 0.01-10 m / s, preferably 0.05-5 m / s, and more preferably 0.1-1 m / s; a catalyst average residence time of 0.1-30 min, preferably 0.5-10 min, and more preferably 1-5 min; and an oxygen volume content in the reheating flue gas of 0-1 Vol%. In addition, the flow ratio of the reheating fuel to the second regenerated catalyst is (0.001-0.5):1, preferably (0.005-0.2):1, and more preferably (0.01-0.1):1.

[0044] The reheating fuel is selected from heavy oil products with a combustion point lower than 380°C, and is preferably one or more of diesel oil, slurry oil, wax oil, hydrocracked heavy oil, and residual oil; and the fluidizing medium includes one or more of water vapor, nitrogen, air, oxygen, carbon dioxide, and regeneration flue gas.

[0045] The reheating catalyst circulation amount is controlled by the reheater lower slide valve 9 arranged on the reheater lower inclined pipe 8, and the catalyst level and residence time in the reheater 4 are controlled.

[0046] The regenerated catalyst, spent catalyst, and reheating regenerated catalyst used in the present disclosure all include zeolite, inorganic oxide, and clay; the content of the zeolite is 0.5-90 wt%, the content of the inorganic oxide is 1-99 wt%, and the content of the clay is 0-80 wt%, based on the total weight of the regenerated catalyst; the zeolite includes mesoporous zeolite, mesoporous zeolite, and optionally macroporous zeolite; the content of the mesoporous zeolite is 10-90 wt%, the content of the mesoporous zeolite is 10-90 wt%, and the content of the macroporous zeolite is 0-50 wt%, based on the total weight of the zeolite.

[0047] In one embodiment, the third regenerated catalyst is made to pass through the regeneration circulation slide valve 12 on the regeneration circulation inclined pipe 11 into the coking drum 1, and the amount of the third regenerated catalyst circulating from the second dense bed 3 to the coking drum 1 is controlled by adjusting the opening of the regeneration circulation slide valve 12 on the regeneration circulation inclined pipe 11, and thus the temperature at the inlet of the coking drum 1 is controlled.

[0048] In one embodiment, the first regenerated catalyst is made to pass through the regeneration inclined pipe 5 into the light hydrocarbon oil catalytic conversion reactor to contact with the light hydrocarbon oil for catalytic conversion reaction, and after a series of separation, the spent catalyst and low-carbon olefins and aromatic hydrocarbons and other products are obtained.

[0049] In one embodiment, the light hydrocarbon oil is a light fraction with a distillation range of 20-300°C, and the light hydrocarbon oil is selected from one or more of catalytic cracking gasoline, catalytic cracking gasoline, straight-run naphtha, coking naphtha, thermal cracking naphtha, thermal cracking naphtha, hydrogenated naphtha, reforming raffinate, straight-run kerosene, and hydrogenated kerosene.

[0050] In one embodiment, as shown in Figure 1 The method for regenerating the light hydrocarbon oil catalytic conversion catalyst includes:

[0051] The spent catalyst is made to pass through the spent inclined pipe 6 into the coking drum 1 to contact with the main air 101 of the coking drum for regeneration treatment, and a mixture of regenerated flue gas and regenerated catalyst is obtained; the mixture is made to flow upward into the dilute phase pipe 2 and is separated by the dilute phase pipe quick separation head 15 to obtain regenerated flue gas entraining a small amount of catalyst and part of the regenerated catalyst; the regenerated flue gas entraining a small amount of catalyst fine powder is made to flow upward into the cyclone separator 16 for further separation to obtain regenerated flue gas with a trace amount of catalyst fine powder and another part of the regenerated catalyst;

[0052] The regenerated catalyst separated by the dilute phase pipe quick separation head 15 and the cyclone separator 16 flows downward into the second dense bed 3; the regenerated catalyst flowing downward into the second dense bed 3 is divided into first regenerated catalyst, second regenerated catalyst, and third regenerated catalyst; the first regenerated catalyst is made to pass through the regeneration inclined pipe 5 into the catalytic conversion reactor, the second regenerated catalyst is made to pass through the upper inclined pipe 7 of the heat supplement device into the heat supplement device 4, and the third regenerated catalyst is made to return to the coking drum 1 through the regeneration circulation inclined pipe 11; the heat supplement fuel produced by the heat supplement fuel source 104 is made to pass through the heat supplement fuel distributor 18 into the heat supplement device 4 and be uniformly distributed on the second regenerated catalyst in the heat supplement device 4, and the fluidization medium produced by the fluidization medium source 105 is made to pass through the fluidization medium distributor 19 into the heat supplement device 4. The injected heat supplement fuel is pre-combusted under oxygen-poor conditions, and most of the heat supplement fuel becomes additional coke on the heat supplement catalyst and is fully mixed and uniformly distributed in a fluidized state. The heat supplement catalyst with additional coke returns to the coking drum 1 through the lower inclined pipe 8 of the heat supplement device for regeneration treatment;

