CN217140431U

CN217140431U - Catalytic cracking regeneration equipment suitable for maintaining heat balance and catalytic cracking system

Info

Publication number: CN217140431U
Application number: CN202123029751.0U
Authority: CN
Inventors: 龚剑洪; 魏晓丽; 张执刚
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: 2022-08-09
Anticipated expiration: 2031-12-03

Abstract

The present application relates to a catalytic cracking regeneration apparatus suitable for maintaining heat balance, comprising an afterburner and a regenerator, the outlet of the afterburner being in fluid communication with the inlet of the regenerator such that material from the afterburner can flow into the regenerator; wherein the afterburner is provided with a spent catalyst inlet, an oxygen-deficient gas inlet and a fuel oil inlet; the regenerator is provided with an oxygen-enriched gas inlet; the bottom of the afterburner is communicated with the bottom of the regenerator through an external catalyst circulating pipe. When the regeneration equipment and the method are used for the fluidized catalytic cracking reaction with less coke generation, not only is the heat balance of the reaction-regeneration process realized, but also the temperature rise of the catalyst is uniform in the coke burning process of the regenerator, no local hot spot exists, and the physical and chemical properties of the catalyst are not damaged.

Description

Catalytic cracking regeneration equipment suitable for maintaining heat balance and catalytic cracking system

Technical Field

The present disclosure relates to the field of fluid catalytic cracking technology, and more particularly, to a catalytic cracking regeneration device and a catalytic cracking system suitable for maintaining heat balance.

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 catalyst flows between the reactor and the regenerator, continuously taking heat from one end and supplying heat to the other. The establishment of the heat balance requires certain conditions on the basis of which the cracking and regeneration can be maintained at the prescribed temperature. The heat balance between the reactor and the regenerator is based on the fact that the reaction can produce enough coke for a catalytic cracking industrial unit, and the coke is burned in 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. However, since catalytic cracking employs a catalyst having a molecular sieve as an active component, the local high temperature generated by the combustion of fuel oil in a regenerator gradually removes the aluminum of the molecular sieve framework, resulting in damage to the catalyst, and this damage is irreversible. 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 regeneration device for maintaining thermal equilibrium catalytic cracking, which solves the problem of thermal equilibrium in the catalytic cracking reaction process and does not influence the physical and chemical properties of a catalyst.

The present application relates to a catalytic cracking regeneration apparatus suitable for maintaining heat balance, characterized in that the catalytic cracking regeneration apparatus comprises an afterburner and a regenerator, the outlet of the afterburner being in fluid communication with the inlet of the regenerator, such that material from the afterburner can flow into the regenerator;

wherein the afterburner is provided with a spent catalyst inlet, an oxygen-deficient gas inlet and a fuel oil inlet;

the regenerator is provided with an oxygen-enriched gas inlet;

the bottom of the afterburner is communicated with the bottom of the regenerator through an external catalyst circulating pipe.

In one embodiment, the afterburner is provided with the oxygen-deficient gas inlet, a connecting port of an external catalyst circulating pipe, a spent catalyst inlet and a fuel oil inlet from bottom to top in sequence.

In one embodiment, the connection port of the external catalyst circulation pipe on the afterburner is at a distance of 5% to 10% of the height of the afterburner from the bottom of the afterburner.

In one embodiment, the fuel oil inlets are each independently disposed mid-upstream of the afterburner.

In one embodiment, the fuel oil inlets are each independently at a distance from the afterburner base of from 20% to 50% of the afterburner height.

In one embodiment, the afterburner bottom is provided with a first gas distributor such that oxygen-depleted gas injected via the oxygen-depleted gas inlet enters the afterburner through the first gas distributor.

In one embodiment, the afterburner outlet is provided with a catalyst distribution plate.

In one embodiment, the afterburner is hollow cylindrical with a length to diameter ratio of 30: 1 to 3: 1.

