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 is reacted with a catalytic cracking catalyst, first products and carbon deposition catalysts are obtained through separation; S2, solid organic waste is pyrolyzed in a solid organic waste treatment system to obtain solid pyrolysis products and / or liquid pyrolysis products; S3, the liquid pyrolysis products are injected into a stripping section to contact and react with the carbon deposition catalysts, and regenerated catalysts and second products are obtained; S4, a mixture containing the regenerated catalysts and unreacted liquid pyrolysis products is transported into a regeneration system and is regenerated by inputting oxygen-containing regeneration gas, and the regenerated catalysts are transported back to the catalytic cracking reaction system for recycling. The method and device provided by the application can efficiently utilize solid organic waste, convert the solid organic waste into high-value products and provide energy for a catalytic cracking device, reduce energy consumption and reduce the emission of carbon dioxide from fossil energy.

Description

Technical Field

[0001] This application 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. However, supplementing heating with fossil fuel combustion is not sustainable in terms of environmental protection and economics, increasing fossil energy consumption and carbon dioxide emissions, and is inconsistent with the current trend of low-carbon development. 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 enables solid organic waste to undergo pyrolysis in a solid organic waste treatment system to obtain solid-phase pyrolysis products and / or liquid-phase pyrolysis products.

[0007] S3 injects the liquid-phase pyrolysis product 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.

[0008] S4 conveys a mixture containing the catalyst to be generated and unreacted liquid-phase pyrolysis products to the regeneration system and introduces oxygen-containing regeneration gas for regeneration treatment. The regenerated catalyst is then conveyed back to the catalytic cracking reaction system for recycling.

[0009] In one embodiment, the solid organic waste is derived from one or more of waste plastics, waste rubber, and wood-plastic composites. Preferably, the waste plastics are selected from polyolefins and polyesters; and the waste rubber is selected from waste tires.

[0010] In one embodiment, the pyrolysis treatment is carried out at a temperature of 300-1000°C in an inert atmosphere, and the pyrolysis catalyst is selected from Y-type and ZSM-5 type molecular sieves.

[0011] In one embodiment, the liquid phase pyrolysis product is injected from the lower part and / or bottom of the stripping section, and the weight ratio of the amount of carbon deposition catalyst to the liquid phase pyrolysis product injected into the stripping section is 10-300:1.

[0012] In one embodiment, after the carbonized catalyst flows to the stripping section, stripping steam is injected for stripping.

[0013] In one embodiment, the method further includes: mixing the solid-phase pyrolysis product with a spent catalyst from a catalytic cracking reaction system in a mixing tank, the mixing tank being disposed in a spent inclined tube connecting the catalytic cracking reaction system and the regeneration system.

[0014] In one embodiment, the weight ratio of the liquid phase pyrolysis product injected into the stripping section to the weight of the solid phase pyrolysis product added to the mixing tank is 10-150:1.

[0015] In one embodiment, the oxygen-containing regenerated gas is oxygen, and the regeneration system is a dual regenerator regeneration system or a two-stage regeneration system.

[0016] In one embodiment, in the dual regenerator regeneration system or the two-stage regeneration system, the regeneration temperature of the first regenerator or the first regeneration stage is 550-720°C, and the catalyst residence time is 2.0-90 seconds; the regeneration temperature of the second regenerator or the second regeneration stage is 580-750°C, and the catalyst residence time is 0.5-5 minutes.

[0017] In one embodiment, after the carbonized catalyst flows to the stripping section, stripping steam is not injected for stripping.

[0018] In one embodiment, the liquid phase pyrolysis product is injected from the bottom of the stripping section, and the weight ratio of the amount of carbon deposition catalyst to the liquid phase pyrolysis product injected into the stripping section is 10-300:1.

[0019] In one embodiment, the method further includes: mixing the solid-phase pyrolysis product with a mixture from a catalytic cracking reaction system in a mixing tank, the mixing tank being connected to the catalytic cracking reaction system and the regeneration system via a waiting inclined tube.

[0020] In one embodiment, the weight ratio of the catalyst to be generated to the solid-phase pyrolysis product added to the mixing tank is 30-300:1.

[0021] In one embodiment, the oxygen-containing regenerated gas is oxygen, and the regeneration system is a dual regenerator regeneration system or a two-stage regeneration system.

[0022] In one embodiment, in the dual regenerator regeneration system or the two-stage regeneration system, the regeneration temperature of the first regenerator or the first regeneration stage is 500-720°C, and the catalyst residence time is 1-6 minutes; the regeneration temperature of the second regenerator or the second regeneration stage is 580-750°C, and the catalyst residence time is 0.5-3 minutes.

[0023] In one embodiment, the method further includes: recycling the regenerated flue gas back to a first regenerator or a first regeneration section, and / or recycling the regenerated flue gas back to a second regenerator or a second regeneration section, such that the oxygen concentration in the first regenerator or the first regeneration section and / or the second regenerator or the second regeneration section is not higher than 28%.

[0024] In one embodiment, the amount of coke burned in the first regenerator or the first regeneration section is 30-50%, and the amount of coke burned in the second regenerator or the second regeneration section is 50-70%.

[0025] 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.

[0026] This application also provides a catalytic cracking reaction-regeneration apparatus, comprising:

[0027] The catalytic cracking reaction system includes:

[0028] A catalytic cracking reactor is used to bring feedstock oil into contact with a catalyst for reaction.

[0029] The oil-gas separation unit is used to separate the catalyst and the oil gas.

[0030] A settling tank, which includes a stripping section and a catalyst for settling and stripping settling;

[0031] Solid organic waste treatment systems include:

[0032] The pyrolysis unit is used to pyrolyze solid organic waste to obtain liquid-phase pyrolysis products and / or solid-phase pyrolysis products;

[0033] Liquid phase storage tanks are used to store liquid phase pyrolysis products;

[0034] Solid storage tanks are used to store solid pyrolysis products;

[0035] The liquid phase storage tank is connected to the stripping section of the settling tank, so that the liquid phase pyrolysis products are injected into the stripping section of the settling tank.

