Catalytic cracking reaction-regeneration process and apparatus

Abstract

The application relates to a catalytic cracking reaction-regeneration method and device, which comprises the following steps: S1, after raw oil and a catalytic cracking catalyst are reacted in a catalytic cracking reactor of a catalytic cracking reaction system, first products and a carbon deposition catalyst are obtained through separation, and the carbon deposition catalyst flows to a stripping section of a settler; S2, bio-oil is introduced into the stripping section to contact and react with the carbon deposition catalyst, thereby obtaining spent catalyst and second products; S3, a mixture containing the spent catalyst and unreacted bio-oil is transported into a regeneration system and is subjected to regeneration treatment by inputting oxygen-containing regeneration gas, and the regenerated catalyst is transported back to the catalytic cracking reaction system for recycling. The method and device can be used for producing high-value products by using bio-oil and reducing carbon dioxide emission from fossil energy.

Description

Technical Field

[0001] This invention relates to the field of catalytic cracking, and in particular to a catalytic cracking reaction-regeneration method and apparatus. Background Technology

[0002] The global refining industry faces numerous challenges, including the need for new energy alternatives and increasingly stringent requirements for energy conservation and emission reduction. Catalytic cracking units are core equipment in refineries, and the heat generated from coking in the regeneration system of these units is used to power the reaction system. Carbon emissions from coking in the catalytic cracking regenerator account for 24-55% of the plant's total carbon emissions and nearly 1% of the nation's total carbon dioxide emissions, making it a key area for carbon reduction in the petrochemical industry.

[0003] Currently, the production model of reducing oil product output and increasing chemical production is conducive to promoting the sustainable development of the refining industry; however, the production process requires more heat of reaction. When the amount of coke burned is insufficient to meet the energy consumption of the unit, it is usually necessary to supplement the heat with fossil fuels, which increases carbon dioxide emissions and wastes resources. Recovering and utilizing emitted carbon dioxide can reduce emissions, but large-scale industrial application remains economically and technologically challenging. Summary of the Invention

[0004] This application provides a catalytic cracking reaction-regeneration method, including:

[0005] After the S1 feedstock and catalytic cracking catalyst react in the catalytic cracking reactor of the catalytic cracking reaction system, they are separated to obtain the first product and the carbonized catalyst. The carbonized catalyst flows to the stripping section of the settler.

[0006] S2 introduces bio-oil into the stripping section to contact and react with the carbonized catalyst to obtain the spent catalyst and the second product. The second product enters the product separation unit.

[0007] S3 transports a mixture containing the catalyst to be generated and unreacted bio-oil to the regeneration system and introduces oxygen-containing regeneration gas for regeneration treatment. The regenerated catalyst is then transported back to the catalytic cracking reaction system for recycling.

[0008] In one embodiment, the bio-oil is selected from liquid products obtained by pyrolysis and liquefaction of biomass feedstock and bio-based crude glycerol and combinations thereof.

[0009] In one embodiment, the bio-based crude glycerol comprises 10-90 wt% glycerol, 1-30 wt% methanol, and 1-30 wt% fatty acids and their esters, based on the total weight of the bio-based crude glycerol.

[0010] In one embodiment, the amount of carbon deposit catalyst to the bio-oil introduced into the stripping section is in a weight ratio of 5-300:1.

[0011] In one embodiment, the oxygen-containing regeneration gas is oxygen.

[0012] The method further includes:

[0013] A portion of the regenerated flue gas is recycled back to the regeneration system to form a mixture with oxygen, wherein the oxygen content of the mixture is not higher than 28% by volume.

[0014] In one embodiment, the regeneration system is a two-stage regeneration system or a dual-regenerator regeneration system.

[0015] In one embodiment, the method further includes introducing a stripping medium into the stripping section.

[0016] In one embodiment, the regeneration system is a dual regenerator regeneration system, wherein the temperature of the first regenerator is 500-700°C and the average residence time of the catalyst is 0.5-5.0 minutes; the temperature of the second regenerator is 550-750°C and the average residence time of the catalyst is 0.5-4.0 minutes.

[0017] In one embodiment, the stripping medium is not introduced in the stripping section of the method.

[0018] In one embodiment, the regeneration system is a dual regenerator regeneration system, wherein the temperature of the first regenerator is 500-700°C and the average residence time of the catalyst is 0.5-4.0 minutes; the temperature of the second regenerator is 550-750°C and the average residence time of the catalyst is 1.0-5.0 minutes.

[0019] In one embodiment, the regeneration system is further provided with one or more heat exchangers for controlling the catalyst bed temperature in the regeneration system to not exceed 750°C.

[0020] This application also provides a catalytic cracking reaction-regeneration apparatus, comprising:

[0021] The catalytic cracking reaction system includes:

[0022] A catalytic cracking reactor is used to bring feedstock oil into contact with a catalyst for reaction.

[0023] The oil-gas separation unit is used to separate the catalyst and the oil gas.

[0024] A settling tank, which includes a stripping section and a catalyst for settling and stripping settling;

[0025] The stripping section is equipped with a bio-oil injection port and an optional stripping steam injection port;

[0026] The regeneration system includes:

[0027] A regenerator, which is fluidly connected to the catalytic cracking reaction system via a regenerator incline, is used to supply the regenerated catalyst from the catalytic cracking reaction system to the regenerator; the regenerator is also fluidly connected to the catalytic cracking reaction system via a regeneration incline, for recycling the regenerated catalyst from the regenerator back to the catalytic cracking reaction system; and

[0028] A heat exchanger is used to transfer heat from the regeneration system to the outside and to control the catalyst bed temperature in the regeneration system to not exceed 750°C.

[0029] In one embodiment, the regenerator is a dual regenerator, comprising:

[0030] The first regenerator is provided with a first oxygen inlet, a pre-regenerating agent inlet and an optional first circulating flue gas inlet, wherein the pre-regenerating inclined tube is connected to the pre-regenerating agent inlet of the first regenerator and is used to transport the pre-regenerated catalyst from the catalytic cracking reaction system to the first regenerator for semi-regeneration via the pre-regenerating agent inlet;

[0031] The second regenerator is provided with a second oxygen inlet, a regenerated catalyst outlet, and an optional second circulating flue gas inlet; wherein, the regeneration inclined tube is connected to the regenerated catalyst outlet of the second regenerator for circulating the regenerated catalyst from the second regenerator back to the catalytic cracking reaction system; the first regenerator and the second regenerator are connected by an external circulation pipe, so that the semi-regenerated catalyst from the first regenerator enters the second regenerator for complete regeneration;

[0032] A cyclone separator, housed inside a first regenerator, is used to separate regenerated flue gas and semi-regenerated catalyst.

