Method and system for regenerating catalytic cracking catalysts using bio-based liquid phase fuels

Abstract

The present disclosure is a catalyst regeneration method suitable for a fluid catalytic cracking unit. The fluid catalytic cracking unit includes a catalytic cracking reactor and a catalyst regenerator. The regeneration method includes the steps of: 1) providing a bio-based liquid phase fuel; 2) introducing the bio-based liquid phase fuel into the steam stripping section of the catalytic cracking reactor or into the catalyst regenerator; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen content of the oxygen-containing gas being 14-28 vol%; 4) feeding a spent catalyst from the catalytic cracking reactor into the catalyst regenerator, and contacting the spent catalyst with the bio-based liquid phase fuel or its residue therein and the oxygen-containing gas therein to perform coke combustion regeneration; The method can greatly reduce the carbon emission of the catalytic cracking unit and can also provide energy for other process units. In addition, a part of the bio-based liquid phase fuel can also be converted into chemical products, thereby realizing the green and low-carbon development of the catalytic cracking process.

Description

Detailed Description of the Invention

[0001] [Technical field] The present application relates to a method and system for regenerating a catalytic cracking catalyst that employs a bio-based liquid phase fuel for the regeneration of a carbon-containing catalytic cracking catalyst.

[0002] 〔background〕 At present, the development of the global oil refining industry is facing multiple challenges, such as new energy substitution, increasingly stringent requirements for energy conservation and emission reduction. Flexible adjustment of the cracking production process, reduction of carbon dioxide emissions, and mitigation of climate change are necessary paths for the transformation of economic growth patterns in the oil refining industry and maintaining sustainable development. It is urgent to achieve carbon peaking in 2030 and carbon neutrality in 2060. The 14th Five-Year Plan formulated a carbon peaking action plan and clearly called for accelerating green development, and China's national emissions trading system was officially launched in 2021. Therefore, it is essential to effectively reduce carbon emissions in the oil refining and chemical production processes, and the research of low-carbon catalytic cracking processes for oil reduction and chemical production increase is an important task for the future of oil refineries. Carbon emissions in the heavy oil processing process mainly include catalytic cracking coke combustion, hydrogen production process, exhaust gas emissions from equipment such as boilers, and energy consumption in technological processes. Catalytic cracking units are the core equipment in oil refineries. The carbon emissions caused by coke combustion in catalytic cracking regenerators account for 24-55% of the total carbon emissions of oil refineries and nearly 1% of the national carbon dioxide emissions. It is a key point in reducing carbon dioxide emissions in the petrochemical industry.

[0003] On the other hand, bio-based liquid fuels such as biomass oil produced from biomass or crude glycerin, a by-product of the biodiesel industry, have complex compositions. Therefore, it is difficult to use them directly, and refining and separation further increase the cost. Effective development and utilization of biological resources has become an urgent problem to be solved.

[0004] CN1600431A discloses an incomplete regeneration flue gas combustion technology. The incomplete regeneration flue gas combustion technology adopts a method of supplementing air in the incomplete regeneration flue gas to continuously burn the CO in the unregenerated flue gas, thereby increasing the temperature of the flue gas, improving the recovery efficiency of the flue gas, and maximizing the pressure of the recovered flue gas, thereby reducing the energy consumption of the device. Although the method can improve the energy utilization efficiency, it cannot effectively reduce carbon dioxide emissions.

[0005] US20080153689A1 discloses a system and method for reducing carbon dioxide emissions in a fluid catalytic cracking unit, the method comprising: compressing a first gas at an inlet pressure to a predetermined elevated pressure to define a compressed gas, and combusting a second gas with said compressed gas to a predetermined temperature to define a heated gas; expanding the heated gas to a predetermined low pressure to define a feed gas; introducing a feed gas into a regenerator; Including, The hot feed gas provides heat to the regenerator to burn off the coke from the spent catalyst in the reactor and achieve a certain ratio of carbon monoxide in the exhaust gas, which reduces the concentration of carbon dioxide in the exhaust gas.

[0006] TW201317354A discloses a method for synthesizing polyhydroxyalkanoates using crude glycerol as raw material and microorganisms. The method includes injecting the crude glycerol into a fermentation tank containing a bacterial strain and fermenting it under specific conditions to obtain polyhydroxyalkanoates. However, the products of this process need to be extracted and separated. In addition, the production efficiency is low. Therefore, there is a limit to large-scale industrial application.

[0007] The reaction-regeneration system of the catalytic cracking unit is a heat balance process of cyclic heat extraction-heat release. The heat generated by the coke combustion in the regeneration system is supplied to the reaction system. The production mode of oil reduction and chemical product increase is beneficial to promoting the sustainable development of the oil refining industry, but more reaction heat is also needed. When the combustion amount is not enough to meet the energy consumption of the unit, additional fossil fuel is generally added to supplement the heat, so that the carbon dioxide emission increases and resources are wasted. There is a contradiction between the development trend and the environmental protection requirements. The optimization of the regeneration process or the reuse of the discharged carbon dioxide can also reduce the carbon dioxide emission to a certain extent. However, the above technical path mainly aims at reducing the emission of carbon dioxide generated in the regeneration process into the atmosphere, and does not reduce the generation of carbon dioxide. Meanwhile, the liquid-phase crude product of bio-based origin is difficult to use directly. Its separation and purification process is complicated and the cost is high. However, the liquid-phase crude product can be added as fuel for direct combustion without cumbersome separation. This can be combined well with the requirement that catalytic cracking units need additional fuel for heat supplementation. Bio-based fuel belongs to green zero-carbon energy and can effectively reduce carbon dioxide emissions.

[0008] Therefore, the utilization of bio-based liquid-phase crude products is combined with catalytic cracking, so that the conflict of development of catalytic cracking units can be alleviated and the approach of utilizing biomass can be broadened. Carbon dioxide emissions are reduced while meeting the energy supply required by the equipment. Low-carbon development is realized.

[0009] DISCLOSURE OF THEINVENTION The present application aims to provide a catalyst regeneration method and a catalyst regeneration system suitable for a fluid catalytic cracking unit, which utilizes a bio-based liquid phase fuel as an energy source for the catalytic cracking unit. The catalyst regeneration method and the catalyst regeneration system can reduce carbon dioxide emissions derived from fossil energy while satisfying the heat balance of the catalytic cracking unit. The catalyst regeneration method and the catalyst regeneration system can partially convert the bio-based liquid phase crude product into a high value-added product, and realize a high efficiency utilization of the crude product.

[0010] In order to achieve the above object, in one aspect, the present application provides a catalyst regeneration method suitable for a fluid catalytic cracking unit including a catalytic cracking reactor and a catalyst regenerator. The regeneration method includes: 1) providing a bio-based liquid phase fuel; 2) introducing the bio-based liquid phase fuel into a catalyst regenerator or into the stripping section of a catalytic cracking reactor; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen-containing gas has an oxygen content of 14 to 28 volume percent; and, 4) delivering the spent catalyst from the catalytic cracking reactor to a catalyst regenerator where the spent catalyst is contacted with the bio-based liquid phase fuel or a residue thereof, and an oxygen-containing gas for coke combustion regeneration; Includes.

[0011] Preferably, the operating temperature of the catalyst regenerator is within the range of 550 to 750° C., and the average catalyst residence time is within the range of 1.0 to 20.0 minutes.

[0012] In another aspect, the present application provides a catalyst regeneration system suitable for use in a fluid catalytic cracking unit, the catalyst regeneration system comprising a biomass processing unit and a catalyst regeneration unit, The biomass processing unit is used for liquefying biomass to obtain a bio-based liquid phase fuel, and includes a biomass liquefaction treatment device, a dehydration device, and a storage tank; The biomass liquefaction treatment device is preferably selected from a biomass hydrolysis fermentation device, a biomass pyrolysis device, a biomass hydrothermal liquefaction device, and a biomass alcohol thermal liquefaction device, or a combination thereof, and includes a biomass inlet and a liquid phase product outlet. The liquid phase product outlet of the biomass liquefaction treatment device is connected to the inlet of the dehydration device, and the outlet of the dehydration device is connected to the inlet of the storage tank. The catalyst regeneration unit is used to regenerate spent catalyst from a catalytic cracking reactor and comprises a catalyst regenerator, the catalyst regenerator including a spent catalyst inlet, an oxygen-containing gas inlet, an optional liquid-phase fuel inlet, a regenerated exhaust gas outlet, and a regenerated catalyst outlet; The outlet of the storage tank is in communication with the liquid phase fuel inlet of the catalyst regenerator or the stripping section of the catalytic cracking reactor.

[0013] Preferably, the regeneration system further comprises a spent catalyst delivery inclined pipe communicating the catalytic cracking reactor with a spent catalyst inlet of the catalyst regenerator; The outlet of the storage tank is connected to the stripping section of the catalytic cracking reactor, so that the bio-based liquid phase fuel from the storage tank enters the stripping section, and then the reaction residue of the bio-based liquid phase fuel is transported together with the spent catalyst through the spent catalyst delivery inclined pipe to the spent catalyst inlet of the catalyst regenerator; Or, alternatively, A mixing tank is disposed on the spent catalyst discharge inclined pipe, and the outlet of the storage tank is connected to the mixing tank, so that the bio-based liquid phase fuel from the storage tank and the spent catalyst are mixed in the mixing tank and then transported to the spent catalyst inlet of the catalyst regenerator via the spent catalyst discharge inclined pipe.

