CN116212971A

CN116212971A - Catalyst regeneration equipment and regeneration method

Info

Publication number: CN116212971A
Application number: CN202111467953.5A
Authority: CN
Inventors: 张执刚; 魏晓丽; 刘宪龙
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: 2023-06-06

Abstract

The present application relates to a catalyst regeneration apparatus and a regeneration method, the catalyst regeneration apparatus comprising: a green coke reactor, an afterburner zone, and a regenerator. When the regeneration equipment and the method are used for the fluid catalytic cracking reaction with less coke generation, the thermal balance of the reaction-regeneration process is realized, 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

Catalyst regeneration equipment and regeneration method

Technical Field

The present application relates to the field of fluid catalytic cracking technology, and more particularly, to a catalytic cracking catalyst regeneration apparatus and regeneration method suitable for maintaining thermal equilibrium.

Background

The fluid catalytic cracking reaction process is an autothermal balance process, and the catalyst scorching regeneration process releases a large amount of heat energy at high temperature so as to just meet the requirements of the cracking reaction process at lower temperature. The catalyst circulating between the reactor and the regenerator has a sufficient amount and heat capacity so that the catalyst can act as both an active site for the reaction and a heat carrier for transferring heat energy. The catalyst flows between the reactor and the regenerator, constantly taking heat from one end and supplying heat to the other. The establishment of the thermal equilibrium requires certain conditions on the basis of which the cracking and regeneration are maintained up to the prescribed temperature. For a catalytic cracking industry, the thermal balance between the reactor and the regenerator is based on the fact that the reaction produces sufficient coke that burns during regeneration to release heat for the reaction.

Along with the development of oil refining technology, particularly the heavy/inferior trend of crude oil is aggravated, and the quality of oil is improved, so that the hydrogenation technology is widely applied. When the raw material subjected to hydrogenation upgrading is used as a catalytic cracking raw material, although the structure and quality of the product are greatly improved, the catalytic cracking device brings about the problem of insufficient coking and insufficient heat supply. In addition, in the catalytic cracking technology using low-carbon olefin as a main target product, the conversion rate of the cracking reaction is high, the reaction temperature is high, the reaction heat is large, more heat is required in the reaction aspect than that of a conventional fluidized catalytic regenerator or other catalytic conversion methods, and the coke generated by self-cracking cannot always meet the self-heat balance requirement of a reaction-regeneration system. When coke formation is insufficient in the reaction process, a mode of supplementing fuel oil to the outside of the regenerator is generally adopted to provide the required heat for the reaction. However, since catalytic cracking employs a catalyst in which molecular sieves are the active components, the local high temperature generated by the combustion of the fuel oil in the regenerator gradually drives out the molecular sieve framework aluminum, resulting in damage to the catalyst, which is irreversible.

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

Disclosure of Invention

The purpose of the application is to provide a catalytic cracking regeneration device and a catalytic cracking regeneration method capable of maintaining thermal equilibrium, which solve the problem of thermal equilibrium in the catalytic cracking reaction process and do not influence the physical and chemical reaction performance of a catalyst.

The present application provides a catalyst regeneration apparatus, characterized in that the catalyst regeneration apparatus comprises:

coke reactor

An afterburner zone, and

the regeneration device comprises a regenerator, a first heat exchanger, a second heat exchanger, a third heat exchanger and a,

wherein the coking reactor is provided with a spent catalyst inlet, an oxygen-deficient gas inlet and a coking reactor fuel oil inlet; the bottom of the coking reactor is also communicated with the bottom of the regenerator through an external catalyst circulating pipe;

the afterburner zone is provided with an afterburner zone fuel oil inlet, and the inlet of the afterburner zone is in fluid communication with the outlet of the coke-producing reactor such that material from the coke-producing reactor can flow into the afterburner zone;

the regenerator is provided with an oxygen-enriched gas inlet and the outlet of the afterburner zone is in fluid communication with the inlet of the regenerator such that material from the afterburner zone can flow into the regenerator.

