CN217120297U

CN217120297U - Fluidized catalytic cracking regenerator and catalytic cracking system

Info

Publication number: CN217120297U
Application number: CN202123028052.4U
Authority: CN
Inventors: 张执刚; 龚剑洪; 魏晓丽
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2021-12-03
Filing date: 2021-12-03
Publication date: 2022-08-05
Anticipated expiration: 2031-12-03

Abstract

The application relates to a fluidized catalytic cracking regenerator and catalytic cracking system, this fluidized catalytic cracking regenerator from the bottom up includes in proper order: a pre-lift zone, a char formation zone, a pre-combustion zone, and a main combustion zone. When the regenerator and the method are used for the fluidized catalytic cracking reaction with less coke generation, not only can the heat balance of the reaction-regeneration process be realized, but also the temperature rise of the catalyst in the coking process of the regenerator is uniform, no local hot spot exists, and the physical and chemical properties of the catalyst are not damaged.

Description

Fluidized catalytic cracking regenerator and catalytic cracking system

Technical Field

The present application relates to the field of fluid catalytic cracking technology, and more particularly, to a fluid catalytic cracking regenerator and a catalytic cracking system.

Background

The fluidized catalytic cracking reaction process is an autothermal equilibrium process, and a large amount of high-temperature heat energy released in the catalyst scorching regeneration process can just meet the requirements of the lower-temperature cracking reaction process. The catalyst circulating between the reactor and the regenerator has sufficient quantity and heat capacity so that the catalyst can act both as an active site for the reaction and as a heat carrier for the transfer of heat energy. The heat carrier flows between the reactor and the regenerator, continuously taking heat from one end and supplying it to the other, the establishment of the heat balance requires certain conditions on the basis of which the cracking and regeneration can be maintained up to the specified temperature. For a catalytic cracking industrial unit, the heat balance between the reactor and the regenerator is based on the fact that the reaction can produce enough coke that is burned during the regeneration process to release heat for the reaction.

With the development of oil refining process, especially the trend of heavy/inferior crude oil is aggravated and the quality of oil products is improved, so that the hydrogenation process is more widely applied. When the hydrogenated and upgraded raw material is used as a catalytic cracking raw material, although the structure and the quality of the product are greatly improved, the catalytic cracking device is lack of coke formation, so that the problem of insufficient heat supply is caused. In addition, in the catalytic cracking technology using low-carbon olefin as a main target product, the conversion rate of cracking reaction is high, the reaction temperature is high, the reaction heat is large, the heat required in the reaction aspect is more than that of a conventional fluidized catalytic regenerator or other catalytic conversion methods, and coke generated by self-cracking cannot meet the self-heat balance requirement of a reaction-regeneration system. When the coke formation is insufficient in the reaction process, the fuel oil is supplemented to the outside of the regenerator to provide the required heat for the reaction. Since catalytic cracking uses a catalyst with a molecular sieve as an active component, the catalyst is damaged irreversibly by the gradual removal of molecular sieve framework aluminum due to the local high temperature generated by the combustion of fuel oil in a regenerator.

The prior art does not fundamentally solve the influence of high-temperature hot spots generated by local combustion of the external fuel oil on the framework structure and the reaction performance of the catalyst.

SUMMERY OF THE UTILITY MODEL

The application aims to provide a catalytic cracking regenerator, which solves the problem of insufficient heat in the catalytic cracking reaction process and does not influence the physical and chemical properties of a catalyst.

The application provides a fluid catalytic cracking regenerator, it from the bottom up includes in proper order:

the pre-lifting area is provided with a pre-lifting area,

a coke-producing area, wherein the coke-producing area,

a precombustion zone, and

the main combustion area is provided with a main combustion area,

wherein the pre-lift zone outlet is in fluid communication with the green coke zone inlet, the green coke zone outlet is in fluid communication with the pre-combustion zone inlet, and the pre-combustion zone outlet is in fluid communication with the primary combustion zone inlet; the pre-combustion zone is communicated with the main combustion zone through an external catalyst circulating pipe;

one or more supplementary fuel oil inlets are arranged on the side wall of the pre-lifting area and/or the side wall of the coking area;

one or more supplementary oxygen-containing gas inlets are formed in the side wall of the pre-combustion zone;

one or more main oxygen-containing gas inlets are arranged on the side wall of the main combustion area.