[0036] The regeneration system includes:

[0037] 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

[0038] 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.

[0039] In one embodiment, the regeneration system further includes a mixing tank disposed outside the regenerator and connected to the regenerator and the catalytic cracking reaction system via the pre-regenerated inclined tube; the mixing tank is also in fluid communication with the solid phase storage tank, so that the solid phase pyrolysis products from the solid phase storage tank are mixed with the pre-regenerated catalyst in the mixing tank to obtain a mixture.

[0040] In one embodiment, the regenerator is a two-stage regenerator, the two-stage regenerator comprising:

[0041] The first regeneration section is provided with a first oxygen inlet, a mixture inlet and an optional first circulating flue gas inlet, wherein the regeneration inclined tube is connected to the mixture inlet of the first regeneration section for conveying the mixture from the mixing tank to the first regeneration section via the mixture inlet;

[0042] The second regeneration section is provided with a second oxygen inlet, a regeneration catalyst outlet, and an optional second circulating flue gas inlet; wherein, the outlet end of the first regeneration section is located inside the second regeneration section, so that part of the regenerant from the first regeneration section is transported to the second regeneration section; the regeneration inclined tube is connected to the regeneration catalyst outlet of the second regeneration section for recycling the regeneration catalyst from the second regeneration section back to the catalytic cracking reaction system;

[0043] A cyclone separator, housed inside a second regeneration section, is used to separate regeneration flue gas and regeneration catalyst.

[0044] In one embodiment, the regenerator is a dual regenerator, comprising:

[0045] The first regenerator is provided with a first oxygen inlet, a mixture inlet and an optional first circulating flue gas inlet, wherein the pre-regenerated inclined tube is connected to the mixture inlet of the first regenerator and is used to transport the mixture from the mixing tank to the first regenerator for semi-regeneration.

[0046] 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;

[0047] A cyclone separator, housed inside a first regenerator, is used to separate regenerated flue gas and semi-regenerated catalyst.

[0048] In one embodiment, the regeneration system further includes:

[0049] A flue gas energy recovery unit, which is connected to the cyclone separator, is used to recover the heat of the regenerated flue gas;

[0050] 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.

[0051] The method and apparatus of this application utilize the pyrolysis products of solid organic waste to drive a catalytic cracking reaction-regeneration unit, enabling efficient utilization of solid organic waste by converting it into high-value products and powering the catalytic cracking reaction-regeneration unit. This invention combines the utilization of solid organic waste with catalytic cracking, partially converting solid organic waste into high-value products and partially powering the catalytic cracking unit, thus reducing energy consumption and carbon emissions, while providing a new method for the efficient utilization of waste.

[0052] The main advantages of this invention are as follows:

[0053] (1) By directly introducing the pyrolysis oil of solid organic waste from the stripping section into the catalytic cracking unit, high-value products can be produced. 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.

[0054] (2) The pyrolysis oil of solid organic waste has a complex composition and is difficult to use directly. Injecting it into the stripping section of the reactor can partially convert it into high-value products, improve its economic value, and expand the recycling path of solid organic waste.

[0055] (3) The heat supply capacity of the catalytic cracking unit is enhanced by the pyrolysis products of solid organic waste. The excess heat generated can be used to generate high-pressure steam to supply other units. The high concentration of carbon dioxide in the flue gas generated during the regeneration process is beneficial to the separation and capture of carbon dioxide, thus achieving negative carbon emissions. Attached Figure Description

[0056] Figure 1 A schematic diagram of one embodiment of a catalytic cracking reaction-regeneration unit is shown.

[0057] Figure 2 A schematic diagram illustrating another embodiment of a catalytic cracking reaction-regeneration unit is shown. Detailed Implementation

[0058] 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.

[0059] 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.

[0060] 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.

[0061] This application provides a catalytic cracking reaction-regeneration method, including:

[0062] 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.

[0063] S2 enables solid organic waste to undergo pyrolysis in a solid organic waste treatment system to obtain solid-phase pyrolysis products and / or liquid-phase pyrolysis products.

[0064] S3 injects the liquid-phase pyrolysis product 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.

[0065] S4 conveys a mixture containing the catalyst to be generated and unreacted liquid-phase pyrolysis products to the regeneration system and introduces oxygen-containing regeneration gas for regeneration treatment. The regenerated catalyst is then conveyed back to the catalytic cracking reaction system for recycling.

[0066] This application also provides a catalytic cracking reaction-regeneration apparatus, comprising:

[0067] The catalytic cracking reaction system includes:

[0068] A catalytic cracking reactor is used to bring feedstock oil into contact with a catalyst for reaction.

[0069] The oil-gas separation unit is used to separate the catalyst and the oil gas.

[0070] A settling tank, which includes a stripping section and a catalyst for settling and stripping settling;

[0071] Solid organic waste treatment systems include:

[0072] The pyrolysis unit is used to pyrolyze solid organic waste to obtain liquid-phase pyrolysis products and / or solid-phase pyrolysis products;

[0073] Liquid phase storage tanks are used to store liquid phase pyrolysis products;

[0074] Solid storage tanks are used to store solid pyrolysis products;

[0075] The liquid phase storage tank is connected to the stripping section of the settling tank, so that the liquid phase pyrolysis products are injected into the stripping section of the settling tank.

[0076] The regeneration system includes:

[0077] 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

[0078] 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.

[0079] 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.

[0080] like Figure 1 and Figure 2 As shown, the catalytic cracking reaction-regeneration unit includes a solid organic waste treatment system 100, which comprises:

[0081] Pretreatment unit 101 is used to properly pretreat solid organic waste.

[0082] The pyrolysis unit 102 is used for pyrolysis treatment of solid organic waste;

[0083] Liquid phase storage tank 103 is used to store liquid phase pyrolysis products;

[0084] Grinding unit 104 is used for grinding solid-phase pyrolysis products; and

[0085] Solid storage tank 105 is used to store ground solid pyrolysis products.