[0033] In one embodiment, the regenerator is a dual regenerator, comprising:

[0034] The first regenerator is provided with a first oxygen inlet, a pre-regenerating agent inlet and an optional first circulating flue gas inlet, wherein the pre-regenerating inclined tube is connected to the pre-regenerating agent inlet of the first regenerator and is used to transport the pre-regenerated catalyst from the catalytic cracking reaction system to the first regenerator for semi-regeneration via the pre-regenerating agent inlet;

[0035] The second regenerator is provided with a second oxygen inlet, a regenerated catalyst outlet, and an optional second circulating flue gas inlet; wherein the regeneration inclined tube is connected to the regenerated catalyst outlet of the second regenerator for circulating the regenerated catalyst from the second regenerator back to the catalytic cracking reaction system;

[0036] The first regenerator is equipped with a first cyclone separator, which is used to separate regenerated flue gas and semi-regenerated catalyst.

[0037] The second regenerator is equipped with a second cyclone separator for separating regenerated flue gas and regenerated catalyst;

[0038] The first regenerator and the second regenerator are connected by an inner riser, allowing the semi-regenerated catalyst from the first regenerator to enter the second regenerator for complete regeneration.

[0039] In one embodiment, the regeneration system further includes:

[0040] A flue gas energy recovery unit, which is connected to the cyclone separator, is used to recover the heat of the regenerated flue gas;

[0041] The CO2 separation unit is used to separate CO2 gas from the regenerated flue gas that has been treated by the flue gas energy recovery unit.

[0042] Bio-resources are a renewable energy source and do not cause environmental problems; they are considered zero-carbon energy. The method and apparatus of this application use bio-oil as a power source for catalytic cracking units, which can reduce the use of fossil fuels, conserve resources, achieve carbon emission reduction, and alleviate the contradiction between the increasing energy demand of catalytic cracking and environmental protection requirements. At the same time, the crude bio-oil product has a complex composition that is difficult to utilize directly, and its price is relatively low. Applying it to catalytic cracking units can also expand the utilization pathways of bio-oil, improve economic efficiency, and generate social benefits. The method and apparatus of this application can use bio-oil to produce high-value products and reduce carbon dioxide emissions from fossil fuels.

[0043] Therefore, the main advantages of the present invention are as follows:

[0044] (1) Bio-oil comes from biological resources. When it is introduced into the catalytic cracking unit from the stripping section, it can produce high-value products. At the same time, the part that enters the regenerator for combustion can supplement the energy consumption of the unit operation, replace the original fossil fuel energy supply, reduce carbon dioxide emissions, and realize the low-carbon development of oil refining.

[0045] (2) The crude bio-oil product has a complex composition and high purification cost. The utilization pathways such as biotransformation are not efficient. This method does not require separation and purification of the crude bio-oil product, and can achieve its efficient utilization, thus expanding the utilization pathway of bio-oil.

[0046] (3) The use of bio-oil enhances the heating capacity of the catalytic cracking unit, and the excess heat generated can be used to generate high-pressure steam to supply other units; the flue gas generated during the regeneration process does not contain nitrogen, which is conducive to the separation and capture of carbon dioxide in it, thus achieving negative carbon emissions. Attached Figure Description

[0047] Figure 1A schematic diagram of one embodiment of a catalytic cracking reaction-regeneration unit is shown.

[0048] Figure 2 A schematic diagram illustrating another embodiment of a catalytic cracking reaction-regeneration unit is shown. Detailed Implementation

[0049] The present application will now be described in further detail with reference to the accompanying drawings and embodiments. Through these descriptions, the features and advantages of the present application will become clearer and more apparent.

[0050] The term “exemplary” as used herein means “serving as an example, embodiment, or illustration.” Any embodiment illustrated herein as “exemplary” is not necessarily to be construed as superior to or better than other embodiments. Although various aspects of embodiments are shown in the accompanying drawings, the drawings are not necessarily drawn to scale unless specifically indicated otherwise.

[0051] Furthermore, the technical features involved in the different embodiments of this application described below can be combined with each other as long as they do not conflict with each other.

[0052] This application provides a catalytic cracking reaction-regeneration method, including:

[0053] After the S1 feedstock and catalytic cracking catalyst react in the catalytic cracking reactor of the catalytic cracking reaction system, they are separated to obtain the first product and the carbonized catalyst. The carbonized catalyst flows to the stripping section of the settler.

[0054] S2 introduces bio-oil into the stripping section to contact and react with the carbonized catalyst to obtain the spent catalyst and the second product. The second product enters the product separation unit.

[0055] S3 transports a mixture containing the catalyst to be generated and unreacted bio-oil to the regeneration system and introduces oxygen-containing regeneration gas for regeneration treatment. The regenerated catalyst is then transported back to the catalytic cracking reaction system for recycling.

[0056] This application also provides a catalytic cracking reaction-regeneration apparatus, comprising:

[0057] The catalytic cracking reaction system includes:

[0058] A catalytic cracking reactor is used to bring feedstock oil into contact with a catalyst for reaction.

[0059] The oil-gas separation unit is used to separate the catalyst and the oil gas.

[0060] A settling tank, which includes a stripping section and a catalyst for settling and stripping settling;

[0061] The stripping section is equipped with a bio-oil injection port and an optional stripping steam injection port;

[0062] The regeneration system includes:

[0063] A regenerator, which is fluidly connected to the catalytic cracking reaction system via a regenerator incline, is used to supply the regenerated catalyst from the catalytic cracking reaction system to the regenerator; the regenerator is also fluidly connected to the catalytic cracking reaction system via a regeneration incline, for recycling the regenerated catalyst from the regenerator back to the catalytic cracking reaction system; and

[0064] A heat exchanger is used to transfer heat from the regeneration system to the outside and to control the catalyst bed temperature in the regeneration system to not exceed 750°C.

[0065] The method described in this application can be performed using the apparatus described in this application. Figure 1 and Figure 2 A specific embodiment of this catalytic cracking reaction-regeneration unit is shown. The following is in conjunction with... Figure 1 and Figure 2 The methods and apparatus described in this application are described.

[0066] like Figure 1 and 2 As shown, the catalytic cracking reaction system 300 includes:

[0067] Catalytic cracking reactor 310 is used to bring feedstock oil into contact with catalyst for reaction;

[0068] Oil separation unit 320 is used to separate catalyst and oil gas;

[0069] Settler 330 includes a stripping section 331 and a catalyst for settling and stripping settling; wherein the stripping section 331 is provided with a bio-oil inlet and an optional stripping steam inlet.