In one embodiment, one or more of said supplemental fuel oil inlets are provided in the sidewall of said pre-lift zone, each at a distance of from 0% to 15% of the height of the pre-lift zone independently from the outlet end of said pre-lift zone; preferably 0% to 10%.

In one embodiment, one or more of said supplemental fuel oil inlets are provided in the side wall of the coking zone, each at a distance of from 0% to 15%, preferably from 0% to 10%, of the height of the coking zone independently from the bottom of the coking zone.

In one embodiment, the supplemental oxygen-containing gas inlet is provided in a lower part of the pre-combustion zone, and the supplemental oxygen-containing gas inlet nozzles are each independently at a distance from the bottom of the pre-combustion zone of from 15% to 30% of the height of the pre-combustion zone.

In one embodiment, the axial angle of the make-up oxygen-containing gas nozzle line is from 5 ° to 85 °, preferably from 15 ° to 75 °.

In one embodiment, the catalyst circulation tube is connected to the pre-combustion zone at a position that is each independently from 0% to 10% of the height of the pre-combustion zone from the bottom of the pre-combustion zone.

In one embodiment, the main combustion zone, the char zone, and the pre-combustion zone are arranged coaxially.

In one embodiment, a catalyst delivery pipe is arranged at the top of the pre-combustion zone outlet, and the pre-combustion zone outlet together with the catalyst delivery pipe is located inside the main combustion zone.

In one embodiment, a gas distributor is provided in a lower portion of the primary combustion zone, the gas distributor being configured to distribute primary regeneration oxygen-containing gas input through one or more primary oxygen-containing gas inlets provided in a sidewall of the primary combustion zone.

In one embodiment, the ratio of the inner diameter of the pre-lift zone to the char-generating zone is 0.2: 1 to 0.8: 1, the ratio of the height of the pre-lifting area to the height of the coking area is 0.5: 1 to 1.5: 1.

in one embodiment, the pre-combustion zone comprises a partial combustion section and an outlet section, the partial combustion section having an inner diameter larger than the inner diameter of the outlet section.

In one embodiment, the ratio of the inner diameter of the partial combustion section to the inner diameter of the outlet section is 10: 1 to 2: 1, the ratio of the height of the partial combustion section to the height of the outlet section being 10: 1 to 2: 1.

the present application provides a catalytic cracking regeneration process, which is carried out in the above-mentioned fluid catalytic cracking regenerator of the present application, comprising the steps of:

introducing a catalyst to be generated into a pre-lifting area of a regenerator, contacting and mixing the catalyst with a pre-lifting medium, and moving upwards;

mixing an atomized medium with combustion oil, injecting the mixture into the fluidized catalytic cracking regenerator at one or more supplementary fuel oil inlets, and contacting with the existing material flow in the fluidized catalytic cracking regenerator to generate a coking reaction to obtain a catalyst with coke;

introducing the coked catalyst into a pre-combustion zone, mixing the coked catalyst with regenerated catalyst which is circulated back to the pre-combustion zone through a catalyst circulation pipe, raising the temperature, and carrying out partial combustion reaction in the presence of oxygen-poor gas introduced from one or more oxygen-supplementing gas inlets;

and (2) feeding part of the coked catalyst into a main combustion area, and carrying out complete combustion reaction in the presence of oxygen-enriched gas introduced from one or more main oxygen-containing gas inlets to obtain a regenerated catalyst.

In one embodiment, the pre-lift medium of the pre-lift zone is nitrogen, water vapor or a mixture thereof; the atomizing medium is nitrogen.

In one embodiment, the mass ratio of atomizing medium to combustion oil is 1:1 to 1: 100.

in one embodiment, the linear velocity of the precombustion zone is between 1.2 m/s and 2.2 m/s; the oxygen content of the oxygen-depleted gas is 1 vol% to 20 vol%, and further preferably, the oxygen content of the oxygen-depleted gas is 5 vol% to 10 vol%.

In one embodiment, the temperature within the pre-combustion zone is 550-.

In one embodiment, the oxygen content of the oxygen-enriched gas in the main combustion zone is 21 vol% to 100 vol%, and further preferably, the oxygen content of the oxygen-enriched gas is 21 vol% to 85 vol%.

