A catalytic cracking regeneration device and regeneration method suitable for maintaining heat balance

Abstract

The present application relates to a catalytic cracking regeneration device and a regeneration method suitable for maintaining thermal balance, the catalytic cracking regeneration device comprises an afterburner and a regenerator, the outlet of the afterburner is fluidly connected to the inlet of the regenerator, so that the material from the afterburner can flow into the regenerator; wherein the afterburner is provided with an inlet for catalyst to be generated, an oxygen-depleted gas inlet and a fuel oil inlet; the regenerator is provided with an oxygen-rich gas inlet; the bottom of the afterburner is connected to the bottom of the regenerator through an external catalyst circulation pipe. When the regeneration device and method of the present application are used for a fluidized catalytic cracking reaction with little coking, not only the thermal balance of the reaction-regeneration process is achieved, but also the catalyst temperature rises evenly during the coking process of the regenerator, without local hot spots, and without damage to the physical and chemical properties of the catalyst.

Description

Technical Field

[0001] The present application relates to the technical field of fluidized catalytic cracking, and more specifically, to a catalytic cracking regeneration device and a regeneration method suitable for maintaining thermal balance. Background Art

[0002] The fluidized catalytic cracking reaction process is a self-heating equilibrium process. The catalyst burning regeneration process releases a large amount of high-temperature heat energy, which can just meet the needs of the lower temperature cracking reaction process. The catalyst circulating between the reactor and the regenerator has a sufficient amount and heat capacity, so the catalyst can be used 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 obtaining heat from one end and supplying heat to the other end. The establishment of heat balance requires certain conditions, on which basis can the cracking and regeneration be maintained at the specified temperature. For a catalytic cracking industrial unit, the basis of the heat balance between the reactor and the regenerator is that the reaction can generate enough coke, which burns during the regeneration process and releases heat for the reaction.

[0003] With the development of oil refining technology, especially the intensification of the heavy / inferior trend of crude oil and the improvement of oil product quality, the hydrogenation process has been more widely used. When the raw materials upgraded by hydrogenation are used as catalytic cracking raw materials, although the product structure and quality have been greatly improved, the catalytic cracking unit itself has insufficient coke production, resulting in insufficient heat supply. In addition, in the catalytic cracking technology with light olefins as the main target product, the cracking reaction conversion rate is high, the reaction temperature is high, and the reaction heat is large. The heat required for the reaction is more than that of the conventional fluidized catalytic regenerator or other catalytic conversion methods. The coke generated by self-cracking often cannot meet the needs of the reaction-regeneration system's own heat balance. When the coke is insufficient during the reaction process, the method of supplementing the regenerator with fuel oil is usually adopted to provide the required heat for the reaction. However, since catalytic cracking uses a catalyst with molecular sieve as the active component, the local high temperature generated by the combustion of fuel oil in the regenerator causes the molecular sieve framework aluminum to gradually escape, resulting in damage to the catalyst, and this damage is irreversible. The prior art does not fundamentally solve the influence of the high-temperature hot spots generated by the local combustion of external supplementary fuel oil on the catalyst skeleton structure and reaction performance. Summary of the invention

[0004] The purpose of the present application is to provide a catalytic cracking regeneration device and method suitable for maintaining thermal balance, solving the problem of thermal balance in the catalytic cracking reaction process without affecting the physical and chemical properties of the catalyst.

[0005] The present application relates to a catalytic cracking regeneration device suitable for maintaining heat balance, characterized in that the catalytic cracking regeneration device comprises an afterburner and a regenerator, the outlet of the afterburner is fluidly connected to the inlet of the regenerator, so that the material from the afterburner can flow into the regenerator;

[0006] Wherein, the afterburner is provided with an inlet for the catalyst to be generated, an inlet for the oxygen-depleted gas and an inlet for the fuel oil;

[0007] The regenerator is provided with an oxygen-rich gas inlet;

[0008] The bottom of the afterburner is connected to the bottom of the regenerator through an external catalyst circulation pipe.