[0014] Compared with existing catalytic cracking catalyst regeneration methods and systems, the method and system of the present application have the following advantages: (1) Bio-based liquid fuel belongs to green zero-carbon energy, which is derived from carbon dioxide taken from the air by plants instead of fossil energy, and is a neutral carbon emission process. Bio-based liquid fuel is used to provide energy to catalytic cracking units, so that the consumption of fossil energy and the emission of carbon dioxide in the operation process can be reduced, and the low-carbon development of oil refining can be realized; (2) Bio-based liquid fuels are easy to obtain and can be obtained by liquefying biomass. The storage capacity of biomass resources is large and the liquefaction process is simple. Bio-based liquid fuels can also be derived from industrial by-products such as biodiesel; (3) The bio-based liquid fuel can be introduced into the catalytic cracking unit without separation or purification, and coupled with the catalytic cracking process, so that the biomass utilization process is simplified, the cost is saved, and the utilization mode and method of biomass energy is expanded; (4) The bio-based liquid fuel can be introduced into the catalytic cracking unit to not only supply energy to the unit, but also be partially converted into chemical products, improving the economic value and causing no adverse effects on the original catalytic cracking reaction process; (5) Bio-based liquid-phase fuels have a high hydrogen content and can generate a large amount of steam in the combustion process. Therefore, on the one hand, by adjusting and controlling the operating conditions of the regeneration process, steam can be used to age the catalyst, so that the selectivity of the target low-carbon olefin products is improved. On the other hand, when the catalyst is required to have high activity, the adverse effect of steam on the activity of the catalyst can be weakened by optimizing the regeneration process, so that the high activity of the catalyst can be maintained; (6) The excess heat generated by the regeneration system can be used to generate high-pressure steam to supply other equipment. After the generated exhaust gas is subjected to energy recovery, the carbon dioxide in the exhaust gas can be separated and captured, thereby achieving negative carbon emissions.

[0015] Additional features and advantages of the present application are set forth in the detailed description that follows.

[0016] 〔drawing〕 The accompanying drawings, which may provide a further understanding of the present application and which constitute a part of this specification, together with the following detailed description, illustrate and do not limit the present application. In the drawings: FIG. 1 is a schematic diagram of a preferred embodiment of the catalyst regeneration method and system of the present application; FIG. 2 is a schematic diagram of another preferred embodiment of the catalyst regeneration method and system of the present application; and, FIG. 3 is a schematic diagram of yet another preferred embodiment of the catalyst regeneration method and system of the present application.

[0017] Detailed Description The following describes the embodiments of the present application in detail with reference to the drawings. It should be understood that the specific embodiments described herein are only used to illustrate and explain the present application, and are not used to limit the present application.

[0018] As used herein, the word "exemplary" means "serving as an embodiment, example, or illustration." Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. While various aspects of the embodiments are illustrated in drawings, the drawings are not necessarily drawn to scale unless specifically indicated.

[0019] Any specific value disclosed herein (including the endpoints of a range of values) is not limited to the exact value, but is understood to encompass all possible values ​​close to the exact value, for example, within ±5% of the exact value. Also, for any range of values ​​disclosed, any combination between the endpoints of the range, between the endpoints and a specific point in the range, and between specific points, can result in one or more new ranges of values, and such new ranges of values ​​are also to be considered specifically disclosed herein.

[0020] In this application, the terms "upstream" and "downstream" are used in reference to the direction of flow of reactants. For example, if the reactants flow from bottom to top, "upstream" refers to a lower position and "downstream" refers to an upper position.

[0021] It should be noted that in this application, the directions or positional relationships specified by terms such as "upper", "lower", "inner", "outer", "front", "rear", "left", "right" and the like are directions or positional relationships based on the implementation state of this application. They are merely for convenience to explain and simplify the description of this application. They do not specify or suggest that the devices or elements referenced must have a particular orientation or must be constructed and operated in a particular direction. Therefore, they should not be understood as limitations of this application.

[0022] It should be noted that in this application, the terms "mounted," "connected," "coupled," and "in communication" are to be broadly interpreted unless expressly specified or limited. The specific meaning of the above terms in this application can be understood by those skilled in the art according to the specific situation. For example, in this application, the term "in communication" includes both the case where two are directly in communication with each other and the case where two are in communication with each other via one or more intermediate devices.

[0023] Unless otherwise defined, terms used herein have the same meaning as commonly understood by one of ordinary skill in the art, and if a term is defined herein and that definition differs from the definition commonly understood in the art, the definition herein shall control.

[0024] In this application, everything not mentioned can be directly applied to what is known in the art without any changes, except as explicitly described. Moreover, any embodiment described in this specification may be freely combined with one or more other embodiments described in this specification, and the technical solutions or concepts formed thereby shall be considered as part of the original disclosure or original specification of this application, and shall not be considered as new matters not disclosed or contemplated in this specification, unless such combination is considered to be obviously unreasonable by those skilled in the art.

[0025] All patent and non-patent literature referenced herein, including but not limited to textbooks and journal articles, is hereby incorporated by reference in its entirety.

[0026] In addition, the technical features related to different embodiments of the present application described below may be combined with each other unless they are mutually contradictory.

[0027] As explained 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 method comprising: 1) providing a bio-based liquid phase fuel; 2) introducing the bio-based liquid phase fuel into a catalyst regenerator or into the stripping section of a catalytic cracking reactor; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen-containing gas has an oxygen content of 14 to 28 volume percent; and, 4) sending spent catalyst from the catalytic cracking reactor to a catalyst regenerator where the spent catalyst is contacted with the bio-based liquid phase fuel or a residue thereof, and an oxygen-containing gas for coke combustion regeneration; The present invention provides a regeneration method, comprising:

[0028] In a preferred embodiment, the operating temperature of the catalyst regenerator is within a range of 550 to 750° C., and the average catalyst residence time is within a range of 1.0 to 20.0 minutes.

[0029] In this application, the term "bio-based liquid phase fuel" refers to liquid phase fuels derived from various biomass sources, such as liquid phase products obtained from the liquefaction process of biomass, and bio-based crude glycerol produced as an industrial by-product, such as biodiesel.

[0030] In some specific embodiments, the bio-based liquid phase fuel is a liquid phase product obtained by liquefaction of biomass. The liquefaction of biomass can be hydrolysis fermentation, pyrolysis, hydrothermal liquefaction, and / or alcohol thermal liquefaction, and the bio-based liquid phase fuel can be alcohol-based fuel and / or biomass oil. The crude bio-based liquid fuel product obtained by liquefaction of biomass only needs to be dehydrated before it can be used in the method of the present application, and does not need to go through other separation and purification processes, thereby achieving efficient utilization of bio-based liquid fuel.

[0031] In another specific embodiment, the bio-based liquid phase fuel is crude glycerol, which is a by-product of biodiesel industry, grease saponification industry, fatty alcohol industry, etc. The bio-based crude glycerol mainly comprises 10-90% by weight glycerol, 1-30% by weight methanol, 1-30% by weight fatty acids (esters), fats, etc., and the balance is water.

[0032] The utilization of biomass is, in short, an indirect solar energy utilization process. The carbon in biomass comes from carbon dioxide taken in from the atmosphere by plants, and the energy consumed by the whole process also comes from solar energy. Therefore, the utilization of biomass energy is also a recycling of carbon elements and a carbon-neutral emission process. The zero-carbon energy bio-based liquid fuel is used as the power source of the catalytic cracking unit, so that the use of fossil energy in the operation process of the unit can be reduced, resources are saved, a reduction in carbon emissions is realized, and the contradiction between the increasing demand for energy supply from catalytic cracking and the environmental protection requirements is alleviated. The injected bio-based liquid fuel can be partially converted into chemical products, which has no impact on the original catalytic cracking process, thus providing a way to efficiently utilize biomass oil. The regeneration process may also adopt pure oxygen regeneration, so that the regeneration exhaust gas contains only carbon dioxide and oxygen, the cost of separation and capture is reduced, and negative carbon emissions can be realized.

[0033] 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 economic crops, waste, domestic wastewater, and industrial organic wastewater, etc. For example, agricultural and forestry biomass includes, but is not limited to, straw, rice husk, cotton stalk, etc., forestry biomass includes, but is not limited to, firewood, fast-growing forest, forestry processing residues, etc., aquatic plants include, but are not limited to, reeds, algae, etc., energy economic crops include, but are not limited to, cassava, canola, etc., waste includes, but is not limited to, waste paper, and domestic wastewater and industrial organic wastewater include, but are not limited to, cooling water, kitchen wastewater, organic wastewater discharged from brewing, food, and other industries.

[0034] In a preferred embodiment, the ratio between the amount of spent catalyst and the amount of bio-based liquid phase fuel introduced in step 2) is 5 to 400:1 by mass; In a preferred embodiment, the oxygen-containing gas is selected from air and diluted oxygen, which is diluted with recycled exhaust gas.

[0035] In a preferred embodiment, in step 2), the bio-based liquid phase fuel is directly injected into the regenerator through a distributor or into a mixing tank located on the spent catalyst delivery incline for transporting the spent catalyst. The bio-based liquid phase fuel is premixed with the spent catalyst from the catalytic cracking reactor in the mixing tank and then fed into the catalyst regenerator together with the spent catalyst. In this embodiment, it is beneficial to mix the spent catalyst with the liquid fuel uniformly, thereby avoiding the occurrence of localized hot spots in the regenerator bed, which may impair catalyst performance.

[0036] In another preferred embodiment, in step 2), the bio-based liquid phase fuel is injected into the stripping section of the catalytic cracking reactor to contact and react with the coked catalyst. The residue portion after the reaction is sent to the catalyst regenerator together with the spent catalyst. In this embodiment, by reacting the bio-based liquid phase fuel with the coked catalyst, a part of the liquid phase fuel can be converted into high-value chemical products, such as propylene. The high-value chemical products, such as propylene, enter a product fractionation unit together with the catalytic cracking products and are recovered as products, thereby achieving full and effective utilization of the bio-based liquid phase fuel.

[0037] In a preferred embodiment, the catalyst regenerator is a single-stage regenerator, and the operating conditions of the regenerator include a temperature of 570 to 750° C., an average catalyst residence time of 3 to 20 minutes, and a superficial linear velocity of the gas of 0.4 to 1.8 m / s.

[0038] Bio-based liquid-phase fuel produced by biomass liquefaction has a high hydrogen content, so a large amount of steam is generated when it is burned in a 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. The liquid-phase fuel is fed only into the coke burning section of the two-stage regenerator or only into the first regenerator of the dual regenerator, or fed into the coke burning section and the regenerating section of the two-stage regenerator or into the first and second regenerators of the dual regenerator simultaneously, preferably fed only into the coke burning section or only into the first regenerator, and the operating conditions in the two-stage regenerator and the dual regenerator are appropriately optimized.