[0070] In the catalytic cracking reaction system 300, the catalytic cracking reactor 310 is used for catalytic cracking reaction: a lifting medium is introduced through its bottom inlet 301 to lift the regenerated catalyst (from the regeneration system 200) entering through the regeneration inclined tube 305; feedstock oil entering from the feedstock inlet 303 (and steam entering from the steam inlet 304) contacts the catalyst to carry out catalytic cracking reaction. The oil and gas products of the reaction are separated by the oil-catalyst separation unit 320, and the separated oil and gas products (first product) are collected in the gas collecting chamber 340 and then fed into the product separation unit 350 for separation to obtain various products. The separated carbonized catalyst flows to the stripping section 331 of the settler 330. In this application, the bio-oil desalting unit 360 is connected to the stripping section 331 of the settling tank 330, so that the bio-oil, after desalting, is injected into the stripping section to contact and react with the carbonized catalyst, yielding a spent catalyst and a second product. This is then separated by the oil-gas separation unit 320. The separated oil and gas product (the second product) is collected in the gas collecting chamber 340 and then fed together with the first product into the product separation unit 350 for further separation. The spent catalyst and unreacted bio-oil are transported together through the spent catalyst inclined tube 335 to the regeneration system 200 for regeneration, thus achieving recycling. The catalytic cracking reactor 310 used in this application can be any type of reactor commonly used in the art, such as a riser reactor, a fluidized bed reactor, a variable diameter reactor, or a combination thereof.

[0071] In this application, the stripping section 331 of the settling tank 330 is provided with a bio-oil injection port 333, which can be connected to the bio-oil desalination unit 360 for injecting desalinated bio-oil into the stripping section. The stripping section 331 of the settling tank 330 is also provided with an optional stripping medium injection port 332, which can be used to inject stripping media such as steam when needed. Of course, in the method of this application, stripping media may not be injected, and only bio-oil may be injected. Figure 1 As shown, the stripping section 331 of the settling tank 330 is also equipped with a stripping medium injection port 332, which can be used to inject stripping media such as steam when needed. Figure 2 As shown, the stripping section 331 of the settling tank 330 is not equipped with a stripping medium injection port, so stripping medium such as steam can be omitted during the reaction-regeneration process.

[0072] According to the present invention, the bio-oil can be derived from biomass oil obtained through the pyrolysis and liquefaction of various types of biomass, or crude glycerol, a byproduct of the biodiesel industry, fatty alcohol industry, etc. Before being injected into the catalytic cracking reaction system, the bio-oil generally needs to undergo desalting treatment to avoid introducing substances harmful to the reaction process and the catalyst. The desalting process of the crude bio-oil product can employ techniques well-known to those skilled in the art, such as electrodialysis, reverse osmosis, and ion exchange resin methods. The desalting process of the crude bio-oil product can be carried out in the bio-oil desalting unit 360.

[0073] The biomass oil used in this application is obtained by pre-treating biomass and then transporting it to a liquefaction unit for liquefaction to obtain crude biomass oil; the crude biomass oil is then dehydrated in a dehydration unit to obtain biomass oil.

[0074] Biomass processing systems may include:

[0075] Biomass pretreatment equipment is used to pretreat biomass.

[0076] A biomass liquefaction unit is used to process pretreated biomass to obtain crude biomass oil.

[0077] A dehydration device is used to dehydrate the crude biomass oil product to obtain biomass oil;

[0078] Storage tanks for storing the biomass oil.

[0079] According to the present invention, biomass includes, but is not limited to, agricultural and forestry biomass, forestry biomass, aquatic plants, and energy and economic crops. For example, agricultural and forestry biomass includes, but is not limited to, straw, rice husks, and cotton stalks; forestry biomass includes, but is not limited to, firewood, fast-growing forests, and forestry processing residues; aquatic plants include, but are not limited to, reeds and algae; and energy and economic crops include, but are not limited to, cassava and rapeseed.

[0080] According to the present invention, the purpose of the biomass pretreatment process is to improve the efficiency of liquefaction. The biomass pretreatment method is selected from one or more of crushing, drying, baking, compression molding and acid washing, and can be selected according to the type and properties of biomass.

[0081] According to the present invention, the biomass liquefaction process can be selected from hydrothermal liquefaction, alcohol thermal liquefaction, pyrolysis, and other processes. According to the present invention, the temperature of the biomass hydrothermal liquefaction process is not lower than 200°C, and the pressure is not lower than 4.0 MPa. The solvent used in alcohol thermal liquefaction is selected from methanol, ethylene glycol, etc. The pyrolysis process is rapid pyrolysis or flash pyrolysis, with a heating rate not lower than 100°C / s and a residence time not higher than 10s.

[0082] According to the present invention, biomass liquefaction yields crude biomass oil, which is then dehydrated to obtain biomass oil, which is used directly as supplementary fuel. The biomass oil is a mixture containing acids, aldehydes, ketones, alcohols, esters, ethers, phenols, sugars, and oligomers.

[0083] According to the present invention, the energy consumed in the biomass liquefaction process comes at least partially or entirely from renewable energy sources such as solar energy, green electricity, and nuclear energy.

[0084] According to the present invention, the bio-oil obtained from biomass pyrolysis liquefaction is a mixture of complex oxygen-containing organic compounds and water. Crude glycerol, a byproduct of the biodiesel industry, oil processing industry, oil saponification industry, and fatty alcohol industry, mainly comprises: 10-90 wt% glycerol, 1-30 wt% methanol, 1-30 wt% fatty acids (esters) and lipids, with the remainder being water. In particular, this bio-based crude glycerol contains a certain amount of water, which, when injected into the stripping section of the settling tank, can also play a certain stripping role, thereby eliminating the need for stripping steam and saving steam resources and energy.

[0085] According to the present invention, in a specific embodiment, the crude bio-oil product is injected through a nozzle into the lower part or bottom of the stripping section of the catalytic cracking reaction system, preferably the bottom. In one embodiment, the weight ratio of the amount of carbonized catalyst to the bio-oil introduced into the stripping section is 5-300:1, for example 10-200:1, for example 20-100:1.

[0086] The regeneration system can be selected from single-regenerator regeneration system, dual-regenerator regeneration system, single-stage regeneration system and two-stage regeneration system, depending on the form of the regenerator.

[0087] Figure 1 One implementation of a dual-regenerator regeneration system is shown. For example... Figure 1 As shown, the dual regenerator 210 includes:

[0088] The first regenerator 211 is provided with a first oxygen inlet 2110, a pre-regenerating agent inlet 2111 and an optional first circulating flue gas inlet 2113, wherein the pre-regenerating inclined tube 335 is connected to the pre-regenerating agent inlet 2111 of the first regenerator and is used to transport the pre-regenerated catalyst from the catalytic cracking reaction system to the first regenerator for semi-regeneration via the pre-regenerating agent inlet.

[0089] The second regenerator 212 is provided with a second oxygen inlet 2120, a regenerated catalyst outlet 2121 and an optional second circulating flue gas inlet 2123; wherein, the regeneration inclined tube 305 is connected to the regenerated catalyst outlet 2121 of the second regenerator for circulating the regenerated catalyst from the second regenerator back to the catalytic cracking reaction system.

[0090] The first regenerator 211 is equipped with a first cyclone separator 2114, which is used to separate regenerated flue gas and semi-regenerated catalyst.