[0009] In one embodiment, the afterburner is provided with the oxygen-depleted gas inlet, the connection port of the external catalyst circulation pipe, the catalyst inlet to be generated and the fuel oil inlet in sequence from bottom to top.

[0010] In one embodiment, the distance between the connection port of the external catalyst circulation pipe on the afterburner and the bottom of the afterburner is 5% to 10% of the height of the afterburner.

[0011] In one embodiment, the fuel oil inlets are each independently arranged in the middle and upstream of the afterburner.

[0012] In one embodiment, the distance between the fuel oil inlet and the bottom of the afterburner is independently 20% to 50% of the height of the afterburner.

[0013] In one embodiment, a first gas distributor is disposed at the bottom of the afterburner, so that the oxygen-depleted gas injected through the oxygen-depleted gas inlet enters the afterburner through the first gas distributor.

[0014] In one embodiment, the afterburner outlet is provided with a catalyst distribution plate.

[0015] In one embodiment, the afterburner is in the shape of a hollow cylinder with a length-to-diameter ratio of 30:1 to 3:1.

[0016] In one embodiment, a second gas distributor is disposed at the bottom of the regenerator, so that the oxygen-rich gas injected through the oxygen-rich gas inlet enters the regenerator through the second gas distributor.

[0017] In one embodiment, the regenerator is fluidically connected to the gas-solid separation device, so that the regeneration flue gas generated by the regenerator is separated by the gas-solid separation device and then introduced into the energy recovery system.

[0018] The present application also provides a method for regenerating a catalytic cracking catalyst, which is carried out in a catalytic cracking regeneration device of the present application and comprises the following steps:

[0019] Injecting oxygen-depleted gas into the afterburner through the oxygen-depleted gas inlet, contacting the regenerated catalyst from the regenerator and the catalyst to be regenerated from the reactor, so that the catalyst to be regenerated is heated and partially burnt;

[0020] Injecting a mixture of atomizing medium and combustion oil into the afterburner through the fuel oil inlet, so that the mixture of atomizing medium and combustion oil contacts the catalyst in the afterburner, causing a coking reaction and a partial coking reaction to occur, thereby obtaining a catalyst with a portion of coke;

[0021] The catalyst with a portion of coke is allowed to enter the regenerator, and is contacted with the oxygen-rich gas injected into the regenerator through the oxygen-rich gas inlet, so that a complete combustion reaction occurs to obtain a regenerated catalyst.

[0022] In one embodiment, the linear speed of the afterburner is 1.2 m / s-2.2 m / s, and the oxygen content in the oxygen-depleted gas is 1% to 20%. More preferably, the oxygen content in the oxygen-depleted gas is 5% to 10%.

[0023] 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.

[0024] In one embodiment, the outlet temperature of the afterburner is 550-650°C.

[0025] In one embodiment, the oxygen content in the oxygen-rich gas of the regenerator is 21 volume % to 100 volume %, and more preferably, the oxygen content in the oxygen-rich gas is 21 volume % to 85 volume %.

[0026] In one embodiment, the temperature in the regenerator is 600-800°C.

[0027] The present application also provides a catalytic cracking system, which includes the catalyst regeneration device of the present application.

[0028] The regeneration equipment of the present application has a simple structure and is easy to implement. It can be implemented by adaptively modifying the regenerator of an existing industrial device. It has strong applicability, especially for catalytic cracking devices with chemical raw materials such as low-carbon olefins as the main target products. It can not only fundamentally solve the problem of heat balance, but also reduce the damage to the catalyst and the regeneration system caused by the traditional method of spraying combustion oil, which not only saves catalyst costs but also improves the economic benefits of the refinery. When the regeneration equipment and method of the present application are used for fluidized catalytic cracking reactions with little coking, it not only achieves the heat balance of the reaction-regeneration process, but also makes the catalyst temperature rise uniform during the coking process of the regenerator, without local hot spots, and does not damage the physical and chemical properties of the catalyst. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] The accompanying drawings are used to provide a further understanding of the present application and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present application but do not constitute a limitation to the present application. In the accompanying drawings:

[0030] Figure 1 A schematic diagram of an implementation scheme of a catalytic cracking regeneration device provided in the present application. DETAILED DESCRIPTION

[0031] The present application is further described in detail below through the accompanying drawings and embodiments. Through these descriptions, the characteristics and advantages of the present application will become clearer and more specific.