[0086] The solid organic waste used in this application may be derived from wood-plastic composite waste, waste plastics, and waste rubber such as waste tires. Waste plastics include, but are not limited to, polyolefins and polyesters, such as polyethylene, polypropylene, polystyrene, polyvinyl chloride, polymethyl methacrylate, polyethylene terephthalate, polycarbonate, polylactic acid, and polybutylene terephthalate.

[0087] The pretreatment performed in the pretreatment unit 101 may include one or more of washing, drying, crushing, screening, metal removal, and melting, for removing surface impurities from solid organic waste and crushing it to a particle size suitable for the next pyrolysis treatment.

[0088] Solid organic waste is pyrolyzed in pyrolysis unit 102 to obtain liquid-phase pyrolysis products and / or solid-phase pyrolysis products. Waste plastics and waste rubber, such as waste tires, can be co-pyrolyzed or pyrolyzed separately. Waste rubber, such as waste tires, and waste plastics can be pyrolyzed or catalytically pyrolyzed to obtain pyrolysis oil (liquid-phase pyrolysis product) and / or pyrolysis carbon black (solid-phase pyrolysis product). In one embodiment, the pyrolysis temperature can be 300-1000℃, and the pyrolysis process is carried out under an inert atmosphere such as nitrogen. The catalytic pyrolysis catalyst can be selected from Y-type and ZSM-5 type molecular sieves.

[0089] According to the present invention, the raw materials for pyrolysis or catalytic pyrolysis are widely available and do not need to be classified. For example, it can be a single waste plastic that is pyrolyzed or catalytically pyrolyzed, or it can be a mixture of multiple waste plastics that is pyrolyzed or catalytically pyrolyzed. It can be waste tires and a single waste plastic that are pyrolyzed or catalytically pyrolyzed, or it can be a mixture of waste tires and multiple waste plastics that is pyrolyzed or catalytically pyrolyzed.

[0090] The liquid-phase pyrolysis products can be directly transported to the liquid-phase storage tank 103 for subsequent use. The solid-phase pyrolysis products, as needed, can be ground into particles of a certain size by the grinding unit 104 and then transported to the solid-phase storage tank 105. The particle size of the solid-phase pyrolysis products matches the particle size of the catalyst to facilitate uniform mixing with the catalyst to be recycled. According to the present invention, the obtained solid-phase pyrolysis products can be ground to achieve a particle size distribution between 30 and 500 micrometers. These processes can be carried out in the grinding unit 104. According to the present invention, the particle size of the solid-phase pyrolysis products introduced into the regeneration system has certain requirements, specifically a particle size of 30 to 500 micrometers. This particle size allows for good and more uniform mixing with the catalyst to be recycled, facilitating heat conduction, more complete combustion, and preventing residual particles or ash from being carried into the reactor along with the catalyst. Subsequently, the granular solid-phase pyrolysis products are mixed with the catalyst to be recycled and then introduced into the regeneration system 200 for regeneration.

[0091] like Figure 1 and 2 As shown, the catalytic cracking reaction system 300 includes:

[0092] Catalytic cracking reactor 310 is used to bring feedstock oil into contact with catalyst for reaction;

[0093] Oil separation unit 320 is used to separate catalyst and oil gas;

[0094] Settler 330, which includes stripping section 331, and catalyst for settling and stripping settling.

[0095] 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 liquid phase storage tank 103 is connected to the stripping section 331 of the settling tank 330, allowing the liquid phase pyrolysis products to be injected into the stripping section and react with the carbonized catalyst to obtain a spent catalyst and a second product. These are then separated by the oil-gas separation unit 320. The separated oil and gas products (the second product) are collected in the gas collecting chamber 340 and then fed together with the first product into the product separation unit 350 for further separation to obtain various oil and gas products. The spent catalyst and unreacted liquid phase pyrolysis products are transported together through the spent catalyst inclined pipe 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.

[0096] like Figure 1 As shown, the catalytic cracking regeneration device of this application includes a regeneration system 200, which includes:

[0097] Regenerator 210, which is fluidly connected to catalytic cracking reaction system 300 via a regeneration inclined tube 335, is used to supply regenerated catalyst from catalytic cracking reaction system 300 to regenerator 210; regenerator 210 is also fluidly connected to catalytic cracking reaction system 300 via regeneration inclined tube 305, for recycling regenerated catalyst from regenerator 210 back to catalytic cracking reaction system 300; and

[0098] Heat exchanger 230 is used to transfer heat from regeneration system 200 to the outside and to control the catalyst bed temperature in regeneration system 200 to not exceed 750°C.

[0099] In one embodiment, the regeneration system 200 further includes a mixing tank 220 disposed outside the regenerator and connected to the stripping section 331 of the settling tank 330 and the regenerator 210 respectively via the pre-regenerated inclined tube 335; the mixing tank 335 is also in fluid communication with the solid phase storage tank 105, so that the solid phase pyrolysis products from the solid phase storage tank are mixed with the pre-regenerated catalyst in the mixing tank to obtain a mixture. Of course, the mixing tank 220 may not be present, so that the pre-regenerated catalyst and the unreacted liquid phase pyrolysis products are directly transported to the regeneration system 200 for regeneration via the pre-regenerated inclined tube 335 without mixing in the solid phase pyrolysis products.

[0100] The regeneration system 200 can be selected from single-regenerator regeneration systems, dual-regenerator regeneration systems, single-stage regeneration systems, and two-stage regeneration systems, depending on the form of the regenerator.

[0101] Figure 1 One implementation of a two-stage regeneration system is shown. For example... Figure 1 As shown, the regenerator 210 includes:

[0102] The first regeneration section 211 is provided with a first oxygen inlet 2110, a mixture inlet 2111 and an optional first circulating flue gas inlet 2112, wherein the pre-regeneration inclined tube 335 is connected to the mixture inlet 2111 of the first regeneration section and is used to transport the mixture from the mixing tank to the first regeneration section 211 via the mixture inlet.