[0053] The regenerated flue gas obtained flows upward into the cyclone 16 to separate catalyst fines and regenerated flue gas; the catalyst fines are returned to the second dense bed 3 through the leg of the regeneration cyclone 16, and the regenerated flue gas enters the plenum 17 and exits the system as regenerated flue gas 103.

[0054] The method provided by the present application is further described below through specific examples, but the present application is not limited by the examples. The catalyst used in the examples is composed of 60 wt% zeolite (composed of 5 wt% mesoporous zeolite, 40 wt% mesoporous zeolite and 15 wt% macroporous zeolite), 20 wt% inorganic oxide (including but not limited to Al2O3, Na2O and SiO2, etc.) and 20 wt% clay. The specific properties are shown in Table 1, and the properties of the light hydrocarbon oil feedstock are shown in Table 2.

[0055] Table 1 Catalyst properties

[0056] Item Unit Value Average particle size μm 50～100 Apparent density g / cm 3 ]] 0.75～0.90 Specific surface area m 2 / g]]> ≥100 Pore volume mL / g ≥0.2 Wear index wt% ≤4.0

[0057] Table 2 Properties of light hydrocarbon oil feedstock

[0058] Item Unit Straight run naphtha Straight run kerosene Coker naphtha Distillation range ℃ 50～188 210～250 30～220 Density (20°C) kg / m 3 ]] 0.7296 0.8189 0.7320 Molecular weight 140 220 160 Hydrogen content wt% 14.30 13.1 13.6

[0059] Example 1

[0060] The spent catalyst is introduced into the decoking tank 1 through the spent catalyst inclined pipe 6 to contact with the decoking main air 101 for regeneration treatment to obtain a mixture of regenerated flue gas and regenerated catalyst; the mixture flows upward into the dilute phase pipe 2 and is separated by the dilute phase pipe quick separation head 15 to obtain regenerated flue gas and regenerated catalyst. The regeneration treatment conditions include: the temperature is 680°C (inlet) / 745°C (outlet), the pressure is 0.17 MPa (g), the average superficial linear velocity of the decoking main air is 1.4 m / s, and the average residence time of the catalyst is 0.3 min; the oxygen content in the mixture is 2.5 Vol%; the decoking main air is air; the operating conditions of the second dense bed 3 include: the temperature is 740°C, the pressure is 0.16 MPa (g), the flow ratio of the supplemental heating fuel to the second regenerated catalyst is 0.02:1, the average gas superficial linear velocity of the second dense bed 3 is 0.05 m / s, and the average residence time of the catalyst is 4 min;

[0061] The regenerated catalyst obtained is flowed downward into the second dense bed 3; the regenerated catalyst flowed downward into the second dense bed 3 is divided into first regenerated catalyst, second regenerated catalyst and third regenerated catalyst; the second regenerated catalyst is flowed into the regenerator 4 through the upper inclined pipe 7 of the regenerator, and the third regenerated catalyst is returned to the coking drum 1 through the regenerated circulation inclined pipe 11; the regenerative fuel produced by the regenerative fuel source 104 is flowed into the regenerator 4 through the regenerative fuel distributor 18, and is uniformly distributed on the second regenerated catalyst in the regenerator 4; the fluidizing medium produced by the fluidizing medium source 105 is flowed into the regenerator 4 through the fluidizing medium distributor 19. The injected regenerative fuel is pre-combusted under the condition of oxygen deficiency, and most of the regenerative fuel becomes additional coke on the second regenerated catalyst and is fully mixed and uniformly distributed in the fluidized state; the second regenerated catalyst with additional coke is returned to the coking drum 1 through the lower inclined pipe 8 of the regenerator for regeneration treatment; the reaction conditions of the regenerative reaction include that the reaction temperature is 670°C, the reaction pressure is 0.12 MPa (g), the average gas superficial linear velocity of the fluidizing medium is 0.05 m / s, and the average residence time of the catalyst is 5 min; the oxygen volume content in the regenerative flue gas is 0.5 Vol%; the regenerative fuel is selected from cracked heavy oil and partially cracked light oil;