[0032] 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. Although various aspects of the embodiments are shown in the drawings, the drawings are not necessarily drawn to scale unless otherwise noted.

[0033] In addition, the technical features involved in different embodiments of the present application described below can be combined with each other as long as they do not conflict with each other.

[0034] Any specific numerical value disclosed herein (including the endpoint of the numerical range) is not limited to the exact value of the numerical value, but should be understood to also cover values ​​close to the exact value, such as all possible numerical values ​​within the range of ±5% of the exact value. In addition, for the disclosed numerical range, the endpoint values ​​of the range, the endpoint values ​​and the specific point values ​​in the range, and the specific point values ​​can be arbitrarily combined to obtain one or more new numerical ranges, and these new numerical ranges should also be regarded as specifically disclosed herein.

[0035] In the present application, the terms "upstream" and "downstream" are based on the flow direction of the reactants. For example, when the reactants flow from bottom to top, "upstream" means the position below, while "downstream" means the position above.

[0036] Unless otherwise specified, the terms used herein have the same meaning as commonly understood by those skilled in the art. If a term is defined herein and its definition is different from the commonly understood meaning in the art, the definition herein shall prevail.

[0037] like Figure 1 As shown, the present application provides a catalytic cracking regeneration device suitable for maintaining thermal balance, which includes a post-burner 1 and a regenerator 2, wherein the outlet of the post-burner 1 is fluidly connected to the inlet of the regenerator 2, so that the material from the post-burner 1 can flow into the regenerator 2.

[0038] In the present application, the catalytic cracking regeneration equipment also includes an afterburner 1. The afterburner 1 is provided with a catalyst inlet 7 to be regenerated, an oxygen-depleted gas inlet 5 and a fuel oil inlet 9. The bottom of the afterburner 1 is connected to the bottom of the regenerator 2 through an external catalyst circulation pipe 8, so that a part of the high-temperature regenerated catalyst in the regenerator 2 can flow into the afterburner 1 for heating the catalyst to be regenerated from the reactor in the afterburner 1, so as to achieve optimal utilization of energy.

[0039] In the present application, the afterburner 1 is a fast fluidized bed. In one embodiment, the afterburner 1 is a hollow cylinder with a length-to-diameter ratio of 30:1 to 3:1.

[0040] In the present application, the catalyst inlet 7 to be regenerated, the connection port of the external catalyst circulation pipe 8, the oxygen-depleted gas inlet 5 and the fuel oil inlet 9, which are independently arranged on the afterburner 1, are located at different heights of the afterburner 1. Preferably, the afterburner 1 is provided with an oxygen-depleted gas inlet 5, a connection port of the external catalyst circulation pipe 8, a catalyst inlet 7 to be regenerated and a fuel oil inlet 9 in sequence from bottom to top, and they are all located at the lower part of the afterburner 1 (the distance from the bottom of the afterburner 1 is not greater than 50% of the height of the afterburner 1).

[0041] In the present application, one or more oxygen-depleted gas inlets 5 are provided at the lower part of the afterburner 1. In one embodiment, the oxygen-depleted gas inlet 5 is located at the bottom of the afterburner 1. Preferably, a first gas distributor 6 is provided at the bottom of the afterburner, so that the oxygen-depleted gas injected through the oxygen-depleted gas inlet 5 enters the afterburner 1 through the first gas distributor 6.

[0042] According to the present application, the first gas distributor 6 can be a main air distributor known to those skilled in the art. For example, the main air distributor can be a distribution plate and a distribution pipe. Preferably, the distribution pipe is an annular distribution pipe and a dendrite distribution pipe.

[0043] According to the present application, the oxygen-depleted gas injected into the afterburner can be selected from oxygen, air, nitrogen, water vapor or a mixture thereof. Preferably, the oxygen content in the oxygen-depleted gas is 1 volume %-20 volume %, preferably, the oxygen content in the oxygen-depleted gas is 5 volume % to 10 volume %.