In one embodiment, the regenerator bottom is provided with a second gas distributor so that oxygen-enriched gas injected via the oxygen-enriched gas inlet enters the regenerator through the second gas distributor.

In one embodiment, the regenerator is in fluid communication with a gas-solid separation device, such that the regenerated flue gas generated by the regenerator is separated by the gas-solid separation device and introduced into the energy recovery system.

The application also provides a regeneration method of the catalytic cracking catalyst, which is carried out in the catalytic cracking regeneration equipment, and comprises the following steps:

injecting oxygen-poor gas into the afterburner through an oxygen-poor gas inlet, contacting with regenerated catalyst from the regenerator and spent catalyst from the reactor, heating the spent catalyst and performing partial coking reaction;

injecting a mixture of an atomized medium and combustion oil into the afterburner through a fuel oil inlet, and enabling the mixture of the atomized medium and the combustion oil to be in contact with a catalyst in the afterburner to perform a coking reaction and a partial coking reaction to obtain a catalyst with partial coke;

and (3) enabling the catalyst with part of coke to enter a regenerator, and contacting with oxygen-enriched gas injected into the regenerator through an oxygen-enriched gas inlet to generate complete combustion reaction to obtain a regenerated catalyst.

In one embodiment, the linear velocity of the afterburner is between 1.2 m/s and 2.2 m/s, and the oxygen content of the oxygen-depleted gas is between 1% and 20%, and more preferably, the oxygen content of the oxygen-depleted gas is between 5% and 10%.

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

in one embodiment, the outlet temperature of the afterburner is 550-.

In one embodiment, the oxygen content of the oxygen-enriched gas in the regenerator is from 21% to 100% by volume, and more preferably, the oxygen content of the oxygen-enriched gas is from 21% to 85% by volume.

In one embodiment, the temperature within the regenerator is 600-.

The present application further provides a catalytic cracking system comprising the catalyst regeneration apparatus of the present application.

The regeneration equipment has the advantages of simple structure, easiness in implementation, capability of being implemented by adaptively modifying the regenerator of the existing industrial device, strong applicability, capability of fundamentally solving the problem of heat balance, reduction of the damage to the catalyst and a regeneration system caused by the conventional oil spraying and burning mode, saving of the catalyst cost and improvement of the economic benefit of a refinery, and particularly, the problem of heat balance of the catalytic cracking device which takes chemical raw materials such as low-carbon olefins as main target products is solved. When the regeneration equipment and the method are used for the fluidized catalytic cracking reaction with less coke formation, not only is the heat balance of the reaction-regeneration process realized, but also the temperature rise of the catalyst is uniform in the coke burning process of the regenerator, local hot spots are avoided, 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 an embodiment of a catalytic cracking regeneration unit 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.

As shown in fig. 1, the present application provides a catalytic cracking regeneration apparatus suitable for maintaining heat balance, comprising an afterburner 1 and a regenerator 2, wherein an outlet of the afterburner 1 is in fluid communication with an inlet of the regenerator 2, such that material from the afterburner 1 can flow into the regenerator 2.

In the present application, the catalytic cracking regeneration apparatus further comprises an afterburner 1. The afterburner 1 is provided with a spent catalyst inlet 7, an oxygen-depleted gas inlet 5 and a fuel oil inlet 9. The bottom of the afterburner 1 is communicated with the bottom of the regenerator 2 through an external catalyst circulating pipe 8, so that a part of high-temperature regenerated catalyst in the regenerator 2 can flow into the afterburner 1 for heating spent catalyst in the afterburner 1 from the reactor, and optimal utilization of energy is realized.