In one embodiment, the temperature within the primary combustion zone is 600-.

The present application also provides a catalytic cracking system comprising the above-described fluid catalytic cracking regenerator of the present application.

When the regenerator and the method are used for the fluidized catalytic cracking reaction with less coke generation, not only can the heat balance of the reaction-regeneration process be realized, but also the temperature rise of the catalyst in the coking process of the regenerator is uniform, no local hot spot exists, and the physical and chemical properties of the catalyst are not damaged.

Drawings

The accompanying drawings, which are included to provide a further understanding of the application and are incorporated in and constitute a part of this specification, illustrate embodiments of the application and together with the description serve to explain the principles of the application and not to limit the application. In the drawings:

FIG. 1 is a schematic diagram of one embodiment of a catalytic cracking regenerator as provided herein.

Detailed Description

The present application is described in further detail below with reference to the figures and examples. The features and advantages of the present application will become more apparent from the description.

The word "exemplary" is used exclusively herein to mean "serving as an example, embodiment, or illustration. Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. While the various aspects of the embodiments are presented in drawings, the drawings are not necessarily drawn to scale unless specifically indicated.

In addition, the technical features described below in the different embodiments of the present application may be combined with each other as long as they do not conflict with each other.

Any specific value disclosed herein (including endpoints of ranges of values) is not to be limited to the precise value of that value, but rather should be construed to also encompass values close to the precise value, for example, all possible values within 5% of the precise value. Also, for the disclosed ranges of values, any combination between the endpoints of the ranges, between the endpoints and specific points within the ranges, and between specific points within the ranges can result in one or more new ranges of values, which should also be considered as specifically disclosed herein.

In the present application, the terms "upstream" and "downstream" are used with reference to the direction of flow of the reactant materials. For example, when the reactant stream flows from bottom to top, "upstream" refers to a position located below, and "downstream" refers to a position located above.

Unless otherwise defined, terms used herein have the same meaning as commonly understood by one of ordinary skill in the art, and if a term is defined herein and its definition is different from that commonly understood in the art, the definition herein controls.

The present application relates to a fluid catalytic cracking regenerator 100, which comprises from bottom to top in sequence interconnected:

the pre-lifting zone 1 is provided with,

the coke-producing zone (2) is provided with a coke-producing zone,

a precombustion zone 3, and

the main combustion zone 4 is provided with a main combustion zone,

wherein the pre-lift zone outlet is in fluid communication with the green coke zone inlet, the green coke zone outlet is in fluid communication with the pre-combustion zone inlet, and the pre-combustion zone outlet is in fluid communication with the primary combustion zone inlet; the pre-combustion zone 3 is communicated with the main combustion zone 4 through an external catalyst circulating pipe 12;

one or more supplementary fuel oil inlets 10 are arranged on the side wall of the pre-lifting area 1 and/or the side wall of the coking area 2;

one or more supplementary oxygen-containing gas inlets 11 are arranged on the side wall of the pre-combustion zone 3;

one or more main oxygen-containing gas inlets 14 are provided in the side wall of the main combustion zone 4.

The fcc regenerator 100 of the present application includes a pre-lift zone 1 disposed lowermost in the fcc regenerator 100, but upstream of the spent catalyst in the flow direction of the fcc regenerator 100. A spent catalyst inlet 9 is also provided at the lower part of the pre-lift zone 1 for feeding spent catalyst from the catalytic cracking reactor to the fluid catalytic cracking regenerator 100 for regeneration. The pre-lift medium is fed from the lower inlet 8 of the pre-lift zone 1 for lifting the fed spent catalyst upwards. The pre-lift medium used in the pre-lift zone may be nitrogen, water vapor or mixtures thereof.

In one embodiment, the pre-lifting section 1 may be in the form of a hollow cylinder of constant diameter, which may have a length to diameter ratio of 30: 1 to 3: 1.

as mentioned above, in the fcc regenerator 100 of the present application, one or more supplemental fuel oil inlets 10 are provided on the sidewall of the pre-lift zone 1 and/or on the sidewall of the coking zone 2 for injecting supplemental fuel oil.

