Method and system for catalytic cracking catalyst regeneration using gaseous bio-based fuels

Abstract

A catalyst regeneration method applicable to a fluid catalytic cracker is disclosed. The fluid catalytic cracker includes a catalytic cracking reactor and a catalyst regenerator. The regeneration method includes: 1) supplying a biomass-derived gaseous fuel containing hydrogen and / or methane; 2) supplying the gaseous fuel directly to a catalyst regenerator without separation and purification; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen content of the oxygen-containing gas being 14% by volume to 28% by volume; and 4) supplying a spent catalyst from a catalytic cracking reactor to a catalyst regenerator, contacting the spent catalyst therein with the gaseous fuel and the oxygen-containing gas, and carrying out coke combustion regeneration. According to the method of the present application, the biomass-derived gaseous fuel for energy supply is introduced into the catalyst regeneration process to replace fossil fuel, thereby fundamentally changing the energy source of the catalytic cracker, greatly reducing the carbon emission of the catalytic cracking unit, realizing the recycling of carbon elements, and supplying energy to other process equipment.

Description

[Technical field]

[0001] This application relates to the regeneration of coke-containing catalytic cracking catalysts, and more particularly to a method and system for catalytic cracking catalyst regeneration using gaseous bio-based fuels. [Background technology]

[0002] Today, the development of the global oil refining industry faces many challenges, such as the replacement of new energy, as well as the strengthening requirements for energy conservation and emission reduction. Flexible adjustment of production plans, reduction of carbon dioxide emissions, and mitigation of climate change have become the only way for the oil refining industry to transform its economic growth model and maintain sustainable development. It is urgent to achieve carbon peak in 2030 and carbon neutrality in 2060. The 14th Five-Year Plan has formulated a carbon peak action plan, which clearly calls for accelerating the promotion of green development. China's national carbon emissions trading market was also officially launched in 2021. Therefore, it is particularly important to effectively reduce carbon emissions in the process of oil refining and chemical production. Research on low-carbon catalytic cracking schemes to reduce oil and increase chemical production is an important task for refineries in the future. Carbon emissions in the heavy oil processing process are mainly exhaust gases emitted from equipment such as catalytic cracking coke combustion, hydrogen production process and boilers, as well as energy consumption in the process. Among them, the catalytic cracking unit is the core equipment of the refinery. Carbon emissions from coke combustion in the catalytic cracking regenerator account for 24%-55% of the plant's total carbon emissions and nearly 1% of the national carbon dioxide emissions. This is the focus of carbon emission reduction in the petrochemical industry.

[0003] CN102698817A discloses a catalytic cracking catalyst regeneration method, which adopts pure oxygen regeneration, combines a steam shift reaction zone after the exhaust gas energy recovery system, uses the CO in the exhaust gas as the raw material for the steam shift reaction, produces hydrogen, and further recycles and recovers the carbon in the exhaust gas. However, this method only focuses on the treatment and recovery of the exhaust gas, and the energy utilization rate is reduced by the incomplete regeneration exhaust gas. It also involves the separation and purification of the raw material and the product in the steam shift reaction zone, which is costly; the energy source of the regenerative energy supply remains unchanged.

[0004] CN113877397A discloses an incomplete regeneration process for reducing carbon dioxide emissions. This process uses pure oxygen to incompletely regenerate the catalyst. In the resulting flue gas, carbon monoxide is used as a chemical raw material, and carbon dioxide is used for storage or oil recovery, thereby reducing carbon dioxide emissions. However, this process mainly involves a post-treatment process of the flue gas, which is costly. This process involves separation of carbon monoxide, carbon dioxide, oxygen, and other gases, and the separation process is also complicated. The incomplete regeneration cannot make full use of the chemical energy of the deposited coke, and the storage of concentrated carbon dioxide causes resource waste.

[0005] US5565089 discloses a catalytic cracking catalyst regeneration process, which first uses air to burn coke, then recovers and recycles the carbon dioxide in the exhaust gas, gradually merges it with an oxygen-containing gas stream until the temperature in the regenerator becomes steady, and finally injects only oxygen and carbon dioxide to regenerate the catalyst. This process focuses on the gas intake system and exhaust gas treatment of the regeneration process, but the carbon dioxide generated by the energy supply is still all derived from fossil energy.

[0006] The energy of the catalytic cracking unit comes from the coke combustion of the catalyst. The higher the gas yield, the higher the production of low-carbon olefins and other chemicals, so more reaction heat is required. When the amount of coke combustion is not enough to meet the energy consumption of the unit, the coke production is usually increased by recycling oil slurry, increasing the proportion of heavy oil in the feed oil to increase the regeneration temperature, or injecting fuel oil for combustion to increase the regeneration temperature. Although all of these three methods can meet the heat balance of the reaction, they all have a certain impact on the operation of the unit. In addition, the auxiliary energy is all derived from fossil energy sources, so it increases the carbon dioxide emissions derived from fossil energy sources and does not contribute to improving the utilization rate of oil resources. By optimizing the regeneration process, the energy utilization efficiency can be improved, thereby reducing the carbon dioxide emissions of the unit to a certain extent; by recycling and recovering the emitted carbon dioxide, carbon dioxide emissions can also be reduced to a certain extent, but the cost is high and the process is relatively complicated. However, the above ideas do not fundamentally change the energy source, and carbon dioxide still comes from fossil energy sources.

[0007] Therefore, it is necessary to develop a catalyst regeneration method that can fundamentally reduce carbon dioxide emissions from fossil energy sources, meet the energy supply requirements of the device while reducing carbon dioxide emissions, and realize low-carbon development. Summary of the Invention

[0008] The objective of the present application is to provide a method and system for catalyst regeneration suitable for a fluid catalytic cracking unit, which introduces biomass-derived gaseous fuel into a catalyst regeneration system for combustion to provide energy and maintain the heat balance of the fluid catalytic cracking unit, thereby fundamentally reducing carbon dioxide emissions from fossil energy sources.

[0009] In order to achieve the above object, on the one hand, the present application provides a catalyst regeneration method suitable for a fluid catalytic cracking apparatus including a catalytic cracking reactor and a catalyst regenerator, the regeneration method comprising: 1) providing a gaseous biomass-derived fuel comprising hydrogen and / or methane; 2) feeding the gaseous fuel directly to the catalyst regenerator without separation and purification; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen-containing gas having an oxygen content of 14% by volume to 28% by volume; and 4) feeding the catalyst to be regenerated from the catalytic cracking reactor to the catalyst regenerator, where the catalyst is contacted with the gaseous fuel and the oxygen-containing gas for coke combustion and regeneration.

[0010] On the other hand, the present application provides a catalyst regeneration system suitable for a biomass treatment device and a fluid catalytic cracking device equipped with a catalyst regenerator, comprising: The biomass treatment device is used for treating biomass to obtain gaseous fuel comprising hydrogen and / or methane, and comprises a gaseous fuel generator and a gaseous fuel storage tank, the gaseous fuel generator is preferably selected from a biomass gasifier, a biomass anaerobic fermenter or a combination thereof, and has a biomass inlet and a gaseous product outlet, the gaseous fuel storage tank has an inlet and a gaseous fuel outlet, the gaseous fuel generator being connected to the inlet of the gaseous fuel storage tank; The catalyst regenerator is used to regenerate a catalyst to be regenerated from the catalytic cracking reactor, and includes a catalyst regenerator, the catalyst regenerator having an inlet for a catalyst to be regenerated, an inlet for an oxygen-containing gas, an inlet for a gaseous fuel, an outlet for a regenerated exhaust gas, and an outlet for a regenerated catalyst; The gas fuel outlet of the gas fuel storage tank is connected to the gas fuel inlet of the catalyst regenerator via a pipeline.

[0011] Compared with existing catalytic cracking catalyst regeneration methods and systems, the main advantages of the catalyst regeneration method and system of the present application are as follows: (1) Biomass is cheap and readily available. Biomass energy is a renewable energy source, and its carbon comes from carbon dioxide captured by plants from the atmosphere, rather than from fossil energy sources. Using biomass as an energy source can fundamentally change the energy source of catalytic crackers, reduce carbon dioxide emissions from fossil energy sources, and achieve low-carbon refining. (2) Gaseous fuels produced from biomass can be used directly without complex separation and purification, thus reducing utilization costs; (3) Biomass-based gaseous fuels have a relatively high hydrogen content. The steam generated by burning the hydrogen contained in the fuel can be used to age the catalyst during the catalyst regeneration process to improve the selectivity to the desired light olefin products. Alternatively, when high activity is required for the catalyst, the adverse effect of steam on the catalyst activity can be reduced by optimizing the regeneration process. (4) When gaseous fuel is used as the combustion medium, the gaseous fuel is more uniformly mixed with the generated catalyst, making the combustion and heat transfer process more stable. (5) When oxygen-enriched regeneration is adopted, the carbon dioxide in the regeneration flue gas can be separated and captured at low cost, contributing to the achievement of negative carbon emissions; (6) The excess heat generated by the regeneration system can be used to supply other units, enabling the catalytic cracking unit to gradually develop into the power center of an integrated refining and chemical enterprise.

[0012] Other features and advantages of the present application will be described in detail in the following specific embodiment section.

[0013] The accompanying drawings are used to provide a further understanding of the present application and constitute a part of this specification. The following specific embodiments are used to explain the present application but are not intended to be limiting of the present application. [Brief description of the drawings]

[0014] [Figure 1] 1 is a schematic diagram of a preferred embodiment of the catalyst regeneration method and system of the present application. [Diagram 2] 2 is a schematic diagram of another preferred embodiment of the catalyst regeneration method and system of the present application. [Diagram 3] 2 is a schematic diagram of yet another preferred embodiment of the catalyst regeneration method and system of the present application. [Figure 4] 2 is a schematic diagram of a further preferred embodiment of the catalyst regeneration method and system of the present application. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0015] Hereinafter, specific embodiments of the present application will be described in detail with reference to the accompanying drawings. It should be understood that the specific embodiments described in this specification are for the purpose of illustrating and explaining the present application, and are not intended to limit the present application.

[0016] As used herein, the word "exemplary" means "serving as an example, embodiment, or illustration." Any embodiment described herein as "exemplary" is not necessarily to be construed as being superior or better than other embodiments. While various aspects of the embodiments are illustrated in drawings, the drawings are not necessarily drawn to scale unless specifically noted.

[0017] Any specific numerical value disclosed herein (including the endpoints of a numerical range) is not limited to the exact value of the numerical value, but should be understood to cover values ​​close to the exact value, such as all possible values ​​within a range of ±5% of the exact value. Furthermore, for any of the disclosed numerical ranges, any combination between the endpoints of the ranges, between the endpoints and the specific points of the ranges, and between the specific points of the ranges, can result in one or more new numerical ranges, which should also be considered to be specifically disclosed herein.