In the present application, the afterburner 1 is a fast fluidized bed. In one embodiment, the afterburner 1 is hollow cylindrical with a length to diameter ratio of 30: 1 to 3: 1.

in the application, a spent catalyst inlet 7, a connecting port of an external catalyst circulating pipe 8, an oxygen-deficient gas inlet 5 and a fuel oil inlet 9 which are independently arranged on the afterburner 1 are positioned at different heights of the afterburner 1. Preferably, the afterburner 1 is provided with an oxygen-poor gas inlet 5, a connecting port of an external catalyst circulating pipe 8, a spent agent inlet 7 and a fuel oil inlet 9 in sequence from bottom to top, and the oxygen-poor gas inlet, the connecting port of the external catalyst circulating pipe and the spent agent inlet 7 are all positioned at the lower part of the afterburner 1 (the distance from the bottom of the afterburner 1 is not more than 50% of the height of the afterburner 1).

In the present application, the afterburner 1 is provided with one or more oxygen-depleted gas inlets 5 in its lower part. In one embodiment, the oxygen-depleted gas inlet 5 is located at the bottom of the afterburner 1. Preferably, the afterburner bottom is provided with a first gas distributor 6, such that oxygen-depleted gas injected via the oxygen-depleted gas inlets 5 enters the afterburner 1 through the first gas distributor 6.

According to the present application, the first gas distributor 6 may be a main wind distributor as known to those skilled in the art. For example, the main wind distributor may be a distribution plate and a distribution pipe. Preferably, the distribution pipes are annular distribution pipes and dendritic distribution pipes.

According to the present application, the oxygen-depleted gas injected into the afterburner can be selected from the group consisting of oxygen, air, nitrogen, water vapor, and mixtures thereof, preferably, the oxygen content of the oxygen-depleted gas is 1 vol% to 20 vol%, and preferably, the oxygen content of the oxygen-depleted gas is 5 vol% to 10 vol%.

In one embodiment, the connection port of the external catalyst circulation pipe 8 on the afterburner 1 is arranged at the lower part of the afterburner 1, preferably, the distance from the bottom of the afterburner is 5 to 10 percent of the height of the afterburner.

In the present application, the afterburner can be provided with one or more, e.g. one, two or more fuel oil inlets 9, which can each be provided independently at the outlet end of the afterburner or at the bottom of the afterburner. Further preferably, said fuel oil inlets 9 are each independently arranged mid-upstream of said afterburner 1. Further preferably, the fuel oil inlets 9 are each independently at a distance from the afterburner bottom of 20% to 50% of the afterburner height. The fuel oil 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, catalytically cracked slurry, coker gasoline, coker diesel and coker gas oil.

In the present application, a catalyst distribution plate, 10, may be provided at the location where the catalyst enters the bottom of the regenerator, for example at the outlet end of the afterburner 1.

The catalyst distribution plate 10 may be any of various types of distribution plates commonly found in the industry, such as one or more of flat, arched, dished, annular, and umbrella-shaped, depending on the application. The catalyst distribution plate is beneficial to enabling the catalyst to be uniformly contacted with the oxygen-enriched gas in the axial direction of the regenerator for a coking reaction, so that the coking efficiency is improved, and the occurrence of local hot spots of a catalyst bed layer is reduced.

The fuel oil is mixed with the catalyst under the low-temperature and oxygen-deficient fluidization condition to form coke by arranging the afterburner 1, and the coke-attached catalyst is back-mixed in the afterburner 1 with the characteristic of a fast fluidized bed, so that the coke is uniformly distributed on the catalyst and is partially combusted, and the gradient rise of the surface temperature of the catalyst is realized.

In the present application, the regenerator 2 may be a conventional regenerator, and only an opening is provided at the bottom thereof, and the outlet of the afterburner 1 is connected to the opening, so that the outlet of the afterburner 1 is in fluid communication with the inlet of the regenerator 2, and the material from the afterburner 1 can flow into the regenerator 2.

A connection port for an external catalyst circulation pipe 8 is further arranged at the lower part of the regenerator 2, so that a part of the regenerated catalyst in the regenerator 2 can flow into the afterburner 1 for heating the spent catalyst in the afterburner 1 from the reactor, thereby realizing the optimal utilization of energy.