[0103] The second regeneration section 212 is provided with a second oxygen inlet 2120, a regeneration catalyst outlet 2121, and an optional second circulating flue gas inlet 2122; wherein, the outlet end of the first regeneration section is located inside the second regeneration section, so that part of the regenerant from the first regeneration section is transported to the second regeneration section; the regeneration inclined tube 305 is connected to the regeneration catalyst outlet 2121 of the second regeneration section for recycling the regeneration catalyst from the second regeneration section back to the catalytic cracking reaction system;

[0104] Cyclone separator 213, which is housed inside the second regeneration section, is used to separate regeneration flue gas and regeneration catalyst.

[0105] In this two-stage regeneration system, oxygen is typically used as the oxygen-containing regeneration gas. The first regeneration stage 211 can be a tubular coking tube, where the mixture from the pre-regeneration inclined tube 335 contacts and reacts with oxygen diluted in the flue gas, partially regenerating the catalyst. Moving upwards to the second regeneration stage 212, it continues to contact the diluted oxygen in the flue gas and undergoes coke combustion, completely regenerating the catalyst. When using oxygen as the oxygen-containing regeneration gas, the regenerated flue gas is recycled back to the first regeneration stage, and / or back to the second regeneration stage, 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 regeneration stages does not exceed 28% (by volume). Coking under this atmosphere increases coking intensity; the absence of nitrogen in the inlet gas reduces energy consumption for gas preheating; and the higher carbon dioxide concentration in the regenerator outlet flue gas facilitates carbon dioxide separation and capture.

[0106] Figure 2 One embodiment of a dual-regenerator regeneration system 400 is shown, wherein the regenerator 410 includes:

[0107] The first regenerator 411 is provided with a first oxygen inlet 4110, a mixture inlet 4111 and an optional first circulating flue gas inlet 4112, wherein the waiting-to-regenerate inclined tube 335 is connected to the mixture inlet 4111 of the first regenerator and is used to transport the mixture from the mixing tank to the first regenerator 411 for semi-regeneration.

[0108] 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;

[0109] Cyclone separator 413, which is housed inside the first regenerator, is used to separate regenerated flue gas and semi-regenerated catalyst.

[0110] Similarly, in one embodiment, the dual regenerator regeneration system 400 further includes a mixing tank 420, which is disposed outside the regenerator and connected to the stripping section 331 of the regenerator 410 and the settling tank 330 respectively via the pre-regenerated inclined tube 335; the mixing tank 335 is also in fluid communication with the solid phase storage tank 105, so that the solid phase pyrolysis products from the solid phase storage tank are mixed with the pre-regenerated catalyst in the mixing tank to obtain a mixture. Of course, the mixing tank 420 may not be present, so that the pre-regenerated catalyst and the unreacted liquid phase pyrolysis products are directly transported to the regeneration system 400 for regeneration via the pre-regenerated inclined tube 335 without mixing in the solid phase pyrolysis products.

[0111] 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.

[0112] 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.

[0113] In one embodiment, the regeneration system 200, 400 further includes:

[0114] Flue gas energy recovery units 240 and 440 are connected to the cyclone separator and are used to recover the heat of the regenerated flue gas.

[0115] 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.

[0116] During regeneration, the catalyst (or mixture) entering through the inclined tube is fed into the first regenerator, where it comes into contact with oxygen, resulting in partial coking. Afterward, it enters the second regenerator via an 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.

[0117] 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.

[0118] In one embodiment, the liquid phase pyrolysis product is injected from the lower and / or bottom (preferably the bottom) of the stripping section, and the weight ratio of the amount of carbon deposition catalyst to the liquid phase pyrolysis product injected into the stripping section is 10-300:1, for example 10-200:1, for example 20-100:1.

[0119] In one embodiment, after the carbonized catalyst flows to the stripping section, stripping steam is injected for stripping. For example... Figure 1As shown, a stripping medium inlet 332 is provided in the stripping section 331 for injecting stripping steam. In this embodiment, the method further includes: mixing the solid-phase pyrolysis product with the spent catalyst from the catalytic cracking reaction system in a mixing tank, the mixing tank being connected to the catalytic cracking reaction system and the regeneration system via a spent catalyst inclined tube. In one embodiment, the weight ratio of the liquid-phase pyrolysis product injected into the stripping section to the weight of the solid-phase pyrolysis product added to the mixing tank is 10-150:1. In one embodiment, the oxygen-containing regeneration gas is oxygen, and the regeneration system is a dual-regenerator regeneration system or a two-stage regeneration system. Further, in the dual-regenerator regeneration system or the two-stage regeneration system, the regeneration temperature of the first regenerator or the first regeneration stage is 550-720°C, and the catalyst residence time is 2.0-90 seconds; the regeneration temperature of the second regenerator or the second regeneration stage is 580-750°C, and the catalyst residence time is 0.5-5 minutes.

[0120] In one embodiment, after the carbonized catalyst flows to the stripping section, stripping steam is not injected for stripping. For example... Figure 2 As shown, no stripping medium inlet is provided in the stripping section 331; therefore, stripping steam is not injected into the stripping section through the stripping medium inlet provided in the stripping section 331. In this embodiment, the method further includes: mixing the solid-phase pyrolysis product with a mixture from the catalytic cracking reaction system in a mixing tank, the mixing tank being disposed in a waiting inclined tube connecting the catalytic cracking reaction system and the regeneration system. The weight ratio of the waiting catalyst to the weight of the solid-phase pyrolysis product added to the mixing tank is 30-300:1. In one embodiment, the oxygen-containing regeneration gas is oxygen, and the regeneration system is a dual regenerator regeneration system or a two-stage regeneration system. Further, in the dual regenerator regeneration system or the two-stage regeneration system, the regeneration temperature of the first regenerator or the first regeneration stage is 500-720°C, and the catalyst residence time is 1-6 minutes; the regeneration temperature of the second regenerator or the second regeneration stage is 580-750°C, and the catalyst residence time is 0.5-3 minutes.