[0018] In this application, the so-called "upstream" and "downstream" are based on the flow direction of the reactants. For example, if the reactants flow from bottom to top, "upstream" means a lower position and "downstream" means an upper position.

[0019] It should be noted that in this application, terms such as "upper", "lower", "middle", "outer", "front", "rear", "left", "right" and the like indicate directions or positional relationships based on directions or positional relationships in the operating state of this application. These are for convenience in explaining and simplifying the description of this application, and do not indicate or imply that the devices or elements referenced have a particular orientation or must be constructed and operated in a particular direction. Thus, they should not be understood as limitations of this application.

[0020] It should be noted that in this application, unless otherwise specified and limited, the terms "install", "connected", "connect" and "couple" should be understood in a broad sense. Those skilled in the art can understand the specific meaning of the above terms in this application according to the specific situation. For example, in this application, the term "connected" includes both a situation in which two things are directly connected and a situation in which two things are connected via one or more intermediate devices.

[0021] Terms used herein have the same meaning as commonly understood by those of ordinary skill in the art, unless otherwise specified. Where a term is defined herein and the definition differs from the meaning commonly understood by those of ordinary skill in the art, the definition herein shall prevail.

[0022] In this application, except for the contents explicitly described, the matters or items not described shall be directly applied to those known in the art without any changes. In addition, any embodiment described in this specification can be freely combined with one or more other embodiments described in this specification, and the technical solutions or technical ideas formed thereby shall be considered as part of the original disclosure or original record of the present invention, and shall not be considered as new contents not disclosed or anticipated in this specification, unless a person skilled in the art considers the combination to be obviously unreasonable.

[0023] All patent and non-patent literature referred to herein, including but not limited to textbooks and journal articles, is hereby incorporated by reference in its entirety.

[0024] Furthermore, the technical features involved in different embodiments of the present application described below can be combined with each other unless they are mutually inconsistent.

[0025] As mentioned above, in a first aspect, the present application provides a catalyst regeneration method suitable for a fluid catalytic cracking unit comprising a catalytic cracking reactor and a catalyst regenerator, the regeneration method comprising: 1) providing a gaseous biomass-derived fuel comprising hydrogen and / or methane; 2) feeding the gaseous fuel directly to a catalyst regenerator without separation and purification; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen-containing gas having an oxygen content of 14% to 28% by volume; and 4) feeding the catalyst to be regenerated from the catalytic cracking reactor to a catalyst regenerator, where the catalyst is contacted with a gaseous fuel and an oxygen-containing gas for coke combustion and regeneration.

[0026] According to the present application, a gaseous biomass-derived fuel may be, for example, a gaseous fuel obtained by gasification or anaerobic fermentation of biomass.

[0027] The method provided in the present application uses gaseous biomass-derived fuel as an auxiliary energy source, and contacts and burns oxygen-containing gas together with the catalyst produced to supply energy, which not only satisfies the heat balance of the catalytic cracking unit, but also reduces carbon dioxide emissions and contributes to the separation and capture of carbon dioxide, becoming a source of negative carbon technology. The use of biomass is essentially an indirect solar energy utilization process. The carbon contained in biomass is not derived from fossil energy, but from carbon dioxide captured by plants from the atmosphere, and the energy consumed in the entire process is also derived from solar energy. Therefore, the use of biomass energy is also a carbon element recycling and a carbon-neutral emission process. At the same time, introducing biomass into the power center of the catalytic cracking unit and supplying biomass energy to the operation of the unit consumes renewable energy and the carbon dioxide emitted is not derived from fossil energy, so that it can fundamentally change the energy source and achieve carbon emission reduction. In addition, pure oxygen regeneration can also be used, so that the regeneration exhaust gas contains only carbon dioxide and oxygen, which can reduce the cost of separation and capture, and realize negative carbon emissions.

[0028] According to the present application, in a preferred embodiment, the biomass includes, but is not limited to, agricultural and forestry biomass, forestry biomass, aquatic plants, energy and cash crops, livestock and poultry manure, urban solid waste, domestic sewage and industrial organic sewage, etc. The agricultural and forestry biomass includes, but is not limited to, straw, rice husk, cotton stalk, etc., the forestry biomass includes, but is not limited to, firewood, fast-growing forest, forestry processing residues, etc., the aquatic plants include, but are not limited to, reed, algae, etc., the energy and cash crops include cassava, rapeseed, etc., the urban solid waste includes household waste, commercial service waste, etc., the domestic sewage and industrial organic sewage includes cooling water, kitchen wastewater, and organic sewage from brewing, food and other industries.

[0029] In a preferred embodiment, the operating temperature of the catalyst regenerator in step 4) is in the range of 550° C. to 750° C., and the average catalyst residence time is 1.0 min to 15.0 min.

[0030] In a preferred embodiment, the gaseous fuel in step 2) is injected into the catalyst regenerator through a gas distributor at a position not lower than the elevation of the inlet of the catalyst to be regenerated.

[0031] In a particular preferred embodiment, the oxygen-containing gas is air or oxygen diluted with recycled exhaust gas. More preferably, when the oxygen-containing gas is air, the amount of gaseous fuel introduced is 13% by volume or less of the amount of air introduced, for example, 3% to 13% by volume; when the oxygen-containing gas is oxygen diluted with recycled exhaust gas, the amount of gaseous fuel introduced is 44% by volume or less of the amount of oxygen introduced, preferably 10% to 44% by volume.

[0032] In certain preferred embodiments, the catalyst regenerator is a single stage regenerator, and the operating conditions of the regenerator include: an operating temperature of 550° C. to 750° C., an average catalyst residence time of 1.0 minutes to 15.0 minutes, and a superficial gas linear velocity of 0.5 m / s to 2.0 m / s.

[0033] Since the gaseous fuel produced from biomass has a high hydrogen content, a relatively large amount of steam is generated when it is burned in the catalyst regenerator. In order to avoid the adverse effect of steam on the activity of the catalyst, the method of the present application is preferably carried out in a two-stage regenerator or a dual regenerator, and the gaseous fuel is supplied only to the coke burning section of the two-stage regenerator or the first regenerator of the dual regenerator, and the operating conditions of the two-stage regenerator and the dual regenerator are appropriately optimized.

[0034] In certain particularly preferred embodiments, the catalyst regenerator is a two-stage regenerator comprising a coke burning section and a regeneration section in fluid connection, and in step 2) a gaseous fuel is supplied to the coke burning section and / or the regeneration section, preferably only to the coke burning section, in step 3) an oxygen-containing gas is introduced into the coke burning section and the bottom of the regeneration section, respectively, and in step 4) the catalyst to be regenerated is supplied to the coke burning section. More preferably, the operating conditions of the coke combustion section include: an operating temperature of 550°C to 720°C, an average catalyst residence time of 10.0 seconds to 120.0 seconds, preferably 15.0 seconds to 90.0 seconds, and a superficial gas linear velocity of 0.5 m / s to 5.0 m / s, preferably 1.0 m / s to 4.0 m / s; and the operating conditions of the regeneration section include: an operating temperature of 600°C to 750°C, an average catalyst residence time of 0.5 minutes to 5.0 minutes, preferably 1.0 minutes to 4.0 minutes, and a superficial gas linear velocity of 0.4 m / s to 2.0 m / s, preferably 0.5 m / s to 1.5 m / s. More preferably, the operating temperature of the regeneration section is 10°C to 150°C higher than the operating temperature of the coke combustion section.

[0035] In a further preferred embodiment, the operating conditions of the coke burning section include: 600°C to 700°C, and an average catalyst residence time of 60.0 seconds to 90.0 seconds; and the operating conditions of the regeneration section include: 650°C to 720°C, and an average catalyst residence time of 2.0 minutes to 4.0 minutes, whereby the steam generated by the combustion of the gaseous fuel can be utilized for aging the catalyst during the catalyst regeneration process, thereby improving the selectivity of the catalyst to the target light olefin product while avoiding the excessive influence of the steam on the catalytic activity, and thus is mainly suitable for the fluid catalytic cracking process for the production of chemicals such as light olefins. In such a preferred embodiment, the gaseous fuel can be injected only into the coke burning section of the regenerator, or can be injected simultaneously into the coke burning section and the regeneration section of the regenerator.

[0036] In some further preferred embodiments, the operating conditions of the coke burning section include: 550°C to 650°C, and an average catalyst residence time of 15.0 seconds to 60.0 seconds; and the operating conditions of the regenerating section include: 600°C to 680°C, and an average catalyst residence time of 1.0 minutes to 3.0 minutes, so that the adverse effect of steam on the catalyst activity can be sufficiently weakened, and the resulting regenerated catalyst has higher catalytic cracking activity and is mainly suitable for fluid catalytic cracking to produce fuel oil. In such preferred embodiments, gaseous fuel is injected only into the coke burning section of the regenerator.

[0037] In another particularly preferred embodiment, the catalyst regenerator is a dual regenerator comprising a first regenerator and a second regenerator in fluid connection, and in step 2), gaseous fuel is supplied to the first regenerator and / or the second regenerator, preferably only to the first regenerator, in step 3), oxygen-containing gas is introduced into the bottom of the first regenerator and the second regenerator, respectively, and in step 4), the catalyst to be regenerated is supplied to the first regenerator. More preferably, the operating conditions of the first regenerator include an operating temperature of 550°C to 720°C, an average catalyst residence time of 20.0 seconds to 240.0 seconds, preferably 30.0 seconds to 150.0 seconds, and a superficial gas velocity of 0.5 m / s to 5.0 m / s, preferably 1.0 m / s to 4.0 m / s; and the operating conditions of the second regenerator include an operating temperature of 600°C to 750°C, an average catalyst residence time of 0.5 minutes to 5.0 minutes, preferably 1.0 minutes to 4.0 minutes, and a superficial gas velocity of 0.4 m / s to 2.0 m / s, preferably 0.5 m / s to 1.5 m / s. More preferably, the second regenerator is operated at a temperature 10°C to 150°C higher than the operating temperature of the first regenerator.

[0038] In a further preferred embodiment, the operating conditions of the first regenerator include: 600°C to 700°C, and an average catalyst residence time of 90.0 seconds to 180.0 seconds; and the operating conditions of the second regenerator include: 650°C to 720°C, and an average catalyst residence time of 2.0 minutes to 4.0 minutes, so that the steam generated by the combustion of the gaseous fuel can be used for aging the catalyst during the catalyst regeneration process, thereby improving the selectivity of the catalyst to the target light olefin product while avoiding the excessive influence of the steam on the catalytic activity, and is therefore suitable for the fluid catalytic cracking process for the production of chemicals such as light olefins. In such a preferred embodiment, the gaseous fuel can be injected only into the first regenerator, or can be injected simultaneously into the first regenerator and the second regenerator.