[0039] In another preferred embodiment, the catalyst regenerator is a two-stage regenerator comprising a coke burning section and a regeneration section in fluid communication. In step 2), the bio-based liquid phase fuel is introduced into the stripping stage of the catalytic cracking reactor or into the coke burning section and / or the regeneration section of the regenerator. In step 3), an oxygen-containing gas is introduced into the bottom of each of the coke burning and regeneration sections. In step 4), the spent catalyst is sent to the coke burning section. More preferably, the operating conditions of the coke burning section include an operating temperature of 560°C to 720°C, an average catalyst residence time of 10 to 150 seconds, and a superficial linear velocity of the gas of 0.8 to 3.0 m / s, and the operating conditions of the regeneration section include an operating temperature of 580 to 750°C, an average catalyst residence time of 1.0 to 5.0 minutes, and a superficial linear velocity of the gas of 0.3 to 0.8 m / s. Even more preferably, the operating temperature of the regenerating section is 10-150° C. higher than the operating temperature of the coke burning section.

[0040] In a further preferred embodiment, the operating conditions of the coke burning section include 600-700°C with an average catalyst residence time of 60.0-120.0 seconds, and the operating conditions of the regeneration section include 650-720°C with an average catalyst residence time of 2.0-4.0 minutes, so that the steam generated by the combustion of the liquid phase fuel can be utilized to age the catalyst in the catalyst regeneration process, thereby improving the selectivity of the catalyst to the target low carbon olefin products, avoiding the excessive influence of the steam on the activity of the catalyst, and suitable for the fluid catalytic cracking process to mainly produce low carbon olefins. In such a preferred embodiment, the liquid phase fuel may be injected only into the coke burning section of the regenerator, or into both the coke burning section and the regeneration section of the regenerator.

[0041] In yet another more preferred embodiment, the operating conditions of the coke burning section include 560°C-650°C with an average catalyst residence time of 10.0-60.0 seconds, and the operating conditions of the regenerator section include 600°C-680°C with an average catalyst residence time of 1.0-3.0 minutes, thereby sufficiently weakening the adverse effect of steam on the activity of the catalyst, so that the resulting regenerated catalyst may have higher catalytic cracking activity and may be suitable for fluid catalytic cracking to produce primarily fuel oil. In such a preferred embodiment, liquid phase fuel is injected only into the coke burning section of the regenerator.

[0042] In another preferred embodiment, the catalyst regenerator is a dual regenerator comprising a first regenerator and a second regenerator in fluid communication. In step 2), the bio-based liquid phase fuel is introduced into the stripping section of the catalytic cracking reactor, the first regenerator, and / or the second regenerator. In step 3), an oxygen-containing gas is introduced into the bottom of the first regenerator and into the bottom of the second regenerator, respectively. In step 4), the spent catalyst is sent to the first regenerator. More preferably, the operating conditions of the first regenerator include an operating temperature of 550-720°C, an average catalyst residence time of 1.0-5.0 minutes, and a superficial linear velocity of the gas of 0.4-1.0 m / s, and the operating conditions of the second regenerator include an operating temperature of 570-750°C, an average catalyst residence time of 1.0-10.0 minutes, and a superficial linear velocity of the gas of 0.3-0.8 m / s. Even more preferably, the operating temperature of the second regenerator is 10 to 150° C. higher than the operating temperature of the first regenerator.

[0043] In a further preferred embodiment, the operating conditions of the first regenerator include 600-700°C with an average catalyst residence time of 2.0-5.0 minutes, and the operating conditions of the second regenerator include 650-720°C with an average catalyst residence time of 3.0-7.0 minutes, so that the steam generated by the combustion of the gas phase fuel can be utilized to age the catalyst in the catalyst regeneration process, thereby improving the selectivity of the catalyst to the target low carbon olefin products, avoiding the excessive influence of the steam on the activity of the catalyst, and suitable for the fluid catalytic cracking process to produce chemical products such as mainly low carbon olefins. In such a preferred embodiment, the liquid phase fuel may be injected only into the first regenerator or into both the first and second regenerators.

[0044] In yet another more preferred embodiment, the operating conditions of the first regenerator include 550°C-650°C with an average catalyst residence time of 1.0-4.0 minutes, and the operating conditions of the second regenerator include 600°C-680°C with an average catalyst residence time of 2.0-5.0 minutes, thereby sufficiently weakening the adverse effect of steam on the activity of the catalyst, so that the resulting regenerated catalyst may have higher catalytic cracking activity and may be suitable for fluid catalytic cracking to mainly produce fuel oil. In such a preferred embodiment, liquid phase fuel is injected only into the first regenerator.

[0045] In a preferred embodiment, step 1) further comprises subjecting biomass to a liquefaction process to obtain the bio-based liquid phase fuel, the liquefaction process being selected from the group consisting of hydrolysis fermentation, pyrolysis, hydrothermal liquefaction, and alcohol thermal liquefaction. The bio-based liquid phase fuel is selected from the group consisting of alcohol-based fuel and biomass oil.

[0046] In a further preferred embodiment, step 1) comprises subjecting the biomass to acid or enzymatic hydrolysis and then subjecting the resulting hydrolysate to microbial fermentation to produce an aqueous alcohol-based fuel. The liquid phase product obtained by fermentation is dehydrated to obtain an alcohol-based fuel, which can be directly used as a liquid phase fuel of the present application without separation. Further preferably, the temperature of the acid hydrolysis is below 200°C, the temperature of the enzymatic hydrolysis is below 70°C, the fermentation temperature is below 50°C, preferably between 35 and 50°C, and the microorganism is selected from bacteria, fungi, and yeasts.

[0047] According to the present application, the energy consumed by the process of preparing alcohol fuel from biomass may be at least partially, or completely, derived from renewable energy sources such as solar energy, green electricity, nuclear energy, etc.

[0048] According to the present application, the alcohol-based fuel comprises primarily ethanol, with minor amounts of methanol, saturated monohydric alcohols having 3 to 5 carbon atoms, organic acids, ethers, esters, ketones, aldehydes, etc. In one embodiment, the alcohol-based fuel comprises more than 90% ethanol, 5% or less water, and less than 10% methanol and C, based on the total weight of the alcohol-based fuel. 3-5 The remainder is a saturated monohydric alcohol.

[0049] In an even more preferred embodiment, step 1) comprises subjecting said biomass to rapid pyrolysis or flash pyrolysis at a heating rate of 100-200° C. / s with a residence time of 2-10 seconds to obtain biomass oil.

[0050] In yet another, more preferred embodiment, step 1) includes subjecting the biomass to hydrothermal liquefaction or alcohol thermal liquefaction at a treatment temperature of 200 to 350°C and a pressure of 4.0 to 7.0 MPa, wherein the solvent for the alcohol thermal liquefaction is selected from methanol and ethylene glycol, to obtain the biomass oil.

[0051] According to the present application, biomass liquefaction (such as pyrolysis, hydrothermal liquefaction, or alcohol thermal liquefaction) is carried out to obtain a biomass oil crude product. The biomass oil obtained after water removal can be directly used as a liquid phase fuel according to the present application. Here, the biomass oil is a mixture and includes acids, aldehydes, ketones, alcohols, esters, ethers, phenols, saccharides, oligomers, etc.

[0052] According to the present application, the energy consumed by the biomass liquefaction process is at least partially or completely derived from renewable energy sources such as solar energy, green electricity, nuclear energy, etc.

[0053] In some embodiments, the biomass oil is directly introduced into the mixing tank without separation, uniformly mixed with the catalyst through a nozzle, and then conveyed to the regenerator to contact with the catalyst and generate a combustion reaction. Preferably, the ratio of the spent catalyst to the introduced biomass oil is 10-300:1 (by weight).

[0054] In a preferred embodiment, the step 1) further includes a step of pretreating the biomass prior to the liquefaction treatment to enhance the efficiency of the hydrolysis or liquefaction treatment. The pretreatment method may be selected from a number of types, such as physical pretreatment, chemical pretreatment, biological pretreatment, physical and chemical pretreatment, and the specific method may be selected from one or more of crushing, drying, calcination, compression molding, ball mill treatment, microwave treatment, acid treatment, alkali treatment, steam explosion (abbreviated as "steam explosion"), carbon dioxide explosion, microbial decomposition, and the like.

[0055] In a preferred embodiment, in step 2), the bio-based liquid phase fuel is introduced into a catalyst regenerator or into the stripping section of a catalytic cracking reactor together with another source of bio-based product, which may be crude glycerol, a by-product from biodiesel industry, grease saponification industry, fatty alcohol industry, etc. Preferably, the crude glycerol comprises 10-90 wt.% glycerol, 1-30 wt.% methanol, 1-30 wt.% fatty acid or fatty acid ester, and the balance water.

[0056] In a preferred embodiment, in step 4), the temperature of the regenerator is controlled by a heat extraction system comprising one or more internal and / or external heat extractors so as not to exceed 750° C., preferably not to exceed 720° C. More preferably, the heat extraction system uses the heat extracted from the regenerator to generate high pressure steam to supply energy to the outside.

[0057] The injection mode of bio-based liquid-phase fuel can be well coordinated with the catalytic cracking process. The bio-based liquid-phase fuel is sprayed onto the spent catalyst for pre-mixing, so that on the one hand the bio-based liquid-phase fuel can be preheated, and on the other hand the local concentration can be prevented from becoming too high, and the local overheating state in the coke combustion process can be avoided. The pure oxygen regeneration process allows the regeneration exhaust gas to contain only carbon dioxide and oxygen, thereby reducing the cost of separation and capture and realizing negative carbon emissions. The bio-based liquid-phase fuel is injected into the stripping section, so that a part of the bio-based liquid-phase fuel can be converted into high-value chemical products, and the remaining part of the bio-based liquid-phase fuel is used to supply energy, so that the economic efficiency is improved and the original catalytic cracking reaction process is not affected.

[0058] In a preferred embodiment, the temperature in the catalyst regenerator is controlled not to exceed 750°C by a heat extraction system comprising 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 that is output to other units for energy supplementation. In such a preferred embodiment, the present application uses the energy generated by the regeneration system of the catalytic cracking unit to supply other operating units to become the power center of the refinery, thereby radically reducing the carbon emission of the refinery. According to the present application, biomass is introduced into the power center of the catalytic cracking unit, the unit operation is supplied with biomass energy, and the carbon dioxide emitted is not derived from fossil energy, so that the energy source can be fundamentally changed and carbon emission reduction is realized.