In one embodiment, one or more supplemental fuel oil inlets 10 are provided in the sidewall of the pre-lift zone 1. In this embodiment, the fuel oil inlet 10 is at a distance L from the exit end of the pre-lift zone ₁₀ Each independently of the pre-lift zone height h ₁ 0% to 15%; preferably 0% to 10%.

In one embodiment, one or more of said supplemental fuel oil inlets 10 are provided in the side wall of the coking zone 2 at a distance from the bottom of the coking zone of from 0% to 15%, preferably from 0% to 10%, of the height of the coking zone, independently of each other.

The injected fuel oil can be mixed with the catalyst under the low-temperature, oxygen-free or oxygen-poor fluidization condition to form coke by injecting the supplementary fuel oil into the pre-lifting area and/or the coke forming area, and the catalyst attached with the coke can be further rectified in the coke forming area, so that the coke can be uniformly distributed on the catalyst.

The fcc regenerator 100 of the present application includes a coke formation zone 2 disposed above the pre-lift zone 1 for further rectifying the coke-laden catalyst in the coke formation zone 2 to uniformly distribute the coke on the catalyst. In one embodiment, the coking zone is a pneumatic conveying bed or a fast fluidized bed.

In one embodiment, the coke forming zone 2 may also be in the form of a hollow cylinder of constant diameter, which may have a length to diameter ratio of 30: 1 to 3: 1. in one embodiment, the ratio of the internal diameters of the pre-lift zone 1 and the char-generating zone 2 may be 0.2: 1 to 0.8: 1, the ratio of the height h1 of the pre-lifting zone 1 to the height h2 of the char-generating zone 2 may be 0.5: 1 to 1.5: 1.

in one embodiment, the coke formation zone 2 and the pre-lift zone 1 may be connected by a first connecting section 21. In one embodiment, the longitudinal section of the first connecting section 21 is an isosceles trapezoid, and the outer inclination angle β of the side of the isosceles trapezoid is 5-85 °.

The fuel oil injected through the supplemental fuel oil inlet 10 may comprise straight run distillate or secondary process distillate. Preferably, the secondary process distillate may be selected from a blend of one or more of catalytically cracked diesel, coker gasoline, coker diesel and coker gas oil. To better disperse the fuel oil, the fuel oil may be mixed with the atomizing medium and the mixture injected through the supplemental fuel oil inlet 10. The atomizing medium may include nitrogen gas and the like. In one embodiment, the mass ratio of fuel oil to atomizing medium is 1:1 to 100: 1, e.g., 1:1 to 50:1, or, 1:1 to 20: 1.

The fluidized catalytic cracking regenerator 100 of the present application comprises a pre-combustion zone 3, said pre-combustion zone 3 being provided with one or more supplemental oxygen-containing gas inlets 11 in its side walls. By arranging the pre-combustion zone 3, the catalyst uniformly attached with coke enters the pre-combustion zone and contacts with the oxygen-containing gas at a relatively low temperature and a relatively high gas linear speed, so that the coke on the catalyst is partially combusted, and the gradient rise of the surface temperature of the catalyst is realized.

In one embodiment, the supplemental oxygen-containing gas inlet 11 is arranged in the lower part of the pre-combustion zone 3, the supplemental oxygen-containing gas inlet nozzle being at a distance L from the bottom of the pre-combustion zone ₁₁ Independently of one another, the height h of the prechamber ₃ 15% to 30%.

In one embodiment, the axial angle α of the make-up oxygen-containing gas nozzle line is from 5 ° to 85 °, preferably from 15 ° to 75 °.

The pre-combustion zone 3 is communicated with the main combustion zone 4 through an external catalyst circulating pipe 12. In one embodiment, the catalyst circulation tube 12 is connected to the pre-combustion zone 3 at a distance L from the bottom of the pre-combustion zone ₁₂ Independently of one another, the height h of the prechamber ₃ 0% to 10%. A portion of the regenerated catalyst in the main combustion zone 4 can be recycled to the pre-combustion zone 3 by means of catalyst recycle conduit 12 and mixed with the catalyst from the coke formation zone 2, which can increase its temperature.