[0039] In another more preferred embodiment, the operating conditions of the first regenerator include: 550°C to 650°C, and an average catalyst residence time of 15.0 seconds to 60.0 seconds; and the operating conditions of the second regenerator include: 600°C to 680°C, and an average catalyst residence time of 1.0 minutes to 3.0 minutes, so that the adverse effect of steam on the catalyst activity can be sufficiently weakened, and the resulting regenerated catalyst has higher catalytic cracking activity and is mainly suitable for fluid catalytic cracking to produce fuel oil. In such a preferred embodiment, gaseous fuel can be injected only into the first regenerator.

[0040] In certain further preferred embodiments, the coke combustion rate in the coke burning section or the first regenerator is between 40% and 70%, preferably between 40% and 50%, and the coke combustion rate in the regenerator section or the second regenerator is between 30% and 60%, preferably between 50% and 60%.

[0041] In certain preferred embodiments, the gaseous fuel is obtained by gasification of biomass and contains, based on the total amount of gaseous fuel, 12% to 60% hydrogen, 15% to 30% carbon monoxide, and 3% to 8% methane, with the remainder being carbon dioxide and / or nitrogen.

[0042] In a further preferred embodiment, step 1) further comprises a step of gasifying the biomass in the presence of a gasifying medium at a gasifying temperature between 500°C and 1500°C, the gasifying medium being selected from air, oxygen / oxygen-enriched gas, and water vapor.

[0043] In another preferred embodiment, the gaseous fuel is obtained by anaerobic fermentation of biomass and contains 40% to 100% by volume of methane, based on the total volume of the gaseous fuel.

[0044] In a further preferred embodiment, step 1) further comprises: subjecting the biomass to anaerobic fermentation in a closed fermenter, wherein the fermentation temperature is 60° C. or lower.

[0045] In some further preferred embodiments, the biomass is pretreated prior to gasification or anaerobic fermentation. Biomass pretreatment processes are well known to those skilled in the art. Preferably, the pretreatment is selected from one or more of grinding, drying, extrusion, steam explosion, acid treatment, alkali treatment, and microbial pretreatment.

[0046] In a particular preferred embodiment, the temperature in the catalyst regenerator is controlled not to exceed 750°C by a heat extraction system including one or more internal and / or external heat extractors. More preferably, the heat extraction system uses the heat extracted from the catalyst regenerator to generate high-pressure steam, which is then exported to other devices for energy supply. In such a preferred embodiment, the present application can use the energy generated by the regeneration system of the catalytic cracker to supply other operating devices, becoming a power center of the refinery and fundamentally reducing the carbon emissions of the refinery. The present application introduces biomass into the power center of the catalytic cracker and uses the biomass energy to supply the operation of the device. Since the carbon dioxide emitted is not derived from fossil energy, the energy source can be fundamentally changed and the reduction of carbon dioxide emissions can be achieved.

[0047] In a second aspect, the present application provides a catalyst regeneration system suitable for a fluid catalytic cracking unit, comprising a biomass treatment device and a catalyst regenerator: The biomass treatment device is used to process biomass to obtain gaseous fuel comprising hydrogen and / or methane, for example by gasification or anaerobic fermentation, and comprises a gaseous fuel generator and a gaseous fuel storage tank, the gaseous fuel generator is preferably selected from a biomass gasifier, a biomass anaerobic fermenter or a combination thereof, and has a biomass inlet and a gas product outlet, the gaseous fuel storage tank has an inlet and a gaseous fuel outlet, and the gaseous fuel generator's gas product outlet is connected to the inlet of the gaseous fuel storage tank; The catalyst regenerator is used to regenerate a catalyst to be regenerated from a catalytic cracking reactor, and includes a catalyst regenerator, the catalyst regenerator having an inlet for the catalyst to be regenerated, an inlet for an oxygen-containing gas, an inlet for a gaseous fuel, an outlet for a regenerated exhaust gas, and an outlet for a regenerated catalyst; The gas fuel outlet of the gas fuel storage tank is connected to the gas fuel inlet of the catalyst regenerator via a pipeline.

[0048] In a preferred embodiment, the biomass treatment apparatus further comprises a biomass pretreatment device and an optional gas product dryer, where the biomass pretreatment device is used to pretreat the biomass, the pretreatment being selected from one or more of grinding, drying, extrusion, steam explosion, acid treatment, alkali treatment, and microbial pretreatment, and the gas product dryer is used to dry the gas product obtained from the biomass anaerobic fermenter.

[0049] In certain preferred embodiments, the catalyst regenerator comprises a coke burner section and a dense phase regeneration section, the dense phase regeneration section being disposed above the coke burner section and an outlet of the coke burner section being received within the dense phase regeneration section, such that the coke burner section is in fluid communication with the dense phase regeneration section; The coke burning section contains: a first oxygen-containing gas inlet provided at the bottom of the coke burning section and used for supplying an oxygen-containing gas to the coke burning section; a gaseous fuel inlet disposed above the first oxygen-containing gas inlet and used for supplying a gaseous fuel; a gas distributor configured to distribute gaseous fuel provided through the gaseous fuel inlet; a catalyst to be regenerated inlet, which is used to transport the catalyst to be regenerated from the catalytic cracking reactor to the interior of the coke burner; and an optional first recycled flue gas inlet is provided which is used to recycle a portion of the flue gas discharged from the dense phase regeneration section back into the coke combustion section; High density phase regeneration section includes: a second oxygen-containing gas inlet disposed at the bottom of the dense phase regenerator section and used to supply oxygen-containing gas to the dense phase regenerator section; an optional second gaseous fuel inlet disposed above the second oxygen-containing gas inlet and used to supply gaseous fuel to the dense phase regenerator section; an optional second gas distributor configured to distribute the gaseous fuel provided from the second gaseous fuel inlet; a regeneration exhaust gas outlet provided at the top of the dense phase regeneration section and used for discharging the regeneration exhaust gas in the dense phase regeneration section; a regenerated catalyst outlet, which is used to return the regenerated catalyst to the catalytic cracking reactor; and an optional second recycled flue gas inlet is provided that is used to recycle a portion of the flue gas discharged from the dense phase regeneration section back into the dense phase regeneration section; Optionally, the dense phase regenerator section is further provided with a heat extractor for transferring heat to the exterior of the regenerator.

[0050] In some other preferred embodiments, the catalyst regenerator comprises a first regenerator and a second regenerator, the second regenerator being disposed downstream of the first regenerator, and the first regenerator and the second regenerator being connected by a catalyst transport pipe that transports catalyst material partially regenerated by the first regenerator to the second regenerator; The first regenerator has: a first oxygen-containing gas inlet provided at the bottom of the first regenerator and used for supplying an oxygen-containing gas to the first regenerator; a gaseous fuel inlet disposed above the first oxygen-containing gas inlet and used for supplying a gaseous fuel; a gas distributor configured to distribute gaseous fuel provided from the gaseous fuel inlet; an inlet for the catalyst to be regenerated, used for transporting the catalyst to be regenerated from the catalytic cracking reactor to the inside of the first regenerator; A first regeneration exhaust gas outlet provided at the top of the first regenerator and used for discharging the regeneration exhaust gas in the first regenerator; and an optional first recycled exhaust gas inlet provided at the bottom of the first regenerator and communicating with the first regenerator exhaust gas outlet for recycling a portion of the exhaust gas discharged from the first regenerator back to the first regenerator; The second regenerator has: a second oxygen-containing gas inlet provided at the bottom of the second regenerator and used for supplying an oxygen-containing gas to the second regenerator; an optional second gaseous fuel inlet disposed above the second oxygen-containing gas inlet and used to supply gaseous fuel to the second regenerator; an optional second gas distributor configured to distribute the gas fuel provided from the second gas fuel inlet; a regenerated catalyst outlet, which is used to return the regenerated catalyst to the catalytic cracking reactor; A second regenerator exhaust gas outlet, which is provided at the top of the second regenerator and is used to discharge the regenerator exhaust gas in the second regenerator; and An optional second recycled exhaust gas inlet is provided at the bottom of the second regenerator and connected to the first regenerated exhaust gas outlet and / or the second regenerated exhaust gas outlet for returning a portion of the exhaust gas to the second regenerator for reuse.

[0051] Preferred embodiments of the regeneration method and system of the present application are described in further detail below in conjunction with the accompanying drawings.

[0052] As shown in Figures 1, 2, 3 and 4, the catalyst regeneration system of the present application is suitable for regenerating a catalyst to be regenerated from a catalytic cracking reaction apparatus 100, and includes biomass treatment apparatuses 300 and 600 and catalyst regeneration apparatuses 200, 400, 500, and 700.

[0053] As shown in FIG. 1 to FIG. 4, in the catalytic cracking reaction system 100, the catalytic cracking reactor 110 is used to carry out the catalytic cracking reaction: the bottom inlet 102 of the catalytic cracking reactor 110 is supplied with a lifting medium for lifting the regenerated catalyst (from the regenerator) entering from the regenerated catalyst inlet 103, and the feed oil entering from the feed oil inlet 101 contacts the catalyst to carry out the catalytic cracking reaction. The oil and the gas product of the reaction are separated by the oil catalyst separation device 120, and the separated oil and gas products are collected by the gas collection chamber 140 and then transported to the product separation device 150 for separation, and various products are obtained. The separated catalyst to be regenerated is stripped by the settler stripping section 130 and then transported to the catalyst regenerator through the catalyst to be regenerated outlet 131, thereby realizing recycling. The catalytic cracking reactor 110 applied in the present application can be various reactors commonly used in the art, such as a riser reactor, a fluidized bed reactor, a variable diameter reactor, and combinations thereof.

[0054] As shown in FIGS. 1 and 2, a biomass treatment device 300 includes: A biomass pre-treatment device 310 used for pre-treatment of biomass; a biomass anaerobic fermenter 320 used for performing anaerobic fermentation on the pretreated biomass to obtain a gaseous fermentation product; a gaseous product dryer 330 used to dry the gaseous fermentation product obtained from the biomass anaerobic fermenter; and A gaseous fuel storage tank 340 is provided which is used to store the gaseous product.