[0059] In a second aspect, the present application provides a catalyst regeneration system suitable for use in a fluid catalytic cracking unit, the catalyst regeneration system comprising a biomass processing unit and a catalyst regeneration unit; The biomass processing unit is used to liquefy biomass to obtain a bio-based liquid phase fuel, and includes a biomass liquefaction treatment device, a dehydration device, and a storage tank; The biomass liquefaction treatment device is preferably selected from a biomass hydrolysis fermentation device, a biomass pyrolysis device, a biomass hydrothermal liquefaction device, and a biomass alcohol thermal liquefaction device, or a combination thereof, and includes a biomass inlet and a liquid phase product outlet; The liquid phase product outlet of the biomass liquefaction treatment device is connected to the inlet of the dewatering device, and the outlet of the dewatering device is connected to the inlet of the storage tank; The catalyst regeneration unit is used to regenerate spent catalyst from a catalytic cracking reactor, and comprises a catalyst regenerator having a spent catalyst inlet, an oxygen-containing gas inlet, an optional liquid-phase fuel inlet, a regenerated exhaust gas outlet, and a regenerated catalyst outlet; The outlet of the storage tank is in communication with the liquid phase fuel inlet of the catalyst regenerator or the stripping section of the catalytic cracking reactor.

[0060] In a preferred embodiment, the biomass processing unit further comprises a biomass pretreatment device for pretreatment of the biomass; The pretreatment is selected from one or more of crushing, drying, torrefaction, compression molding, ball milling, microwave treatment, acid treatment, alkali treatment, steam explosion, carbon dioxide explosion, and microbial degradation.

[0061] In a preferred embodiment, the regeneration system further includes a spent catalyst delivery inclined pipe communicating the catalytic cracking reactor with a spent catalyst inlet of the catalyst regenerator; The outlet of the storage tank is connected to the stripping section of the catalytic cracking reactor, so that the bio-based liquid phase fuel from the storage tank enters the stripping section, and then the reaction residue, together with the spent catalyst, is transported to the spent catalyst inlet of the catalyst regenerator via the spent catalyst delivery inclined pipe.

[0062] In another preferred embodiment, the regeneration system further comprises a spent catalyst delivery incline pipe connecting the catalytic cracking reactor to the spent catalyst inlet of the catalyst regenerator. A mixing tank is disposed on the spent catalyst delivery incline pipe, and an outlet of the storage tank is connected to the mixing tank, so that the bio-based liquid phase fuel from the storage tank and the spent catalyst are mixed in the mixing tank and then transported to the spent catalyst inlet of the catalyst regenerator via the spent catalyst delivery incline pipe.

[0063] In another preferred embodiment, the liquid phase fuel inlet of the catalyst regenerator further comprises a liquid phase fuel distributor for injecting liquid phase fuel directly into the regenerator.

[0064] In a preferred embodiment, the catalyst regenerator comprises a coke burning section and a rich phase regeneration section, the rich phase regeneration section being located above the coke burning section, the outlet of the coke burning section being contained within the rich phase regeneration section, such that the coke burning section is in fluid communication with the rich phase regeneration section; The combustion section comprises: a first oxygen-containing gas inlet disposed at a bottom of the coke burning section for injecting an oxygen-containing gas into the coke burning section; an optional first liquid phase fuel inlet and an optional first liquid phase fuel distributor positioned above the first oxygen-containing gas inlet for direct injection of the bio-based liquid phase fuel from the storage tank into the coke combustion section; a spent catalyst inlet used for transporting spent catalyst from a catalytic cracking reactor to the interior of the coke burning section; and an optional first recycle exhaust gas inlet used to recycle a portion of the exhaust gas leaving the dense phase regeneration section back into the interior of the coke combustion section.

[0065] The dense phase regeneration section comprises: a second oxygen-containing gas inlet disposed at the bottom of the dense phase regeneration section and used for introducing an oxygen-containing gas into the dense phase regeneration section; an optional second liquid phase fuel inlet and an optional second liquid phase fuel distributor disposed above the second oxygen-containing gas inlet and used to direct the bio-based liquid phase fuel from the storage tank into the rich phase regeneration section; a regeneration exhaust gas outlet arranged at an upper portion of the dense phase regeneration section and used for discharging the regeneration exhaust gas in the dense phase regeneration section; the regenerated catalyst outlet used to return the regenerated catalyst to the catalytic cracking reactor; and an optional second recycle exhaust gas inlet used to recycle a portion of the exhaust gas discharged from the dense phase regeneration section back into the interior of the dense phase regeneration section.

[0066] In a further preferred embodiment, the dense phase regeneration section is further arranged with a heat extraction system comprising one or more internal and / or external heat extractors for controlling the temperature of the dense phase regeneration section and, optionally, generating high pressure steam to supply energy to the outside.

[0067] In another preferred embodiment, the catalyst regenerator comprises a first regenerator and a second regenerator, the second regenerator being disposed downstream of the first regenerator, the first and second regenerators being connected by a catalyst transfer line, and the catalyst material partially regenerated by the first regenerator being transferred to the second regenerator.

[0068] The first regenerator comprises: a first oxygen-containing gas inlet disposed at the bottom of the first regenerator and used for injecting an oxygen-containing gas into the first regenerator; an optional first liquid phase fuel inlet and an optional first liquid phase fuel distributor disposed above the first oxygen-containing gas inlet and used to supply the bio-based liquid phase fuel from the storage tank directly into a first regenerator; the spent catalyst inlet, used for transporting the spent catalyst from the catalytic cracking reactor to the inside of the first regenerator; and a first regenerator exhaust gas outlet, which is disposed at an upper portion of the first regenerator and is used to discharge the regenerator exhaust gas in the first regenerator.

[0069] The second regenerator comprises: a second oxygen-containing gas inlet disposed at the bottom of the second regenerator and used for injecting an oxygen-containing gas into the second regenerator; an optional second liquid phase fuel inlet and an optional second liquid phase fuel distributor disposed above the second oxygen-containing gas inlet and used to supply the bio-based liquid phase fuel from the storage tank directly into a second regenerator; the regenerated catalyst outlet used to return the regenerated catalyst to the catalytic cracking reactor; and a second regenerator exhaust gas outlet, which is disposed at an upper portion of the second regenerator and is used to discharge the regenerator exhaust gas in the second regenerator.

[0070] In a further preferred embodiment, the first and second regenerators further comprise a heat extraction system comprising one or more internal and / or external heat extractors for controlling the temperature of the first and second regenerators and, optionally, generating high pressure steam to effect an external power supply.

[0071] Preferred embodiments of the regeneration method and system of the present application are described in further detail below in conjunction with the accompanying drawings.

[0072] As shown in Figures 1, 2, and 3, the catalyst regeneration system of the present application is adapted to regenerate spent catalyst from a catalytic cracking reaction unit 100, and includes biomass processing units 300 and 500, and catalyst regeneration units 200, 400, and 600.

[0073] As shown in Figures 1, 2 and 3, in the catalytic cracking reaction unit 100, the catalytic cracking reactor 110 serves to carry out catalytic cracking reaction. A lifting medium is provided from its bottom inlet 102 to lift the regenerated catalyst (from the regenerator) entering through the regenerated catalyst inlet 103, and the feed oil entering through the feed oil inlet 101 contacts the catalyst to carry out catalytic cracking reaction. The oil and gas products of the reaction are separated by the oil separator 120. The separated oil and gas products are collected in the gas collection chamber 140 and then sent into the product separator 150 for separation to obtain various products. The separated spent catalyst is transported to the regeneration unit through the settler stripping section 130 and the spent catalyst outlet 131 for regeneration, thereby realizing reuse. The catalytic cracking reactor 110 suitable for this application may be various reactors commonly used in the art, such as a riser reactor, a fluidized bed reactor, a variable diameter reactor, and combinations thereof.

[0074] The biomass processing unit 300 shown in FIG. A biomass pretreatment device 310 for pretreatment of biomass; a biomass hydrolyzer 320 for subjecting the pretreated biomass to hydrolysis to obtain a hydrolysate; a hydrolysate fermenter 330 for carrying out a fermentation process on the hydrolysate to obtain a liquid phase product; a dehydration unit 340 for dehydrating the liquid phase product to obtain an alcohol-based fuel; and a storage tank 350 for storing the alcohol-based fuel.

[0075] As shown, biomass may be delivered to a pretreatment unit 310. After pretreatment, the biomass is delivered to a hydrolysis unit 320 to obtain a hydrolysate. The hydrolysate is transported to a fermentation unit 330, and the liquid phase product obtained by fermentation is transported to a dewatering unit 340 to remove water and then transported to a storage tank 350 for further reclamation processing.

[0076] The biomass processing unit 500 shown in FIG. A biomass pretreatment device 510 for biomass pretreatment; a biomass liquefaction processor 520 for processing the pretreated biomass to obtain a crude biomass oil product; a dehydration system 530 for performing a dehydration process on the crude biomass oil product to obtain a biomass oil; and a storage tank 540 for storing the biomass oil.

[0077] FIG. 1 shows a schematic diagram of a first preferred embodiment of the catalyst regeneration method and system of the present application. As shown in FIG. 1, the catalyst regeneration unit 200 includes a first regenerator 210, a first heat extractor 215, a second regenerator 240, and a second heat extractor 241, and the first regenerator 210 and the second regenerator 240 are in communication with each other so that the material of the first regenerator can enter the second regenerator. The first heat extractor 215 is configured to extract excess heat from the first regenerator for delivery to an external device. The second heat extractor 241 is configured to extract excess heat from the second regenerator for delivery to an external device.

[0078] In one embodiment, the first regenerator 210 is disposed below the second regenerator 240 and communicates with the second regenerator 240 through a riser 243. The riser 243 has one end opening into the interior of the first regenerator 210 and the other end opening into the interior of the second regenerator 240, such that the first regenerator 210 and the second regenerator 240 communicate with each other through the riser 243. This allows the material in the first regenerator 210 to enter the second regenerator 240 through the riser 243.