As shown in fig. 1, in an embodiment the pre-combustion zone 3 comprises a partial combustion section 31 and an outlet section 32, the inner diameter of the partial combustion section 31 being larger than the inner diameter of the outlet section 32. In one embodiment, the ratio of the inner diameter of the partial combustion section 31 to the inner diameter of the outlet section 32 is 10: 1 to 2: 1, the ratio of the height of said partial combustion section 31 to the height of said outlet section 32 being 10: 1 to 2: 1.

in one embodiment, the pre-lift zone, char zone, pre-combustion zone are all in the form of hollow cylinders and may be arranged coaxially.

The fcc regenerator 100 of the present application includes a main combustion zone 4 for contacting the partially coked catalyst in the pre-combustion zone with oxygen-enriched gas to complete combustion reaction, releasing heat, and recycling the coke-burned high-temperature regenerated catalyst for reaction.

In one embodiment, the main combustion zone and the pre-combustion zone may be arranged coaxially or in high-low juxtaposition. In one embodiment, a catalyst outlet 13 is provided at the top of the pre-combustion zone outlet, and the pre-combustion zone outlet together with the catalyst outlet 13 is located inside the main combustion zone 4, so that the catalyst from the pre-combustion zone 3 can be directly introduced into the main combustion zone 4 through the catalyst outlet 13, thereby completely burning and regenerating in the main combustion zone 4. The main combustion zone 4 of the present application may be of an existing conventional catalytic cracking single stage regenerator configuration and may be open at its lower portion such that the pre-combustion zone outlet together with the catalyst delivery tube 13 is accommodated inside the main combustion zone 4 through this opening. In the main combustion zone 4, under the action of high-temperature oxygen-enriched gas, the catalyst which burns off part of coke is fully burnt to release heat and supply heat required by reaction, so that the burning environment on the catalyst is mild, gradual temperature rise on the catalyst is realized, and the physical and chemical properties of the catalyst are protected to the maximum extent.

As previously described, a connection of the catalyst circulation pipe 12 is provided at the lower portion of the main combustion zone 3 so that a part of the regenerated catalyst in the main combustion zone 4 is circulated back into the pre-combustion zone 3.

In the catalytic cracking regenerator 100 provided herein, one or more primary oxygen-containing gas inlets 14 are provided in the side wall of the primary combustion zone 4 for introducing oxygen-enriched gas into the primary combustion zone 4. In one embodiment, the primary combustion zone 4 is provided with a primary air distributor 7 at the bottom and one or more primary oxygen-containing gas inlets 14 in the lower side wall, said gas distributor 7 being configured to distribute primary regeneration oxygen-containing gas fed through the one or more primary oxygen-containing gas inlets 14 provided in the side wall of said primary combustion zone. The main wind distributor 7 may be a main wind distributor known to those skilled in the art. For example, the main wind distributor may be a distribution plate and a distribution pipe, for example, the distribution pipe may be an annular distribution pipe and a dendritic distribution pipe. The catalyst completely regenerated in the main combustion zone 4 is sent out of the regenerator through an outlet 15 for recycling of catalytic cracking reaction.

The main combustion zone 4 is also in fluid communication with an inlet of a gas-solid separation device 5, and the regenerated flue gas enters an energy recovery system through a pipeline 6 after being separated from entrained catalyst by the gas-solid separation device 5. The gas-solid separation apparatus 5 may employ apparatuses well known to those skilled in the art. For example, the gas-solid separation device may comprise a cyclone.

The catalytic cracking regenerator has a simple structure, is easy to implement, can be implemented by adaptively modifying the regenerator of the conventional industrial device, has strong operability, particularly can fundamentally solve the problem of heat balance by using chemical raw materials such as low-carbon olefin and the like as main target products, reduces the damage to a catalyst and regeneration equipment caused by the conventional fuel oil spraying mode, saves the catalyst cost and improves the economic benefit of a refinery.

The present application also provides a catalytic cracking regeneration process, which is carried out in the above-described fluid catalytic cracking regenerator of the present application, comprising the steps of:

and (3) feeding the partially coked catalyst into a main combustion area, and carrying out complete combustion reaction in the presence of oxygen-enriched gas introduced from one or more main oxygen-containing gas inlets to obtain a regenerated catalyst.

In one embodiment, the mass ratio of atomizing medium to combustion oil is 1:1 to 1: 100. in practical operation, the injection amount of the mixture of the atomizing medium and the combustion oil is adjusted according to the feeding amount of the raw oil in the reactor connected with the regenerator, and is used for controlling the temperature of the regenerated catalyst after regeneration to be 600-800 ℃.