[0055] As shown in the figure, the anaerobic fermentation process of biomass can be carried out in a biomass anaerobic fermenter 320, such as a closed fermenter, the fermentation substrate can be a mixed biomass feedstock, and the fermentation temperature is below 60° C. According to the present application, in a more preferred embodiment, urea, biomass charcoal, etc. can be added to enhance the fermentation process.

[0056] According to the present application, the anaerobic fermentation product mainly includes methane, carbon dioxide, water, etc. Moisture has a negative effect on the subsequent processes, so a drying process is necessary. Drying can be performed in a gas product dryer 330 to remove moisture from the fermentation product, so that the moisture content is reduced to 1.0 g / m 3 It will be less than.

[0057] After drying, the dried gas product is stored in the gas fuel storage tank 340 for further processing. In the dried gas product, methane can account for more than 40%, for example 40%-50%, can account for more than 60%, and can account for more than 75%, based on the total volume of the gas product.

[0058] According to the present application, the energy consumed in the anaerobic fermentation process is derived from other products of the fermentation process or at least partially / wholly from renewable energy sources such as solar energy, green electricity, nuclear energy, etc., thereby reducing carbon emissions throughout the life cycle.

[0059] As shown in FIGS. 3 and 4, the biomass treatment device 600 comprises: A biomass pre-treatment device 610, used for pre-treatment of biomass; a biomass gasifier 620 used to gasify the pretreated biomass to obtain a gas product; and A gaseous fuel storage tank 630 is provided which is used to store the gaseous product.

[0060] As shown, biomass can be transported to a biomass pre-processor 610 where it is processed by grinding, drying, etc., and then transported to a biomass gasifier 620. In the biomass gasifier 620, the biomass is gasified to obtain a gaseous product that is transported to a gaseous fuel storage tank 630 for subsequent regeneration processing, and the remaining product is withdrawn or sent to other equipment for processing. In a specific embodiment, the biomass material is crushed or crushed to a granular material with a particle size of 0.2 mm to 40 mm, and then dried to a moisture content of less than 10%.

[0061] The biomass is then gasified. The gasification temperature can be in the range of 500°C to 1500°C. The gasification medium used in the gasification process can be selected from air, oxygen / oxygen-enriched gas, water vapor, etc. According to the present application, the energy consumed in the biomass gasification process can be derived from other products of the gasification process or at least partially / wholly from renewable energy sources such as solar energy, green electricity, nuclear energy, etc., reducing carbon emissions throughout the entire life cycle.

[0062] According to the present application, the main components of the gas product obtained are hydrogen, carbon monoxide, carbon dioxide and a small amount of methane gas. Generally speaking, based on the total volume of the gas product, hydrogen accounts for 12%-60%, carbon monoxide accounts for 15%-30%, and methane accounts for 3%-8%. The remaining components may be carbon dioxide and / or nitrogen.

[0063] 1 is a schematic diagram of a first preferred embodiment of the present catalyst regeneration method and system, in which the regeneration process is a single-stage regeneration. As shown in FIG. 1, a regeneration apparatus 200 includes a regenerator 210, which includes: an oxygen-containing gas inlet 211 for supplying oxygen-containing gas to the regenerator, the oxygen-containing gas inlet 211 being located at the bottom of the regenerator; a distribution plate 212 configured to distribute the oxygen-containing gas provided through the oxygen-containing gas inlet 211; a gas fuel inlet 214 provided above the distribution plate 212 and used to supply gas fuel (the gas product from the gas fuel storage tank 340); a gas distributor 213 configured to distribute gaseous fuel provided through the gaseous fuel inlet 214; A catalyst to be regenerated inlet 216, which is used to transport the catalyst to be regenerated from the catalytic cracking reactor to the interior of the regenerator; and A regenerated catalyst outlet 217 is provided which is used to transport the regenerated catalyst to the catalytic cracking reactor.

[0064] The gaseous fuel storage tank 340 is connected to the gaseous fuel inlet 214 so that the gaseous fuel can be transported inside the regenerator and burned to regenerate the catalyst being regenerated.

[0065] Both the distribution plate 212 and the gas distributor 213 are provided inside the regenerator 210 to uniformly distribute the oxygen-containing gas and gaseous fuel to the catalyst to be regenerated inside the regenerator, so that the catalyst can be burned uniformly during the regeneration process to avoid local overheating. In general, both the distribution plate 212 and the gas distributor 213 are provided at the lower part inside the regenerator 210 to make the catalyst to be regenerated in a fluidized state inside the regenerator during the regeneration process in the regenerator.

[0066] The regenerator is a dense bed, and the density of the catalyst bed is 300 kg / m 3 ~700kg / m 3 The gaseous fuel is injected through a gas distributor at an elevation equal to or greater than the elevation of the inlet of the catalyst to be regenerated. In this embodiment, the gas distributor 213 is located below the dense bed of the regenerator to distribute the gaseous fuel more evenly.

[0067] In a specific embodiment, the conditions of the regeneration process are: the oxygen-containing gas is air, the regeneration temperature is 550°C to 750°C, the average catalyst residence time is 1.0 minutes to 15.0 minutes, and the gas superficial linear velocity is 0.7 m / s to 2.0 m / s.

[0068] The gaseous fuel and the catalyst to be regenerated are transported together to the bottom of the regenerator and contacted with oxygen-containing gas for coke combustion regeneration and energy supply. A large amount of heat is generated during the regeneration process due to the injection of the gaseous fuel. If the temperature in the regenerator is too high, it will have a negative effect on the activity of the catalyst. Therefore, the regenerator 200 is also provided with a heat extractor 215 for removing excess heat from the regenerator. The heat extractor can be an internal heat extractor (located inside the regenerator) or / and an external heat extractor (located outside the regenerator). There are one or more heat extractors, which can be used to supply excess energy generated by the regenerator to other devices. The excess heat of the regeneration system can be used to generate high-pressure steam through the heat extractor and then exported to other devices for energy supply. In a specific embodiment, by providing a heat extractor, the temperature of the regenerator bed is controlled not to exceed 750°C, for example not to exceed 720°C.

[0069] 1, the regenerator 200 further includes a cyclone separator 220, through which the regenerator exhaust gas exits the regenerator and enters the exhaust gas energy recovery system 230 to recover energy. The cyclone separator 220 may be provided inside the regenerator 210.

[0070] 2 is a schematic diagram of a second preferred embodiment of the present catalyst regeneration method and system, in which the regeneration process employs dual regenerator regeneration. The regeneration apparatus 400 includes a first regenerator 410 and a second regenerator 420. The two regenerators are linked together, and the second regenerator 420 is located downstream of the first regenerator 410 and connected by a catalyst transport pipe 417, which transports the catalyst material of the first regenerator to the second regenerator.

[0071] The first regenerator 410 includes: a first oxygen-containing gas inlet 411 provided at the bottom of the first regenerator and used to supply oxygen to the first regenerator; a gaseous fuel inlet 414 disposed above the first oxygen-containing gas inlet and used to supply a gaseous fuel; a gas distributor 416 configured to distribute the gas fuel provided through the gas fuel inlet; and a catalyst to be regenerated inlet 418 (connected to the inclined tube to be regenerated), used to transport the catalyst to be regenerated from the catalytic cracking reactor to the inside of the first regenerator; a first exhaust gas outlet 419 provided at the top of the first regenerator; The second regenerator 420 includes: a second oxygen-containing gas inlet 421 provided at the bottom of the second regenerator and used to supply oxygen to the second regenerator; A regenerated catalyst outlet 439 (connected to a regeneration inclined tube) used to transport the regenerated catalyst to the catalytic cracking reactor; and A second exhaust gas outlet 429 is provided at the top of the second regenerator.

[0072] During regeneration operation, gaseous fuel is introduced into the first regenerator 410 from the gaseous fuel inlet 414 through the gas distributor 416, and the catalyst to be regenerated enters the first regenerator from the catalytic cracking reactor through the inclined tube to be regenerated (connected to the outlet 131 of the catalyst to be regenerated) and the inlet 418 of the catalyst to be regenerated, contacts with oxygen entering from the first oxygen-containing gas inlet 411, and carries out a partial coking combustion reaction (first stage regeneration) in the first regenerator; the partially regenerated catalyst is transported to the second regenerator 420 through the catalyst transport tube 417, contacts with oxygen entering from the second oxygen-containing gas inlet 421, and then a coke combustion reaction occurs to fully regenerate.

[0073] In a specific embodiment, a first recycled exhaust gas inlet 431 is provided at the bottom of the first regenerator, and the first recycled exhaust gas inlet 431 is connected to the first exhaust gas outlet 419, so that a portion of the exhaust gas discharged from the first regenerator enters the first regenerator through the first recycled exhaust gas inlet.

[0074] In a specific embodiment, a second recycled exhaust gas inlet 432 is provided at the bottom of the second regenerator, and the second recycled exhaust gas inlet 432 is connected to the first exhaust gas outlet 419, so that a portion of the exhaust gas discharged from the first regenerator enters the second regenerator through the second recycled exhaust gas inlet.

[0075] In a specific embodiment, the bottom of the first regenerator and the bottom of the second regenerator are connected via a catalyst transport pipe 417 .

[0076] Thus, after the exhaust gas generated by the first regenerator is separated by the cyclone separator 413, a part of the exhaust gas enters the exhaust gas energy recovery device 430 to recover energy; the remaining part of the exhaust gas is split into two parts and circulated back to the regenerator, one part is transported to the first regenerator to dilute the introduced oxygen, and the other part is transported to the second regenerator to dilute the oxygen.

[0077] The tail gas from the second regenerator is separated by cyclone separator 423 and enters tail gas energy recovery unit 430 through second recycled tail gas outlet 429 for energy recovery, where it is transported to carbon dioxide separation system 460 for capture of carbon dioxide gas. The regenerated catalyst is circulated back to the catalytic cracking reactor through regenerated catalyst inlet 439 and regeneration inclined tube (connected to regenerated catalyst inlet 103).

[0078] In a specific embodiment, the operating conditions of the first regenerator are: temperature of 550°C to 700°C, average catalyst residence time of 20.0 seconds to 240.0 seconds, and superficial gas linear velocity of 0.5 m / s to 5.0 m / s. The operating conditions of the second regenerator are: temperature of 600°C to 750°C, average catalyst residence time of 0.5 minutes to 5.0 minutes, and superficial gas linear velocity of 0.4 m / s to 2.0 m / s.