[0079] The first regenerator 210 is an alcohol-based fuel inlet 214 for injecting alcohol-based fuel from a storage tank into the first regenerator; a distributor 213 configured to distribute the alcohol-based fuel injected via the alcohol-based fuel inlet; a first oxygen-containing gas inlet 211 provided at the bottom of the first regenerator and used to inject a first oxygen-containing gas into the first regenerator; a spent catalyst inlet 216 for delivering spent catalyst from the catalytic cracking reactor to the inside of the first regenerator; The storage tank 350 is in communication with the alcohol-based fuel inlet 214 so that the alcohol-based fuel can be delivered to the interior of the first regenerator 210 .

[0080] Inside the first regenerator 210, the alcohol-based fuel is introduced through the spent catalyst inlet 216 and distributor 213 and mixed with the spent catalyst. Inside the first regenerator, the spent catalyst completes partial regeneration in the presence of a first oxygen-containing gas. In one embodiment, the operating conditions of the first regenerator include a temperature of 580° C. to 720° C., an average catalyst residence time of 1.0 to 5.0 minutes, and a superficial linear velocity of the gas of 0.4 to 1.0 m / s.

[0081] The exhaust gas produced in the first regenerator 210 may be separated by a first cyclone separation system 219 and then introduced into an exhaust gas energy recovery device 230 for energy recovery. The catalyst separated by the first cyclone separation system 219 enters the second regenerator 240 via a riser 243.

[0082] Due to the injection of alcohol-based fuel, a large amount of heat is generated during the regeneration process. If the temperature in the first regenerator is too high, it may adversely affect the activity of the catalyst. Therefore, the first regenerator 210 further comprises a heat extractor 215 for extracting excess heat from the first regenerator. The heat extractor may be an internal heat extractor (located inside the regenerator) or / and an external heat extractor (located outside the regenerator). The heat extractor may be one or more and may be used to supply excess energy generated by the first regenerator to other devices. The excess heat of the regeneration system may be used to generate high pressure steam by the heat extractor and output to other devices for energy supply. In one embodiment, the first regenerator bed temperature is controlled not to exceed 720° C. by comprising a heat extractor.

[0083] The second regenerator 240 is a second oxygen-containing gas inlet 242 at the bottom of the second regenerator for injecting a second oxygen-containing gas into the second regenerator; The catalytic cracking reactor is provided with a regenerated catalyst outlet 217 for delivering the regenerated catalyst.

[0084] Thus, the partially regenerated catalyst in the first regenerator 210 enters the second regenerator 240 via the riser to complete the regeneration. In one embodiment, the operating conditions of the second regenerator include a temperature of 570-750°C, an average catalyst residence time of 3.0-10.0 minutes, and a superficial linear velocity of gas of 0.3-0.8 m / s.

[0085] Optionally, an alcohol-based fuel is also introduced into the second regenerator 240. In one embodiment, the second regenerator 240 comprises: a second alcohol-based fuel inlet for injecting alcohol-based fuel from the storage tank into the second regenerator; and a second distributor configured to distribute the alcohol-based fuel injected via the second alcohol-based fuel inlet.

[0086] Similarly, a large amount of heat is generated during regeneration in the second regenerator. If the temperature in the second regenerator is too high, it may adversely affect the activity of the catalyst. The second regenerator 240 therefore also comprises a heat extractor 241 for extracting excess heat from said second regenerator. The heat extractor may be an internal heat extractor (located inside the regenerator) or / and an external heat extractor (located outside the regenerator). The heat extractor may be one or more and may be used to supply excess energy generated by the second regenerator to other devices. The excess heat of the regeneration system may be used to generate high pressure steam by the heat extractor and output to other devices for energy supply. In one embodiment, the second regenerator bed temperature is controlled by comprising a heat extractor so as not to exceed 750°C, for example not to exceed 720°C.

[0087] The exhaust gas produced in the second regenerator 240 may be separated by the second cyclone separator 220 and then introduced into the exhaust gas energy recovery system 230 for energy recovery.

[0088] In one embodiment, the alcohol-based fuel is introduced through a distributor into the first regenerator and optionally directly into the second regenerator to contact the catalyst and undergo a combustion reaction. The alcohol-based fuel is introduced into the first regenerator in a ratio of 60-100% by weight. The distributor is selected from a nozzle and a distribution pipe. In one embodiment, the ratio of spent catalyst to the introduced alcohol-based fuel is 10-400:1 (by weight).

[0089] In one embodiment, the first oxygen-containing gas and the second oxygen-containing gas are both air. The two-stage regeneration can improve the coke burning intensity and reduce the catalyst amount. Moreover, the two-stage regeneration can weaken the effect of steam on the catalyst in the regeneration process. In a further preferred embodiment, the steam can age the catalyst and enhance the product selectivity by further optimizing the operating conditions of the first and second regenerators.

[0090] Figure 2 shows a schematic diagram of a second preferred embodiment of the catalyst regeneration method and system of the present application. As shown in Figure 2, a regeneration unit 400 includes a regenerator 440, which includes a coke burning section 410 and a rich-phase regeneration section 450. The rich-phase regeneration section 450 is disposed above the coke burning section 410, and the outlet of the coke burning section is accommodated inside the rich-phase regeneration section, such that the coke burning section is in fluid communication with the rich-phase regeneration section. Thus, the rich-phase regeneration section 450 is connected to the coke burning section 410, so that the material from the coke burning section 410 can enter the rich-phase regeneration section 450 for complete regeneration.

[0091] The coke burning section 410 is a first oxygen inlet 411 located at the bottom of the coke burning section and used for injecting oxygen into said coke burning section; a spent catalyst inlet 416 for conveying spent catalyst from the catalytic cracking reactor to the interior of the coke burning section; The spent catalyst inlet 416 is connected to a spent catalyst delivery incline pipe which is in communication with the catalytic cracking reaction unit, and the mixing tank 550 is disposed in the spent catalyst delivery incline pipe; The storage tank 540 is in communication with the mixing tank 550, so that the biomass oil in the storage tank is transported to the mixing tank, mixed with the spent catalyst, and then transported to the regenerator 410. Optionally, the lower part of the coke burning section also includes a first recycle exhaust gas inlet 431, which is used to recycle a portion of the exhaust gas recovered by the regeneration section back into the inside of the coke burning section.

[0092] The dense phase regeneration section 450 is a second oxygen inlet 453 disposed at the bottom of the dense phase regeneration section and used for injecting oxygen into the dense phase regeneration section; A second circulation exhaust gas inlet 452 for circulating a portion of the exhaust gas recovered from the dense phase regeneration section and returning it to the inside of the dense phase regeneration section; and an exhaust gas outlet 432 disposed at an upper portion of the dense phase regeneration section; The dense phase regenerator section further comprises a heat extractor 415 for transporting heat outside the regenerator.

[0093] A portion of the coke burning section 410 is disposed outside the rich phase regeneration section 450 and a portion of the coke burning section 410 is disposed inside the rich phase regeneration section 450. The portion of the coke burning section 410 disposed outside the rich phase regeneration section 450 may have a larger cross-sectional area than the portion of the coke burning section 410 disposed inside the rich phase regeneration section 450. In one embodiment, the portion of the coke burning section 410 disposed outside the rich phase regeneration section 450 is in communication with the interior of the rich phase regeneration section 450 via a communication pipe 470. An outlet end of the communication pipe 470 is disposed inside the rich phase regeneration section 450.

[0094] When regeneration operation is performed, the biomass oil in the storage tank 540 is sprayed into the mixing tank 550 and mixed with the spent catalyst, then enters the coke burning section 410 to contact with the first oxygen entering through the oxygen-containing gas inlet 411, where a part of the coke burning reaction occurs. Then enters the dense phase regeneration section 450 for complete regeneration. At this time, pure oxygen is supplied through the oxygen inlet 452 to contact the partially coke burning catalyst, thereby further regenerating and burning the catalyst and the incompletely regenerated tail gas. The regenerated catalyst falls back into the dense phase regeneration section after separation in the cyclone separator 420, is discharged through the catalyst outlet 417, and is recycled back to the catalytic cracking reactor. A part of the tail gas discharged from the tail gas outlet 432 is subjected to energy recovery by the tail gas energy recovery system 430, and then separated by the carbon dioxide separation system 460, so that the carbon dioxide is captured. Another portion of the flue gas discharged from the flue gas outlet 432 is recycled to the bottom of the coke combustion section and to the bottom of the rich phase regeneration section.

[0095] In one embodiment, both gases injected through the first oxygen inlet 411 and the second oxygen inlet 452 are oxygen. However, the oxygen supplied through the first oxygen inlet 411 is mixed with the recycled exhaust gas after entering the coke combustion section to form an oxygen-carbon dioxide mixed gas. The amount of oxygen and / or recycled exhaust gas is controlled so that the oxygen concentration in the mixture does not exceed 28% by volume. Similarly, the oxygen introduced through the second oxygen inlet 453 is mixed with the recycled exhaust gas, etc. after entering the regeneration section to form an oxygen-carbon dioxide mixed gas. The amount of oxygen and / or recycled exhaust gas is controlled so that the oxygen concentration in the mixture does not exceed 28% by volume. The coke is burned under this atmosphere, so that the coke combustion intensity is improved. The inlet gas does not contain nitrogen, so that the energy consumed by gas preheating can be reduced. The concentration of carbon dioxide in the exhaust gas at the outlet of the regenerator is higher, which is convenient for separating and collecting carbon dioxide.

[0096] In one embodiment, the operating conditions of the coke combustion section include an operating temperature of 560-720° C., an average catalyst residence time of 10-120 seconds, and a superficial linear velocity of gas of 0.8-3.0 m / s.

[0097] In one embodiment, the operating conditions of the dense phase regeneration section include an operating temperature of 580-750° C., an average catalyst residence time of 1.0-5.0 minutes, and a superficial linear velocity of gas of 0.3-0.8 m / s.

[0098] In a specific embodiment, the coke burning ratio in the coke burning section is 40-50%, and the coke burning ratio in the dense phase regeneration section is 50-60%. The present application adopts pure oxygen for regeneration, and the regeneration flue gas only contains carbon dioxide and oxygen, which is convenient for separating and capturing carbon dioxide for further conversion and utilization, and realizes negative carbon emission.

