Catalytic cracking coke drum, regeneration system, and regeneration method

Abstract

This application relates to a catalytic cracking coke generator, a regeneration system, and a regeneration method. The coke generator, from bottom to top, includes a pre-lifting zone, a reaction zone (either a bubbling fluidized bed or a turbulent fluidized bed), and an outlet zone. The pre-lifting zone is connected to the bottom of the reaction zone and the regenerator, while the top of the reaction zone is connected to the outlet zone. At least one fuel oil inlet is provided at the outlet of the pre-lifting zone or at the bottom of the reaction zone. When the coke generator and system of this application are used in fluidized catalytic cracking reactions with high reaction heat, a coke source can be provided from the reaction system to the regenerator, solving the reaction heat balance problem without affecting the regeneration process and without damaging the physical and chemical properties of the catalyst.

Description

Technical Field

[0001] This application relates to the field of fluidized catalytic cracking technology, and more specifically, to a catalytic cracking coke generator, regeneration system, and regeneration method suitable for maintaining thermal equilibrium. Background Technology

[0002] Fluidized catalytic cracking is a self-heating equilibrium process. The high-temperature heat released during catalyst coking and regeneration is sufficient to meet the needs of the lower-temperature cracking reaction. The catalyst circulating between the reactor and regenerator has sufficient quantity and heat capacity, thus serving as both an active site for the reaction and a heat carrier for energy transfer. The catalyst flows between the reactor and regenerator, continuously acquiring heat from one end and supplying heat to the other. Establishing thermal equilibrium requires certain conditions to maintain the cracking and regeneration at the specified temperatures. For an industrial catalytic cracking unit, the basis for thermal equilibrium between the reactor and regenerator is that the reaction produces enough coke, which burns during regeneration, releasing heat for the reaction to use.

[0003] With the development of refining processes, especially the increasing trend of heavy / inferior crude oil and the improvement of oil product quality, hydrotreating processes are being used more widely. While hydrotreated feedstocks significantly improve product structure and quality when used as feedstock for catalytic cracking, they also lead to insufficient coke production in the catalytic cracking unit, resulting in inadequate heat supply. Furthermore, in catalytic cracking technologies targeting low-carbon olefins, the cracking reaction has high conversion rates, high temperatures, and large heat of reaction, requiring more heat than conventional fluidized bed catalytic regenerators or other catalytic conversion methods. The coke generated by the cracking process itself often cannot meet the heat balance requirements of the reaction-regeneration system. When insufficient coke production occurs during the reaction, fuel oil is typically added to the regenerator to provide the necessary heat. However, because catalytic cracking uses molecular sieves as the active catalyst, the localized high temperatures generated by fuel oil combustion in the regenerator cause aluminum to gradually detach from the molecular sieve framework, damaging the catalyst irreversibly. This does not fundamentally address the impact of the high-temperature hotspots generated by the localized combustion of externally added fuel oil on the catalyst framework structure and reaction performance.

[0004] To address this issue, existing technologies all focus on the regenerator system. Examples include creating an oxygen-deficient zone within the regenerator, introducing fuel oil into this oxygen-deficient zone to mix with the catalyst, and then burning it in the regenerator for regeneration; or installing heaters within the regenerator and using fuel nozzles configured to inject a mixture of fuel and oxygen-containing gas to supplement combustion heat; or injecting methane, relying on the heat released from methane combustion to supplement the reaction heat. While these methods mitigate the adverse effects on the catalyst, they do not fundamentally solve the problem of the high-temperature hotspots generated by the localized combustion of externally supplied fuel oil affecting the catalyst's skeletal structure and reaction performance. Summary of the Invention

[0005] The purpose of this application is to provide a catalytic cracking coke generator, coke generation system, and method to solve the problem of heat balance in the catalytic cracking reaction process from the perspective of the reaction system, without affecting the physical and chemical properties of the catalyst.

[0006] On the one hand, this application provides a catalytic cracking coke generator, which comprises, from bottom to top:

[0007] Pre-upgrade area

[0008] The coking reaction zone, wherein the coking reaction zone is a bubbling fluidized bed or a turbulent fluidized bed, and

[0009] Export area

[0010] The top of the pre-lifting zone is connected to the coking reaction zone, and the top of the coking reaction zone is connected to the outlet zone.