[0079] Due to the injection of gaseous fuel, a large amount of heat is generated during the regeneration process. If the temperature inside the regenerator is too high, it will have a negative effect on the activity of the catalyst. Therefore, the regeneration device 400 is also provided with heat extractors 415, 425 for transferring heat to the outside of the first regenerator and the second regenerator. The heat extractor can be an internal heat extractor (located inside the regenerator) or / and an external heat extractor (located outside the regenerator), and the heat extractor is one or more, and extracts excess energy from the first regenerator and the second regenerator for supplying to other devices. The excess heat of the regeneration system can be exported to other devices for energy supply after being used to generate high-pressure steam through the heat extractor. In a specific embodiment, by providing the heat extractor 415, the temperature of the bed of the first regenerator is controlled not to exceed 700°C, and by providing the heat extractor 425, the temperature of the bed of the second regenerator is controlled not to exceed 750°C, for example not to exceed 720°C.

[0080] The gaseous product obtained from biomass is rich in methane, which may account for more than 40%, such as 40%-50%, such as more than 60%, such as more than 75%, based on the total volume of the gaseous product. The molecular formula for methane is CH 4 and its hydrogen content reaches 25%. In the art, it is generally believed that excessive steam in the regeneration process is harmful to the activity of catalytic cracking catalyst, and mixed gas with high hydrogen content is generally not used as auxiliary fuel for the regeneration process. In the preferred embodiment shown in FIG. 2, the regeneration process adopts a pure oxygen regeneration process, and by adopting double regenerator regeneration, the catalyst can be better protected and the influence of steam can be avoided. In some further preferred embodiments, steam can be used to age the catalyst and improve the product selectivity by further optimizing the operating conditions of the first regenerator and the second regenerator.

[0081] In some specific embodiments, a playback method implemented in a playback system including the playback device 400 includes: 1) transporting the pretreated biomass to a biomass anaerobic fermentation system for anaerobic fermentation to obtain a gaseous fermentation product; 2) drying the gaseous fermentation product and storing the dried gaseous fuel in a gaseous fuel storage tank; 3) transporting the gaseous fuel into the first regenerator and contacting it with the catalyst to be regenerated from the catalytic cracking reactor and oxygen, thereby partially coking the catalyst to be regenerated; 4) feeding the material from the first regenerator to a second regenerator and injecting oxygen into the second regenerator through a second oxygen-containing gas inlet to fully regenerate the catalyst.

[0082] 3 is a schematic diagram of a third preferred embodiment of the catalyst regeneration method and system of the present invention, in which the regeneration process employs dual regenerator regeneration. The regeneration apparatus 500 includes a first regenerator 510 and a second regenerator 520 coupled together, the second regenerator 520 being located downstream of the first regenerator 510 and connected by a U-shaped catalyst transport pipe 517, through which the catalyst material of the first regenerator is transported to the second regenerator.

[0083] The first regenerator 510 includes: a first oxygen-containing gas inlet 511 provided at the bottom of the first regenerator and used to supply oxygen to the first regenerator; a gaseous fuel inlet 514 disposed above the first oxygen-containing gas inlet and used to supply gaseous fuel; a gas distributor 516 configured to distribute gaseous fuel provided through the gaseous fuel inlet; A catalyst to be regenerated inlet 518 (connected to the inclined tube to be regenerated) used to transport the catalyst to be regenerated from the catalytic cracking reactor to the inside of the first regenerator; and a first exhaust gas outlet 519 provided at the top of the first regenerator; The second regenerator 520 includes: a second oxygen-containing gas inlet 521 provided at the bottom of the second regenerator and used to supply oxygen to the second regenerator; A regenerated catalyst outlet 539 (connected to the regeneration incline tube) used to transport the regenerated catalyst to the catalytic cracking reactor; and A second exhaust gas outlet 529 is provided at the top of the second regenerator.

[0084] During regeneration operation, gaseous fuel is introduced into the first regenerator 510 from the gaseous fuel inlet 514 through the gas distributor 516, and the catalyst to be regenerated from the catalytic cracking reactor enters the first regenerator through the inclined tube to be regenerated (connected to the outlet 131 of the catalyst to be regenerated) and the inlet 518 of the catalyst to be regenerated, contacts with oxygen entering from the oxygen-containing gas inlet 511 through the fluid distribution plate 512, and carries out a partial coking combustion reaction (first stage regeneration) in the first regenerator; the partially regenerated catalyst is transported to the second regenerator 520 through the U-shaped catalyst transport tube 517, contacts with oxygen entering from the oxygen-containing gas inlet 521 through the fluid distribution plate 522, and then a coke combustion reaction occurs for full regeneration.

[0085] In a specific embodiment, a first recycled exhaust gas inlet 533 is provided at the bottom of the first regenerator, and the first recycled exhaust gas inlet 533 is connected to the first exhaust gas outlet 519, so that a portion of the exhaust gas discharged from the first regenerator enters the first regenerator through the first recycled exhaust gas inlet.

[0086] In a specific embodiment, a second recycled exhaust gas inlet 532 is provided at the bottom of the second regenerator, and the second recycled exhaust gas inlet 532 is connected to the first exhaust gas outlet 519, so that a portion of the exhaust gas discharged from the first regenerator enters the second regenerator through the second recycled exhaust gas inlet.

[0087] In a specific embodiment, the bottom of the first regenerator and the bottom of the second regenerator are connected via a U-shaped catalyst transport pipe 517 .

[0088] The U-shaped catalyst transport tube is provided with an opening 531 which communicates with the first exhaust gas outlet 519 so that a portion of the exhaust gas discharged from the first regenerator enters the U-shaped catalyst transport tube through the opening.

[0089] Thus, after the exhaust gas generated by the first regenerator is separated by the cyclone separator 513, a part of the exhaust gas enters the exhaust gas energy recovery device 530 to recover energy; the remaining part of the exhaust gas is divided into three parts and circulated back to the regenerator. One part is transported to the first regenerator to dilute the introduced oxygen, one part is transported to the U-shaped catalyst transport tube to transport the semi-regenerated catalyst to the second regenerator, and the last part is transported to the second regenerator to dilute the introduced oxygen. The amount of oxygen and / or the amount of recycled exhaust gas is controlled so that the oxygen concentration in the mixed gas in the first regenerator and the second regenerator is 28% or less. Coke combustion under this atmosphere improves the coke combustion intensity; the intake gas does not contain nitrogen, so the energy consumed by gas preheating can be reduced; and the exhaust gas at the outlet of the regenerator has a high carbon dioxide concentration, which contributes to the separation and recovery of carbon dioxide.

[0090] The tail gas from the second regenerator, after being separated by the cyclone separator 523, enters the tail gas energy recovery unit 530 through the second recycled tail gas outlet 529 for energy recovery, where it is transported to the carbon dioxide separation system 560 for capturing the carbon dioxide gas. The regenerated catalyst is circulated back to the catalytic cracking reactor through the regenerated catalyst inlet 539 and the regeneration inclined tube (connected to the regenerated catalyst inlet 103).

[0091] In a specific embodiment, the operating conditions of the first regenerator are: temperature of 550°C to 700°C, average catalyst residence time of 20.0 seconds to 240.0 seconds, and superficial gas linear velocity of 0.5 m / s to 5.0 m / s. The operating conditions of the second regenerator are: temperature of 600°C to 750°C, average catalyst residence time of 0.5 minutes to 5.0 minutes, and superficial gas linear velocity of 0.4 m / s to 2.0 m / s.

[0092] Due to the injection of gaseous fuel, a large amount of heat is generated during the regeneration process. If the temperature in the regenerator is too high, it will have a negative effect on the activity of the catalyst. Therefore, the regeneration device 500 is also provided with heat extractors 515, 525 for removing excess heat from the first regenerator and the second regenerator, and optionally transporting the heat to the outside. The heat extractor can be an internal heat extractor (located inside the regenerator) or / and an external heat extractor (located outside the regenerator), and the heat extractor is one or more, and extracts the excess energy generated by the first regenerator and the second regenerator to supply to other devices. The excess heat of the regeneration system can be exported to other devices for energy supply after being used to generate high-pressure steam through the heat extractor. In a specific embodiment, by providing the heat extractor 515, the temperature of the bed of the first regenerator is controlled not to exceed 700°C; by providing the heat extractor 525, the temperature of the bed of the second regenerator is controlled not to exceed 750°C, for example not to exceed 720°C.

[0093] The gaseous product obtained by gasification of biomass contains a certain amount of hydrogen, for example, hydrogen accounts for 12%-60%, carbon monoxide accounts for 15%-30%, and methane accounts for 3%-8%, based on the total volume of the gaseous product. In the art, it is generally believed that excessive steam in the regeneration process is harmful to the activity of catalytic cracking catalysts, so mixed gas containing hydrogen is generally not used as auxiliary fuel for the regeneration process. In a preferred embodiment shown in FIG. 3, the regeneration process adopts a pure oxygen regeneration process, and by adopting double regenerator regeneration, the catalyst can be better protected and the influence of steam can be avoided. In a further preferred specific embodiment, the operating conditions of the first regenerator and the second regenerator can be further optimized to use steam to age the catalyst and improve the product selectivity.

[0094] In a specific embodiment, a playback method implemented in a playback system including the playback device 500 includes: 1) transporting the pretreated biomass to a gasifier for gasification to obtain a gas product; 2) transporting the gaseous product into the first regenerator and contacting it with the catalyst to be regenerated from the catalytic cracking reactor and oxygen, thereby partially coking the catalyst to be regenerated; 3) feeding the material from the first regenerator to a second regenerator and injecting oxygen into the second regenerator to fully regenerate the catalyst.

[0095] 4 is a schematic diagram of a fourth preferred embodiment of the present catalyst regeneration method and system, in which the regeneration process employs two-stage regeneration. As shown in the figure, the regeneration apparatus 700 includes a regenerator 740, which includes a coke burning section 710 and a regeneration section 750, the regeneration section 750 being in fluid communication with the coke burning section 710 and located above the coke burning section 710; the regeneration section 750 is separated from the coke burning section 710 by a fluid distribution plate 751. In this way, the regeneration section 750 and the coke burning section 710 are connected to each other. After being distributed by the fluid distribution plate 751, the material from the coke burning section 710 enters the regeneration section 750 for complete regeneration.

[0096] The coke burning section 710 includes: a first oxygen-containing gas inlet 711 for supplying oxygen to the coke burning section, the first oxygen-containing gas inlet being provided at the bottom of the coke burning section; a gaseous fuel inlet 714 disposed above the first oxygen-containing gas inlet and used to supply a gaseous fuel; a gas distributor 713 configured to distribute gaseous fuel provided through the gaseous fuel inlet; A catalyst to be regenerated inlet 716 used to transport the catalyst to be regenerated from the catalytic cracking reactor to the interior of the coke burner section; and A first recycled flue gas inlet 731 is provided which is used to recycle a portion of the flue gas recovered from the regeneration section back into the coke burning section.