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

In one embodiment, the raw coke reactor fuel oil inlets are each independently disposed upstream of the raw coke reactor.

In one embodiment, the distance of the coke reactor fuel oil inlet from the coke reactor bottom is each independently 20% to 50% of the coke reactor height.

In one embodiment, a first gas distributor is provided at the bottom of the green coke reactor such that the oxygen-depleted gas injected via the oxygen-depleted gas inlet enters the green coke reactor through the first gas distributor.

In one embodiment, the connection port of the external catalyst circulation tube on the coke formation reactor is located at a distance of 5% to 10% of the height of the coke formation reactor from the bottom of the coke formation reactor.

In one embodiment, the green coke reactor is integrally connected with the afterburning zone, and the outlet of the afterburning zone is provided with a catalyst rapid separator.

In one embodiment, the green coke reactor and the afterburner zone are hollow cylindrical, and the aspect ratio of the green coke reactor is 30:1 to 3:1, the aspect ratio of the afterburner zone is 30:1 to 3:1, the ratio of the inner diameter of the coke formation reactor to the inner diameter of the afterburner zone is 10:1 to 2:1, the ratio of the length of the coke formation reactor to the length of the afterburner zone is 10:1 to 0.5:1.

in one embodiment, the coke formation reactor is connected with the afterburning zone through a first connecting section, the longitudinal section of the first connecting section is an isosceles trapezoid, and the camber angle beta of the side edge of the isosceles trapezoid is 5-85 degrees.

In one embodiment, the afterburner zone is housed inside the regenerator along with the first connection section and a catalyst flash separator.

In one embodiment, a second gas distributor is provided at the bottom of the regenerator such 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 regeneration flue gas produced by the regenerator is introduced to an energy recovery system after separation by the gas-solid separation device.

The present application also provides a method for regenerating a catalytic cracking catalyst, which is performed in the catalytic cracking regeneration device of the present application, and comprises the following steps:

injecting an oxygen-depleted gas into the coking reactor through an oxygen-depleted gas inlet, contacting the regenerated catalyst from the regenerator and the spent catalyst from the reactor, heating the spent catalyst and generating partial coking reaction;

injecting a mixture of an atomizing medium and combustion oil into the coking reactor through a fuel oil inlet of the coking reactor, so that the mixture of the atomizing medium and the combustion oil contacts with a catalyst in the coking reactor to generate coking reaction and partial coking reaction;

injecting combustion oil into the coking reactor through a fuel oil inlet of the afterburning zone, and contacting with a material flow from the coking reactor to obtain a catalyst for depositing coke;

and enabling the catalyst deposited with coke to enter a regenerator, contacting with oxygen-enriched gas injected into the regenerator through an oxygen-enriched gas inlet, and performing complete combustion reaction to obtain the regenerated catalyst.

In one embodiment, the linear velocity of the green coke reactor is from 1.2 m/s to 2.2 m/s, and the oxygen content of the oxygen-depleted gas is from 1% to 20%, and more preferably, the oxygen content of the oxygen-depleted gas is from 5% to 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 oxygen-enriched gas of the regenerator has an oxygen content of 21 to 100% by volume, and more preferably the oxygen-enriched gas has an oxygen content of 21 to 85% by volume.

In one embodiment, the temperature within the regenerator is 600-800 ℃.

The present application also relates to a catalytic cracking system comprising the catalyst regeneration apparatus of the present application.

The regeneration equipment provided by the application enables injected fuel oil to be mixed with the catalyst and form coke under the low-temperature and oxygen-deficient fluidization condition through the setting of the coking reactor, and the catalyst attached with the coke enables the coke to be uniformly distributed on the catalyst and to be partially combusted through back mixing in the coking reactor with the characteristic of a rapid fluidized bed, so that the gradient rising of the surface temperature of the catalyst is realized.