[0044] 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% of the height of the afterburner.

[0045] In the present application, the afterburner may be provided with one or more, for example, one, two or more fuel oil inlets 9, and the one or more fuel oil inlets may be independently arranged at the outlet end of the afterburner, or at the bottom of the afterburner. Further preferably, the fuel oil inlets 9 are independently arranged in the middle and upstream of the afterburner 1. Further preferably, the distance between the fuel oil inlet 9 and the bottom of the afterburner is independently 20% to 50% of the height of the afterburner. The fuel oil may include straight run distillate or secondary processed distillate. Preferably, the secondary processed distillate may be selected from a mixed oil of one or more of catalytic cracking diesel, catalytic cracking slurry, coker gasoline, coker diesel and coker wax oil.

[0046] In the present application, a catalyst distribution plate 10 may be provided at the position where the catalyst enters the bottom of the regenerator, for example, at the outlet end of the afterburner 1 .

[0047] According to the present application, the catalyst distribution plate 10 can be any type of distribution plate commonly used in the industry, such as one or more of a flat plate, an arch, a dish, an annular shape, and an umbrella shape. The use of a catalyst distribution plate helps to make the catalyst in the axial direction of the regenerator uniformly contact with the oxygen-rich gas for a charring reaction, thereby improving the charring efficiency and reducing the occurrence of local hot spots in the catalyst bed.

[0048] By setting up the afterburner 1, the injected fuel oil is mixed with the catalyst to form coke under low temperature and oxygen-deficient fluidized conditions. The catalyst with coke attached is back-mixed in the afterburner 1 with fast fluidized bed characteristics, so that the coke is evenly distributed on the catalyst and partially burned, thereby achieving a step-by-step increase in the catalyst surface temperature.

[0049] In the present application, the regenerator 2 can adopt the existing commonly used regenerator structure. It only needs to set an opening at its bottom and connect the outlet of the afterburner 1 to the opening, that is, the outlet of the afterburner 1 can be fluidly connected to the inlet of the regenerator 2, so that the material from the afterburner 1 can flow into the regenerator 2.

[0050] A connection port for an external catalyst circulation pipe 8 is also provided at the lower portion of the regenerator 2, so that a portion of the regenerated catalyst in the regenerator 2 can flow into the afterburner 1 for heating the catalyst to be regenerated from the reactor in the afterburner 1, thereby optimizing energy utilization.

[0051] The regenerator 2 is provided with an oxygen-rich gas inlet 11 for injecting oxygen-rich gas into the regenerator for regeneration of the catalyst entering the regenerator 2. In one embodiment, the oxygen content in the oxygen-rich gas entering the regenerator is 21 volume % to 100 volume %, and more preferably, the oxygen content in the oxygen-rich gas is 21 volume % to 85 volume %. In the present application, the oxygen-rich gas injected into the regenerator can be air.

[0052] In one embodiment, a second gas distributor 12 is provided at the bottom of the regenerator, so that the oxygen-enriched gas injected through the oxygen-enriched gas inlet 11 enters the regenerator 2 through the second gas distributor 12. According to the present application, the second gas distributor 12 can adopt a main air distributor well known to those skilled in the art. For example, the main air distributor can be a distribution plate and a distribution pipe. Preferably, the distribution pipe is an annular distribution pipe and a dendrite distribution pipe.

[0053] In one embodiment, the regenerator 2 is fluidically connected to the gas-solid separation device 3, so that the regeneration flue gas generated by the regenerator 2 is separated by the gas-solid separation device 3 and then introduced into the energy recovery system through the regeneration flue gas pipeline 4 for recycling. In the present application, the gas-solid separation device 3 can be a device well known to those skilled in the art. For example, the gas-solid separation device 3 can include a cyclone separator.

[0054] 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 use in a reaction cycle.

[0055] In the present application, the regenerator 2 and the afterburner 1 can be arranged coaxially or in parallel at different heights.