[0011] The bottom end of the pre-lifting zone and / or the bottom end of the coking reaction zone are configured to be connected to the regenerator for conveying the catalyst of the regenerator to the coking reactor.

[0012] At least one fuel oil inlet is provided in the middle and upper reaches of the coking reaction zone.

[0013] In one embodiment, the coking unit is provided with a pre-lift gas inlet, a catalyst inlet, and a fuel oil inlet from bottom to top.

[0014] In one embodiment, each fuel oil inlet is independently located in the middle to upper part of the coking unit; preferably, the distance between each fuel oil inlet and the bottom of the coking unit is independently 5% to 15% of the height of the coking unit.

[0015] In one embodiment, the coking reaction zone is a hollow cylinder with a length-to-diameter ratio of 20:1 to 2:1;

[0016] In one embodiment, the pre-lifting region is a hollow cylinder with a length-to-diameter ratio of 10:1 to 2:1.

[0017] The export area is a hollow cylinder with a length-to-diameter ratio of 30:1 to 5:1.

[0018] In one embodiment, the ratio of the inner diameters of the pre-lifting zone, the coking reaction zone, and the outlet zone is from 1:2:1 to 1:10:2.

[0019] In one embodiment, the outlet area of ​​the coking unit is configured to be in fluid communication with a gas-solid separation and collection device, wherein the gas-solid separation and collection device is connected to the product separation system and the regenerator respectively, so that the reaction oil and gas and the coke-containing catalyst generated by the coking unit are separated by the gas-solid separation and collection device and introduced into the product separation system and the regenerator respectively.

[0020] On the other hand, this application provides a catalytic cracking regeneration system, comprising:

[0021] The catalytic cracking coke generator of this application;

[0022] Gas-solid separation and collection equipment, and

[0023] Regenerator,

[0024] The bottom end of the pre-lifting zone and / or the bottom end of the coking reaction zone are configured to be connected to the regenerator for conveying the catalyst of the regenerator to the coking reactor.

[0025] The outlet area of ​​the catalytic cracking coke generator is in fluid communication with the gas-solid separation and collection device, so that the material from the coke generator is separated into oil and gas and coke-containing catalyst by the gas-solid separation and collection device.

[0026] The gas-solid separation and collection device is connected to the regenerator, so that the coke-bearing catalyst is transported to the regenerator.

[0027] In one embodiment, the gas-solid separation and collection device includes:

[0028] A gas-solid separation device is connected to the outlet area of ​​the catalytic cracking coke generator, so that the material from the coke generator is separated into oil and gas and coke-containing catalyst by the gas-solid separation device.

[0029] A settling device configured to collect the coke-bearing catalyst; the settling device is connected to the regenerator, such that the coke-bearing catalyst is transported to the regenerator.

[0030] In one embodiment, the gas-solid separation device is housed inside the settler.

[0031] The settling device includes a stripping section located at the lower part of the settling device, the stripping section being configured for stripping and collecting coke-laden catalyst; and the regenerator is connected to the stripping section such that the stripped coke-laden catalyst is conveyed to the regenerator.

[0032] This application also provides a method for regenerating a catalytic cracking catalyst, performed in the catalytic cracking regeneration system of this application, comprising the following steps:

[0033] Pre-lift gas is injected into the pre-lift zone of the coking unit through the pre-lift gas inlet, and comes into contact with the regenerated catalyst from the regenerator;

[0034] A mixture of atomizing medium and combustion oil is injected into the coking unit through the fuel oil inlet, so that the mixture of atomizing medium and combustion oil comes into contact with the catalyst in the coking unit, and a coking reaction occurs, resulting in a catalyst with coke and reaction oil gas.

[0035] The coke-coated catalyst and the reaction oil and gas are separated by a gas-solid separation and collection device. The separated coke-coated catalyst is introduced into a regenerator to regenerate the catalyst for recycling.

[0036] In one embodiment, the catalyst with coke is stripped and then introduced into the regenerator.

[0037] In one embodiment, the linear velocity of the coking reaction zone of the coking device is 0.3 m / s to 1.2 m / s, and the catalyst particle density is 300 kg / m³ to 700 kg / m³.