[0099] Due to the injection of biomass oil, a large amount of heat is generated during the regeneration process. If the temperature in the regenerator is too high, it may adversely affect the activity of the catalyst. Therefore, the regeneration unit 400 also includes a heat extractor 415 for extracting excess heat from the regenerator. The heat extractor may be an internal heat extractor (located inside the regenerator) or / and an external heat extractor (located outside the regenerator). The heat extractor may be one or more and may be used to supply excess energy generated by the regenerator to other devices. The excess heat of the regeneration system may be used to generate high pressure steam by the heat extractor and output to other devices for energy supply. In one embodiment, the regenerator bed temperature is controlled by including a heat extractor so as not to exceed 750°C, for example not to exceed 720°C.

[0100] Figure 3 shows a schematic diagram of the third preferred embodiment of the catalyst regeneration method and system of the present application. As shown in Figure 3, the pre-lifting medium enters the bottom of the riser reactor 110 through the pipeline 101, and the regenerated catalyst from the spent catalyst delivery inclined pipe 618 moves upward under the action of the pre-lifting medium. The pre-heated feedstock oil is injected into the riser reactor through the pipeline 102 together with the atomized steam from the pipeline 103, contacts and reacts with the catalyst, and moves upward. The generated reaction products and the deactivated spent catalyst enter the cyclone separator in the settler 120 through the outlet section to realize the separation of the spent catalyst and the reaction products. The reaction products enter the gas collection chamber 150, and the catalyst returns to the settler through the dipleg. The desalted biomass oil is injected into the stripping section through the pipeline 131 to contact and react with the spent catalyst, and the product and stripped oil gas enter the gas collection chamber 150 after being subjected to cyclone separation. The oil and gas in the gas collection chamber 150 pass through a large oil and gas pipeline to the subsequent product fractionation unit 160. The unreacted biomass oil and spent catalyst enter the dense bed 612 of the first regenerator through the spent catalyst delivery inclined pipe 611 to carry out a combustion reaction in contact with oxygen diluted by the circulating exhaust gas. The catalyst is partially regenerated, and the liquid phase fuel is burned in the first regenerator to provide power. The partially regenerated catalyst enters the second regenerator 616 through the semi-regenerated catalyst pipe 614 for complete regeneration. After cyclone separation, a part of the exhaust gas is circulated to the regenerator, and a part of the exhaust gas enters the exhaust gas energy recovery system 630 to recover energy, and then enters the carbon dioxide separation and capture system 640. The fully regenerated catalyst is returned to the reactor through the regeneration pipeline 618 to achieve recycling.

[0101] In one embodiment, the crude biomass oil product may have one or more injection ports, preferably at the bottom and / or lower part of the stripping section. In one embodiment, the ratio of the amount of catalyst to the amount of biomass oil injected into the stripping section is 5-300:1 by mass.

[0102] In one embodiment, the regeneration process injects pure oxygen and the oxygen content in the regenerator is controlled below 28% by circulating the exhaust gas.

[0103] In one embodiment, the first regenerator is operated at 550-720°C, the average catalyst residence time is 1.0-5.0 minutes, and the gas superficial linear velocity is 0.4-1.0 m / s. The second regenerator is operated at 570-750°C, the average catalyst residence time is 1.0-10.0 minutes, and the gas superficial linear velocity is 0.3-0.8 m / s.

[0104] In one embodiment, when biomass oil is supplemented in the regenerator as fuel, more heat is generated, causing the temperature of the regenerator to be much higher, and the bed temperature of the regenerator is controlled by the heat extractor not to exceed 750°C, thereby preventing the influence on the catalyst. The heat extractor is an inner heat extractor or / and an outer heat extractor. The heat extractor may be one or more, and is used to control the temperature of the bed layer and collect the excess heat. The excess heat of the regenerative system is used to generate high-pressure steam through the heat extractor, and the high-pressure steam is output to other devices for energy supply.

[0105] In a specific embodiment, oxygen is directly introduced for coke combustion, the combustion efficiency is higher, the carbon dioxide concentration in the regeneration flue gas is higher, and the separation and capture of carbon dioxide in the flue gas is easier.

[0106] The catalyst suitable for use in 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 is not particularly limited. In an embodiment, the catalyst comprises a zeolite, an inorganic oxide, and optionally a clay. These components comprise 1-50 wt% of the zeolite, 5-99 wt% of the inorganic oxide, and 0-70 wt% of the clay, based on the weight of the total catalyst. The zeolite is an active component selected from the group consisting of mesoporous zeolites and / or optionally macroporous zeolites, the mesoporous zeolites representing 10 wt% to 100 wt% of the total weight of the zeolites, and the macroporous zeolites representing 0 wt% to 90 wt% of the total weight of the zeolites. The mesoporous zeolites are selected from one or more of ZSM series zeolites and / or ZRP zeolites. These zeolites may be modified with nonmetals such as phosphorus and / or transition metals such as iron, cobalt, and nickel. The macroporous zeolite is selected from one or more of hydrogen Y, rare earth Y, rare earth hydrogen Y, ultra-stable Y, and the like.

[0107] [Example] The present application is further illustrated below by means of examples, but the present application is not limited thereby.

[0108] The properties of the feedstock A used in the following Examples and Comparative Examples are shown in Table 1.

[0109] [Table 1]

[0110] Catalyst a was TCC, and the preparation process was as follows: 969g of halloysite (product of China Gaolian Earth Company, with a solid content of 73%) was pulped with 4300g of decationized water, 781g of pseudoboehmite (product of Shandong Shibo Stone Factory, with a solid content of 64%) and 144ml of hydrochloric acid (with a concentration of 30% and a specific gravity of 1.56) were added, stirred uniformly, and the mixture was left to stand at 60°C for 1 hour for aging. The pH was kept between 2 and 4. The mixture was cooled to room temperature. Then 5000g of the prepared high silica-alumina ratio mesopore shape selective ZSM-5 zeolite slurry containing chemical water was added. The mixture was stirred uniformly and spray-dried. Free Na + The aging process was as follows: Aging was performed in water vapor at 800°C for 15 hours. The properties are listed in Table 2.

[0111] [Table 2]

[0112] The preparation process of catalyst b was as follows: (1) NH4Cl (20g) was dissolved in 1000g of water. 100g (dry basis) of crystallized product ZRP-1 molecular sieve (manufactured by Qilu Petrochemical Company's Chemical Substance Factory, SiO2 / Al2O3=30, rare earth content RE2O3=2.0wt%) was added into the solution. After exchanging at 90℃ for 0.5 hours, a filter cake was obtained after filtration. 4.0g of H3PO4 (having a concentration of 85%) and 4.5g of Fe(NO3)3 were added and dissolved in 90g of water, and the filter cake was mixed with them, soaked and dried. Then the filter cake was roasted at a temperature of 550℃ for 2 hours to obtain MFI mesoporous molecular sieve containing phosphorus and iron. The obtained molecular sieve was 0.1Na2O・5.1Al2O3・2.4P2O5・1.5Fe2O3・3.8RE2O3・88.1SiO2 The elemental analytical chemical composition was:

[0113] (2) 75.4 kg of halloysite (an industrial product of Suzhou Porcelain Company, with a solid content of 71.6% by weight) was slurried with 250 kg of decationized water. 54.8 kg of pseudoboehmite (an industrial product of Dongyu Factory, with a solid content of 63% by weight) was added. The pH was adjusted to 2-4 with hydrochloric acid. It was stirred uniformly, left to stand and aged at 60-70°C for 1 hour. The pH was maintained at 2-4. The temperature was reduced to below 60°C. 41.5 kg of alumina sol (a product of Qilu Petrochemical Company's Chemical Modifier Factory, with an Al2O3 content of 21.7% by weight) was added and stirred for 40 minutes to obtain a mixed slurry.

[0114] (3) The phosphorus- and iron-containing MFI mesoporous molecular sieve (2 kg dry basis) prepared in step (1) was added to the mixed slurry obtained in step (2). It was stirred uniformly, spray-dried and molded. It was washed with an aqueous ammonium dihydrogen phosphate solution (phosphorus content is 1 wt%). Free Na + was then washed off and dried to obtain catalytic conversion catalyst sample b. Based on the total weight of catalyst b on a dry basis, the composition of catalyst b on a dry basis included 2 wt.% of MFI mesoporous molecular sieve containing phosphorus and iron, 36 wt.% of pseudoboehmite, 8 wt.% of alumina sol, and the balance of kaolin.

[0115] <Example 1> The experiments were carried out using the equipment shown in Figure 1, where the catalytic cracking reactor structure can be found as reactor 302 in Figure 4 of CN111718230A.

[0116] The process for producing biomass alcohol based fuel included the following steps: In the biomass processing unit 300, the biomass was subjected to a pretreatment of steam explosion. The pretreated biomass was subjected to acid hydrolysis. The hydrolyzate was transported to a fermenter and fermented at 35°C to obtain a fermentation liquid. The fermentation liquid was subjected to a dehydration process to obtain an alcohol-based fuel, where the alcohol content was 90%, the moisture content was 3%, and the balance was methanol and C, based on the total weight of the alcohol-based fuel. 3-5 It was a saturated monohydric alcohol.

[0117] The feedstock A was used as the reaction feedstock, and the catalytic conversion catalyst a was used as the catalyst. The spent catalyst was regenerated according to the method of the present application. The spent catalyst was conveyed from the spent catalyst delivery inclined pipe to the first regenerator and contacted with air and alcohol-based fuel (the weight ratio of the spent catalyst to the alcohol-based fuel was 60:1). The alcohol-based fuel was introduced into the first regenerator from the bottom of the first regenerator through a distribution pipe, so that a combustion reaction was generated. The exhaust gas was subjected to cyclone separation and then entered into the exhaust gas energy recovery system. A part of the regenerated catalyst entered into the second regenerator through a riser pipe for continuous regeneration. The exhaust gas was subjected to cyclone separation and then entered into the exhaust gas energy recovery system. The surplus energy generated by the regenerator was used to supply energy to the outside through a heat extractor.

[0118] The operating temperature of the first regenerator was 640°C, the average catalyst residence time was 3 minutes, and the gas superficial velocity was 0.5 m / s. The second regenerator was operated at 680°C, had an average catalyst residence time of 7 minutes, and a gas superficial velocity of 0.5 m / s. The regenerated catalyst was circulated back to the reactor and contacted with the feedstock to carry out the catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 3.