[0097] In this manner, the catalyst to be regenerated is first coke fired in the coke firing section 710 and the gaseous fuel is partially combusted, thereby avoiding hydrothermal deactivation of the catalyst by the water produced during the hydrogen combustion process.

[0098] The playback section 750 includes: a second oxygen-containing gas inlet 752 located at the bottom of the regeneration section and used to supply oxygen to the regeneration section; A second recycled exhaust gas inlet 753, used to recycle a portion of the exhaust gas recovered from the regeneration section back into the regeneration section; and An exhaust gas outlet 732; provided at the top of the regeneration section; The regenerator section 750 is also provided with a heat extractor 715 for transferring heat to the exterior of the regenerator.

[0099] During regeneration operation, gaseous fuel from the gaseous fuel storage tank 630 is supplied to the coke burning section 710 through the gaseous fuel inlet 714 and the gas distributor 713. The catalyst to be regenerated from the catalytic cracking reactor enters the coke burning section 710 through the catalyst to be regenerated inlet 716, contacts with oxygen entering through the first oxygen-containing gas inlet 711, and undergoes partial coke burning reaction in the coke burning section; then, after passing through the fluid distribution plate 751, enters the regeneration section 750 for complete regeneration. At this time, pure oxygen is supplied from the second oxygen-containing gas inlet 752 and contacts with the partially coke-burned catalyst, thereby further regenerating and burning the catalyst and the incompletely regenerated exhaust gas. After being separated in the cyclone separator 720, the regenerated catalyst falls back to the regeneration section, is discharged from the catalyst outlet 717, and circulates back to the catalytic cracking reactor. A portion of the exhaust gas discharged from the exhaust gas outlet 732 is recovered by the exhaust gas energy recovery system 730 and then separated by the carbon dioxide separation system 760 to achieve carbon dioxide recovery; the remainder of the exhaust gas is circulated back to the bottom of the coke combustion section.

[0100] In a specific embodiment, the operating conditions of the coke combustion section are a temperature of 550°C to 720°C, an average catalyst residence time of 10.0 seconds to 120.0 seconds, preferably 15.0 seconds to 90.0 seconds, and a superficial gas linear velocity of 0.5 m / s to 5.0 m / s, preferably 1.0 m / s to 4.0 m / s.

[0101] In a specific embodiment, the operating conditions of the regeneration section are a temperature of 600°C to 750°C, an average catalyst residence time of 0.5 to 5.0 minutes, preferably 1.0 to 4.0 minutes, and a superficial gas linear velocity of 0.4 m / s to 2.0 m / s, preferably 0.5 to 1.5 m / s. The catalyst is completely regenerated in the regeneration section, and the biomass-derived gaseous fuel is completely combusted in the regeneration section. In a specific embodiment, the regeneration section is a dense bed, and the catalyst density is 300 kg / m 3 ~700kg / m 3 It is.

[0102] In a specific embodiment, the gas supplied through the first oxygen-containing gas inlet 711 and the gas supplied through the second oxygen-containing gas inlet 752 are both oxygen. However, the oxygen supplied through the first oxygen-containing gas inlet 711 is mixed with the recycled flue gas after entering the coke combustion section to form an oxygen-carbon dioxide mixed gas. The amount of oxygen and / or recycled flue gas is controlled so that the oxygen concentration in the mixed gas does not exceed 28% by volume. Similarly, the oxygen supplied through the second oxygen-containing gas inlet 752 is mixed with the recycled flue gas, etc. after entering the regeneration section to form an oxygen-carbon dioxide mixed gas. The amount of oxygen and / or recycled flue gas is controlled so that the oxygen concentration in the mixed gas is 28% or less. Coke combustion under this atmosphere improves the coke combustion intensity; the suction gas does not contain nitrogen, so the energy consumed by gas preheating can be reduced; and the flue gas at the regenerator outlet has a higher carbon dioxide concentration, which is favorable for carbon dioxide separation and capture.

[0103] In a specific embodiment, the coke combustion ratio in the coke burning section is 40-70%, and the coke combustion ratio in the regeneration section is 30-60%. In a specific embodiment, pure oxygen is used for regeneration, and the regeneration exhaust gas only contains carbon dioxide and oxygen, which is convenient for separating and capturing carbon dioxide for further conversion and utilization, thereby achieving negative carbon emission. According to the present application, the gaseous fuel obtained by biomass gasification is introduced through a gas distributor.

[0104] In the preferred embodiment shown in Figure 4, the regeneration process adopts a pure oxygen regeneration process, and two-stage regeneration is carried out in the connected coke burning section and regeneration section, which can improve the coke burning intensity and achieve better regeneration effect, and at the same time, weaken the influence of steam on the catalyst. In a further preferred embodiment, by further optimizing the operating conditions of the coke burning section and the regeneration section, steam can be used to age the catalyst and improve the product selectivity.

[0105] Due to the injection of gaseous fuel, a large amount of heat is generated during the regeneration process. If the temperature inside the regenerator is too high, it will have a negative effect on the activity of the catalyst. Therefore, the regenerator 700 is also provided with a heat extractor 715 for transferring heat to the outside of the regenerator. The heat extractor can be an internal heat extractor (located inside the regenerator body) or / and an external heat extractor (located outside the regenerator body). There are one or more heat extractors, which supply the surplus energy generated by the regenerator to other devices. The surplus heat of the regeneration system can be exported to other devices for energy supply after being used to generate high-pressure steam through the heat extractor. In a specific embodiment, by providing a heat extractor, the temperature of the bed of the regenerator is controlled not to exceed 750°C, for example not to exceed 720°C. In the present application, by providing a heat extractor 715 in the regenerator, the heat of the bed of the regenerator is extracted and transported to the outside of the regenerator, and the temperature of the bed of the regenerator is controlled.

[0106] In a specific embodiment, the temperature of the bed in the regenerator section is controlled by a heat extractor to below 750°C, preferably below 720°C.

[0107] 4, the regenerator 700 further includes a cyclone separator 720. The regenerator exhaust gas exits the regenerator through the cyclone separator 720 and enters the exhaust gas energy recovery system 730 to recover energy. The cyclone separator 720 may be provided inside the regenerator 740.

[0108] The catalyst suitable for the catalyst regeneration method and system of the present application may be a catalyst conventionally used in various catalytic cracking processes, and the present application has no particular limitations. In some specific embodiments, the catalyst includes a zeolite, an inorganic oxide, and an optional clay, each component being based on the total weight of the catalyst: zeolite is 1% to 50% by weight; inorganic oxide is 5% to 99% by weight; and clay is 0% to 70% by weight. Here, the zeolite is an active component, and is selected from medium pore zeolite and / or any large pore zeolite, the medium pore zeolite is 10% to 100% by weight of the total weight of the zeolite, and the large pore zeolite is 0% to 90% by weight of the total weight of the zeolite. The medium pore zeolite is selected from one or more of ZSM series zeolite and / or ZRP zeolite, and the above zeolite can be modified with a nonmetal such as phosphorus, and / or a transition metal such as iron, cobalt, nickel. The large pore zeolite is one or more selected from hydrogen Y, rare earth Y, rare earth hydrogen Y, ultrastable Y, and the like. EXAMPLES

[0109] The present application will be further described below with reference to examples, but the present application is not limited thereto in any way.

[0110] The properties of feedstock oils A and B used in the following Examples and Comparative Examples are shown in Tables 1 and 2, respectively, and the composition of feedstock C is shown in Table 3.

[0111] [Table 1]

[0112] [Table 2]

[0113] [Table 3]

[0114] Catalyst a is the commercial catalyst ASC-2, the properties of which are shown in Table 4.

[0115] [Table 4]

[0116] Catalyst b was a TCC catalyst and was used after aging. The aging conditions were steam aging at 800°C for 15 hours. The preparation process of catalyst b was as follows:

[0117] 969g of halloysite (product of China Kaolin Company, solid content 73%) was slurried with 4300g of decationized water, then 781g of pseudoboehmite (product of Shandong Zibo bauxite factory, solid content 64%) and 144ml of hydrochloric acid (concentration 30%, specific gravity 1.56) were added, and the mixture was stirred uniformly. Then, the mixture was left to stand and mature at 60°C for 1 hour, the pH value was kept at 2-4, and cooled to room temperature, and 5000g of mesoporous shape-selective ZSM-5 zeolite slurry with high silicon-aluminum ratio that contained pre-prepared chemical water was added and stirred uniformly, spray-dried, and the free Na was removed. + The catalyst was obtained by washing and removing the residue. The properties are shown in Table 5.

[0118] [Table 5]

[0119] The preparation process of catalyst c is as follows:

[0120] (1) 20 g of NH 4 Cl was dissolved in 1000 g of water, and the crystallized product ZRP-1 molecular sieve (manufactured by Qilu Petrochemical Company Catalyst Plant, SiO 2 / Al 2 O 3 =30, rare earth content RE 2 O 3 = 2.0 wt%) 100 g (dry basis), exchanged at 90 °C for 0.5 h, and filtered to obtain a filter cake. 3 PO 4 (concentration 85%) and 4.5 g of Fe(NO 3 ) 3 was added, mixed with the filter cake, impregnated and dried, and then calcined at 550°C for 2 hours to obtain MFI mesoporous molecular sieve containing phosphorus and iron. The elemental analysis chemical composition of the obtained molecular sieve was: 0.1Na 2 O 5.1Al 2 O 3 2.4P 2 O 5 1.5Fe 2 O 3 3.8RE 2 O 3 88.1SiO 2 It is.

[0121] (2) 75.4 kg of halloysite (an industrial product of Suzhou Porcelain Company, solid content 71.6 wt%) was slurried with 250 kg of decationized water, and then 54.8 kg of pseudo-boehmite (an industrial product of Youdong Aluminum Factory, solid content 63 wt%) was added. The pH value was adjusted to 2-4 with hydrochloric acid, and the mixture was stirred uniformly. The mixture was allowed to stand and mature at 60°C-70°C for 1 hour, and the pH value was maintained at 2-4. The temperature was lowered to below 60°C, and 41.5 kg of aluminum sol (a product of Qilu Petrochemical Company's Catalyst Factory, Al 2 O 3 The mixture was stirred for 40 minutes to obtain a mixed slurry.

[0122] (3) The phosphorus- and iron-containing MFI mesoporous molecular sieve (2 kg on a dry basis) prepared in step (1) is added to the mixed slurry obtained in step (2), uniformly stirred, spray-dried to form a shape, and washed with an ammonium dihydrogen phosphate solution (phosphorus content 1 wt%) to obtain free Na + The catalyst c was removed and dried to obtain a sample of catalytic conversion catalyst c. Based on the total dry basis weight of catalyst c, the dry basis composition of catalyst c includes: 2 wt% MFI mesoporous molecular sieve containing phosphorus and iron, 36 wt% pseudoboehmite, and 8 wt% aluminum sol, and the balance is kaolin.