[0091] The second regenerator 212 is equipped with a second cyclone separator 2124, which is used to separate regeneration flue gas and regeneration catalyst.

[0092] The first regenerator 211 and the second regenerator 212 are connected by an inner riser 213, so that the semi-regenerated catalyst from the first regenerator enters the second regenerator for complete regeneration.

[0093] In this dual-regenerator regeneration system, oxygen is typically used as the oxygen-containing regeneration gas. In the first regenerator 211, the catalyst from the pre-regenerated inclined tube 335 comes into contact with oxygen diluted in the flue gas and reacts, resulting in partial catalyst regeneration. The catalyst then moves upwards to the second regenerator 212, where it continues to come into contact with oxygen diluted in the flue gas and undergoes coke combustion, resulting in complete catalyst regeneration. When oxygen is used as the oxygen-containing regeneration gas, the regenerated flue gas is recycled back to the first regenerator, and / or back to the second regenerator, forming an oxidation-carbon dioxide mixture. The amount of oxygen and / or recycled flue gas is controlled so that the oxygen concentration in the mixture in the first and / or second regenerator does not exceed 28% (by volume). In one embodiment of this application, a portion of the flue gas separated by the first cyclone separator 2114 may enter the second regenerator through the second recycled flue gas inlet 2123; the remaining flue gas, after mixing with the flue gas separated by the first cyclone separator 2114, enters the first regenerator through the first recycled flue gas inlet 2113. Therefore, the regenerated flue gas is recycled back to the first regenerator, and / or, recycled back to the second regenerator. Coking is performed in this atmosphere, increasing the coking intensity; the inlet gas contains no nitrogen, reducing the energy consumed in gas preheating; and the regenerator outlet flue gas has a higher carbon dioxide concentration, facilitating carbon dioxide separation and capture.

[0094] Figure 2 One embodiment of a dual-regenerator regeneration system 400 is shown, wherein the regenerator 410 includes:

[0095] The first regenerator 411 is provided with a first oxygen inlet 4110, a pre-regenerating agent inlet 4111 and an optional first circulating flue gas inlet 4112, wherein the pre-regenerating inclined tube 335 is connected to the pre-regenerating agent inlet 4111 of the first regenerator and is used to transport the pre-regenerated catalyst from the catalytic cracking reaction system to the first regenerator 411 for semi-regeneration via the pre-regenerating agent inlet;

[0096] The second regenerator 412 is provided with a second oxygen inlet 4120, a regenerated catalyst outlet 4121, and an optional second circulating flue gas inlet 4123; wherein, the regeneration inclined pipe 305 is connected to the regenerated catalyst outlet 4121 of the second regenerator for circulating the regenerated catalyst from the second regenerator back to the catalytic cracking reaction system 300; the first regenerator and the second regenerator are connected by an external circulation pipe 414, so that the semi-regenerated catalyst from the first regenerator enters the second regenerator for complete regeneration;

[0097] Cyclone separator 413, which is housed inside the first regenerator, is used to separate regenerated flue gas and semi-regenerated catalyst.

[0098] In one embodiment, the first regenerator 411 is located above the second regenerator 412. The first and second regenerators are connected by an external circulation pipe 414, allowing the catalyst material from the first regenerator to enter the second regenerator via the external circulation pipe 414. The first regenerator 411 and the second regenerator 412 are separated by a flue gas distribution plate 415, allowing the flue gas generated by the second regenerator to enter the first regenerator via the flue gas distribution plate 415. The flue gas distribution plate 415 allows the flue gas generated by the second regenerator to pass through, but the catalyst does not pass through; the catalyst material from the first regenerator enters the second regenerator via the external circulation pipe 415.

[0099] In this dual-regenerator regeneration system, oxygen is typically used as the oxygen-containing regeneration gas. When using oxygen as the oxygen-containing regeneration gas, the regenerated flue gas is recycled back to the first regenerator and / or back to the second regenerator, forming an oxide-carbon dioxide mixture. The amount of oxygen and / or recycled flue gas is controlled so that the oxygen concentration in the mixture in the first and / or second regenerators does not exceed 28%. Coking is performed under this atmosphere, which increases the coking intensity; the absence of nitrogen in the inlet gas reduces the energy consumed in gas preheating; and the higher carbon dioxide concentration in the regenerator outlet flue gas facilitates carbon dioxide separation and capture.

[0100] In one embodiment, the regeneration system 200, 400 further includes:

[0101] Flue gas energy recovery unit 240, 440, the flue gas energy recovery unit is connected to the cyclone separator and is used to recover the heat of the regenerated flue gas;

[0102] CO2 separation units 250 and 450 are used to separate CO2 gas from the regenerated flue gas treated by the flue gas energy recovery unit.

[0103] During regeneration, the catalyst awaiting regeneration enters the first regenerator through the inclined tube and comes into contact with oxygen, undergoing partial coking. Afterward, it enters the second regenerator via the external circulation pipe for complete regeneration. At this point, pure oxygen is introduced through the second oxygen inlet, contacting the partially coked catalyst for further regeneration and combustion. The regenerated catalyst is discharged through the regenerated catalyst outlet and recycled back to the catalytic cracking reactor. The flue gas discharged from the first regenerator via the cyclone separator is partially processed by the flue gas energy recovery system 240 for energy recovery, followed by carbon dioxide separation by the carbon dioxide separation system 250 for carbon dioxide capture; the remaining flue gas is recycled back to both the first and second regenerators.

[0104] According to the present invention, in a specific embodiment, the addition of waste-derived fuel to the regenerator generates more heat, leading to excessively high regenerator temperatures. A heat extraction system controls the regenerator bed temperature to not exceed 750°C to prevent damage to the catalyst and simultaneously transfers heat to the outside of the regenerator. The heat extractor can be an internal heat extractor (located inside the regenerator) or / and an external heat extractor (located outside the regenerator), with one or more heat extractors, to use the excess energy generated by the regenerator to supply other devices. The heat extractor can also be used to generate high-pressure steam, which can then be supplied to other devices for energy. In one embodiment, by installing a heat extractor, the regenerator bed temperature is controlled to not exceed 750°C, for example, not exceeding 720°C.

[0105] like Figure 1 As shown, heat exchangers 230 can be installed in both the first and second regenerators. Figure 2 As shown, a heat exchanger 430 can be installed in the second regenerator.

[0106] In one embodiment, the catalytic cracking reaction-regeneration method of this application further includes introducing a stripping medium, such as steam, into the stripping section. In this embodiment, the regeneration system is a dual-regenerator regeneration system, wherein the temperature of the first regenerator is 500-700°C and the average residence time of the catalyst is 0.5-5.0 minutes; the temperature of the second regenerator is 550-750°C and the average residence time of the catalyst is 0.5-4.0 minutes.