In one embodiment, the temperature within the pre-combustion zone is 550-.

In one embodiment, the temperature within the primary combustion zone is 600-.

It should be noted that the above embodiments regarding the fluidized catalytic cracking regenerator are also applicable to the regeneration method of the present application, and are not described herein again.

The present application also provides a catalytic cracking system comprising the fluidized catalytic cracking regenerator of the present application.

In addition, the catalytic cracking system also comprises a catalytic cracking reaction device, an oil agent separation device, a stripping device and an optional reaction product separation device.

In one embodiment, the catalytic cracking reactor apparatus comprises one or more catalytic cracking reactors. The fluidized catalytic cracking regenerator of the present application may be coupled to the one or more catalytic cracking reactors such that spent catalyst from the one or more catalytic cracking reactors is regenerated by the fluidized catalytic cracking regenerator of the present application and the regenerated catalyst is recycled back to the one or more catalytic cracking reactors for reuse.

In the catalytic cracking system provided by the present application, the catalytic cracking reactor, the stripping device, the oil separation device, the reaction product separation device, and the like can all adopt devices known to those skilled in the art, and the connection manner between the devices can also be carried out according to the manner known in the art. For example, the oil separation device can comprise a cyclone separator and an outlet quick separator. In certain embodiments, the oil separation device comprises a settler arranged coaxially or in high-low parallel with the catalytic cracking reactor.

The regenerator and the method are particularly suitable for the fluidized catalytic cracking reaction with less coke generation, not only can realize the heat balance of the reaction-regeneration process, but also can ensure that the temperature rise of the catalyst is uniform in the coking process of the regenerator, no local hot spot exists, and no damage is caused to the physical and chemical properties of the catalyst.

The present application will be further described with reference to preferred embodiments shown in the drawings, but the application is not limited thereto.

Fig. 1 shows a preferred embodiment of the catalytic cracking regenerator of the present application, wherein the catalytic cracking regenerator comprises, from bottom to top, a pre-lift zone 1, a coke-generating zone 2, a pre-combustion zone 3 and a main combustion zone 4. The lower part of the pre-lifting area 1 is provided with a spent catalyst inlet 9, and the tail end of the pre-lifting area 1 is provided with a fuel oil inlet 10. The lower side wall of the pre-combustion zone 3 is provided with one or more oxygen containing gas inlets 11. The bottom of the primary combustion zone is provided with a primary wind distributor 7 and the lower side wall is provided with one or more, e.g. one, two or more, primary wind inlets 14.

The pre-lift medium, which may be nitrogen, steam or a mixture thereof, enters the catalytic cracking regenerator from the bottom of pre-lift zone 1 via line 8. Spent catalyst from the spent catalyst inlet 9 enters the lower part of the pre-lifting zone 1 and moves upwards under the lifting action of the pre-lifting medium. Fuel oil and atomized medium are injected into the end of the pre-lifting zone 1 through a fuel oil inlet 10, and are mixed and contacted with the catalyst in the regenerator to generate coking reaction. The catalyst with coke flows upwards, enters the pre-combustion zone 3, is mixed with the high-temperature regenerant returned by the catalyst circulating pipe 12, is heated, and then contacts with the oxygen-containing gas injected through the oxygen-containing gas inlet 11 to perform partial coking reaction, so that partial coke on the catalyst is burned off. Part of the catalyst with carbon enters the main combustion area 4 through the delivery pipe 13, contacts with main air injected through the main air inlet 14 and the main air distributor 7 and generates complete combustion reaction, heat is completely released, and the regenerated catalyst is sent out of the regenerator through the outlet 15 for reaction recycling; the regenerated flue gas enters an energy recovery system through a pipeline 6 after the entrained catalyst is separated by a cyclone separator 5.

Examples

The following examples further illustrate the present application but are not intended to limit the same. The catalyst used in the test is spent catalyst, the carbon content is 0.8 wt%, and the combustion oil is catalytic cracking diesel oil.