[0123] Example 1 The test was carried out using the apparatus shown in FIG. 1, and the specific preparation process of the gaseous fuel was as follows:

[0124] The biomass was pretreated in the pretreatment device by washing with water or acid, followed by crushing, grinding, etc. The pretreated biomass was fermented in the anaerobic fermenter at a fermentation temperature of 37° C. After the fermentation product was dehydrated by a dryer, a gas product was obtained in which methane accounted for more than 40% (based on the volume of the gas product), and was stored in a storage tank to await use.

[0125] The feedstock A was used as the reaction feedstock, and the catalytic conversion catalyst a was used as the catalyst. The catalyst to be regenerated was regenerated according to the method of the present application. The catalyst to be regenerated from the inclined tube to be regenerated was contacted with the gas fuel and air introduced from the gas distributor at the bottom of the regenerator, and a coke combustion reaction occurred. The excess energy generated in the regeneration system was used to supply energy to the outside through a heat extraction system. The operating temperature of the regenerator was 685°C, the average catalyst residence time was 5 minutes, and the gas superficial linear velocity was 1.0 m / s. For the catalytic cracking reaction, the regenerated catalyst was placed in a reactor and contacted with the feedstock oil. The excess energy was used to supply other devices through a heat extraction system. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 6.

[0126] Comparative Example 1 The test was carried out with reference to Example 1, except that no biomass treatment device was used, light oil was injected into the regenerator as fuel oil, and fuel oil was used as an auxiliary energy source. The coke combustion temperature of the regenerator was 685°C. The average catalyst residence time was 5 minutes, and the gas superficial linear velocity was 1.0 m / s. The regenerated catalyst was placed in a reactor and contacted with the feedstock oil for the catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 6.

[0127] [Table 6]

[0128] From the data in Table 6, it can be seen that when the embodiment uses gaseous biomass fuel as an auxiliary energy source and the regeneration system produces the same amount of energy, the amount of carbon dioxide emitted is significantly reduced compared to the comparative example, and more energy can be transferred to other devices, which contributes to fundamentally reducing carbon dioxide emissions.

[0129] Example 2 Tests were conducted using the apparatus shown in FIG. 2, where the reactor 110 was a conventional riser reactor, and where a flue gas energy recovery system 430 and a carbon dioxide separation system 460 were provided.

[0130] The specific preparation process of the gaseous fuel was as follows:

[0131] The biomass was pretreated in the pretreatment device by washing with water or acid, followed by crushing, grinding, etc. The pretreated biomass was fermented in the anaerobic fermenter at a fermentation temperature of 37° C. After the fermentation product was dehydrated by a dryer, a gas product was obtained in which methane accounted for more than 40% (based on the volume of the gas product), and was stored in a storage tank to await use.

[0132] Raw material B was used as the reaction raw material, and catalytic conversion catalyst b was used as the catalyst. The catalyst to be regenerated was regenerated according to the method of the present application. Gaseous fuel was introduced into the first regenerator through a gas distributor, and a combustion reaction was carried out with the catalyst to be regenerated that entered the first regenerator through the inclined tube to be regenerated, and a coke combustion reaction was partially carried out in the first regenerator (first stage regeneration), and the partially regenerated catalyst was transported to the second regenerator through the catalyst transport tube, and a coke combustion reaction was carried out for complete regeneration. At the same time, a part of the exhaust gas discharged from the regeneration cyclone separation system was returned to the first regenerator and the second regenerator, and the oxygen content was controlled not to exceed 28%. The surplus energy generated in the regeneration system was used to supply energy to the outside through a heat extractor.

[0133] The operating temperature of the first regenerator was 650°C, the average catalyst residence time in the first regenerator was 120 seconds, and the gas superficial velocity was 1.5 m / s. The operating temperature of the second regenerator was 670°C, the average catalyst residence time in the second regenerator was 3.0 minutes, and the gas superficial velocity was 1.0 m / s. For the catalytic cracking reaction, the regenerated catalyst was placed in a reactor and contacted with the feedstock. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 7.

[0134] Comparative Example 2 The test was carried out with reference to Example 2, except that diesel fuel was used as the fuel oil, which was injected into the pipeline to be regenerated and premixed with the catalyst to be regenerated before entering the regenerator as an auxiliary energy source. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 7.

[0135] [Table 7]

[0136] From the data in Table 7, it can be observed that when the gaseous fuel obtained by gasification of biomass is used as the auxiliary energy source in the embodiment and the regeneration system produces the same amount of energy, the amount of carbon dioxide emitted is significantly reduced compared to the comparative example, which is conducive to fundamentally reducing carbon dioxide emissions. Meanwhile, the propylene yield in the embodiment 2 is also improved to a certain extent, which indicates that the selectivity of the regenerated catalyst to propylene is improved.

[0137] Example 3 Tests were conducted using the apparatus shown in FIG. 3, where the reactor 110 was a conventional riser reactor, and where a flue gas energy recovery system 530 and a carbon dioxide separation system 560 were installed.

[0138] Biomass processing apparatus 600 includes a biomass pre-processor 610, a biomass gasifier 620, and a gaseous fuel storage tank 630. The operating conditions of biomass gasifier 620 were a temperature of 950° C., a gasification medium of steam, and volume fractions of hydrogen, carbon monoxide, and methane in the resulting gas product of 50%, 25%, and 7%, respectively, based on the volume of the gas product.

[0139] The raw material C was used as the reaction raw material, and the catalytic conversion catalyst c was used as the catalyst. The catalyst to be regenerated was regenerated according to the method of the present application. Pure oxygen gas was introduced into the first regenerator and the second regenerator, respectively, and the gaseous fuel from the gaseous fuel storage tank 630 was introduced from the gas distributor of the first regenerator, and a combustion reaction was carried out with the catalyst to be regenerated from the inclined tube. At the same time, a part of the exhaust gas discharged from the regenerative cyclone separation system 520 was returned to the bottom of the first regenerator and the second regenerator, and the oxygen content was controlled not to exceed 28%. The surplus energy generated in the regeneration system was used to supply energy to the outside through a heat extractor.

[0140] The operating temperature of the first regenerator was 630°C, the average catalyst residence time in the first regenerator was 40 seconds, and the gas superficial velocity was 1.0 m / s. The operating temperature of the second regenerator was 665°C, the average catalyst residence time in the second regenerator was 1.5 minutes, and the gas superficial velocity was 1.0 m / s. The regenerated catalyst was placed in a reactor and contacted with the feedstock for catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 8.

[0141] Comparative Example 3 The test was carried out with reference to Example 3, except that diesel fuel was used as the fuel oil, which was injected into the pipeline to be regenerated and premixed with the catalyst to be regenerated before entering the regenerator as an auxiliary energy source. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 8.

[0142] [Table 8]

[0143] From the data in Table 8, it can be observed that when gaseous fuel is used as an auxiliary energy source in the embodiment and the regenerative system produces the same amount of energy, the amount of carbon dioxide emitted is significantly reduced compared to the comparative example, which contributes to fundamentally reducing carbon dioxide emissions.

[0144] Example 4 The regeneration was carried out using the apparatus shown in FIG. 4, which is equipped with a tail gas energy recovery system 730 and a carbon dioxide separation system 760, and in which the reactor 110 is a conventional riser reactor.

[0145] Biomass processing apparatus 600 includes a biomass pre-processor 610, a biomass gasifier 620, and a gaseous fuel storage tank 630. The operating conditions of biomass gasifier 620 were a temperature of 950° C., a gasification medium of steam, and volume fractions of hydrogen, carbon monoxide, and methane in the resulting gas product of 50%, 25%, and 7%, respectively, based on the volume of the gas product.

[0146] Raw material B was used as the reaction raw material, and catalytic conversion catalyst b was used as the catalyst. The catalyst to be regenerated was regenerated according to the method of the present application. Pure oxygen gas was introduced into the coke combustion section and the regeneration section, respectively, and gaseous fuel from the gaseous fuel storage tank 630 was introduced from a gas distributor at the bottom of the coke combustion section, and a combustion reaction was carried out together with the catalyst to be regenerated from the inclined tube. At the same time, a part of the exhaust gas discharged from the regeneration cyclone separation system 720 was returned to the bottom of the coke combustion section and the regeneration section, and the oxygen content was controlled not to exceed 28%. The surplus energy generated in the regeneration system was used to supply energy to the outside through a heat extractor.

[0147] The operating temperature of the coke combustion section was 630°C, the average catalyst residence time in the coke combustion section was 40 seconds, and the gas superficial velocity was 1.2 m / s. The operating temperature of the dense phase regeneration section was 670°C, the average catalyst residence time in the dense phase regeneration section was 1.5 minutes, and the gas superficial velocity was 0.8 m / s. The regenerated catalyst was placed in a reactor and contacted with the feedstock for the catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 9.

[0148] Comparative Example 4 The test was carried out with reference to Example 4, except that diesel fuel was used as the fuel oil, which was injected into the pipeline to be regenerated and premixed with the catalyst to be regenerated before entering the regenerator as an auxiliary energy source. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 9.

[0149] [Table 9]

[0150] From the data in Table 9, it can be observed that when the gaseous fuel obtained by biomass gasification is used as an auxiliary energy source in the embodiment and the regeneration system produces the same amount of energy, the amount of carbon dioxide emitted is significantly reduced compared to the comparative example, which is helpful in fundamentally reducing carbon dioxide emissions.

[0151] Although the preferred embodiments of the present application have been described in detail above, the present application is not limited to the specific contents in the above embodiments. Within the technical idea of ​​the present application, various simple modifications can be made to the technical solutions of the present application, and all of these simple modifications fall within the protection scope of the present application.

[0152] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner unless they are inconsistent, and in order to avoid unnecessary repetition, the present application will not further describe the various possible combinations.

[0153] In addition, the respective embodiments of the present application can be combined in any manner as long as it is not contrary to the concept of the present application, and such combinations should also be considered as contents disclosed in the present application.