[0062] The regenerated flue gas obtained is flowed upward into the cyclone separator 16 for separation, and catalyst fine powder and separated regenerated flue gas are obtained; the catalyst fine powder is returned to the second dense bed 3 through the leg of the regenerated cyclone separator 16, and the separated regenerated flue gas is flowed into the gas collecting chamber 17 and is discharged from the system as regenerated flue gas 103;

[0063] The first regenerated catalyst is flowed into the catalytic conversion reactor through the regenerated inclined pipe 5, and is contacted with light hydrocarbon oil raw material (straight-run naphtha) preheated to 300°C to perform catalytic conversion reaction; after the high-temperature reaction oil gas and spent catalyst obtained are separated, the reaction oil gas is flowed into a product separation unit, and low-carbon olefins (ethylene, propylene), low-carbon aromatic hydrocarbons (benzene, toluene, xylene), methane hydrogen, ethane, propane, mixed carbon four, mixed carbon five, cracked naphtha, cracked light oil and cracked heavy oil and other products are obtained by separation. The carbon content of the first regenerated catalyst at the outlet of the second dense bed 3 is 0.05 wt%, and the product distribution is shown in Table 3.

[0064] Example 2

[0065] A method for regenerating a catalytic conversion catalyst of light hydrocarbon oil is the same as that in Example 1, except that the light hydrocarbon oil raw material for catalytic conversion reaction is straight-run kerosene. The carbon content of the first regenerated catalyst is 0.05 wt%, and the product distribution and catalyst consumption are shown in Table 3.

[0066] Example 3

[0067] A method for regenerating a catalytic conversion catalyst for light hydrocarbon oil is the same as that in Example 1, except that the light hydrocarbon oil feedstock for the catalytic conversion reaction is coking naphtha. The carbon content of the first regenerated catalyst is 0.05wt%, and the product distribution and catalyst consumption are shown in Table 3.

[0068] Comparative Example 1

[0069] A method for regenerating a catalytic conversion catalyst for light hydrocarbon oil is the same as that in Example 1, except that the heat exchanger 4 is not provided and the supplemental combustion fuel is directly injected into the regenerator. The carbon content of the first regenerated catalyst is 0.05wt%, and the product distribution and catalyst consumption are shown in Table 3.

[0070] Table 3 Product distribution

[0071]

[0072]

[0073] As can be seen from Table 3, by comparing the data in Example 1 and Comparative Example 1, it can be seen that by providing a heat exchanger in the system, the amount of coke in the regenerated catalyst returned to the coking drum can be increased, not only ensuring the heat balance of the light hydrocarbon oil catalytic conversion reaction and regeneration system, but also avoiding the problem of catalyst breakage and deactivation caused by directly injecting fuel into the regenerator, which is conducive to improving the reaction efficiency, increasing the yield of low-carbon olefins and aromatic hydrocarbons, and reducing catalyst consumption and operating costs. In addition, by comparing the data in Example 1, Example 2 and Example 3, it can be seen that the system can be independently provided, not only improving the safety of the system, but also being applicable to the regeneration treatment of catalysts used in a variety of light hydrocarbon oils, and having high applicability.

[0074] The preferred embodiments of the present disclosure are described in detail above with reference to the accompanying drawings, but the present disclosure is not limited to the specific details in the above-described embodiments, and various simple modifications can be made to the technical solutions of the present disclosure within the technical concept of the present disclosure, and these simple modifications all belong to the protection scope of the present disclosure.

[0075] In addition, it should be noted that each specific technical feature described in the above specific embodiments can be combined in any appropriate manner without contradiction. In order to avoid unnecessary repetition, various possible combinations are not described again in the present disclosure.

[0076] In addition, any combination of various different embodiments of the present disclosure can also be made, as long as it does not deviate from the idea of the present disclosure, and it should also be considered as disclosed in the present disclosure.