[0107] In one embodiment, the catalytic cracking reaction-regeneration method of this application does not introduce a stripping medium in the stripping section. In this embodiment, the regeneration system is a dual regenerator system, wherein the temperature of the first regenerator is 500-700°C and the average residence time of the catalyst is 0.5-4.0 minutes; the temperature of the second regenerator is 550-750°C and the average residence time of the catalyst is 1.0-5.0 minutes.

[0108] According to the present invention, the catalyst comprises zeolite, inorganic oxides, and optionally clay, with each component accounting for the following percentages by weight of the total catalyst: zeolite 1% to 50% by weight, inorganic oxides 5% to 99% by weight, and clay 0% to 70% by weight. The zeolite is the active component, selected from mesoporous zeolite and / or optionally macroporous zeolite, with mesoporous zeolite accounting for 10% to 100% by weight of the total zeolite weight and macroporous zeolite accounting for 0% to 90% by weight of the total zeolite weight. The mesoporous zeolite is selected from one or more of the ZSM series zeolites and / or ZRP zeolite, and the zeolite 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, and ultrastable Y.

[0109] This invention directly injects crude bio-oil into the stripping section of a catalytic cracking unit, partially converting it into high-value products, while the remainder, along with the spent catalyst, enters a catalyst regeneration unit for coke combustion regeneration. Bio-oil originates from renewable biological resources, is inexpensive, and is a green resource. Biomass energy is a zero-carbon renewable energy source, and its utilization is a carbon-neutral process. Crude bio-oil is a mixture containing multiple compounds, and its separation and purification processes are complex and costly, thus hindering its efficient utilization. The method and apparatus of this application directly inject the crude bio-oil into the catalytic cracking stripping section, eliminating the need for separation and purification, reducing utilization costs, and improving efficiency. The method and apparatus of this application utilize bio-oil to power a catalytic cracking unit. Besides meeting the heat requirements of the reaction system, excess heat can be used to generate high-pressure steam for external energy supply. Coupling biomass energy into the catalytic cracking unit in a suitable manner achieves low-carbon energy supply, thereby fundamentally reducing refinery carbon emissions. Therefore, the method and apparatus provided by this invention successfully introduce biomass energy into the catalytic cracking energy supply system, supplementing the catalytic cracking unit with biomass energy while expanding the utilization pathways of bio-oil. Furthermore, it can efficiently utilize bio-oil, eliminating the energy-intensive and complex refining process, and converting it into high-value products and powering the catalytic cracking unit. This reduces the energy consumption of the catalytic cracking unit and decreases carbon dioxide emissions from fossil fuels, meeting the requirements of green chemistry.

[0110] The method provided by the present invention will be further described below with reference to the accompanying drawings, but this does not limit the present invention.

[0111] like Figure 1As shown, the pre-lifting medium enters from the bottom of the riser reactor 310 through the bottom inlet 301, and rises with the regenerated catalyst in the regeneration inclined tube 305 under the action of the pre-lifting medium. Preheated feedstock oil is injected into the riser reactor through the feedstock oil inlet 303 along with atomized steam from the steam inlet 304, where it reacts with the catalyst and moves upwards. The resulting reaction products and deactivated catalyst are separated by the oil-catalyst separation unit 320, separating the catalyst from the reaction products. The reaction products enter the gas collecting chamber 340, and the catalyst flows to the stripping section 331 of the settler 330. The desalted crude bio-oil is injected into the stripping section through the bio-oil inlet 333 to react with the catalyst. The product is separated from the stripped oil and gas (stripping steam is injected through the stripping medium inlet 332) and enters the gas collecting chamber 340. The oil and gas in the gas collecting chamber 340 are fed into the product separation unit 350 for separation to obtain various products. Unreacted bio-oil and the catalyst awaiting regeneration enter the first regenerator 211 through the awaiting regeneration inclined tube 335. There, they come into contact with oxygen diluted from the circulating flue gas and undergo a combustion reaction, resulting in partial catalyst regeneration. The flue gas, after being separated by a cyclone separator, is partly recycled to the second regenerator 212 and partly enters the flue gas energy recovery system 240 to recover energy before entering the carbon dioxide separation and capture system 250. The partially regenerated catalyst is transported to the second regenerator 212 for complete regeneration through the inner riser 213. After energy recovery, the flue gas enters the carbon dioxide separation and capture system 250. The fully regenerated catalyst is returned to the reactor through the regeneration inclined tube 305, achieving recycling.

[0112] like Figure 2As shown, the pre-lifting medium enters from the bottom of the riser reactor 310 through the bottom inlet 301, and rises with the regenerated catalyst in the regeneration inclined tube 305 under the action of the pre-lifting medium. Preheated feedstock oil is injected into the riser reactor through the feedstock oil inlet 303 along with atomized steam from the steam inlet 304, reacting with the catalyst and moving upwards. The resulting reaction products and deactivated catalyst are separated by the oil-catalyst separation unit 320, separating the catalyst from the reaction products. The reaction products enter the gas collecting chamber 340, and the catalyst flows to the stripping section 331 of the settling tank 330. The desalted crude bio-oil is injected into the stripping section through the bio-oil inlet 333 to react with the catalyst. The product and the stripped oil gas (bio-based crude glycerol contains a certain amount of water, which can play a certain stripping role) are separated and enter the gas collecting chamber 340. The oil gas in the gas collecting chamber 340 is fed into the product separation unit 350 for separation to obtain various products. Unreacted bio-oil and the catalyst awaiting regeneration enter the first regenerator 211 through the awaiting regeneration inclined tube 335. There, they come into contact with oxygen diluted from the circulating flue gas and undergo a combustion reaction, resulting in partial catalyst regeneration. The flue gas, after being separated by a cyclone separator, is partly recycled to the second regenerator 212 and partly enters the flue gas energy recovery system 240 to recover energy before entering the carbon dioxide separation and capture system 250. The partially regenerated catalyst is transported to the second regenerator 212 for complete regeneration through the external circulation pipe 214. After energy recovery, the flue gas enters the carbon dioxide separation and capture system 250. The fully regenerated catalyst is returned to the reactor through the regeneration inclined tube 305, achieving recycling.

[0113] The present invention will be further illustrated by the following examples, but the present invention is not limited thereto. The properties of the feedstock A and feedstock B used in the examples and comparative examples are listed in Tables 1-1 and 1-2, respectively.

[0114] Catalyst a is TCC, and its preparation process is as follows: 969 g of hydrous kaolin (product of China Kaolin Company, solid content 73%) is slurried with 4300 g of decationized water. Then, 781 g of pseudoboehmite (product of Zibo Boehmite Plant, Shandong, solid content 64%) and 144 ml of hydrochloric acid (concentration 30%, specific gravity 1.56) are added and stirred evenly. The mixture is then aged at 60℃ for 1 hour, maintaining the pH at 2-4. After cooling to room temperature, 5000 g of pre-prepared high silica-alumina ratio mesoporous shape-selective ZSM-5 zeolite slurry containing chemical water is added, stirred evenly, spray-dried, and free Na is washed away. + After aging, it is used. The aging process is: aging in water vapor at 800℃ for 15 hours. The properties are listed in Table 2.