The regenerator 2 is provided with an oxygen-enriched gas inlet 11 for injecting oxygen-enriched gas into the regenerator for regenerating the catalyst entering the regenerator 2. In one embodiment, the oxygen content of the oxygen-enriched gas entering the regenerator is from 21% to 100% by volume, and more preferably, the oxygen content of the oxygen-enriched gas is from 21% to 85% by volume. In this application, the oxygen-enriched gas injected into the regenerator may be air.

In one embodiment, the regenerator bottom is provided with a second gas distributor 12, such that oxygen-enriched gas injected via the oxygen-enriched gas inlet 11 passes through the second gas distributor 12 into the regenerator 2. The second gas distributor 12 may, according to the present application, be a main wind distributor as known to the person skilled in the art. For example, the main wind distributor may be a distribution plate and a distribution pipe. Preferably, the distribution pipes are annular distribution pipes and dendritic distribution pipes.

In one embodiment, the regenerator 2 is in fluid communication with a gas-solid separation device 3, so that the regenerated flue gas generated by the regenerator 2 is separated by the gas-solid separation device 3 and then introduced into an energy recovery system through a regenerated flue gas pipeline 4 for recycling. In the present application, the gas-solid separation apparatus 3 may be any apparatus known to those skilled in the art. For example, the gas-solid separation device 3 may comprise a cyclone.

The regenerator 2 is also provided with a regenerated catalyst outlet 13 for sending the regenerated high-temperature regenerated catalyst out of the regenerator 2 for reaction recycling.

In the present application, the regenerator 2 and the afterburner 1 may be arranged coaxially or in high-low parallel.

In the present application, after the catalyst with a part of coke burned off enters the regenerator, the catalyst is fully burned off and releases heat under the action of high-temperature oxygen-rich gas, and the heat required by the reaction is supplied. By adopting the device, the burning environment on the catalyst can be alleviated, gradual temperature rise on the catalyst is realized, and the physical and chemical properties of the catalyst are protected to the maximum extent.

The catalytic cracking device has the advantages of simple structure, easy implementation, strong applicability, and especially, the catalytic cracking device which takes chemical raw materials such as low-carbon olefin and the like as main target products can not only fundamentally solve the problem of heat balance, but also reduce the damage to the catalyst and a regeneration system caused by the traditional fuel oil spraying and burning mode, thereby saving the catalyst cost and improving the economic benefit of a refinery.

injecting oxygen-poor gas into the afterburner through the oxygen-poor gas inlet, contacting with regenerated catalyst from the regenerator and spent catalyst from the reactor, heating the spent catalyst and carrying out partial coking reaction;

injecting a mixture of an atomized medium and combustion oil into the afterburner through a fuel oil inlet, and enabling the mixture of the atomized medium and the combustion oil to be in contact with a catalyst in the afterburner to perform a coke-forming reaction and a partial coke-burning reaction to obtain a catalyst with partial coke;

In one embodiment, the atomizing medium is nitrogen, and the mass ratio of the atomizing medium to the combustion oil is 1: 1 to 1: 100. in one embodiment, the fuel oil comprises 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.

In one embodiment, the outlet temperature of the afterburner is 550-.

In one embodiment, the temperature within the regenerator is 600-; the gas superficial linear velocity is between 0.2 and 1.0 m/s, preferably between 0.3 and 0.8 m/s, and the mean residence time of the catalyst is between 0.5 and 10 minutes, preferably between 1 and 5 minutes.

The catalytic cracking regeneration equipment is suitable for catalytic cracking reaction-regeneration systems with various raw materials and insufficient coke formation, such as reactions for producing low-carbon olefins by catalytic cracking of petroleum hydrocarbons and oxygenated hydrocarbons, particularly for producing low-carbon olefins by catalytic cracking of light hydrocarbons or light distillate oil.