Claims

1. A system for the regeneration of a catalyst for the catalytic conversion of light hydrocarbon oils, characterized in that, The system comprises a coke burning tank (1), a dilute phase pipe (2), a double dense bed (3) and a heat supplement device (4); The coke burning tank (1), the dilute phase pipe (2) and the double dense bed (3) are coaxially arranged; the coke burning tank (1) is integrally arranged below the double dense bed (3); the dilute phase pipe (2) is arranged above the coke burning tank (1) and inside the double dense bed (3); the inlet of the dilute phase pipe (2) is communicated with the outlet of the coke burning tank (1); The coke burning tank (1) comprises a main air inlet, a spent catalyst inlet, a heat supplement catalyst inlet and a third regenerated catalyst inlet; the shell of the double dense bed (3) is provided with a first regenerated catalyst outlet, a second regenerated catalyst outlet, a third regenerated catalyst outlet and a heat supplement flue gas inlet; the upper part of the heat supplement device (4) is provided with a second regenerated catalyst inlet, the lower part is provided with a heat supplement catalyst outlet and the top is provided with a heat supplement flue gas outlet; The main air inlet of the coke burning tank (1) is used for being communicated with a main air source, the spent catalyst inlet of the coke burning tank (1) is used for being communicated with a spent catalyst source through a spent catalyst inclined pipe (6); the first regenerated catalyst outlet of the double dense bed (3) is used for being communicated with a light hydrocarbon oil catalytic conversion reactor through a regenerated catalyst inclined pipe (5); the second regenerated catalyst outlet of the double dense bed (3) is communicated with the second regenerated catalyst inlet of the heat supplement device (4) through a heat supplement device upper inclined pipe (7); the heat supplement catalyst outlet of the heat supplement device (4) is communicated with the heat supplement catalyst inlet of the coke burning tank (1) through a heat supplement device lower inclined pipe (8); the heat supplement flue gas outlet of the heat supplement device (4) is communicated with the heat supplement flue gas inlet of the double dense bed (3) through a heat supplement device flue gas return pipe (10); the third regenerated catalyst outlet of the double dense bed (3) is communicated with the third regenerated catalyst inlet of the coke burning tank (1) through a regenerated catalyst circulation inclined pipe (11).

2. The system of claim 1, wherein, The inside of the heat supplement device (4) is provided with a heat supplement fuel distributor (18) and a fluidized medium distributor (19) arranged below the heat supplement fuel distributor (18); the inlet of the heat supplement fuel distributor (18) is used for being communicated with a heat supplement fuel source (104); the inlet of the fluidized medium distributor (19) is used for being communicated with a fluidized medium source (105); The heat supplement fuel distributor (18) is provided with a plurality of downward opening injection holes; the fluidized medium distributor (19) is provided with a plurality of upward opening injection holes.

3. The system of claim 1, wherein, The bottom of the coke burning tank (1) is provided with a coke burning tank main air distributor (13); the lower part of the double dense bed (3) is provided with at least one set of double dense bed main air distributors (14); the coke burning tank main air distributor (13) and the double dense bed main air distributors (14) are each independently selected from one or more of a dendritic distribution pipe, a distribution ring and a distribution nozzle; The regenerated catalyst circulation inclined pipe (11) is provided with a regenerated catalyst circulation slide valve (12); the heat supplement device lower inclined pipe (8) is provided with a heat supplement device lower slide valve (9).

4. The system of claim 1, wherein, The dilute phase pipe (2) is provided with a dilute phase pipe quick separation head (15); the outlet of the dilute phase pipe (2) is communicated with the inlet of the dilute phase pipe quick separation head (15); The dilute phase pipe quick separation head (15) comprises one or more of inverted L-shaped quick separation, T-shaped quick separation, multi-leaf quick separation, cyclone quick separation and coarse cyclone quick separation.

5. The system of claim 1, wherein, The inner part of the second dense bed (3) is provided with a gas collecting chamber (17) and a cyclone separator (16); the upper part of the dilute phase pipe (2) is located in the middle and upper part of the second dense bed (3); the gas collecting chamber (17) is located above the dilute phase pipe (2), and the separation part of the cyclone separator (16) is located above the dilute phase pipe (2) and / or the bottom of the leg is located above and / or below the dilute phase pipe (2); The top of the second dense bed (3) comprises a regenerated flue gas outlet, the gas collecting chamber (17) comprises a regenerated flue gas inlet and a regenerated flue gas outlet, and the cyclone separator (16) comprises a gas outlet, a catalyst outlet and a gas inlet; The gas outlet of the cyclone separator (16) is in communication with the regenerated flue gas inlet of the gas collecting chamber (17); the outlet of the gas collecting chamber (17) is in communication with the regenerated flue gas outlet of the second dense bed (3); and the catalyst outlet of the cyclone separator (16) is located above and / or below the dense phase bed layer of the regenerated catalyst in the second dense bed (3).