The regeneration equipment provided by the application can flexibly adjust the fuel oil supplementing quantity and the position according to the requirement of reaction heat by arranging the afterburning zone, so that the fuel oil is injected into the regeneration system at multiple points, coke is uniformly distributed on the catalyst, and a stable and uniform regeneration process is facilitated. The rapid separator arranged at the outlet of the afterburning zone changes the flow direction of the catalyst, so that the catalyst is in countercurrent contact with oxygen-containing gas, and the burning intensity is enhanced.

In the regeneration equipment provided by the application, the catalyst to be regenerated is gradually burnt and afterburned in the oxygen-deficient environment in the coke-producing reactor and the afterburning zone, the catalyst which can enter the regenerator is uniformly provided with carbon, and after the catalyst which is uniformly provided with carbon enters the regenerator, the catalyst is fully burnt and releases heat under the action of high-temperature and oxygen-enriched gas, so that the heat required by the reaction is supplied. The regeneration equipment provided by the application can alleviate the scorching environment on the catalyst, realize gradual temperature rise and furthest protect the physical and chemical properties of the catalyst.

The catalytic cracking device is simple in structure and easy to implement, can be implemented by adaptively reforming the existing industrial device regenerator, is high in applicability, and particularly can fundamentally solve the problem of heat balance by taking chemical raw materials such as low-carbon olefin and the like as main target products, and reduces the damage to a catalyst and a regeneration system caused by the traditional fuel injection mode, so that the catalyst cost is saved, and the economic benefit of a refinery is improved. When the regeneration equipment and the method are used for the fluid catalytic cracking reaction with less coke generation, the thermal balance of the reaction-regeneration process is realized, 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.

Drawings

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

fig. 1 is a schematic diagram of an embodiment of a catalytic cracking regeneration apparatus provided herein.

Detailed Description

The present application is further described in detail below by way of the accompanying drawings and examples. The features and advantages of the present application will become more apparent from the description.

The word "exemplary" is used 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. Although various aspects of the embodiments are illustrated in the accompanying 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 collide with each other.

Any particular value disclosed herein (including the endpoints of the numerical ranges) is not limited to the precise value of the value, and is to be understood to also encompass values near the precise value, such as all possible values within the range of + -5% of the precise value. Also, for a range of values disclosed, any combination of one or more new ranges of values between the endpoints of the range, between the endpoints and the specific points within the range, and between the specific points is contemplated as being specifically disclosed herein.

In this application, both "upstream" and "downstream" are based on the direction of flow of the reaction mass. For example, when the reactant stream flows from bottom to top, "upstream" means a location below, and "downstream" means a location above.

Unless otherwise indicated, 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 the ordinary understanding in the art, then the definition herein controls.

As shown in fig. 1, the present application provides a catalyst regeneration apparatus, comprising:

coke reactor 1

Afterburner zone 14, and

the regenerator (2) is provided with a plurality of heat exchangers,

wherein the raw coke reactor 1 is provided with a spent catalyst inlet 7, an oxygen-depleted gas inlet 5 and a raw coke reactor fuel oil inlet 9; the bottom of the coking reactor 1 is also communicated with the bottom of the regenerator 2 through an external catalyst circulating pipe 8;

the afterburner zone 14 is provided with an afterburner zone fuel oil inlet 15, and the inlet of the afterburner zone 14 is in fluid communication with the outlet of the coke-generating reactor 1 such that material from the coke-generating reactor 1 can flow into the afterburner zone 14;

the regenerator 2 is provided with an oxygen-enriched gas inlet 11 and the outlet of the afterburner zone 14 is in fluid communication with the inlet of the regenerator 2 so that material from the afterburner zone 14 can flow into the regenerator 2.

In the present application, the catalytic cracking regeneration apparatus further comprises a coke formation reactor 1. The raw coke reactor 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 raw coke reactor 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 raw coke reactor 1 to heat the catalyst to be regenerated from the reactor in the afterburner 1, thereby realizing the optimal utilization of energy.