[0115] The preparation process of catalyst b is as follows:

[0116] (1) Dissolve 20 g of NH4Cl in 1000 g of water, add 100 g (dry basis) of crystallized ZRP-1 molecular sieve (produced by Qilu Petrochemical Company Catalyst Plant, SiO2 / Al2O3 = 30, rare earth content RE2O3 = 2.0 wt%) to this solution, exchange at 90℃ for 0.5 hours, and filter to obtain filter cake; add 4.0 g of H3PO4 (concentration 85%) and 4.5 g of Fe(NO3)3 dissolved in 90 g of water, mix with the filter cake, impregnate and dry; then calcine at 550℃ for 2 hours to obtain MFI mesoporous molecular sieve containing phosphorus and iron. The elemental analysis chemical composition of the obtained molecular sieve is: 0.1Na2O·5.1Al2O3·2.4P2O5·1.5Fe2O3·3.8RE2O3·88.1SiO2.

[0117] (2) Use 250 kg of deionized water to slurry 75.4 kg of hydrous kaolin (an industrial product of Suzhou Porcelain Clay Company, with a solid content of 71.6 wt%), then add 54.8 kg of pseudoboehmite (an industrial product of Donglu Aluminum Plant, with a solid content of 63 wt%), adjust the pH to 2-4 with hydrochloric acid, stir evenly, let it stand at 60-70℃ for 1 hour, keep the pH at 2-4, lower the temperature to below 60℃, add 41.5 kg of aluminum sol (a product of Qilu Petrochemical Company Catalyst Plant, with an Al2O3 content of 21.7 wt%), stir for 40 minutes to obtain a mixed slurry.

[0118] (3) Add the phosphorus- and iron-containing MFI mesoporous molecular sieve (2 kg dry basis) prepared in step (1) to the mixed slurry obtained in step (2), stir evenly, spray dry to form, and wash with ammonium dihydrogen phosphate solution (phosphorus content 1% by weight) to remove free Na. + After drying, the catalytic conversion catalyst sample c is obtained. Based on the total dry weight of catalyst b, the dry weight composition of catalyst b includes: 2% by weight of phosphorus and iron-containing MFI mesoporous molecular sieve, 36% by weight of pseudoboehmite and 8% by weight of aluminum sol, with the balance being kaolin.

[0119] Example 1

[0120] Example 1 in Figure 1 The procedure is performed on the apparatus shown, wherein,

[0121] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0122] The bio-oil used in the examples is bio-based crude glycerol, with the following composition: 80% by weight glycerol, 12% by weight methanol, 2% methyl oleate, and the remainder being water.

[0123] Using feedstock oil A as the reactant and catalytic conversion catalyst a as the catalyst, feedstock oil A reacts with catalyst a to obtain a spent catalyst and a first product. The spent catalyst enters the stripping section, where it contacts and reacts with desalted bio-based crude glycerol (the weight ratio of spent catalyst to bio-based crude glycerol is 28:1) to obtain a second product. The second product, along with stripped oil and gas (obtained by stripping steam injected through the stripping medium inlet), enters the gas collecting chamber and, together with the first product, enters the product separation unit for separation according to distillation range to obtain various oil and gas products. Unreacted bio-based crude glycerol and spent catalyst enter the regenerator through the spent catalyst inclined tube, where they react with oxygen diluted by the circulating flue gas to undergo coke combustion. Partial regeneration occurs first in the first regenerator, then the gas flows upward through the inner riser to the second regenerator to complete regeneration. Simultaneously, part of the flue gas from the regenerator cyclone separator system returns to the regenerator, controlling the oxygen content in the regenerator to not exceed 28%. Excess energy generated by the regenerator is used for external power supply through a heat exchanger.

[0124] The first regenerator temperature is 630℃ with a residence time of 3 minutes, and the second regenerator temperature is 650℃ with a residence time of 3 minutes. The regenerated catalyst is recycled back to the reactor to contact the feedstock oil for catalytic cracking. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 3.

[0125] Comparative Example 1

[0126] Comparative Example 1 was conducted on the same apparatus as Example 1, with the same reaction and regeneration conditions. The difference was that bio-based glycerol was not injected into the stripping section; instead, heat was supplemented by injecting fuel oil (feedstock oil A) to achieve heat balance. The regenerated catalyst was recycled back to the reactor to undergo catalytic cracking in contact with the feedstock oil. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 3.

[0127] Example 2

[0128] Implementation examples in Figure 1 The procedure is performed on the apparatus shown, wherein,

[0129] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0130] The bio-oil used in the examples is bio-based crude glycerol, with the following composition: 80% by weight glycerol, 12% by weight methanol, 2% methyl oleate, and the remainder being water.

[0131] Using feedstock B as the reactant and catalytic conversion catalyst b as the catalyst, the reaction and regeneration are carried out according to the method proposed in this invention: In the stripping section, desalted bio-based crude glycerol (the weight ratio of the recycled catalyst to the bio-based crude glycerol is 64:1) is injected and reacts with the carbonized catalyst to obtain a second product. The second product, along with stripping oil and gas (obtained by stripping through the stripping medium injection port by injecting stripping steam), enters the gas collecting chamber and, together with the catalytic cracking products of feedstock B, enters the product separation unit to obtain various oil and gas products. Unreacted crude bio-based crude glycerol and heavier products, along with the recycled catalyst, are transported from the recycled inclined tube to the regenerator, where they come into contact with oxygen diluted by the circulating flue gas and undergo coke combustion. The bio-based crude glycerol is combusted in the first reactor, partially regenerating the catalyst. The partially regenerated catalyst then enters the second regenerator for complete regeneration through the inner riser. After cyclone separation, a portion of the flue gas is recycled back to the regenerator to control the oxygen content, while the remainder, after energy recovery, enters the carbon dioxide separation and capture device. Excess energy from the regenerator is used to generate high-pressure steam for external energy supply through the heat extraction system.

[0132] The first regenerator temperature is 630℃ with a residence time of 3 minutes, and the second regenerator temperature is 680℃ with a residence time of 2 minutes. The regenerated catalyst is recycled back to the reactor to contact the feedstock oil for catalytic cracking. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 4.

[0133] Comparative Example 2

[0134] The comparative example and Example 2 were carried out on the same apparatus, and the reaction and regeneration were performed under the same methods and conditions. Bio-based crude glycerol was not injected into the stripping section, and the insufficient heat supply meant that fuel oil (feed oil A) served as a supplementary energy source. Regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 4.

[0135] As can be observed from the data in Tables 3 and 4, injecting bio-based crude glycerol into the stripping section in Examples 1 and 2 resulted in an increase in the yield of low-carbon olefins and other products, and a significant reduction in carbon dioxide emissions compared to the comparative example. This is beneficial for fundamentally reducing carbon dioxide emissions.