[0038] In one embodiment, the pre-lifting gas is selected from water vapor, nitrogen, dry gas, rich gas, C4 fraction and combinations thereof, and the mass ratio of the pre-lifting gas to fuel oil is 0.01:1 to 0.05:1;

[0039] Preferably, the fuel oil atomizing medium is nitrogen, and the mass ratio of the atomizing medium to the combustion oil is 0.01:1 to 0.5:1;

[0040] Preferably, the fuel oil is selected from straight-run distillate oil or secondary processed distillate oil; preferably, the secondary processed distillate oil may be selected from one or more of the following: catalytic cracking diesel oil, catalytic cracking slurry oil, coking gasoline, coking diesel oil and coking wax oil.

[0041] In one embodiment, the outlet temperature of the coking device is 460-560°C.

[0042] This application also relates to a catalytic cracking coke-forming system, including the coke-forming device of this application.

[0043] The coking unit of this application can further form coke on the catalyst, which enters the regeneration system without affecting its operation. Furthermore, there are no localized hot spots during the coking process in the regenerator, thus causing no damage to the catalyst's physical and chemical properties. The coking unit of this application has a simple structure, is easy to implement, and has strong applicability. It is particularly suitable for catalytic cracking units using low-carbon olefins and other chemical feedstocks as the main target products, fundamentally solving the heat balance problem from the reaction system end. It also reduces the damage to the catalyst and regeneration system caused by traditional fuel oil injection, saving catalyst costs and improving the refinery's economic efficiency. Attached Figure Description

[0044] The accompanying drawings are provided to further illustrate the present application and form part of the specification. They are used together with the following detailed description to explain the present application, but do not constitute a limitation thereof. In the drawings:

[0045] Figure 1 A schematic diagram of a catalytic cracking coke generator according to one embodiment of this application;

[0046] Figure 2 A schematic diagram of a coking system according to one embodiment of this application;

[0047] Figure 3 This is a schematic diagram of one implementation of a catalytic cracking reaction-regeneration system. Detailed Implementation

[0048] 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.

[0049] 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.

[0050] 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.

[0051] Any specific numerical values ​​disclosed herein (including the endpoints of numerical ranges) are not limited to their exact values, but should be understood to also include values ​​close to the exact value, such as all possible values ​​within ±5% of the exact value. Furthermore, with respect to the disclosed numerical ranges, one or more new numerical ranges can be obtained by arbitrarily combining the endpoint values ​​of the range, the endpoint values ​​with specific point values ​​within the range, and the specific point values ​​themselves; these new numerical ranges should also be considered as specifically disclosed herein.

[0052] In this application, the terms "upstream" and "downstream" refer to the direction of reaction material flow. For example, when the reaction material flows from bottom to top, "upstream" refers to the position located at the bottom, while "downstream" refers to the position located at the top.

[0053] Unless otherwise stated, the terms used herein have the same meaning as commonly understood by those skilled in the art, and if a term is defined herein and its definition differs from the common understanding in the art, the definition herein shall prevail.

[0054] like Figure 1 As shown, this application provides a catalytic cracking coke generator 300, which is suitable for regulating thermal balance. The coke generator 300 includes, from bottom to top: a pre-lifting zone I, a coke-forming reaction zone II, and an outlet zone III.

[0055] The coking reactor 300 is provided with a pre-lift gas inlet 301, a catalyst inlet 303, and a fuel oil inlet 302, arranged sequentially from bottom to top. The pre-lift gas inlet 301 is typically located in the pre-lift zone I, and generally at the bottom of the pre-lift zone I. The catalyst inlet 303 can be located in the pre-lift zone I and / or the coking reaction zone II, but is generally located in the pre-lift zone I, at the lower part of the pre-lift zone I, but above the pre-lift gas inlet 301, so that the pre-lift gas can lift the input catalyst. This allows the regenerated catalyst to be pre-accelerated and pre-fluidized, improving the catalyst distribution and facilitating uniform contact and rapid mixing with the fuel oil.

[0056] The bottom of the regenerator 500 (e.g.) Figure 2 (As shown) The catalyst inlet 303 is connected to the coking unit 300, allowing the catalyst to enter the coking unit and coke to form a coke-bearing catalyst. The top of the coking unit 300 is connected to the gas-solid separation and collection device 200, which separates the coke-bearing catalyst from the reaction oil and gas.

[0057] In one embodiment, the pre-lifting zone I, the coking reaction zone II, and the outlet zone III are connected in sequence, that is, the top of the pre-lifting zone I is connected to the coking reaction zone II, and the top of the coking reaction zone II is connected to the outlet zone III.