In the present application, the green coke reactor 1 is a fast fluidized bed. In one embodiment, the green coke reactor 1 is hollow cylindrical with an aspect 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-lean gas inlet 5 and a fuel oil inlet 9 which are respectively and independently arranged on the coking reactor 1 are positioned at different heights of the afterburner 1. Preferably, the coke formation reactor 1 is provided with an oxygen-depleted gas inlet 5, a connection port of an external catalyst circulation pipe 8, a spent agent inlet 7 and a fuel oil inlet 9 in sequence from bottom to top, and are all positioned at the lower part of the coke formation reactor 1 (the distance from the bottom of the coke formation reactor 1 is not more than 50% of the height of the coke formation reactor 1).

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

According to the present application, the first gas distributor 6 may be a main wind distributor known to those skilled in the art. For example, the main wind distributor may be a distributor plate and a distributor 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 coke formation reactor 1 may be selected from oxygen, air, nitrogen, steam or a mixture thereof, preferably the oxygen content in the oxygen-depleted gas is 1 to 20% by volume, and preferably the oxygen content in the oxygen-depleted gas is 5 to 10% by volume.

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

In this application, the raw coke reactor 1 may be provided with one or more, for example one, two or more fuel oil inlets 9, which may each be provided independently at the outlet end of the raw coke reactor 1 or at the bottom of the raw coke reactor 1. It is further preferred that the fuel oil inlets 9 are each independently provided upstream of the raw coke reactor 1. Further preferably, the distance of the fuel oil inlet 9 from the bottom of the coke formation reactor is each independently 20% to 50% of the coke formation reactor height. The fuel oil may include a straight distillate or a secondary processing distillate. Preferably, the secondary processing distillate oil can be selected from a mixed oil of one or more of catalytic cracking diesel oil, catalytic cracking slurry oil, coker gasoline, coker diesel oil and coker wax oil.

In the present application, the catalytic cracking regeneration apparatus further includes an afterburner zone 14, and at least one afterburner zone fuel oil inlet 15 is disposed on a sidewall of the afterburner zone 14, which may be disposed at any position of the afterburner zone 14 independently of each other. The catalyst may be further supplemented with a quantity of fuel oil by means of the afterburner fuel oil inlet 15. The fuel oil may include a straight distillate or a secondary processing distillate. Preferably, the secondary processing distillate oil can be selected from a mixed oil of one or more of catalytic cracking diesel oil, catalytic cracking slurry oil, coker gasoline, coker diesel oil and coker wax oil.

In one embodiment, the outlet of the afterburner zone 14 is provided with a catalyst flash separator 10. The catalyst rapid separator can be various types of rapid separators commonly used in industry, such as one or more of T-shaped, inverted L-shaped, inverted U-shaped and umbrella hat-shaped. The use of a rapid catalyst separator helps to change the flow direction of the catalyst, allowing countercurrent contact of the catalyst with an oxygen-containing gas, and helps to char strength and char efficiency.

In one embodiment, the raw coke reactor 1 is integrally connected with the afterburning zone 14, the raw coke reactor 1 and the afterburning zone 14 are hollow cylinders, and the aspect ratio of the raw coke reactor 1 is 30:1 to 3:1, the post-combustion zone 14 has an aspect ratio of 30:1 to 3:1, the ratio of the inner diameter of the raw coke reactor 1 to the inner diameter of the afterburner zone 14 is 10:1 to 2:1, length h of the coking reactor 1 ₁ Length h of afterburner 14 ₁₄ The ratio is 10:1 to 05:1.

in one embodiment, the raw coke reactor 1 is connected to the afterburner zone 14 by a first connection 101. In one embodiment, the longitudinal section of the first connecting section 101 is an isosceles trapezoid, and the camber angle β of the side of the isosceles trapezoid is 5 ° to 85 °.

In one embodiment, the afterburner zone 14 is housed inside the regenerator 2, along with the first connection section 101 and the catalyst flash separator 10, such that catalyst from the afterburner zone 14 directly enters the regenerator 2 for complete combustion.