[0056] In the present application, after the catalyst with part of the coke burned off enters the regenerator, it is fully burned and released heat under the action of high temperature and oxygen-rich gas to supply the heat required for the reaction. The equipment of the present application can make the burning environment on the catalyst moderate, achieve gradual temperature rise on the catalyst, and protect the physical and chemical properties of the catalyst to the greatest extent.

[0057] The present application has a simple structure and is easy to implement. It can be implemented by adaptively modifying the regenerator of an existing industrial device and has strong applicability, especially for catalytic cracking devices with chemical raw materials such as low-carbon olefins as the main target products. It can not only fundamentally solve the problem of heat balance, but also reduce the damage to the catalyst and the regeneration system caused by the traditional method of spraying combustion oil, thereby saving catalyst costs and improving the economic benefits of the refinery.

[0058] The present application also provides a method for regenerating a catalytic cracking catalyst, which is carried out in a catalytic cracking regeneration device of the present application and comprises the following steps:

[0059] Injecting oxygen-depleted gas into the afterburner through the oxygen-depleted gas inlet, contacting the regenerated catalyst from the regenerator and the catalyst to be regenerated from the reactor, so that the catalyst to be regenerated is heated and partially burnt;

[0060] Injecting a mixture of atomizing medium and combustion oil into the afterburner through the fuel oil inlet, so that the mixture of atomizing medium and combustion oil contacts the catalyst in the afterburner, causing a coking reaction and a partial coking reaction to occur, thereby obtaining a catalyst with a portion of coke;

[0061] The catalyst with a portion of coke is allowed to enter the regenerator, and is contacted with the oxygen-rich gas injected into the regenerator through the oxygen-rich gas inlet, so that a complete combustion reaction occurs to obtain a regenerated catalyst.

[0062] In one embodiment, the linear speed of the afterburner is 1.2 m / s-2.2 m / s, and the oxygen content in the oxygen-depleted gas is 1% to 20%. More preferably, the oxygen content in the oxygen-depleted gas is 5% to 10%.

[0063] 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 processed distillate. Preferably, the secondary processed distillate can be selected from a mixed oil of one or more of catalytic cracking diesel, coker gasoline, coker diesel and coker gas oil.

[0064] In one embodiment, the outlet temperature of the afterburner is 550-650°C.

[0065] In one embodiment, the oxygen content in the oxygen-rich gas of the regenerator is 21 volume % to 100 volume %, and more preferably, the oxygen content in the oxygen-rich gas is 21 volume % to 85 volume %.

[0066] In one embodiment, the temperature in the regenerator is 600-800°C, preferably 650-750°C; the gas superficial velocity is 0.2-1.0 m / s, preferably 0.3-0.8 m / s, and the average residence time of the catalyst is 0.5-10 minutes, preferably 1-5 minutes.

[0067] The catalytic cracking regeneration equipment of the present application is applicable to catalytic cracking reaction-regeneration systems with various raw materials and insufficient coke generation, such as catalytic cracking of petroleum hydrocarbons and oxygen-containing hydrocarbons to produce light olefins, especially catalytic cracking of light hydrocarbons or light distillate oil to produce light olefins.

[0068] For example, the light hydrocarbons or light distillate oils can be gaseous hydrocarbons, petroleum hydrocarbons with a distillation range of 25 to 350° C., oxygen-containing compounds, distillate oils generated from biomass or waste plastics; the gaseous hydrocarbons can be selected from a mixture of one or more of saturated liquefied gas, unsaturated liquefied gas and C4 fractions; the petroleum hydrocarbons can be selected from a mixture of one or more of primary processed straight-run naphtha, straight-run kerosene, and straight-run diesel; a mixed oil of one or more of secondary processed topped oil, raffinate oil, C4 fraction, hydrocracking light naphtha, pentane oil, coker gasoline, Fischer-Tropsch synthetic oil, fluidized catalytic cracking light gasoline, hydrogenated gasoline, and hydrogenated diesel.

[0069] The present application also provides a catalytic cracking system, which includes the catalyst regeneration device of the present application.

[0070] In addition, the catalytic cracking system further comprises a catalytic cracking reaction device, an oil agent separation device, a steam stripping device and an optional reaction product separation device.