[0058] In this application, the pre-lift gas inlet 301, regeneration catalyst inlet 303, and fuel oil inlet 302, each independently provided on the coking unit 300, are located at different heights on the coking unit 300. Preferably, the coking unit 1 is provided with the pre-lift gas inlet 301, regeneration catalyst inlet 303, and fuel oil inlet 302 sequentially from bottom to top, and all of them are located at the lower part of the coking unit 300.

[0059] In this application, the reaction zone II of the coking device 300 is a bubbling bed or a turbulent fluidized bed. In one embodiment, the reaction zone II is a hollow cylinder with a length-to-diameter ratio of 20:1 to 2:1.

[0060] In this application, the coking unit may be provided with one or more, for example, one, two or more fuel oil inlets 302. These fuel oil inlets may be independently located at the outlet end of the pre-lifting zone I of the coking unit, or at the bottom or side wall of the coking reaction zone II. More preferably, each fuel oil inlet 302 is independently located in the middle to upper reaches of the coking unit 300. More preferably, the distance h from each fuel oil inlet 302 to the bottom of the coking unit is independently 5% to 15% of the coking unit height.

[0061] In this application, the fuel oil injected through fuel oil inlet 302 may include straight-run distillate or secondary processed distillate. Preferably, the secondary processed distillate may be selected from one or more blends of catalytic cracking diesel, catalytic cracking slurry oil, coking gasoline, coking diesel, and coking wax oil.

[0062] In one embodiment, the pre-lifting zone I is a hollow cylinder with a length-to-diameter ratio of 10:1 to 2:1. In one embodiment, the outlet zone III is a hollow cylinder with a length-to-diameter ratio of 30:1 to 5:1. In one embodiment, the ratio of the inner diameters of the pre-lifting zone I, the coking reaction zone II, and the outlet zone III is 1:2:1 to 1:10:1.

[0063] In one embodiment, the outlet zone III of the coking unit is configured to be connected with the gas-solid separation and collection device 200 (e.g., Figure 2 (As shown) fluid communication. The gas-solid separation and collection device 200 is connected to both the product separation system (not shown) and the regenerator 500, allowing the reaction oil and gas and coke-laden catalyst generated by the coking unit to be separated by the gas-solid separation and collection device and then introduced into the product separation system and regenerator 500 respectively. For example... Figure 2As shown, in one embodiment, the coking unit 300 is fluidly connected to the gas-solid separation and collection device 200, so that the reaction oil and coke-laden catalyst produced by the coking unit 300 are separated by the gas-solid separation and collection device 200. The reaction oil and gas are collected through the gas collection chamber 202 and introduced into the product separation system for recycling via the oil and gas pipeline 203. The catalyst with coke-laden material enters the stripping section 205 at the bottom of the settling tank 200. After stripping, it is introduced into the regenerator for coking through the standpipe 206, releasing heat. In this application, the gas-solid separation and collection device 200 can be any equipment well known to those skilled in the art. For example, the gas-solid separation and collection device 200 may include a gas-solid separation device 201, such as a cyclone separator, and a settling tank 210. The gas-solid separation device 201 can be housed inside the settling tank 210, so that the separated coke-laden catalyst can be collected. The settling tank 210 includes a stripping section 205 at its bottom for stripping the coke-laden catalyst. The catalyst after stripping can be introduced into regenerator 500, where it undergoes a complete combustion reaction, releasing heat and yielding a regenerated catalyst.

[0064] In this application, by setting up a coking unit 300, fuel oil can be mixed with the catalyst under low-temperature, oxygen-free fluidized bed conditions, and a coking reaction occurs in a reaction zone with the characteristics of a bubbling bed or turbulent fluidized bed. This not only results in high coke selectivity but also ensures uniform distribution of coke on the catalyst, which is beneficial for uniform combustion within the regeneration system. Furthermore, in this application, the coke generated on the catalyst in the coking unit can be mixed with the coke generated in the catalytic cracking reactor and enter the regeneration system. Under the action of high temperature and oxygen-enriched gas, sufficient coking exothermic reaction occurs, supplying the heat required for the reaction, achieving thermal balance, and without damaging the catalyst properties.

[0065] like Figure 2 As shown, this application provides a catalytic cracking regeneration system, comprising:

[0066] 300 catalytic cracking coke generator;

[0067] Gas-solid separation and collection equipment 200, and

[0068] Regenerator 500.