In this application, the regenerator 2 may be of a conventional regenerator structure, and it is only necessary to provide an opening at the bottom thereof, and to accommodate the afterburner zone 14 together with the first connection section 101 and the catalyst flash separator 10 inside the regenerator 2 through the opening, so that the outlet of the afterburner zone 14 is in fluid communication with the inlet of the regenerator 2, and the material from the afterburner zone 14 can flow into the regenerator 2.

The lower part of the regenerator 2 is also provided with a connecting port for an external catalyst circulating pipe 8, so that a part of regenerated catalyst in the regenerator 2 can flow into the afterburner 1 to heat the spent catalyst from the reactor in the coking reactor 1, 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-enriched gas entering the regenerator has an oxygen content of 21 to 100% by volume, and more preferably the oxygen-enriched gas has an oxygen content of 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 the oxygen-enriched gas injected via the oxygen-enriched gas inlet 11 enters the regenerator 2 through the second gas distributor 12. The second gas distributor 12 may be a main wind distributor known to those skilled in the art, in accordance with the present application. For example, the main wind distributor may be a distributor plate and a distributor 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, such 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 for recycling through a regenerated flue gas line 4. In the present application, the gas-solid separation apparatus 3 may employ an apparatus well known to those skilled in the art. For example, the gas-solid separation apparatus 3 may comprise a cyclone separator.

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 coke making reactor 1 may be coaxially arranged or arranged in parallel.

The catalytic cracking device is simple in structure and easy to implement, can be implemented by adaptively reforming the existing industrial device regenerator, is high in applicability, and particularly can fundamentally solve the problem of heat balance by taking chemical raw materials such as low-carbon olefin and the like as main target products, and reduces the damage to a catalyst and a regeneration system caused by the traditional fuel injection mode, so that the catalyst cost is saved, and the economic benefit of a refinery is improved.

The regeneration equipment provided by the application is suitable for a catalytic cracking reaction-regeneration system with various raw materials and insufficient coke generation, such as the reaction of producing low-carbon olefin by catalytic cracking of petroleum hydrocarbon and oxygenated hydrocarbon, in particular to the reaction of producing low-carbon olefin by catalytic cracking of light hydrocarbon or light distillate oil.

For example, the light hydrocarbon or light distillate may be a gaseous hydrocarbon, a petroleum hydrocarbon having a distillation range of 25 to 350 ℃, an oxygenate, a biomass or waste plastic-producing oil distillate. The gaseous hydrocarbon may be selected from one or more of saturated liquefied gas, unsaturated liquefied gas, and carbon four fraction; the petroleum hydrocarbon can be selected from one or more of primary processing distillate oil, such as straight run naphtha, straight run kerosene, straight run diesel oil, and vacuum wax oil; secondary processing distillate oil, such as topped oil, raffinate oil, pentane oil, fischer-Tropsch synthetic oil, catalytic cracking gasoline, catalytic cracking diesel oil, hydrogenated gasoline, hydrogenated diesel oil, hydrogenated wax oil, coker gasoline, coker diesel oil, and a mixture of one or more coker wax oils.

In one embodiment, wherein the linear velocity of the green coke reactor is from 1.2 m/s to 2.2 m/s, the oxygen content of the oxygen-depleted gas is from 1% to 20%, and more preferably, the oxygen content of the oxygen-depleted gas is from 5% to 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 fuel oil comprises a straight run distillate or a secondary process distillate. Preferably, the secondary processing distillate oil can be selected from a blend oil of one or more of catalytic cracking diesel, coker gasoline, coker diesel, and coker wax oil.

In one embodiment, the green coke reactor has an outlet temperature of 550 to 650 ℃ and the afterburner zone has an outlet temperature of 530 to 630 ℃.

In one embodiment, the temperature within the regenerator is 600-800 ℃, preferably 650-750 ℃; the gas superficial linear velocity is 0.2 to 1.0 m/s, preferably 0.3 to 0.8 m/s, and the average residence time of the catalyst is 0.5 to 10 minutes, preferably 1 to 5 minutes.