For example, the light hydrocarbon or light distillate oil can be gas hydrocarbon, petroleum hydrocarbon with the distillation range of 25-350 ℃, oxygen-containing compound, biomass or distillate oil of waste plastic generated oil; the gaseous hydrocarbon may be selected from a mixture of one or more of a saturated liquefied gas, an unsaturated liquefied gas and a carbon four fraction; the petroleum hydrocarbon may be selected from one or more of primary processed straight run naphtha, straight run kerosene, straight run diesel; the secondary processed topping oil, raffinate oil, carbon four fraction, hydrocracking light naphtha, pentane oil, coker gasoline, Fischer-Tropsch synthetic oil, fluid catalytic cracking light gasoline, hydrogenation gasoline and one or more of hydrogenation diesel oil.

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 catalyst regeneration apparatus of the present application may be connected to the one or more catalytic cracking reactors, such that spent catalyst from the one or more catalytic cracking reactors is introduced into the catalyst regeneration apparatus of the present application for regeneration, 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 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 regeneration plant of the present application, wherein the catalytic cracking regeneration plant comprises, from bottom to top, an afterburner 1 and a regenerator 2. The bottom of the afterburner 1 is provided with an oxygen-poor inlet 5 and a gas distribution plate 6. The side wall below the afterburner 1 is provided with a spent catalyst inlet 7 and a connecting port of an external catalyst circulating pipe 8, and the middle upstream of the afterburner 1 is provided with a fuel oil inlet 9. The regenerator is provided at the bottom with a main wind distributor 12 and at the lower side wall with one or more, e.g. one, two or more, main wind inlets 11.

Oxygen-depleted gas, which may be oxygen, air, nitrogen, water vapor or a mixture thereof, enters the afterburner 1 from the bottom of the afterburner 1 through the oxygen-depleted inlet 5. The high-temperature regenerated catalyst from the external catalyst circulating pipe 8 enters the lower part of the afterburner 1, is mixed with oxygen-poor gas and moves upwards, is contacted with the spent catalyst from the spent catalyst inlet 7 and generates partial coking reaction, and the reactant flow continuously moves upwards, is contacted with the supplementary fuel oil from the fuel oil inlet 9 and generates coking reaction and partial coking reaction; the catalyst with the carbon coke flows upwards, enters the regenerator 2 through the catalyst distributor 10, contacts with the oxygen-enriched gas injected through the oxygen-enriched gas inlet 11 and the main air distributor 12 and generates complete combustion reaction, heat is completely released, and the regenerated catalyst is sent out of the regenerator through a regenerated catalyst outlet 13 for reaction recycling; the regenerated flue gas enters an energy recovery system through a pipeline 4 after the entrained catalyst is separated by the cyclone separator 3.

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 configuration is shown in figure 1. The regenerator configuration is shown in figure 1. The fast bed reactor of the medium-sized device is used as an afterburner, and the regenerator of the medium-sized device is used as a regenerator. Wherein the content of the first and second substances,

wherein, the inner diameter of the afterburner is 0.3 meter, and the height is 2 meters; the fuel oil inlet 9 of the afterburner is at a distance of 30% of the height of the afterburner from the bottom of the afterburner. The outlet of the afterburner is directly communicated with the bottom opening of the regenerator, and a catalyst distributor is arranged at the outlet.

Introducing a mixture of nitrogen and air with the oxygen content of 5% into the bottom of the afterburner 1, and mixing the mixture with the regenerated catalyst and the spent catalyst in sequence to move upwards so as to heat the spent catalyst and enable the spent catalyst to be carbonized to perform partial combustion reaction; injecting the fuel oil atomized by the nitrogen into the afterburner, and contacting with a stream in the afterburner to generate a coking reaction and a small amount of coking reaction; the catalyst with coke enters the regenerator and contacts with air to generate complete fuel reaction and release heat. The regeneration main operating conditions and regenerator temperature profile changes are shown in table 1.

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

As can be seen from Table 1, in this example, the outlet temperature of the afterburner was 675 deg.C, the temperatures at different locations in the middle of the regenerator were 687 deg.C and 681 deg.C, the radial temperature difference was only 6 deg.C, the upper temperature of the regenerator was 695 deg.C, and the axial temperature difference was about 10 deg.C.