[0136] Example 3

[0137] Example 3 in Figure 2 The procedure is performed on the apparatus shown, wherein,

[0138] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0139] The example uses bio-based glycerol as an example. The bio-based crude glycerol consists of 65% glycerol by weight, 13% methanol by weight, 2% methyl oleate, and the remainder is water.

[0140] Using feedstock oil A as the reactant and catalytic conversion catalyst a as the catalyst, feedstock oil A reacts with catalyst a to obtain a carbonized catalyst and a first product. The carbonized catalyst enters the stripping section and contacts desalted bio-based crude glycerol (the weight ratio of the catalyst to the bio-based crude glycerol is 22:1), reacting to obtain a second product. Simultaneously, some oil and gas from the catalyst are stripped (the bio-based crude glycerol contains a certain amount of water, which can play a role in stripping). The second product and stripped oil and gas enter the gas collecting chamber and, together with the first product, enter the product separation unit for separation according to the distillation range to obtain various oil and gas products. Unreacted bio-based crude glycerol and heavier products, along with the catalyst, enter the regenerator through the catalyst incline tube, where they react with oxygen diluted by the circulating flue gas to undergo coke combustion. Partial regeneration occurs first in the first regenerator, then the remaining product is transported through an external circulation pipe to the second regenerator for complete regeneration. Simultaneously, part of the flue gas from the regenerator's cyclone separation system returns to the regenerator, controlling the oxygen content in the regenerator to not exceed 28%. Excess energy generated by the regenerator is used for external power supply through a heat exchanger.

[0141] The first regenerator temperature is 640℃ with a residence time of 2 minutes, and the second regenerator temperature is 670℃ with a residence time of 3 minutes. The regenerated catalyst is recycled back to the reactor to contact the feedstock oil for catalytic cracking. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 5.

[0142] Comparative Example 3

[0143] Comparative Example 3 was conducted on the same apparatus as Example 3, with the same reaction and regeneration conditions. The difference was that instead of injecting bio-based crude glycerol into the stripping section, stripping steam of the same amount as water in the bio-based crude glycerol of Example 3 was injected. Furthermore, heat balance was achieved by injecting fuel oil (feedstock oil A) into the second regenerator. The regenerated catalyst was recycled back to the reactor to undergo catalytic cracking in contact with the feedstock oil. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 5.

[0144] Example 4

[0145] Implementation examples in Figure 2 The procedure is performed on the apparatus shown, wherein,

[0146] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0147] The example uses bio-based glycerol as an example. The bio-based crude glycerol consists of 65% glycerol by weight, 13% methanol by weight, 2% methyl oleate, and the remainder is water.

[0148] With mixed olefins (molar ratio C5) ＝ :C6 ＝ :C7＝ :C8 ＝ Using a reaction feedstock (ratio 1:1:1:1) and catalytic conversion catalyst b as the catalyst, the reaction and regeneration are carried out according to the method proposed in this invention: In the stripping section, desalted bio-based crude glycerol is injected to replace the stripping steam (the weight ratio of the recycled catalyst to the bio-based crude glycerol is 59:1) to contact the carbonized catalyst and react to obtain the second product. Simultaneously, some oil and gas in the catalyst are stripped (the bio-based crude glycerol contains a certain amount of water, which can play a certain stripping role). The second product and the stripped oil and gas enter the gas collection chamber and, together with the first catalytic cracking products, enter the product separation unit to obtain various oil and gas products. Unreacted crude bio-based crude glycerol and heavier products, along with the recycled catalyst, are transported from the recycled inclined tube to the regenerator, where they contact with oxygen diluted by the circulating flue gas and undergo coke combustion. The bio-based crude glycerol is burned in the first reactor, partially regenerating the catalyst. The partially regenerated catalyst then enters the second regenerator for complete regeneration through the external circulation pipe. After cyclone separation, part of the flue gas is recycled back to the regenerator to control the oxygen content, and the remainder, after energy recovery, enters the carbon dioxide separation and capture device. Excess energy from the regenerator is converted into high-pressure steam through a heat extraction system for external energy supply.

[0149] The first regenerator temperature is 630℃ with a residence time of 4 minutes, and the second regenerator temperature is 680℃ with a residence time of 2 minutes. The regenerated catalyst is recycled back to the reactor to contact the feedstock oil for catalytic cracking. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 6.

[0150] Comparative Example 4

[0151] Comparative Example 4 and Example 4 were carried out on the same apparatus, and the reaction and regeneration were performed under the same methods and conditions. Bio-based crude glycerol was not injected into the stripping section; instead, stripping steam of the same amount as water in the bio-based crude glycerol of Example 4 was injected for stripping. Insufficient heat supply was used to inject fuel oil (feed oil A) into the second regenerator as a supplementary energy source. Regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 6.

[0152] As can be observed from the data in Tables 5 and 6, in Examples 3 and 4, replacing the stripping steam injection in the stripping section with bio-based crude glycerol resulted in an increase in the yield of low-carbon olefins and other products, and a significant reduction in carbon dioxide emissions compared to the comparative example. This is beneficial for fundamentally reducing carbon dioxide emissions.

[0153] In the description of this application, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", "left", "right", etc., indicate the orientation or positional relationship based on the orientation or positional relationship in the working state of this application. They are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application.

[0154] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. Those skilled in the art can understand the specific meaning of these terms in this application based on the specific circumstances.

[0155] The present application has been described above with reference to preferred embodiments; however, these embodiments are merely exemplary and illustrative. Various substitutions and modifications can be made to the present application based on these embodiments, all of which fall within the protection scope of the present application.

[0156] Table 1-1 Properties of Crude Oil A

[0157] Feed properties Raw material oil A Density, kg / m³ (20℃) 843.7 C, weight % 86.59 H, weight % 13.41 S, μg / g 5800 N, μg / g 62 Initial boiling point, ℃ 226 50% distillation temperature, ℃ 287 Alkanes, % by weight 40.5 Cycloalkanes, % by weight 33.3 Aromatics, % by weight 26.2

[0158] Table 1-2 Properties of Raw Material B

[0159]

[0160] Table 2

[0161]

[0162] Table 3

[0163]

[0164] Based on processing 100g of raw material; CO2 emission indicators refer to the amount of CO2 emitted from fossil fuels for every 1 MJ of energy produced by the coking process in the regeneration system; the combustion of bio-based crude glycerol is a neutral carbon emission process.

[0165] Table 4

[0166]

[0167] Based on processing 100g of raw material; CO2 emission indicators refer to the amount of CO2 emitted from fossil fuels for every 1 MJ of energy produced by the coking process in the regeneration system; the combustion of bio-based crude glycerol is a neutral carbon emission process.

[0168] Table 5

[0169]

[0170] Based on processing 100g of raw material; CO2 emission indicators refer to the amount of CO2 emitted from fossil fuels for every 1 MJ of energy produced by the coking process in the regeneration system; the combustion of bio-based crude glycerol is a neutral carbon emission process.