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

In addition, the catalytic cracking system 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 reaction device comprises one or more catalytic cracking reactors. The catalyst regeneration apparatus 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 enters 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 application, the catalytic cracking reactor, the stripping device, the oil agent separation device, the reaction product separation device and the like can be all devices known to those skilled in the art, and the connection manner between the devices can also be performed according to the known manner in the art. For example, the oil separation device may comprise a cyclone separator, an outlet flash separator. In certain embodiments, the oil separation device comprises a settler arranged coaxially or in parallel with the catalytic cracking reactor.

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

Fig. 1 shows a preferred embodiment of the catalytic cracking regeneration apparatus of the present application, comprising, from bottom to top, a coke formation reactor 1 and a regenerator 2. The bottom of the coking reactor 1 is provided with an oxygen-deficient gas inlet 5 and a gas distribution plate 6. The lower side wall of the coking reactor 1 is provided with a spent catalyst inlet 7 and a connecting port of an external catalyst circulating pipe 8, and the upstream of the coking reactor 1 is provided with a coking reactor fuel oil inlet 9. The outlet of the coking reactor 1 is communicated with an afterburning zone 14, and the afterburning zone 14 is provided with an afterburning zone fuel oil inlet 15 and an outlet rapid separator 10. The regenerator bottom is provided with a main wind distributor 12 and the lower side wall is provided with one or more, e.g. one, two or more main wind inlets 11.

The oxygen-depleted gas, which may be oxygen, air, nitrogen, water vapor or a mixture thereof, enters the regeneration device from the bottom of the green coke reactor 1 via an oxygen-depleted gas inlet 5 and a gas distributor 6. The high-temperature regenerated catalyst from the external catalyst circulation pipe 8 enters the lower part of the coking reactor 1, is mixed with oxygen-deficient gas to move upwards, contacts with the spent catalyst from the spent catalyst inlet 7 and generates partial coking reaction, and the reactant flow continues to move upwards, contacts with fuel oil from the fuel oil inlet 9 of the coking reactor and generates coking reaction and partial coking reaction; the catalyst with charcoal coke flows upwards to enter the afterburning zone 14, contacts with the supplementary fuel oil injected through the fuel oil inlet 15 of the afterburning zone to generate coke deposition reaction, enters the regenerator 2 through the catalyst rapid separator 10, contacts with the oxygen-enriched gas injected through the main air inlet 11 and the main air distributor 12 to generate complete combustion reaction, thoroughly emits heat, and the regenerated catalyst is recycled to the regenerator through the pipeline 13 for reaction; the regenerated flue gas enters an energy recovery system through a pipeline 4 after the entrained catalyst is separated by a 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 a spent catalyst, the carbon content is 0.8 weight percent, and the combustion oil is catalytic cracking diesel oil.

Example 1

The structure of the regeneration device is shown in fig. 1. A fast bed reactor of a medium-sized device is used as a coking reactor, and a regenerator of the medium-sized device is used as a regenerator of the present application.

Wherein the inner diameter of the coking reactor is 0.3 meter, and the height h1 is 2 meters; the distance from the fuel oil inlet of the coking reactor to the bottom of the coking reactor is 30% of the height h1 of the coking reactor;

the internal diameter of the afterburning zone is 0.1 m, the height h ₁₄ 1 meter; the distance from the fuel oil inlet of the post-combustion zone to the bottom of the post-combustion zone is the height h of the post-combustion zone ₁₄ 60% of (C).