[0071] In one embodiment, the catalytic cracking reaction device includes one or more catalytic cracking reactors. The catalyst regeneration device of the present application can be connected to the one or more catalytic cracking reactors, so that the catalyst to be regenerated from the one or more catalytic cracking reactors enters the catalyst regeneration device of the present application for regeneration, and the regenerated catalyst is circulated back to the one or more catalytic cracking reactors for reuse.

[0072] In the catalytic cracking system provided in the present application, the catalytic cracking reactor, the stripping device, the oil agent separation device, the reaction product separation device, etc. can all be devices well known to those skilled in the art, and the connection between these devices can also be carried out in a manner known in the art. For example, the oil agent separation device may include a cyclone separator and an outlet rapid separator. In some specific embodiments, the oil agent separation device includes a settler arranged coaxially with the catalytic cracking reactor or arranged in parallel at a high and low level.

[0073] The present application will be further described below with reference to the preferred implementation modes shown in the accompanying drawings, but the present application is not limited thereby.

[0074] Figure 1 A preferred embodiment of the catalytic cracking regeneration device of the present application is given, wherein the catalytic cracking regeneration device comprises an afterburner 1 and a regenerator 2 from bottom to top. An oxygen-depleted inlet 5 and a gas distribution plate 6 are provided at the bottom of the afterburner 1. A connection port for a catalyst inlet 7 to be generated and an external catalyst circulation pipe 8 is provided on the lower side wall of the afterburner 1, and a fuel oil inlet 9 is provided in the middle and upper reaches of the afterburner 1. A main air distributor 12 is provided at the bottom of the regenerator, and one or more, for example, one, two or more main air inlets 11 are provided on the lower side wall.

[0075] Oxygen-depleted gas enters the afterburner 1 from the bottom of the afterburner 1 through the oxygen-depleted inlet 5. The oxygen-depleted gas can be oxygen, air, nitrogen, water vapor or a mixture thereof. The high-temperature regenerated catalyst from the external catalyst circulation pipe 8 enters the lower part of the afterburner 1, mixes with the oxygen-depleted gas and moves upward, contacts the catalyst to be regenerated from the catalyst to be regenerated inlet 7 and undergoes a partial charring reaction, and the reaction flow continues to move upward, contacts the supplementary fuel oil from the fuel oil inlet 9 and undergoes a coking reaction and a partial charring reaction; the catalyst with char and coke flows upward, enters the regenerator 2 through the catalyst distributor 10, contacts the oxygen-rich gas injected through the oxygen-rich gas inlet 11 and the main air distributor 12 and undergoes a complete combustion reaction, completely releasing heat, and the regenerated catalyst is sent out of the regenerator through the regenerated catalyst outlet 13 for use in the reaction cycle; the regenerated flue gas separates the entrained catalyst through the cyclone separator 3 and enters the energy recovery system through the pipeline 4.

[0076] Example

[0077] The following examples will further illustrate the present application, but are not intended to limit the present application. The catalyst used in the test is a spent catalyst with a carbon content of 0.8% by weight, and the combustion oil is catalytic cracking diesel.

[0078] Example 1

[0079] The regenerator structure is as follows Figure 1 The regenerator structure is shown in Figure 1 As shown. The medium-sized unit fast bed reactor is used as the afterburner, and the medium-sized unit regenerator is used as the regenerator.

[0080] The inner diameter of the afterburner is 0.3 meters and the height is 2 meters. The distance between the fuel oil inlet 9 of the afterburner and the bottom of the afterburner is 30% of the height of the afterburner. The outlet of the afterburner is directly connected to the bottom opening of the regenerator, and a catalyst distributor is arranged at the outlet.

[0081] A nitrogen and air mixture with an oxygen content of 5% is introduced into the bottom of the afterburner 1, and is mixed with the regenerated catalyst and the catalyst to be regenerated in turn and moves upward, so that the catalyst to be regenerated is heated and the carbon on the catalyst to be regenerated undergoes a partial combustion reaction; the fuel oil atomized by nitrogen is injected into the afterburner, and contacts with the flow in the afterburner to produce a coke reaction and a small amount of a charring reaction; the catalyst with coke enters the regenerator, contacts with the air to produce a complete fuel reaction, and releases heat. The main regeneration operating conditions and the temperature distribution changes of the regenerator are shown in Table 1.