Example 1

The regenerator structure used in this embodiment is as shown in fig. 1, and comprises a pre-lifting zone 1, a coke-producing zone 2, a pre-combustion zone 3 and a main combustion zone 4 which are connected with each other in sequence from bottom to top. The lower part of the pre-lifting area 1 is provided with a spent catalyst inlet 9, and the tail end of the pre-lifting area 1 is provided with a fuel oil inlet 10. The lower side wall of the pre-combustion zone 3 is provided with one or more oxygen containing gas inlets 11. The bottom of the main combustion area is provided with a main air distributor 7, and the lower side wall is provided with a main air inlet 14; the bottom of the main combustion zone is also connected with the lower part of the pre-combustion zone 3 through an external catalyst circulating pipe 12.

Wherein the inner diameter of the pre-lifting area 1 is 0.05 meter, and the length is 1 meter; the inner diameter of the coke-producing zone 2 is 0.08 m, and the length is 1; the precombustion zone 3 had an internal diameter of 0.3 m and a length of 2 m. The distance between the fuel oil inlet 10 and the outlet end of the pre-lifting area is 5% of the height of the pre-lifting area, and the distance between the position of the oxygen-supplementing gas inlet 11 and the bottom of the pre-combustion area is 20% of the height of the pre-combustion area.

The pre-lifting nitrogen enters the bottom of the pre-lifting area 1, is mixed with a catalyst to be generated and moves upwards, contacts with fuel oil injected from the pre-lifting bottom, is mixed and enters the coke generation area 2 to generate a carbon hanging reaction, and is continuously rectified while moving upwards, so that the coke is uniformly distributed; the catalyst after carbon hanging enters the pre-combustion zone 3, contacts with oxygen-deficient gas injected from the side wall of the pre-combustion zone and carries out pre-combustion reaction, and part of coke is burnt; the catalyst with partial coke enters the main combustion zone 4 and contacts with air to react completely, and heat is released.

At the same height, the axial distance from the bottom of the main combustion zone is 40% of the axial height of the main combustion zone, two temperature measuring points (the angle between the two points relative to the axial direction is 180 degrees) are arranged at the positions close to the wall of the main combustion zone, and the middle temperature of different positions at the same height is measured; and setting a temperature measuring point at the top of the main combustion area to measure the upper temperature of the main combustion area.

The regeneration main operating conditions and regenerator temperature profile changes are shown in table 1. As can be seen from Table 1, in the regenerator of this example, the temperatures in the middle parts at different positions at the same radial height of the main combustion zone were 683 deg.C and 687 deg.C, respectively, the difference in radial temperature was 4 deg.C, and the temperature difference between the upper part of the main combustion zone and the middle part was 701 deg.C.

Comparative example 1

The comparative example employed a conventional catalytic cracking single stage regenerator having the same structure and dimensions as the main combustion zone of example 1, with a fuel oil injection port provided only in the lower dense bed zone of the catalyst.

The spent catalyst enters the lower part of the regenerator and contacts with the air which is distributed by the main air distributor and enters the regenerator to generate a coking reaction, the fuel oil is injected into the catalyst dense-phase bed layer, and the fuel oil contacts with the high-temperature air to generate the coking reaction and release heat.

Similarly, two temperature measuring points (the angle of the two points relative to the axial direction is 180 degrees) are arranged at the same height, the axial distance from the bottom of the regenerator is 40% of the axial height of the regenerator, and the middle temperature of different positions at the same height is measured; and a temperature measuring point is arranged at the top of the regenerator, and the upper temperature of the regenerator is measured.

The regenerator main operating conditions and regenerator temperature profile changes are shown in table 1. As can be seen from Table 1, the temperatures in the middle of the regenerator of this comparative example at different positions at the same radial height were 668 ℃ and 725 ℃, respectively, the difference in the radial temperature was 57 ℃ and the temperature in the upper part of the regenerator was 737 ℃.

From the results of the above examples and comparative examples, it can be seen that when the regenerator and the method of the present application are used for catalyst regeneration, the coke combustion environment in the regenerator is mild and stable, and the radial and axial catalyst temperature gradients are small, which helps to maintain the physical and chemical properties of the catalyst.