Introducing a nitrogen and air mixture with the oxygen content of 5% into the bottom of the coking reactor 1, sequentially mixing with the regenerated catalyst and the spent catalyst, and moving upwards to heat the spent catalyst and enable the carbon on the spent catalyst to undergo partial combustion reaction; the fuel oil atomized by the nitrogen is injected into the coking reactor 1 through a fuel oil inlet 9 of the coking reactor, contacts with the material flow in the coking reactor and generates coking reaction and a small amount of coking reaction; the catalyst with charcoal coke flows upwards to enter the afterburning zone 14, contacts with the supplementary fuel oil injected through the fuel oil inlet 15 of the afterburning zone to generate coke deposition reaction, enters the regenerator 2 through the catalyst rapid separator 10, contacts with the oxygen-enriched gas injected through the main air inlet 11 and the main air distributor 12 to generate complete combustion reaction, and thoroughly emits 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 coking reactor, and measuring the outlet temperature of the coking reactor; setting a temperature measuring point at an outlet of the afterburning zone, and measuring the outlet temperature of the afterburning zone; at the same height of 40% of the regenerator axial height from the bottom of the regenerator, two temperature measuring points (the angles of the two temperature measuring points relative to the axial direction are 180 degrees) are arranged at positions close to the wall of the regenerator, 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 coke formation reactor was 675 ℃, the temperatures at different positions in the middle of the regenerator were 687 ℃ and 685 ℃ respectively, the radial temperature difference was only 2 ℃, the upper temperature of the regenerator was 697 ℃, and the axial temperature difference was about 12 ℃ at the highest.

Comparative example 1

The comparative example used a conventional catalytic cracking regenerator. The regenerator has the same structure and dimensions as the regenerator of example 1, with a fuel oil injection port provided only in the lower dense catalyst bed zone.

The spent catalyst enters the lower part of the regenerator and contacts with air which is distributed by the main air distributor and enters the regenerator to generate a scorching reaction, fuel oil is injected into the catalyst dense bed layer, and the fuel oil contacts with high-temperature air to generate the scorching reaction and release heat. The regeneration main operating conditions and regenerator temperature profile changes are shown in table 1.

At the same height of 40% of the regenerator axial height from the bottom of the regenerator, two temperature measuring points (the angles of the two temperature measuring points relative to the axial direction are 180 degrees) are arranged at positions close to the wall of the regenerator, 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 the middle and different positions of the regenerator in the comparative example are 668 ℃ and 725 ℃ respectively, the radial temperature difference is only 57 ℃, the upper temperature of the regenerator is 737 ℃, and the axial temperature difference is large.

Table 1 comparison of the regeneration results of examples and comparative examples

	Examples	Comparative example
			Coke reactor
Inlet temperature of spent catalyst, DEG C	580	580
			Outlet temperature, DEG C	675
Fuel oil dosage in kg/hr	218	211
			Oxygen content in oxygen-depleted gas, wt%	5	/
Afterburning zone
			Fuel oil dosage in kg/hr	20	/
Outlet temperature, DEG C	670	/
			Regenerator device
The temperature of the middle part of the regenerator is 1 DEG C	688	725
			The temperature of the middle part of the regenerator is 2 DEG C	685	668
Regenerator upper temperature, DEG C	697	737

From the results of the above examples and comparative examples, it can be seen that the regeneration device of the present application is used for catalyst regeneration, the coke combustion environment in the regenerator is mild and stable, and the temperature difference between the radial and axial catalyst is small, which is helpful for maintaining the physical and chemical properties of the catalyst.

In the description of the present application, it should be noted that the directions or positional relationships indicated by the terms "upper", "lower", "inner", "outer", "front", "rear", "left", "right", etc. are based on the directions or positional relationships in the working state of the present application, are merely for convenience of description and simplification of description, and do not indicate or imply that the apparatus or element to be referred to must have a specific orientation, be configured and operated in a specific orientation, 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 explicitly specified and limited otherwise. The specific meaning of the terms in this application will be understood by those of ordinary skill in the art in a specific context.

The present application has been described in connection with the preferred embodiments, but these embodiments are merely exemplary and serve only as illustrations. On the basis of this, many alternatives and improvements can be made to the present application, which fall within the scope of protection of the present application.