[0121] In one embodiment, when regeneration is performed in a two-stage regeneration system or a dual-regenerator regeneration system, the amount of coke burned in the first regenerator or the first regeneration stage is 30-50%, and the amount of coke burned in the second regenerator or the second regeneration stage is 50-70%.

[0122] 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.

[0123] On the one hand, the amount of solid organic waste such as waste plastics and waste tires is increasing daily, but existing recycling technologies are far from meeting the huge demand for the disposal of such organic solid waste. The massive amount of solid organic waste generated each year represents a huge waste of energy and resources, and the recycling of solid waste is an important research direction in the current context. The accumulation of solid organic waste such as waste plastics and waste tires has brought serious environmental problems. How to achieve efficient and clean disposal and reasonable resource recycling of solid organic waste such as waste plastics and waste tires has become a century-old challenge faced by all economies in the world. Landfill disposal produces carbon dioxide and methane, and the greenhouse effect of methane is 28 times that of carbon dioxide; moreover, plastics are difficult to classify, and the products of pyrolysis of mixed plastics have a complex composition, making further refining difficult. The pyrolysis oil obtained from solid organic waste has a complex composition and is difficult to use directly. Existing upgrading methods and processes are relatively complex. The method and apparatus of this application directly inject the pyrolysis oil of solid organic waste into the stripping section of a catalytic cracking unit, partially converting it into high-value products, and the remaining part, along with the spent catalyst, enters the catalyst regeneration unit for coking regeneration. The method and apparatus provided by this invention are highly efficient at treating solid organic waste, improving economic value and releasing fewer greenhouse gases compared to landfilling. Furthermore, in addition to meeting the heat requirements of the catalytic cracking reaction system, excess heat can be used to generate high-pressure steam for external energy supply, achieving carbon dioxide enrichment. The method and apparatus provided in this application successfully couple waste treatment with catalytic cracking, increasing the production of high-value products while creating social benefits.

[0124] 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.

[0125] like Figure 1As shown, waste plastics or waste tires first enter the pretreatment unit 101 for pretreatment, and then are transported to the pyrolysis unit 102 to obtain pyrolysis products. The liquid phase pyrolysis products are transported to the storage tank 103, and the solid phase pyrolysis products are ground into particles of a certain size by the grinding unit 104 and then transported to the storage tank 105. The liquid phase pyrolysis products are transported to the stripping section 331 to contact with the carbon deposit catalyst and react. The resulting second reaction product, together with the stripping oil and gas (and simultaneously injected with stripping steam through the stripping medium inlet 332), enters the gas collecting chamber 340. The unreacted pyrolysis oil and the catalyst to be recycled enter the catalyst mixing tank 220 through the catalyst recycling inclined pipe 335. In the tank, the catalyst is mixed with the solid phase pyrolysis products from the storage tank 10 and then transported to the coking pipe (first regeneration section) 211 to contact with the oxygen diluted by the flue gas and react. The catalyst is partially regenerated and then continues to contact with the oxygen diluted by the flue gas after moving to the second regeneration section 212 to undergo coke combustion reaction, completing the regeneration. The regenerated catalyst enters the bottom of the reactor through the regeneration inclined tube 305, rises under the action of pre-lifting steam, contacts and reacts with the feed oil atomized by the atomizing steam, and the first and second products obtained after cyclone separation enter the subsequent product separation unit 350. The obtained carbonized catalyst enters the stripping section for recycling. The regenerated flue gas, after energy recovery, enters the carbon dioxide separation system 250.

[0126] like Figure 2 As shown, waste plastics or waste tires first enter the pretreatment unit 101 for pretreatment, and then are transported to the pyrolysis unit 102 to obtain pyrolysis products. The liquid phase pyrolysis products are transported to the storage tank 103, and the solid phase pyrolysis products are ground into particles of a certain size by the grinding unit 104 and then transported to the storage tank 105. The liquid phase pyrolysis products are transported to the stripping section 331 to replace the original stripping steam (no stripping steam is injected), and the resulting second reaction products enter the gas collecting chamber 340. Unreacted pyrolysis oil and the catalyst to be recycled enter the mixing tank 220 through the recycling inclined pipe 335. In the tank, the catalyst is selectively mixed with the solid phase pyrolysis products from the storage tank 10 and then transported to the first regenerator 411 to contact with the oxygen diluted by the flue gas and react, and the catalyst is partially regenerated. After being transported to the second regenerator 412 through the external circulation pipe 414, it continues to contact with the oxygen diluted by the flue gas to undergo coke combustion reaction, completing the regeneration. The regenerated catalyst enters the bottom of the reactor through the regeneration inclined tube 305, rises under the action of pre-lifting steam, contacts and reacts with the feed oil atomized by the atomizing steam, and the first and second products obtained after cyclone separation enter the subsequent product separation unit 350. The obtained carbonized catalyst enters the stripping section for recycling. The regenerated flue gas, after energy recovery, enters the carbon dioxide separation system 250.

[0127] The present invention will be further illustrated by the following examples, but the present invention is not limited thereto. The feedstock oil A and feedstock oil B used in the examples and comparative examples are listed in Tables 1-1 and 1-2, respectively.

[0128] 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.

[0129] The preparation process of catalyst b is as follows:

[0130] (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.

[0131] (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.

[0132] (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.

[0133] Example 1

[0134] Example 1 in Figure 1 The procedure is performed on the apparatus shown, wherein,

[0135] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0136] Waste plastic oil is obtained by pyrolyzing PE at 500℃. Its 50% distillation temperature is 180℃, its 90% distillation temperature is 280℃, and its density is 790 kg / m³. 3 The sulfur content is 45 mg / kg, the moisture content is 0.03%, and the calorific value is 42 MJ / kg. The solid pyrolysis product is pyrolytic carbon black with a calorific value of 30 MJ / kg.