[0082] A temperature measuring point is set at the outlet of the afterburner to measure the outlet temperature of the afterburner; two temperature measuring points are set close to the regenerator wall at the same height of 40% of the axial height of the regenerator from the bottom axially (the angles of the two relative to the axial direction are 180 degrees), and the middle temperatures at different positions at the same height are measured; a temperature measuring point is set at the top of the regenerator to measure the upper temperature of the regenerator.

[0083] It can be seen from Table 1 that in this embodiment, the afterburner outlet temperature is 675°C, the temperatures at different positions in the middle of the regenerator are 687°C and 681°C respectively, with a radial temperature difference of only 6°C, the upper temperature of the regenerator is 695°C, and the axial temperature difference is about 10°C.

[0084] Comparative Example 1

[0085] The comparative example uses a conventional catalytic cracking regenerator, which has the same structure and size as the regenerator of Example 1, except that a fuel oil injection port is provided in the lower catalyst dense phase bed area.

[0086] The catalyst to be regenerated enters the lower part of the regenerator and contacts the air distributed by the main air distributor to cause a scorching reaction. Fuel oil is injected into the catalyst dense phase bed. The fuel oil contacts the high-temperature air and causes a scorching reaction, releasing heat. The main operating conditions of regeneration and the temperature distribution changes of the regenerator are shown in Table 1.

[0087] At the same height of the regenerator, which is 40% of the axial height of the regenerator from the bottom, two temperature measuring points are set close to the regenerator wall (the angles of the two relative to the axial direction are 180 degrees), and the middle temperatures at different positions at the same height are measured; a temperature measuring point is set at the top of the regenerator to measure the upper temperature of the regenerator.

[0088] It can be seen from Table 1 that the temperatures at different positions in the middle of the regenerator in the comparative example are 668°C and 725°C respectively, with a radial temperature difference of only 57°C. The temperature at the top of the regenerator is 737°C, with a large axial temperature difference.

[0089] It can be seen from the results of the above embodiments and comparative examples that when the regeneration equipment of the present application is used for catalyst regeneration, the coke combustion environment in the regenerator is moderate and stable, and the radial and axial catalyst temperatures are helpful to maintain the physical and chemical properties of the catalyst.

[0090] In the description of the present application, it should be noted that the terms "upper", "lower", "inside", "outside", "front", "back", "left", "right", etc. indicate directions or positional relationships based on the directions or positional relationships in the working state of the present application. They are only for the convenience of describing the present application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific direction, be constructed and operated in a specific direction. Therefore, they should not be understood as limitations on the present application.

[0091] In the description of this application, it should be noted that, unless otherwise clearly specified and limited, the terms "install", "connect" and "connect" should be understood in a broad sense. For ordinary technicians in this field, the specific meanings of the above terms in this application can be understood according to specific circumstances.

[0092] The present application has been described above in conjunction with preferred embodiments, but these embodiments are only exemplary and serve only as an illustration. On this basis, various replacements and improvements may be made to the present application, all of which fall within the scope of protection of the present application.

[0093] Table 1 Comparison of regeneration results of the embodiment and the comparative example

[0094] Example Comparative Example Afterburner Catalyst inlet temperature 580 580 Outlet temperature 675 Fuel oil consumption, kg / h 218 211 Oxygen content in oxygen-depleted gas, weight % 5 / Regenerator Regenerator middle temperature 1, ℃ 687 725 Regenerator middle temperature 2, ℃ 681 668 Regenerator upper temperature, ℃ 695 737

Claims

1. A catalytic cracking regeneration device suitable for maintaining thermal balance, It is characterized in that The catalytic cracking regeneration device comprises an afterburner and a regenerator, wherein the outlet of the afterburner is fluidly connected to the inlet of the regenerator so that the material from the afterburner can flow into the regenerator; Wherein, the afterburner is provided with an inlet for the catalyst to be generated, an inlet for the oxygen-depleted gas and an inlet for the fuel oil; The regenerator is provided with an oxygen-rich gas inlet; The bottom of the afterburner is connected to the bottom of the regenerator through an external catalyst circulation pipe; The regenerator and the afterburner are arranged coaxially; an opening is provided at the bottom of the regenerator, and the outlet of the afterburner is connected to the opening; The distance between the fuel oil inlet and the bottom of the afterburner is independently 20% to 50% of the height of the afterburner.