Claims

1. A catalyst regeneration apparatus, characterized in that the catalyst regeneration apparatus comprises:

coke reactor

An afterburner zone, and

2. The catalyst regeneration apparatus according to claim 1, wherein the coke formation reactor is provided with the oxygen-lean gas inlet, a connection port of an external catalyst circulation pipe, a spent catalyst inlet, and a coke formation reactor fuel oil inlet in this order from bottom to top.

3. The catalyst regeneration apparatus of claim 1, wherein the raw coke reactor fuel oil inlets are each independently disposed upstream of the raw coke reactor.

4. The catalytic cracking regeneration apparatus of claim 1, wherein the distance of the coke reactor fuel oil inlet from the coke reactor bottom is each independently 20% to 50% of the coke reactor height.

5. Catalytic cracking regeneration unit according to claim 1, characterized in that the bottom of the raw coke reactor is provided with a first gas distributor such that the oxygen-depleted gas injected via the oxygen-depleted gas inlet enters the raw coke reactor through the first gas distributor.

6. The catalytic cracking regeneration apparatus of claim 1, wherein the connection port of the external catalyst circulation tube on the coke formation reactor is located at a distance of 5% to 10% of the height of the coke formation reactor from the bottom of the coke formation reactor.

7. The catalytic cracking regeneration apparatus of claim 1, wherein the green coke reactor is integrally connected to the afterburner zone, and an outlet of the afterburner zone is provided with a rapid catalyst separator.

8. The catalytic cracking regeneration apparatus of claim 1, wherein the green coke reactor is integrally connected to the afterburner zone, and an outlet of the afterburner zone is provided with a rapid catalyst separator.

9. The catalytic cracking regeneration apparatus of claim 8, wherein the green coke reactor and the afterburner zone are hollow cylindrical, and the green coke reactor has an aspect ratio of 30:1 to 3:1, the aspect ratio of the afterburner zone is 30:1 to 3:1, the ratio of the inner diameter of the coke formation reactor to the inner diameter of the afterburner zone is 10:1 to 2:1, the ratio of the length of the coke formation reactor to the length of the afterburner zone is 10:1 to 0.5:1.

10. the catalytic cracking regeneration apparatus according to claim 9, wherein the coke formation reactor and the afterburning zone are connected by a first connecting section, the longitudinal section of the first connecting section is isosceles trapezoid, and the camber angle β of the side of the isosceles trapezoid is 5-85 °.

11. The catalytic cracking regeneration apparatus of claim 9, wherein the afterburner zone is housed inside the regenerator along with the first connection section and a catalyst flash separator.

12. Catalytic cracking regeneration unit according to claim 1, characterized in that the regenerator bottom is provided with a second gas distributor such that the oxygen-enriched gas injected via the oxygen-enriched gas inlet enters the regenerator through the second gas distributor.

13. The catalytic cracking regeneration apparatus of claim 1, wherein the regenerator is in fluid communication with a gas-solid separation apparatus such that regeneration flue gas produced by the regenerator is introduced to an energy recovery system after separation by the gas-solid separation apparatus.

14. A method of regenerating a catalytic cracking catalyst, carried out in the catalytic cracking regeneration apparatus according to any one of claims 1 to 13, comprising the steps of:

15. The regeneration process according to claim 14, wherein the linear velocity of the green coke reactor is 1.2 m/s to 2.2 m/s, the oxygen content in the oxygen-depleted gas is 1% to 20%, further preferably the oxygen content in the oxygen-depleted gas is 5% to 10%.

16. The regeneration method of claim 14, wherein the atomizing medium is nitrogen gas, and the mass ratio of the atomizing medium to the combustion oil is 1:1 to 1:100.

17. the regeneration process according to claim 14, wherein the oxygen-enriched gas of the regenerator has an oxygen content of 21 to 100% by volume, further preferably the oxygen-enriched gas has an oxygen content of 21 to 85% by volume.

18. The regeneration process of claim 14, wherein the temperature within the regenerator is 600-800 ℃.

19. A catalytic cracking system comprising the catalyst regeneration apparatus of any one of claims 1-13.