TABLE 1 comparison of regeneration results for examples and comparative examples

	Examples	Comparative example
			Pre-lifting zone
Spent catalyst temperature, deg.C	580	/
			Coke formation zone
Temperature, C	570	/
			Amount of fuel oil, g	216	211
Pre-combustion zone
			Temperature, C	635	/
Oxygen content in oxygen-poor gas,% by weight	5	/
			Main combustion zone
The temperature in the middle of the main combustion zone is 1 DEG C	683	725
			The middle temperature of the main combustion zone is 2 DEG C	687	668
Upper temperature of main combustion zone, DEG C	701	737

In the description of the present application, it is to be noted that the terms "mounted," "connected," and "connected" are to be construed broadly unless otherwise explicitly stated or limited. The specific meaning of the above terms in the present application can be understood in a specific case by those of ordinary skill in the art.

The present application has been described above with reference to preferred embodiments, but these embodiments are merely exemplary and merely illustrative. On the basis of the above, the present application can be subjected to various substitutions and improvements, and the substitutions and the improvements are all within the protection scope of the present application.

Claims

1. A fluid catalytic cracking regenerator, comprising from bottom to top:

the pre-lifting area is provided with a pre-lifting area,

a coke-producing area, wherein the coke-producing area,

a precombustion zone, and

the main combustion area is provided with a main combustion area,

2. The fcc regenerator of claim 1, wherein one or more of the supplemental fuel oil inlets are disposed on the sidewall of the pre-lift zone, the fuel oil inlets being each independently at a distance of 0% to 15% of the height of the pre-lift zone from the outlet end of the pre-lift zone.

3. The fcc regenerator of claim 2, wherein the fuel oil inlet is each independently located at a distance of 0% to 10% of the height of the pre-lift zone from the outlet end of the pre-lift zone.

4. The fcc regenerator of claim 1, wherein one or more of the supplemental fuel oil inlets are provided in the side wall of the coking zone, the fuel oil inlets being each independently at a distance from the bottom of the coking zone of from 0% to 15% of the height of the coking zone.

5. The fcc regenerator of claim 4, wherein the fuel oil inlet is each independently at a distance from the bottom of the coking zone of from 0% to 10% of the height of the coking zone.

6. The fcc regenerator of claim 1, wherein the supplemental oxygen-containing gas inlet is disposed in a lower portion of the pre-combustion zone, and the supplemental oxygen-containing gas inlet nozzles are each independently at a distance from the bottom of the pre-combustion zone of from 15% to 30% of the height of the pre-combustion zone.

7. The fluid catalytic cracking regenerator of claim 6, wherein the axial angle of the make-up oxygen-containing gas nozzle line is between 5 ° and 85 °.

8. The fluid catalytic cracking regenerator of claim 7, wherein the axial angle of the make-up oxygen-containing gas nozzle line is between 15 ° and 75 °.

9. The fcc regenerator of claim 1, wherein the catalyst circulation tubes are connected to the pre-combustion zone at a location that is each independently 0% to 10% of the height of the pre-combustion zone from the bottom of the pre-combustion zone.

10. The fcc regenerator of claim 1, wherein the primary combustion zone, the coking zone, and the pre-combustion zone are coaxially arranged.

11. The fcc regenerator of claim 10, wherein a catalyst delivery pipe is provided at the top of the pre-combustion zone outlet, and the pre-combustion zone outlet together with the catalyst delivery pipe is located inside the main combustion zone.

12. The fcc regenerator of claim 1, wherein the lower portion of the primary combustion zone is provided with a gas distributor configured to distribute primary regeneration oxygen-containing gas input through one or more primary oxygen-containing gas inlets provided in the sidewall of the primary combustion zone.

13. The fcc regenerator of claim 1, wherein the ratio of the internal diameters of the pre-lift zone and the coking zone is 0.2: 1 to 0.8: 1, the ratio of the height of the pre-lifting area to the height of the coking area is 0.5: 1 to 1.5: 1.

14. the fluid catalytic cracking regenerator of claim 1, wherein the pre-combustion zone comprises a partial combustion section and an outlet section, the partial combustion section having an inner diameter greater than an inner diameter of the outlet section.

15. The fcc regenerator of claim 14, wherein the ratio of the internal diameter of the partial combustion section to the internal diameter of the outlet section is 10: 1 to 2: 1, the ratio of the height of the partial combustion section to the height of the outlet section being 10: 1 to 2: 1.

16. a catalytic cracking system, characterized in that it comprises a fluid catalytic cracking regenerator according to any of claims 1-15.