[0119] <Comparative Example 1> The experiment was carried out with reference to Example 1, except that instead of using a biomass processing unit, diesel, which served as a complementary energy source, was introduced from the first regenerator as fuel oil. The temperature of the first regenerator was 640°C, the average catalyst residence time was 3 minutes, and the superficial gas velocity was 0.5 m / s. The second regenerator had a temperature of 680°C, an average catalyst residence time of 7 minutes, and a superficial gas velocity of 0.5 m / s. The regenerated catalyst was circulated back to the reactor and contacted with the feedstock oil to carry out the catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 3.

[0120] [Table 3]

[0121] *Based on 100g of processed ingredients. **: Carbon dioxide emission index refers to the amount of carbon dioxide derived from fossil energy released when 1MJ of energy is generated by coke combustion in the regenerative system. The calculation method refers to the "Greenhouse Gas Emissions Calculation Method and Reporting Guidelines for China's Petrochemical Enterprises (Trial Implementation)" (hereinafter the same). Carbon dioxide generated by bio-based alcohol-based fuel is derived from carbon dioxide existing in the atmosphere, and is a neutral carbon emission process.

[0122] It can be observed from the data in Table 3 that in Example 1, when the bio-based alcohol-based fuel is used as a supplementary energy source, the regenerative system produces the same amount of energy, and the amount of carbon dioxide emitted is significantly reduced compared to that of Comparative Example 1, which is advantageous for radically reducing the amount of carbon dioxide emitted.

[0123] <Example 2> The experiments were carried out using the equipment shown in Figure 2, where the catalytic cracking reactor structure can be found as reactor 302 in Figure 4 of CN111718230A.

[0124] The biomass oil production process included the following steps: In the processing unit 500, the biomass was crushed and crushed, and the pretreated biomass was subjected to hydrothermal liquefaction. The liquefaction device has a temperature of 300° C., a pressure of 12 MPa, and a residence time of 10 minutes. Biomass oil fuel was obtained after the liquefaction product was dehydrated.

[0125] C5-C8 mixed olefins were the reaction raw materials (the molar ratio of C5:C6:C7:C8 olefins was 1:1:1:1). The catalytic conversion catalyst b was the catalyst. The method of the present application was used to regenerate the spent catalyst. In the mixing tank on the spent routine, biomass oil was sprayed onto the catalyst and mixed them uniformly. Here, the weight ratio of the spent catalyst to the introduced biomass oil was 135:1. The spent catalyst mixed with biomass oil was introduced into the regenerator and contacted with pure oxygen gas diluted by the circulating exhaust gas, and a combustion reaction occurred. First, partial regeneration occurred in the coke burning section, and then it rose to the dense phase regeneration section to complete the regeneration, and at the same time, a part of the exhaust gas from the cyclone separation system of the regenerator was returned to the coke burning section and the dense phase regeneration section. Here, the oxygen content of the coke burning section and the dense phase regeneration section was controlled not to exceed 28%. The surplus energy generated by the regenerator was used to supply energy to the outside through a heat extractor.

[0126] The coke combustion section had an operating temperature of 640°C, an average catalyst residence time of 90 seconds, and a superficial gas velocity of 1.0 m / s. The dense phase regeneration section had an operating temperature of 655°C, an average catalyst residence time of 1.5 minutes, and a superficial gas velocity of 0.5 m / s. The regenerated catalyst was circulated back to the reactor and contacted with the feedstock for catalytic cracking reactions. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 4.

[0127] <Comparative Example 2> The experiment was carried out with reference to Example 2, except that instead of using a biomass processing unit, diesel oil introduced from the coke burning section was used as a supplementary energy source. The coke burning section had a temperature of 640°C, an average catalyst residence time of 90 seconds, and a superficial gas velocity of 1.0 m / s. The dense phase regeneration section had a temperature of 655°C, an average catalyst residence time of 1.5 minutes, and a superficial gas velocity of 0.5 m / s. The regenerated catalyst was circulated back to the reactor and contacted with the feedstock for catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 4.

[0128] [Table 4]

[0129] *Based on 100g of processed ingredients. **: Carbon dioxide emission index refers to the amount of carbon dioxide derived from fossil energy released when 1 MJ of energy is produced by coke combustion in a regenerative system. Carbon dioxide produced by biomass oil is derived from carbon dioxide present in the atmosphere, and is a neutral carbon emission process.

[0130] It can be observed from the data in Table 4 that when light feedstock is used as cracking feedstock, the amount of carbon deposition is low, which is far from meeting the energy requirements of the device. In Example 2, when biomass oil is used as a supplementary energy source, the regeneration system produces the same amount of energy, and the amount of carbon dioxide emitted is greatly reduced compared with that of Comparative Example 2, which is beneficial for radically reducing the amount of carbon dioxide emission.

[0131] <Example 3> The experiments were carried out using the equipment shown in Figure 3, where the catalytic cracking reactor structure can be found as reactor 302 in Figure 4 of CN111718230A.

[0132] Example 3 used bio-based glycerol as the liquid phase fuel. The bio-based crude glycerol contained 65% by weight glycerol, 13% by weight methanol, 2% by weight methyl oleate, and the balance water.

[0133] Feedstock A was used as the reaction feedstock, and catalytic conversion catalyst a was used as the catalyst. After feedstock A reacted with catalyst a, coked catalyst and the first product were obtained. The coked catalyst entered the stripping section and contacted with the desalted bio-based crude glycerol (the weight ratio of the spent catalyst to the bio-based crude glycerol was 22:1). After the reaction, the second product was obtained. Meanwhile, part of the oil gas in the catalyst was stripped. The second product and the stripped oil gas entered the gas collection chamber and, together with the first product, entered the fractionator where they were separated into products by distillation range. The unreacted bio-based crude glycerol, heavier products, and spent catalyst entered the regenerator through the spent catalyst delivery inclined pipe, and contacted with oxygen diluted by the circulating exhaust gas to cause a coke combustion reaction. First, partial regeneration was carried out in the first regenerator, and then transported to the second regenerator through the semi-regenerated catalyst pipe to complete the regeneration. Meanwhile, part of the separated exhaust gas from the cyclone separation system of the regenerator was returned to the regenerator. The oxygen content in the regenerator was controlled not to exceed 28%. The surplus energy generated by the regenerator was used to supply energy to the outside via a heat extractor.

[0134] The first regenerator had an operating temperature of 640°C, an average catalyst residence time of 2 minutes, and a superficial gas velocity of 0.5 m / s. The second regenerator had an operating temperature of 670°C, an average catalyst residence time of 3 minutes, and a superficial gas velocity of 0.5 m / s. The regenerated catalyst was circulated back to the reactor and contacted with the feedstock for catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 5.

[0135] <Comparative Example 3> An experiment was carried out with reference to Example 3, except that instead of injecting bio-based glycerol into the stripping section, stripping steam was injected in the same amount as the bio-based glycerol used in Example 3. In addition, the heat balance was met by spraying diesel oil as fuel oil into the bottom of the first regenerator to supplement the heat. The first regenerator had an operating temperature of 640°C, an average catalyst residence time of 2 minutes, and a gas superficial velocity of 0.5 m / s. The second regenerator had an operating temperature of 670°C, an average catalyst residence time of 3 minutes, and a gas superficial velocity of 0.5 m / s. The regenerated catalyst was circulated back to the reactor and contacted with the feedstock oil to carry out the catalytic cracking reaction. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 5.

[0136] [Table 5]

[0137] *Based on 100g of processed ingredients. **:CO2 emission index refers to the amount of fossil-derived CO2 released per MJ of energy produced by coke combustion in a renewable system. Bio-based liquid-phase fuel combustion is a carbon-neutral process.

[0138] In Example 3, bio-based crude glycerol is injected into the stripping section instead of steam, and the yield of low carbon olefins in the product is increased. It can be observed from the data in Table 5 that when the regeneration system produces the same energy, the carbon dioxide emission is greatly reduced compared with that of Comparative Example 3. This is beneficial to fundamentally reduce the carbon dioxide emission.

[0139] Although the preferred embodiments of the present application have been described in detail, the present application is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solutions of the present application within the technical spirit of the present application, and all of these simple modifications are within the protection scope of the present application.

[0140] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction, and in order to avoid unnecessary repetition, the present application will not further describe the various possible combinations.

[0141] In addition, various embodiments of the present application may be combined in any manner, and as long as they are not contrary to the concept of the present application, they should also be considered as contents disclosed in the present application. [Brief description of the drawings]

[0142] [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.

Claims

1. 1. A catalyst regeneration method suitable for use in a fluid catalytic cracking unit comprising a catalytic cracking reactor and a catalyst regenerator, comprising: 1) providing a bio-based liquid phase fuel; 2) introducing the bio-based liquid phase fuel into a catalyst regenerator or into the stripping section of a catalytic cracking reactor; 3) introducing an oxygen-containing gas into the catalyst regenerator, the oxygen-containing gas has an oxygen content of 14 to 28 volume percent; Preferably, the oxygen-containing gas is selected from air and diluted oxygen, which is diluted with recycled exhaust gas; and, 4) transferring the spent catalyst from the catalytic cracking reactor to a catalyst regenerator where the spent catalyst is contacted with the bio-based liquid phase fuel or a residue thereof and an oxygen-containing gas for coke combustion regeneration; Preferably, the catalyst regenerator has an operating temperature of from 550 to 750° C. and an average catalyst residence time of from 1.0 to 20.0 minutes; A playback method comprising:

2. 2. The process of claim 1, wherein the ratio between the amount of spent catalyst and the amount of bio-based liquid phase fuel introduced in step 2) is 5-400:1 by mass.

3. In step 2), The bio-based liquid phase fuel is injected directly into the catalyst regenerator via a distributor. or 3. The process of claim 1 or 2, wherein the bio-based liquid phase fuel is injected into a mixing tank equipped on a spent catalyst delivery incline pipe for transporting spent catalyst, pre-mixed with the spent catalyst from the catalytic cracking reactor, and then fed into the catalyst regenerator together with the spent catalyst.

4. In step 2), the bio-based liquid phase fuel is injected into the stripping section of the catalytic cracking reactor and contacts and reacts with the coked catalyst; 3. The process of claim 1 or 2, wherein the reaction residue portion is sent together with the spent catalyst to a catalyst regenerator.