6. A method for the regeneration of a catalyst for the catalytic conversion of light hydrocarbon oils using the system according to any one of claims 1 to 5, characterized in that The method comprises: The spent catalyst is introduced into the coking tank (1) through the spent inclined pipe (6) to contact with the coking main air for regeneration treatment to obtain a mixture of regenerated flue gas and regenerated catalyst; The mixture flows upward into the dilute phase pipe (2) to separate to obtain regenerated flue gas entraining catalyst and part of the regenerated catalyst; The regenerated flue gas entraining catalyst fines flows upward and is further separated to obtain regenerated flue gas and another part of the regenerated catalyst; Part of the regenerated catalyst and another part of the regenerated catalyst flow downward into the second dense bed (3) as regenerated catalyst, and the regenerated catalyst is divided into first regenerated catalyst, second regenerated catalyst and third regenerated catalyst; the first regenerated catalyst is introduced into the light hydrocarbon oil catalytic conversion reactor through the regeneration inclined pipe (5), and the third regenerated catalyst is returned to the coking tank (1) through the regeneration circulating inclined pipe (11); The second regenerated catalyst is introduced into the heat supplementing device (4) through the upper inclined pipe (7) of the heat supplementing device to mix with the heat supplementing fuel for heat supplementing reaction to obtain heat supplementing regenerated catalyst and heat supplementing flue gas; the heat supplementing regenerated catalyst is introduced into the coking tank (1) through the lower inclined pipe (8) of the heat supplementing device, and the heat supplementing flue gas is introduced into the second dense bed (3) through the heat supplementing flue gas return pipe (10).

7. The method of claim 6, wherein, The reaction conditions of the heat supplementing reaction include: the reaction temperature is 450-850℃, the reaction pressure is 0.01-1.0 MPaG, and the flow ratio of the heat supplementing fuel to the second regenerated catalyst is (0.001-0.5):1; The average gas superficial linear velocity of the heat supplementing device (4) is 0.01-10 m / s, and the average catalyst residence time is 0.1-30 min; The oxygen volume content in the heat supplementing flue gas is 0-5 Vol%; The heat supplementing fuel is selected from heavy oil products with a combustion point lower than 380℃; The fluidization medium comprises one or more of water vapor, nitrogen, air, oxygen, carbon dioxide and regenerated flue gas.

8. The method of claim 7, wherein, The heat supplement fuel is selected from one or more of diesel oil, slurry oil, wax oil, hydrocracked heavy oil and residual oil.

9. The method of claim 6, wherein, The operating conditions of the second dense bed (3) include: a temperature of 450-850 DEG C, a pressure of 0.01-1.0 MPaG, an average gas superficial linear velocity of the dense phase bed layer of the second dense bed (3) of 0.01-0.5 m / s, an average catalyst residence time of 0.5-20 min, and an average gas superficial linear velocity of the dilute phase section of the second dense bed (3) of 0.1-1.5 m / s.

10. The method of claim 6, wherein, The conditions of the regeneration treatment include: a temperature of 450-850 DEG C, a pressure of 0.01-1.0 MPaG, an apparent linear velocity of the coking main air of 0.5-3.5 m / s, and an average catalyst residence time of 0.01-5.0 min. The oxygen volume content in the mixture is 0-10 Vol%. The coking main air includes one or more of a mixture of air, oxygen and nitrogen, a mixture of air and flue gas, a mixture of oxygen and flue gas, and a mixture of oxygen and carbon dioxide.

11. The method of claim 6, wherein, The regenerated catalyst includes zeolite, inorganic oxide and clay; the content of the zeolite is 0.5-90 wt% based on the total weight of the regenerated catalyst, the content of the inorganic oxide is 1-99 wt%, and the content of the clay is 0-80 wt%. The zeolite includes mesoporous zeolite and mesoporous zeolite; the content of the mesoporous zeolite is 10-90 wt% based on the total weight of the zeolite, and the content of the mesoporous zeolite is 10-90 wt%.

12. The method of claim 11, wherein, The zeolite also includes macroporous zeolite; the content of the macroporous zeolite is 0-50 wt% based on the total weight of the zeolite.

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