2. The catalytic cracking regeneration equipment according to claim 1, It is characterized in that The afterburner is provided with the oxygen-depleted gas inlet, the connection port of the external catalyst circulation pipe, the catalyst inlet to be generated and the fuel oil inlet in sequence from bottom to top.

3. The catalytic cracking regeneration equipment according to claim 2, It is characterized in that The distance between the connection port of the external catalyst circulation pipe on the afterburner and the bottom of the afterburner is 5% to 10% of the height of the afterburner.

4. The catalytic cracking regeneration equipment according to claim 1, It is characterized in that A first gas distributor is disposed at the bottom of the afterburner, so that the oxygen-depleted gas injected through the oxygen-depleted gas inlet enters the afterburner through the first gas distributor.

5. The catalytic cracking regeneration equipment according to claim 1, It is characterized in that The outlet of the afterburner is provided with a catalyst distribution plate.

6. The catalytic cracking regeneration equipment according to claim 1, It is characterized in that The afterburner is in a hollow cylindrical shape, and its length-to-diameter ratio is 30:1 to 3:

1.

7. The catalytic cracking regeneration equipment according to claim 1, It is characterized in that A second gas distributor is disposed at the bottom of the regenerator, so that the oxygen-rich gas injected through the oxygen-rich gas inlet enters the regenerator through the second gas distributor.

8. The catalytic cracking regeneration equipment according to claim 1, It is characterized in that The regenerator is fluidly connected to the gas-solid separation device, so that the regenerated flue gas generated by the regenerator is separated by the gas-solid separation device and then introduced into the energy recovery system.

9. A method for regenerating a catalytic cracking catalyst, carried out in the catalytic cracking regeneration equipment according to any one of claims 1 to 8, comprising the following steps: Injecting oxygen-depleted gas into the afterburner through the oxygen-depleted gas inlet, contacting the regenerated catalyst from the regenerator and the catalyst to be regenerated from the reactor, so that the catalyst to be regenerated is heated and partially burnt; Injecting a mixture of atomizing medium and combustion oil into the afterburner through the fuel oil inlet, so that the mixture of atomizing medium and combustion oil contacts the catalyst in the afterburner, causing a coking reaction and a partial coking reaction to occur, thereby obtaining a catalyst with a portion of coke; The catalyst with a portion of coke is allowed to enter the regenerator, and is contacted with the oxygen-rich gas injected into the regenerator through the oxygen-rich gas inlet, so that a complete combustion reaction occurs to obtain a regenerated catalyst.

10. The regeneration method according to claim 9, in, The linear speed of the afterburner is 1.2 m / s-2.2 m / s, and the oxygen content in the oxygen-depleted gas is 1 volume % to 20 volume %.

11. The regeneration method according to claim 10, in, The oxygen content in the oxygen-depleted gas is 5 volume % to 10 volume %.

12. The regeneration method according to claim 9, in, The atomizing medium is nitrogen, and the mass ratio of the atomizing medium to the combustion oil is 1:1 to 1:

100.

13. The regeneration method according to claim 9, in, The outlet temperature of the afterburner is 550-650°C.

14. The regeneration method according to claim 9, in, The oxygen content of the oxygen-rich gas in the regenerator is 21 volume % to 100 volume %.

15. The regeneration method according to claim 14, in, The oxygen content of the oxygen-rich gas is 21 volume % to 85 volume %.

16. The regeneration method according to claim 9, in, The temperature in the regenerator is 600-800°C.

17. A catalytic cracking system comprising the catalyst regeneration device according to any one of claims 1 to 8.

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