5. the catalyst regenerator is a single stage regenerator; 5. The process of claim 1, wherein the regenerator operating conditions include a temperature of 570 to 750° C., an average catalyst residence time of 3 to 20 minutes, and a superficial linear velocity of the gas of 0.4 to 1.8 m / s.

6. the catalyst regenerator is a two-stage regenerator comprising a coke burner section and a regenerator section in fluid communication; In step 2), the bio-based liquid phase fuel is introduced into the stripping stage of the catalytic cracking reactor or into the coke burning section and / or regeneration section of the regenerator; In step 3), an oxygen-containing gas is introduced into the bottom of each of the coke combustion section and the regeneration section; In step 4), the spent catalyst is fed into the coke burning section; Preferably, the operating conditions of the coke combustion section include an operating temperature of 560° C. to 720° C., an average catalyst residence time of 10 to 150 seconds, a superficial linear velocity of the gas of 0.8 to 3.0 m / s, and The operating conditions of the regeneration section include an operating temperature of 580 to 750° C., an average catalyst residence time of 1.0 to 5.0 minutes, and a superficial linear velocity of the gas of 0.3 to 0.8 m / s; More preferably, the operating temperature of the regenerator section is 10 to 150° C. higher than the operating temperature of the coke combustion section.

7. the catalyst regenerator is a dual regenerator comprising a first regenerator and a second regenerator in fluid communication; In step 2), the bio-based liquid phase fuel is introduced into the stripping section of the catalytic cracking reactor, into the first regenerator, and / or into the second regenerator; In step 3), an oxygen-containing gas is introduced into the bottom of the first regenerator and into the bottom of the second regenerator, respectively; In step 4), the spent catalyst is sent to the first regenerator; Preferably, the operating conditions of the first regenerator include an operating temperature of 550 to 720° C., an average catalyst residence time of 1.0 to 5.0 minutes, and a superficial linear velocity of the gas of 0.4 to 1.0 m / s, and the operating conditions of the second regenerator include an operating temperature of 570 to 750° C., an average catalyst residence time of 1.0 to 10.0 minutes, and a superficial linear velocity of the gas of 0.3 to 0.8 m / s; More preferably, the operating temperature of the second regenerator is 10 to 150° C. higher than the operating temperature of the first regenerator.

8. The step 1) further comprises subjecting biomass to a liquefaction process to obtain the bio-based liquid phase fuel; The liquefaction process is selected from the group consisting of hydrolysis fermentation, pyrolysis, hydrothermal liquefaction, and alcohol thermal liquefaction; The bio-based liquid phase fuel is selected from the group consisting of alcohol-based fuels and biomass oils; Preferably, the step 1) comprises: subjecting the biomass to acid or enzymatic hydrolysis and subjecting the resulting hydrolysate to microbial fermentation at a fermentation temperature of 35-50°C to obtain the hydrous alcohol-based fuel, wherein the microorganism is selected from bacteria, fungi, and yeasts; subjecting the biomass to rapid pyrolysis or flash pyrolysis to obtain biomass oil, the heating rate being 100-200° C. / sec and the residence time being 2-10 seconds; and, performing hydrothermal liquefaction or alcohol thermal liquefaction treatment on the biomass to obtain the biomass oil, wherein the treatment temperature is 200-350° C., the pressure is 4.0-7.0 MPa, and the solvent for the alcohol thermal liquefaction treatment is selected from methanol and glycol; The process according to any one of claims 1 to 7, comprising one or more of the following steps:

9. 9. The process of claim 8, wherein step 1) further comprises subjecting the biomass to a pretreatment selected from one or more of the following prior to the liquefaction treatment: crushing, drying, torrefaction, compression molding, ball milling, microwave treatment, acid treatment, alkali treatment, steam explosion, carbon dioxide explosion, and microbial degradation.

10. In step 2), the bio-based liquid phase fuel is introduced into the catalyst regenerator or into the stripping section of the catalytic cracking reactor together with another source of bio-based product, which is crude glycerol, a by-product from the biodiesel industry, the grease saponification industry, and / or the fatty alcohol industry; 10. The process of any one of claims 1 to 9, wherein the crude glycerol comprises 10-90% by weight glycerol, 1-30% by weight methanol, and 1-30% by weight fatty acid or fatty acid ester.

11. 1. A catalyst regeneration system suitable for use in a fluid catalytic cracking unit, comprising a biomass processing unit and a catalyst regeneration unit, The biomass processing unit is used to liquefy biomass to obtain a bio-based liquid phase fuel, and includes a biomass liquefaction treatment device, a dehydration device, and a storage tank; The biomass liquefaction treatment device is preferably selected from a biomass hydrolysis fermentation device, a biomass pyrolysis device, a biomass hydrothermal liquefaction device, and a biomass alcohol thermal liquefaction device, or a combination thereof, and has a biomass inlet and a liquid phase product outlet; The liquid phase product outlet of the biomass liquefaction treatment device is connected to the inlet of the dewatering device, and the outlet of the dewatering device is connected to the inlet of the storage tank; The catalyst regeneration unit is used to regenerate spent catalyst from a catalytic cracking reactor, and comprises a catalyst regenerator having a spent catalyst inlet, an oxygen-containing gas inlet, an optional liquid-phase fuel inlet, a regenerated exhaust gas outlet, and a regenerated catalyst outlet; A catalyst regeneration system, wherein the outlet of the storage tank is in communication with the liquid phase fuel inlet of the catalyst regenerator or with the stripping section of the catalytic cracking reactor.

12. The biomass processing unit further comprises a biomass pretreatment device used to pretreat the biomass; 12. The catalyst regeneration system of claim 11, wherein the pretreatment is selected from one or more of the following: crushing, drying, torrefaction, compression molding, ball milling, microwave treatment, acid treatment, alkali treatment, steam explosion, carbon dioxide explosion, and microbial degradation.

13. a spent catalyst delivery inclined pipe communicating the catalytic cracking reactor with a spent catalyst inlet of the catalyst regenerator; The outlet of the storage tank is connected to the stripping section of the catalytic cracking reactor, so that the bio-based liquid phase fuel from the storage tank enters the stripping section, and then the reaction residue is transported together with the spent catalyst through the spent catalyst delivery incline pipe to the spent catalyst inlet of the catalyst regenerator; Or, alternatively, 13. The regeneration system of claim 11 or 12, wherein a mixing tank is disposed on the spent catalyst discharge inclined pipe, and the outlet of the storage tank is connected to the mixing tank, so that the bio-based liquid phase fuel from the storage tank and the spent catalyst are mixed in the mixing tank and then transported to the spent catalyst inlet of the catalyst regenerator via the spent catalyst discharge inclined pipe.

14. The catalyst regenerator comprises a coke combustion section and a rich phase regeneration section; the dense phase regeneration section is located above the coke combustion section; an outlet of the coke burning section is received within the dense phase regenerating section, the coke burning section being in fluid communication with the dense phase regenerating section; The combustion section comprises: a first oxygen-containing gas inlet disposed at a bottom of the coke burning section for injecting an oxygen-containing gas into the coke burning section; an optional first liquid phase fuel inlet and an optional second liquid phase fuel distributor disposed above the first oxygen-containing gas inlet and used for direct injection of the bio-based liquid phase fuel from the storage tank into the coke combustion section; a spent catalyst inlet used for transporting spent catalyst from a catalytic cracking reactor to the interior of the coke burning section; an optional first circulation exhaust gas inlet used to circulate a portion of the exhaust gas leaving the dense phase regeneration section back into the coke combustion section; The dense phase regeneration section comprises: a second oxygen-containing gas inlet disposed at the bottom of the dense phase regeneration section and used for introducing an oxygen-containing gas into the dense phase regeneration section; an optional second liquid phase fuel inlet and an optional second liquid phase fuel distributor disposed above the second oxygen-containing gas inlet and used to direct the bio-based liquid phase fuel from the storage tank into the rich phase regeneration section; a regeneration exhaust gas outlet arranged at an upper portion of the dense phase regeneration section and used for discharging the regeneration exhaust gas in the dense phase regeneration section; the regenerated catalyst outlet used to return the regenerated catalyst to the catalytic cracking reactor; an optional second recycle exhaust gas inlet used to recycle a portion of the exhaust gas leaving the dense phase regeneration section back into the interior of the dense phase regeneration section; Optionally, the dense phase regeneration section further comprises a heat extraction system comprising one or more internal and / or external heat extractors for controlling the temperature of the dense phase regeneration section. The catalyst regeneration system of any one of claims 11 to 13.

15. The catalyst regenerator comprises a first regenerator and a second regenerator, The second regenerator is disposed downstream of the first regenerator, the first and second regenerators are connected by a catalyst transfer line, and the catalyst material partially regenerated by the first regenerator is transferred to the second regenerator; The first regenerator comprises: a first oxygen-containing gas inlet disposed at the bottom of the first regenerator and used for injecting an oxygen-containing gas into the first regenerator; an optional first liquid phase fuel inlet and an optional first liquid phase fuel distributor disposed above the first oxygen-containing gas inlet for supplying the bio-based liquid phase fuel from the storage tank directly into a first regenerator; a spent catalyst inlet used to transport the spent catalyst from the catalytic cracking reactor to the inside of the first regenerator; The first regenerator has a first regenerator exhaust gas outlet, the first regenerator exhaust gas outlet being disposed at an upper portion of the first regenerator and being used for discharging the regenerator exhaust gas in the first regenerator; The second regenerator comprises: a second oxygen-containing gas inlet disposed at the bottom of the second regenerator and used for injecting an oxygen-containing gas into the second regenerator; an optional second liquid phase fuel inlet and an optional second liquid phase fuel distributor disposed above the second oxygen-containing gas inlet and used to supply the bio-based liquid phase fuel from the storage tank directly into a second regenerator; the regenerated catalyst outlet used to return the regenerated catalyst to the catalytic cracking reactor; a second regenerator exhaust gas outlet, which is disposed at an upper portion of the second regenerator and is used to discharge the regenerator exhaust gas in the second regenerator; Optionally, the first and second regenerators further comprise a heat extraction system comprising one or more internal and / or external heat extractors for controlling the temperature of the first and second regenerators. A catalyst regeneration system according to any one of claims 11 to 13.

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