[0137] 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, where it contacts and reacts with waste plastic oil (the weight ratio of the catalyst to the waste plastic oil is 45:1) to obtain a second product. The second product, along with stripping gas (generated by stripping steam injected into the stripping section), enters the gas collecting chamber and, together with the first product, enters the fractionation unit for distillation according to the distillation range to obtain various oil and gas products. Unreacted waste plastic oil and the catalyst are transported to a mixing tank on the inclined tube, where they are mixed with pyrolytic carbon black (the weight ratio of pyrolytic oil to pyrolytic carbon black is 16.7:1) and transported to the coking tube (first regeneration section) for partial regeneration. The mixture then ascends to the second regeneration section to complete regeneration. Simultaneously, some of the flue gas from the cyclone separator in the second regeneration section returns to both the first and second regeneration sections, controlling the oxygen content in the mixed atmosphere to not exceed 28% (by volume). Excess energy generated by the regenerator is used for external power supply through a heat exchanger.

[0138] The temperature in the first regeneration section is 640℃, and the residence time is 75 seconds. The temperature in the second regeneration section is 645℃, and the residence time is 5.0 minutes. The regenerated catalyst is recycled back to the reactor and comes into contact with the feedstock oil for catalytic cracking. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 3.

[0139] Comparative Example 1

[0140] Comparative Example 1 was conducted on the same apparatus as Example 1, with the same reaction and regeneration conditions. The difference was that waste plastic oil was not injected into the stripping section, nor was pyrolytic carbon black introduced for heat replenishment. Instead, heat was replenished by injecting fuel oil (feedstock oil A) into the second regeneration section to achieve heat balance. The regenerated catalyst was 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.

[0141] Example 2

[0142] Implementation examples in Figure 1 The procedure is performed on the apparatus shown, wherein,

[0143] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0144] Waste plastic oil is obtained by pyrolyzing PE at 500℃. Its 50% distillation temperature is 180℃, its 90% distillation temperature is 280℃, and its density is 790 kg / m³. 3 The sulfur content is 45 mg / kg, the moisture content is 0.03%, and the calorific value is 42 MJ / kg. The solid pyrolysis product is pyrolytic carbon black with a calorific value of 30 MJ / kg.

[0145] Using feedstock oil 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: Waste plastic oil (the weight ratio of the catalyst to the waste plastic oil is 100:1) is injected into the stripping section to contact the carbonized catalyst and react to obtain a second product. The second product, along with stripping oil and gas (generated by stripping steam injected into the stripping section), enters the fractionation unit to obtain various oil and gas products. Unreacted waste plastic oil and heavier products, along with the catalyst to be recycled, are transported from the recycled inclined tube to the recycled mixing tank and mixed with pyrolytic carbon black (the weight ratio of pyrolytic oil to pyrolytic carbon black is 16:1). This mixture is then transported to the regeneration system to contact with oxygen diluted in the circulating flue gas and undergo coke combustion. The catalyst is partially regenerated in the coke burning tube (first regeneration section), and the partially regenerated catalyst is then moved upwards to the second regeneration section for complete regeneration. After cyclone separation, a portion of the flue gas is recycled back to the first and second regeneration sections 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.

[0146] The first regeneration section has a temperature of 640℃ and a residence time of 60 seconds, while the second regeneration section has a temperature of 645℃ and a residence time of 4.0 minutes. The regenerated catalyst is recycled back to the reactor to undergo catalytic cracking with the feedstock. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 4.

[0147] Comparative Example 2

[0148] The comparative example and Example 2 were carried out on the same apparatus, and the reaction and regeneration were conducted under the same methods and conditions. Waste plastic oil was not injected into the stripping section, nor was pyrolytic carbon black supplied to supplement heat. Fuel oil (feed oil A) was added to the second regeneration section as a supplementary energy source to compensate for insufficient heat supply. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 4.

[0149] As can be observed from the data in Tables 3 and 4, injecting waste plastic oil into the stripping section in the embodiment increased the product yield and significantly reduced the consumption of fossil energy, which is conducive to the low-carbon development of catalytic cracking.

[0150] Example 3

[0151] Example 3 in Figure 2 The procedure is performed on the apparatus shown, wherein,

[0152] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0153] Waste plastic oil is obtained by pyrolyzing PE and packaging materials at 500℃. Its 50% distillation temperature is 188℃, its 90% distillation temperature is 314℃, and its density is 802 kg / m³. 3 It has a sulfur content of 60 mg / kg, a moisture content of 2.04%, and a calorific value of 40 MJ / kg.

[0154] 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 (in this embodiment, stripping steam is not introduced into the stripping section) and reacts with waste plastic oil (the weight ratio of the catalyst to waste plastic oil is 44:1) to obtain a second product. The second product enters the gas collecting chamber and, together with the first product, enters the fractionation unit to be cut according to the distillation range to obtain various oil and gas products. Unreacted waste plastic oil and the catalyst to be generated are transported to the first regenerator for partial regeneration, and then transported to the second regenerator through an external circulation pipe to complete the regeneration. At the same time, part of the flue gas from the cyclone separation system of the first regenerator is returned to the regeneration system, and the oxygen content of the mixed gas in the first and second regenerators is controlled to not exceed 28% (by volume). The excess energy generated by the regeneration system is used for external power supply through a heat exchanger.

[0155] The first regenerator temperature was 630℃ with a residence time of 5.0 minutes, and the second regenerator temperature was 645℃ with a residence time of 2.5 minutes. The regenerated catalyst was 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.

[0156] Comparative Example 3

[0157] Comparative Example 3 was conducted on the same apparatus as Example 3, with the same reaction and regeneration conditions as Example 1. The difference was that waste plastic oil was not injected into the stripping section, stripping steam was injected instead, and pyrolytic carbon black was not introduced for supplemental heating. Heat was supplemented by injecting fuel oil (feed oil A) into the second regenerator to achieve heat balance. The regenerated catalyst was recycled back to the reactor to contact the feed oil for catalytic cracking. The regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 5.