Claims

1. A catalyst regeneration method suitable for a fluid catalytic cracking unit having a catalytic cracking reactor and a catalyst regenerator, comprising: 1) providing a gaseous biomass-derived fuel, including hydrogen and / or methane, obtained, for example, by gasification or anaerobic fermentation of biomass; 2) feeding the gaseous fuel directly to the catalyst regenerator without separation and purification; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen-containing gas having an oxygen content of 14% to 28% by volume; and 4) feeding the catalyst to be regenerated from the catalytic cracking reactor to the catalyst regenerator, wherein the catalyst is contacted with the gaseous fuel and the oxygen-containing gas for coke combustion and regeneration; Preferably, the operating temperature of the catalyst regenerator is in the range of 550° C. to 750° C. and the average catalyst residence time is in the range of 1.0 min to 15.0 min.

2. The gaseous fuel is injected into the catalyst regenerator through a gas distributor at a position equal to or higher than the inlet height of the catalyst to be regenerated, and the oxygen-containing gas is air or oxygen diluted with recycled exhaust gas; The method according to claim 1, wherein, preferably, when the oxygen-containing gas is air, the amount of the gaseous fuel introduced is 13% by volume or less, preferably between 3% by volume and 13% by volume, of the amount of air introduced, or, when the oxygen-containing gas is oxygen diluted with recycled exhaust gas, the amount of the gaseous fuel introduced is 44% by volume or less, preferably between 10% by volume and 44% by volume, of the amount of oxygen introduced.

3. 3. The method of claim 1 or 2, wherein the catalyst regenerator is a single stage regenerator, and the operating conditions of the regenerator include an operating temperature of 550° C. to 750° C., an average catalyst residence time of 1.0 min to 15.0 min, and a superficial gas velocity of 0.5 m / s to 2.0 m / s.

4. The catalyst regenerator is a two-stage regenerator comprising a coke burning section and a regenerating section in fluid communication; and in step 2), the gaseous fuel is supplied to the coke burning section and / or the regenerating section, preferably only to the coke burning section; in step 3), the oxygen-containing gas is introduced into the coke burning section and the bottom of the regenerating section, respectively; and in step 4), the catalyst to be regenerated is supplied to the coke burning section; Preferably, the operating conditions of the coke burner section include: an operating temperature of 550° C. to 720° C., an average catalyst residence time of 10.0 seconds to 120.0 seconds, preferably 15.0 seconds to 90.0 seconds, and a superficial gas velocity of 0.5 m / s to 5.0 m / s, preferably 1.0 m / s to 4.0 m / s; and the operating conditions of the regeneration section include an operating temperature of 600° C. to 750° C., an average catalyst residence time of 0.5 minutes to 5.0 minutes, preferably 1.0 minutes to 4.0 minutes, and a superficial gas linear velocity of 0.4 m / s to 2.0 m / s, preferably 0.5 m / s to 1.5 m / s; More preferably, the method according to claim 1 or 2, wherein the operating temperature of the regenerator section is 10° C. to 150° C. higher than the operating temperature of the coke burning section.

5. The catalyst regenerator is a dual regenerator comprising a first regenerator and a second regenerator in fluid communication; and in step 2), the gaseous fuel is supplied to the first regenerator and / or the second regenerator, preferably only to the first regenerator; in step 3), the oxygen-containing gas is introduced into the bottom of the first regenerator and the second regenerator, respectively; and in step 4), the catalyst to be regenerated is supplied to the first regenerator; Preferably, the operating conditions of the first regenerator include an operating temperature of 550° C. to 720° C., an average catalyst residence time of 20.0 seconds to 240.0 seconds, preferably 30.0 seconds to 150.0 seconds, and a superficial gas linear velocity of 0.5 m / s to 5.0 m / s, preferably 1.0 m / s to 4.0 m / s; and the operating conditions of the second regenerator comprising an operating temperature of 600° C. to 750° C., an average catalyst residence time of 0.5 minutes to 5.0 minutes, preferably 1.0 minutes to 4.0 minutes, and a superficial gas linear velocity of 0.4 m / s to 2.0 m / s, preferably 0.5 m / s to 1.5 m / s; More preferably, the process according to claim 1 or 2, wherein the operating temperature of the second regenerator is 10° C. to 150° C. higher than the operating temperature of the first regenerator.

6. The method according to claim 4 or 5, wherein the coke burning rate in the coke burning section or the first regenerator is 40% to 70%, preferably 40% to 50%; and the coke burning rate in the regenerator section or the second regenerator is 30% to 60%, preferably 50% to 60%.

7. The gaseous fuel is obtained by gasification of biomass and contains, based on the total amount of the gaseous fuel, 12% to 60% hydrogen, 15% to 30% carbon monoxide, and 3% to 8% methane, with the remainder being carbon dioxide and / or nitrogen; or 7. The method according to any one of claims 1 to 6, wherein the gaseous fuel is obtained by anaerobic fermentation of biomass and comprises 40% to 100% by volume of methane, based on the total volume of the gaseous fuel.

8. Step 1) is Gasifying the biomass in the presence of a gasification medium at a gasification temperature between 500°C and 1500°C, said gasification medium being selected from air, oxygen / oxygen-enriched gas, and steam; or subjecting the biomass to anaerobic fermentation in a closed fermenter, the fermentation temperature being 60° C. or less; The method of any one of claims 1 to 7, further comprising:

9. 9. The method of claim 8, wherein the biomass is pretreated prior to gasification or anaerobic fermentation, the pretreatment being selected from one or more of grinding, drying, extrusion, steam explosion, acid treatment, alkali treatment, and microbial pretreatment.

10. 1. A catalyst regeneration system suitable for a fluid catalytic cracking unit having a biomass treatment device and a catalyst regenerator, comprising: The biomass treatment device is used to process biomass to obtain gaseous fuel comprising hydrogen and / or methane, for example by gasification or anaerobic fermentation, and comprises a gaseous fuel generator and a gaseous fuel storage tank, the gaseous fuel generator is preferably selected from a biomass gasifier, a biomass anaerobic fermenter or a combination thereof, and has a biomass inlet and a gas product outlet, the gaseous fuel storage tank has an inlet and a gaseous fuel outlet, the gaseous fuel generator being connected to the inlet of the gaseous fuel storage tank; The catalyst regenerator is used to regenerate a catalyst to be regenerated from the catalytic cracking reactor, and includes a catalyst regenerator having an inlet for a catalyst to be regenerated, an inlet for an oxygen-containing gas, an inlet for a gaseous fuel, an outlet for a regenerated exhaust gas, and an outlet for a regenerated catalyst; and A catalyst regeneration system, wherein the gas fuel outlet of the gas fuel storage tank is connected to the gas fuel inlet of the catalyst regenerator via a pipeline.

11. 11. The catalyst regeneration system of claim 10, wherein the biomass treatment device further comprises a biomass pretreatment device and an optional gas product dryer, the biomass pretreatment device is used to pretreat the biomass, the pretreatment being selected from one or more of grinding, drying, extrusion, steam explosion, acid treatment, alkali treatment, and microbial pretreatment, and the gas product dryer is used to dry the gas product obtained from the biomass anaerobic fermenter.

12. the catalyst regenerator comprises a coke burner section and a dense phase regeneration section, the dense phase regeneration section being disposed above the coke burner section, and an outlet of the coke burner section being received within the dense phase regeneration section, thereby fluidly connecting the coke burner section with the dense phase regeneration section; The coke burning section comprises: a first oxygen-containing gas inlet provided at the bottom of the coke burning section and used for supplying an oxygen-containing gas to the coke burning section; a gaseous fuel inlet disposed above the first oxygen-containing gas inlet and used for supplying a gaseous fuel; a gas distributor configured to distribute the gas fuel provided from the gas fuel inlet; a catalyst to be regenerated inlet used to transport the catalyst to be regenerated from the catalytic cracking reactor to the interior of the coke burner section; and an optional first recycled flue gas inlet is provided, which is used to recycle a portion of the flue gas discharged from the dense phase regeneration section into the coke combustion section; The dense phase regeneration section includes: a second oxygen-containing gas inlet at a bottom of the dense phase regeneration section and used to supply oxygen-containing gas to the dense phase regeneration section; an optional second gaseous fuel inlet disposed above the second oxygen-containing gas inlet and used to supply gaseous fuel to the dense phase regenerator section; an optional second gas distributor configured to distribute gaseous fuel provided from the second gaseous fuel inlet; a regeneration exhaust gas outlet provided at an upper portion of the dense phase regeneration section and used for discharging the regeneration exhaust gas in the dense phase regeneration section; a regenerated catalyst outlet, which is used to return the regenerated catalyst to the catalytic cracking reactor; and an optional second recycled exhaust gas inlet is provided which is used to recycle a portion of the exhaust gas discharged from the dense phase regeneration section back to the dense phase regeneration section; 12. The catalyst regeneration system according to claim 10 or 11, optionally, the dense phase regeneration section is further provided with a heat extractor for transferring heat to the outside of the regenerator.

13. The catalyst regenerator comprises a first regenerator and a second regenerator, the second regenerator is disposed downstream of the first regenerator, and the first regenerator and the second regenerator are connected by a catalyst transport pipe that transports the catalyst material partially regenerated by the first regenerator to the second regenerator; The first regenerator comprises: a first oxygen-containing gas inlet provided at the bottom of the first regenerator and used for supplying an oxygen-containing gas to the first regenerator; a gaseous fuel inlet disposed above the first oxygen-containing gas inlet and used for supplying a gaseous fuel; a gas distributor configured to distribute gaseous fuel provided from the gaseous fuel inlet; an inlet for a catalyst to be regenerated, used for transporting the catalyst to be regenerated from the catalytic cracking reactor to the inside of the first regenerator; a first regeneration exhaust gas outlet provided at an upper portion of the first regenerator and used for discharging the regeneration exhaust gas in the first regenerator; and an optional first recycled exhaust gas inlet provided at the bottom of the first regenerator and communicating with the first regenerator exhaust gas outlet for recycling a portion of the exhaust gas discharged from the first regenerator back to the first regenerator; The second regenerator comprises: a second oxygen-containing gas inlet provided at the bottom of the second regenerator and used to supply an oxygen-containing gas to the second regenerator; an optional second gaseous fuel inlet disposed above the second oxygen-containing gas inlet and used to supply gaseous fuel to the second regenerator; an optional second gas distributor configured to distribute the gas fuel provided from the second gas fuel inlet; a regenerated catalyst outlet, which is used to return the regenerated catalyst to the catalytic cracking reactor; a second regeneration exhaust gas outlet provided at an upper portion of the second regenerator and used for discharging the regeneration exhaust gas in the second regenerator; and 12. The catalyst regeneration system of claim 10 or 11, further comprising an optional second recycled exhaust gas inlet provided at the bottom of the second regenerator and connected to the first regenerated exhaust gas outlet and / or the second regenerated exhaust gas outlet for recycling a portion of the exhaust gas back to the second regenerator.

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