[0171] Table 6

[0172]

[0173] Based on processing 100g of raw material; CO2 emission indicators refer to the amount of CO2 emitted from fossil fuels for every 1 MJ of energy produced by the coking process in the regeneration system; the combustion of bio-based crude glycerol is a neutral carbon emission process.

Claims

1. A catalytic cracking reaction-regeneration method, comprising: S1 feedstock oil and catalytic cracking catalyst react in the catalytic cracking reactor of the catalytic cracking reaction system, and are then separated to obtain the first product and the carbonized catalyst. The carbonized catalyst flows to the stripping section of the settler. S2 introduces bio-oil into the stripping section to contact and react with the carbonized catalyst to obtain a spent catalyst and a second product. The second product enters the product separation unit. The bio-oil is selected from bio-based crude glycerol, or a combination of bio-based crude glycerol and liquid products obtained by pyrolysis and liquefaction of biomass raw materials. In bio-based crude glycerol, glycerol accounts for 10-90 wt%, methanol accounts for 1-30 wt%, fatty acids and their esters account for 1-30 wt%, and the remaining component is water, based on the total weight of bio-based crude glycerol; S3 transports a mixture containing the catalyst to be generated and unreacted bio-oil to the regeneration system and introduces oxygen-containing regeneration gas for regeneration treatment. The regenerated catalyst is then transported back to the catalytic cracking reaction system for recycling.

2. The catalytic cracking reaction-regeneration method according to claim 1, wherein, The weight ratio of the amount of carbon deposit catalyst to the bio-oil introduced into the stripping section is 5-300:

1.

3. The catalytic cracking reaction-regeneration method according to claim 1, wherein, The oxygen-containing regeneration gas is oxygen. The method further includes: A portion of the regenerated flue gas is recycled back to the regeneration system to form a mixture with oxygen, wherein the oxygen content in the mixture is not higher than 28% by volume.

4. The catalytic cracking reaction-regeneration method according to claim 3, wherein, The regeneration system is a two-stage regeneration system or a dual-regenerator regeneration system.

5. The catalytic cracking reaction-regeneration method according to claim 3, wherein, The method further includes introducing a stripping medium into the stripping section.

6. The catalytic cracking reaction-regeneration method according to claim 5, wherein, The regeneration system is a dual regenerator system. The temperature of the first regenerator is 500-700℃, and the average residence time of the catalyst is 0.5-5.0 minutes. The temperature of the second regenerator is 550-750℃, and the average residence time of the catalyst is 0.5-4.0 minutes.

7. The catalytic cracking reaction-regeneration method according to claim 3, wherein, In the method described, no stripping medium is introduced in the stripping section.

8. The catalytic cracking reaction-regeneration method according to claim 7, wherein, The regeneration system is a dual regenerator system. The temperature of the first regenerator is 500-700℃, and the average residence time of the catalyst is 0.5-4.0 minutes. The temperature of the second regenerator is 550-750℃, and the average residence time of the catalyst is 1.0-5.0 minutes.

9. The catalytic cracking reaction-regeneration method according to any one of claims 1-8, wherein, The regeneration system is also equipped with one or more heat exchangers to control the catalyst bed temperature in the regeneration system to not exceed 750°C.

10. The catalytic cracking reaction-regeneration method according to claim 1, wherein, The method employs a catalytic cracking reaction-regeneration unit, including: The catalytic cracking reaction system includes: A catalytic cracking reactor is used to bring feedstock oil into contact with a catalyst for reaction. The oil-gas separation unit is used to separate the catalyst and the oil gas. A settling tank, which includes a stripping section and a catalyst for settling and stripping settling; The stripping section is equipped with a bio-oil injection port and an optional stripping steam injection port; The regeneration system includes: A regenerator, which is fluidly connected to the catalytic cracking reaction system via a regenerator incline, is used to supply the regenerated catalyst from the catalytic cracking reaction system to the regenerator; the regenerator is also fluidly connected to the catalytic cracking reaction system via a regeneration incline, for recycling the regenerated catalyst from the regenerator back to the catalytic cracking reaction system; and A heat exchanger is used to transfer heat from the regeneration system to the outside and to control the catalyst bed temperature in the regeneration system to not exceed 750°C.

11. The catalytic cracking reaction-regeneration method according to claim 10, wherein, The regenerator is a dual regenerator, including: The first regenerator is provided with a first oxygen inlet, a pre-regenerating agent inlet and an optional first circulating flue gas inlet, wherein the pre-regenerating inclined tube is connected to the pre-regenerating agent inlet of the first regenerator and is used to transport the pre-regenerated catalyst from the catalytic cracking reaction system to the first regenerator for semi-regeneration via the pre-regenerating agent inlet; The second regenerator is provided with a second oxygen inlet, a regenerated catalyst outlet, and an optional second circulating flue gas inlet; wherein, the regeneration inclined tube is connected to the regenerated catalyst outlet of the second regenerator for circulating the regenerated catalyst from the second regenerator back to the catalytic cracking reaction system; the first regenerator and the second regenerator are connected by an external circulation pipe, so that the semi-regenerated catalyst from the first regenerator enters the second regenerator for complete regeneration; A cyclone separator, housed inside a first regenerator, is used to separate regenerated flue gas and semi-regenerated catalyst.

12. The catalytic cracking reaction-regeneration method according to claim 10, wherein, The regenerator is a dual regenerator, including: The first regenerator is provided with a first oxygen inlet, a pre-regenerating agent inlet and an optional first circulating flue gas inlet, wherein the pre-regenerating inclined tube is connected to the pre-regenerating agent inlet of the first regenerator and is used to transport the pre-regenerated catalyst from the catalytic cracking reaction system to the first regenerator for semi-regeneration via the pre-regenerating agent inlet; The second regenerator is provided with a second oxygen inlet, a regenerated catalyst outlet, and an optional second circulating flue gas inlet; wherein the regeneration inclined tube is connected to the regenerated catalyst outlet of the second regenerator for circulating the regenerated catalyst from the second regenerator back to the catalytic cracking reaction system; The first regenerator is equipped with a first cyclone separator, which is used to separate regenerated flue gas and semi-regenerated catalyst. The second regenerator is equipped with a second cyclone separator for separating regenerated flue gas and regenerated catalyst; The first regenerator and the second regenerator are connected by an inner riser, allowing the semi-regenerated catalyst from the first regenerator to enter the second regenerator for complete regeneration.

13. The catalytic cracking reaction-regeneration method according to claim 11, wherein, The regeneration system also includes: A flue gas energy recovery unit, which is connected to the cyclone separator, is used to recover the heat of the regenerated flue gas; The CO2 separation unit is used to separate CO2 gas from the regenerated flue gas that has been treated by the flue gas energy recovery unit.

Images