[0158] Example 4

[0159] Example 4 in Figure 2 The procedure is performed on the apparatus shown, wherein,

[0160] The structure of the catalytic cracking reactor can be found in Figure 4, reactor 302, of CN 111718230 A.

[0161] Waste plastic oil is obtained by pyrolyzing PE and packaging materials at 500℃. Its 50% distillation temperature is 188℃, its 90% distillation temperature is 314℃, and its density is 802 kg / m³. 3 It has a sulfur content of 60 mg / kg, a moisture content of 2.04%, and a calorific value of 40 MJ / kg.

[0162] Using C5-C8 olefins (where the molar ratio of C5 olefins:C6 olefins:C7 olefins:C8 olefins is 1:1:1:1) 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: Waste plastic oil (the weight ratio of the catalyst to the waste plastic oil is 85:1) is injected into the stripping section to replace the stripping steam and contact the carbonized catalyst to react (in this embodiment, stripping steam is not introduced into the stripping section). The product enters the gas collecting chamber and, together with the catalytic cracking products of feedstock oil B, enters the fractionation unit to obtain various oil and gas products. Unreacted waste plastic oil and heavier products, along with the catalyst to be recycled, are transported from the recycled inclined tube to the regeneration system to contact with oxygen diluted by the circulating flue gas and undergo coke combustion. The catalyst is partially regenerated in the first regenerator, and the partially regenerated catalyst is then transported through the external circulation pipe to the second regenerator for complete regeneration. After being separated by a cyclone separator, a portion of the flue gas is recycled back to the regeneration system, ensuring that the oxygen content of the mixed gas in the first and second regenerators does not exceed 28% (by volume). The remaining portion, after energy recovery, enters the carbon dioxide separation and capture device. Excess energy from the regenerators is converted into high-pressure steam through a heat extraction system for external energy supply.

[0163] The first regenerator temperature was 640℃ with a residence time of 5.0 minutes, and the second regenerator temperature was 645℃ with a residence time of 2.0 minutes. The regenerated catalyst was 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.

[0164] Comparative Example 4

[0165] Comparative Example 4 and Example 4 were carried out on the same apparatus, with the same reaction and regeneration methods and conditions. Waste plastic oil was not injected into the stripping section; instead, stripping steam was injected, and pyrolytic carbon black was not supplied to supplement heat. Insufficient heat was used to supplement fuel oil (feed oil A) as an energy source for the second regenerator. Regeneration conditions, reaction conditions, and carbon dioxide emissions are shown in Table 6.

[0166] As can be observed from the data in Tables 5 and 6, the product yield increased and the consumption of fossil energy decreased significantly when waste plastic oil was used instead of stripping steam in the stripping section in the embodiment. This is conducive to the low-carbon development of catalytic cracking.

[0167] 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.

[0168] 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.

[0169] 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.

[0170] Table 1-1 Properties of Crude Oil A

[0171] 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

[0172] Table 1-2 Properties of Crude Oil B

[0173]

[0174] Table 2

[0175]

[0176] Table 3

[0177]

[0178] Based on processing 100g of raw material.

[0179] *: During catalytic cracking, coke produced from feedstock oil will adhere to the catalyst. For Example 1, this amount refers to the amount of feedstock oil that produces coke, based on processing 100g of feedstock. For Comparative Example 1, this amount refers to the total amount of feedstock oil that produces coke and the added fuel oil, based on processing 100g of feedstock.

[0180] Table 4

[0181]

[0182] Based on processing 100g of raw material.

[0183] *: During catalytic cracking, the catalyst will be coated with feedstock oil and coke produced from the feedstock. For Example 2, this amount refers to the amount of feedstock oil that produces coke, based on processing 100g of feedstock. For Comparative Example 2, this amount refers to the total amount of feedstock oil that produces coke and the added fuel oil, based on processing 100g of feedstock.

[0184] Table 5

[0185]

[0186] Based on processing 100g of raw material.

[0187] #: External energy delivery refers to the excess energy generated by the regeneration system when processing 1 ton of crude oil.

[0188] *: During catalytic cracking, coke produced from feedstock oil will adhere to the catalyst. For Example 3, this amount refers to the amount of feedstock oil that produces coke, based on processing 100g of feedstock. For Comparative Example 3, this amount refers to the total amount of feedstock oil that produces coke and the added fuel oil, based on processing 100g of feedstock.

[0189] Table 6

[0190]

[0191] Based on processing 100g of raw material.

[0192] *: During catalytic cracking, coke produced from feedstock oil will adhere to the catalyst. For Example 4, this amount refers to the amount of feedstock oil that produces coke, based on processing 100g of feedstock. For Comparative Example 4, this amount refers to the total amount of feedstock oil that produces coke and the added fuel oil, based on processing 100g of feedstock.

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 enables solid organic waste to undergo pyrolysis in a solid organic waste treatment system to obtain solid-phase pyrolysis products and liquid-phase pyrolysis products; S3 injects the liquid-phase pyrolysis product 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. S4 conveys a mixture containing the catalyst to be recycled and unreacted liquid-phase pyrolysis products to the regeneration system and introduces oxygen-containing regeneration gas for regeneration. The regenerated catalyst is then returned to the catalytic cracking reaction system for recycling. The liquid-phase pyrolysis products are injected from the lower part and / or bottom of the stripping section, and the weight ratio of the amount of carbon deposition catalyst to the liquid-phase pyrolysis products injected into the stripping section is 10-300:

1.

2. The catalytic cracking reaction-regeneration method according to claim 1, wherein, The solid organic waste is derived from one or more of waste plastics, waste rubber, and wood-plastic composite materials.

3. The catalytic cracking reaction-regeneration method according to claim 2, wherein, The pyrolysis treatment is carried out at a temperature of 300-1000℃ in an inert atmosphere, and the pyrolysis catalyst is selected from Y-type and ZSM-5 type molecular sieves.