Comparative example 1

The comparative example employed a conventional catalytic cracking regenerator having the same structure and dimensions as the regenerator of example 1, with a fuel 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. The regeneration main operating conditions and regenerator temperature profile changes are shown in table 1.

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

As can be seen from table 1, the temperatures at different locations in the middle of the regenerator in the comparative example were 668 ℃ and 725 ℃, respectively, with a radial temperature difference of only 57 ℃, and the upper regenerator temperature was 737 ℃ with a large axial temperature difference.

From the results of the above examples and comparative examples, it can be seen that when the regeneration apparatus of the present application is used for catalyst regeneration, the coke combustion environment in the regenerator is mild and stable, and the radial and axial catalyst temperatures help to maintain the physical and chemical properties of the catalyst.

In the description of the present application, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", "left", "right", and the like indicate orientations or positional relationships based on operational states of the present application, and are only used for convenience in describing and simplifying the present application, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present application.

In the description of the present application, it should be noted that the terms "mounted," "connected," and "connected" are to be construed broadly unless otherwise explicitly specified 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.

TABLE 1 comparison of regeneration results for examples and comparative examples

	Examples	Comparative example
			Afterburning device
Spent catalyst inlet temperature	580	580
			Outlet temperature	675
Amount of fuel oil in kg/hr	218	211
			Oxygen content in oxygen-poor gas,% by weight	5	/
Regenerator
			The temperature in the middle of the regenerator is 1 deg.C	687	725
The temperature of the middle part of the regenerator is 2 DEG C	681	668
			Regenerator top temperature,. deg.C	695	737

Claims

1. Catalytic cracking regeneration apparatus adapted to maintain heat balance, characterized in that the catalytic cracking regeneration apparatus comprises an afterburner and a regenerator, the outlet of the afterburner being in fluid communication with the inlet of the regenerator such that material from the afterburner can flow into the regenerator;

the regenerator is provided with an oxygen-enriched gas inlet;

2. The catalytic cracking regeneration equipment of claim 1, wherein the afterburner is provided with the oxygen-poor gas inlet, a connecting port of an external catalyst circulation pipe, a spent catalyst inlet and a fuel oil inlet in sequence from bottom to top.

3. The catalytic cracking regeneration apparatus of claim 2, wherein the connection port of the external catalyst circulation pipe on the afterburner is located at a distance of 5% to 10% of the height of the afterburner from the bottom of the afterburner.

4. The catalytic cracking regeneration apparatus of claim 1, wherein the fuel oil inlets are each independently disposed mid-upstream of the afterburner.

5. The catalytic cracking regeneration apparatus of claim 1, wherein the fuel oil inlets are each independently located from 20% to 50% of the afterburner height from the bottom of the afterburner.

6. The catalytic cracking regeneration apparatus of claim 1, wherein the afterburner bottom is provided with a first gas distributor such that oxygen-depleted gas injected via the oxygen-depleted gas inlet enters the afterburner through the first gas distributor.

7. The catalytic cracking regeneration apparatus of claim 1, wherein the afterburner outlet is provided with a catalyst distribution plate.

8. The catalytic cracking regeneration apparatus of claim 1, wherein the afterburner is hollow cylindrical with a length to diameter ratio of 30: 1 to 3: 1.

9. the catalytic cracking regeneration apparatus of claim 1, wherein the regenerator bottom is provided with a second gas distributor so that oxygen-rich gas injected through the oxygen-rich gas inlet enters the regenerator through the second gas distributor.

10. The catalytic cracking regeneration device of claim 1, wherein the regenerator is in fluid communication with a gas-solid separation device, so that the regenerated flue gas generated by the regenerator is separated by the gas-solid separation device and introduced into an energy recovery system.

11. A catalytic cracking system, characterized in that it comprises a catalytic cracking regeneration unit according to any one of claims 1 to 10.