4. The catalytic cracking reaction-regeneration method according to claim 1, wherein, After the carbonized catalyst flows to the stripping section, stripping steam is injected for stripping.

5. The catalytic cracking reaction-regeneration method according to claim 4, wherein, The method further includes: mixing the solid-phase pyrolysis product with a spent catalyst from a catalytic cracking reaction system in a mixing tank, the mixing tank being disposed in a spent inclined tube connecting the catalytic cracking reaction system and the regeneration system.

6. The catalytic cracking reaction-regeneration method according to claim 5, wherein, The weight ratio of the liquid phase pyrolysis product injected into the stripping section to the weight of the solid phase pyrolysis product added to the mixing tank is 10-150:

1.

7. The catalytic cracking reaction-regeneration method according to claim 5, wherein, The oxygen-containing regenerated gas is oxygen, and the regeneration system is a dual regenerator regeneration system or a two-stage regeneration system.

8. The catalytic cracking reaction-regeneration method according to claim 7, wherein, In a dual-regenerator regeneration system or a two-stage regeneration system, the regeneration temperature of the first regenerator or the first regeneration stage is 550-720℃, and the catalyst residence time is 2.0-90 seconds; the regeneration temperature of the second regenerator or the second regeneration stage is 580-750℃, and the catalyst residence time is 0.5-5 minutes.

9. The catalytic cracking reaction-regeneration method according to claim 1, wherein, After the carbonized catalyst flows to the stripping section, no stripping steam is injected for stripping.

10. The catalytic cracking reaction-regeneration method according to claim 9, wherein, The liquid-phase pyrolysis products are injected from the bottom of the stripping section.

11. The catalytic cracking reaction-regeneration method according to claim 10, wherein, The method further includes: mixing the solid-phase pyrolysis product with a mixture from a catalytic cracking reaction system in a mixing tank, the mixing tank being connected to the catalytic cracking reaction system and the regeneration system via a waiting inclined tube.

12. The catalytic cracking reaction-regeneration method according to claim 11, wherein, The weight ratio of the catalyst to the solid pyrolysis product added to the mixing tank is 30-300:

1.

13. The catalytic cracking reaction-regeneration method according to claim 12, wherein, The oxygen-containing regenerated gas is oxygen, and the regeneration system is a dual regenerator regeneration system or a two-stage regeneration system.

14. The catalytic cracking reaction-regeneration method according to claim 13, wherein, In a dual-regenerator regeneration system or a two-stage regeneration system, the regeneration temperature of the first regenerator or the first regeneration stage is 500-720℃, and the catalyst residence time is 1-6 minutes; the regeneration temperature of the second regenerator or the second regeneration stage is 580-750℃, and the catalyst residence time is 0.5-3 minutes.

15. The catalytic cracking reaction-regeneration method according to any one of claims 8 or 14, wherein, The method further includes: recycling the regenerated flue gas back to the first regenerator or the first regeneration section, and / or recycling the regenerated flue gas back to the second regenerator or the second regeneration section, such that the oxygen concentration in the first regenerator or the first regeneration section and / or the second regenerator or the second regeneration section is not higher than 28%.

16. The catalytic cracking reaction-regeneration method according to any one of claims 8 or 14, wherein, The amount of coke burned in the first regenerator or the first regeneration section is 30-50%, and the amount of coke burned in the second regenerator or the second regeneration section is 50-70%.

17. The catalytic cracking reaction-regeneration method according to claim 1, 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.

18. 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; Solid organic waste treatment systems include: The pyrolysis unit is used to pyrolyze solid organic waste to obtain liquid-phase pyrolysis products and solid-phase pyrolysis products; Liquid phase storage tanks are used to store liquid phase pyrolysis products; Solid storage tanks are used to store ground solid pyrolysis products. The liquid phase storage tank is connected to the stripping section of the settling tank, so that the liquid phase pyrolysis products are injected into the stripping section of the settling tank. 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.

19. The catalytic cracking reaction-regeneration method according to claim 18, further comprising a mixing tank disposed outside the regenerator and connected to the regenerator and the catalytic cracking reaction system respectively via the pre-regenerated inclined tube; the mixing tank is also in fluid communication with the solid phase storage tank, such that the solid phase pyrolysis products from the solid phase storage tank are mixed with the pre-regenerated catalyst in the mixing tank to obtain a mixture.

20. The catalytic cracking reaction-regeneration method according to claim 19, wherein, The regenerator is a two-stage regenerator, wherein the two-stage regenerator includes: The first regeneration section is provided with a first oxygen inlet, a mixture inlet and an optional first circulating flue gas inlet, wherein the regeneration inclined tube is connected to the mixture inlet of the first regeneration section for conveying the mixture from the mixing tank to the first regeneration section via the mixture inlet; The second regeneration section is provided with a second oxygen inlet, a regeneration catalyst outlet, and an optional second circulating flue gas inlet; wherein, the outlet end of the first regeneration section is located inside the second regeneration section, so that part of the regenerant from the first regeneration section is transported to the second regeneration section; the regeneration inclined tube is connected to the regeneration catalyst outlet of the second regeneration section for recycling the regeneration catalyst from the second regeneration section back to the catalytic cracking reaction system; A cyclone separator, housed inside a second regeneration section, is used to separate regeneration flue gas and regeneration catalyst.

21. The catalytic cracking reaction-regeneration method according to claim 18, wherein, The regenerator is a dual regenerator, including: The first regenerator is provided with a first oxygen inlet, a mixture inlet and an optional first circulating flue gas inlet, wherein the pre-regenerated inclined tube is connected to the mixture inlet of the first regenerator and is used to transport the mixture from the mixing tank to the first regenerator for semi-regeneration. 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.

22. The catalytic cracking reaction-regeneration method according to any one of claims 20-21, 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.

23. The catalytic cracking reaction-regeneration method according to claim 2, wherein, The waste plastics are selected from polyolefins and polyesters; the waste rubber is selected from waste tires.

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