[0069] As described above, the bottom end of the pre-lifting zone I of the catalytic cracking coke generator 300 and / or the bottom end of the coke reaction zone II are configured to communicate with the regenerator 500 for conveying the catalyst of the regenerator to the coke generator.

[0070] The outlet zone III of the catalytic cracking coke generator 300 is in fluid communication with the gas-solid separation and collection device 200, so that the material from the coke generator 300 is separated into oil and gas and coke-containing catalyst by the gas-solid separation and collection device 200.

[0071] The gas-solid separation and collection device 200 is connected to the regenerator 500, so that the coke-bearing catalyst is transported to the regenerator 500 for regeneration.

[0072] like Figure 2 As shown, the gas-solid separation and collection device 200 includes:

[0073] Gas-solid separation device 201 is connected to outlet zone III of the catalytic cracking coke generator 300, so that the material from the coke generator 300 is separated into oil and gas and coke-containing catalyst by the gas-solid separation device 201.

[0074] Settler 210 is configured to collect the coke-bearing catalyst; the settler 210 is connected to the regenerator 500 so that the coke-bearing catalyst is delivered to the regenerator 500.

[0075] In one embodiment, the outlet end 304 of the catalytic cracking coke generator 300 is connected to the inlet of the gas-solid separation device 201.

[0076] In one embodiment, the gas-solid separation device 201 is housed inside the settler 210.

[0077] The settling tank 210 includes a stripping section 205 located at the lower part of the settling tank, the stripping section 205 being configured for stripping and collecting coke-laden catalyst; and the regenerator 500 is connected to the stripping section 205, such that the stripped coke-laden catalyst is transported to the regenerator 500. A stripping gas inlet 207 is provided at the lower part of the stripping section 205 for inputting stripping gas such as water vapor.

[0078] It should be noted that the gas-solid separation and collection device 200 can also be connected to the outlet of the catalytic cracking reactor (not shown), so that the material of the catalytic cracking reactor is also separated by the gas-solid separation and collection device 200, and the separated spent catalyst enters the catalytic cracking regeneration system for regeneration and recycling.

[0079] In one embodiment, the coking unit 300 is in fluid communication with the gas-solid separation device 201, so that the reaction oil and coke-containing catalyst produced by the coking unit 300 are separated by the gas-solid separation device 201. The reaction oil and gas are collected in the gas collecting chamber 202 and introduced into the product separation system for recycling via the oil and gas pipeline 203. The catalyst containing coke enters the stripping section 205 at the bottom of the settling tank 200, and after stripping, it is introduced into the regeneration system for coking through the standpipe 206 to release heat. In this application, the gas-solid separation device 201 can be any equipment well known to those skilled in the art. For example, the gas-solid separation device 201 may include a cyclone separator. In this application, the gas-solid separation and collection device 200 and the coking unit 300 can be arranged coaxially or side-by-side at different heights. Figure 2 The arrangement of the gas-solid separation and collection device 200 and the coking unit 300 is shown.

[0080] This application also relates to a method for regenerating a catalytic cracking catalyst, carried out in the above-mentioned catalytic cracking regeneration system, comprising the following steps:

[0081] Pre-lift gas is injected into the pre-lift zone I of the coking unit 300 via the pre-lift gas inlet 301, and comes into contact with the regenerated catalyst from the regenerator 500;

[0082] A mixture of atomizing medium and combustion oil is injected into the coking unit 300 through the fuel oil inlet 302, so that the mixture of atomizing medium and combustion oil comes into contact with the catalyst in the coking unit, and a coking reaction occurs, resulting in a catalyst with coke and reaction oil gas.

[0083] The coke-containing catalyst and the reaction oil and gas are separated by the gas-solid separation and collection device 200. The separated coke-containing catalyst is introduced into the regenerator 500 to regenerate the catalyst for recycling.

[0084] In the above process, pre-lift gas is injected into the pre-lift zone of the coking unit through the pre-lift gas inlet, and comes into contact with the regenerated catalyst from the regenerator, so that the regenerated catalyst is pre-accelerated and pre-fluidized, improving the distribution of the catalyst and facilitating uniform contact and rapid mixing with fuel oil.

[0085] A mixture of atomizing medium and combustion oil is injected into the coking unit through the fuel oil inlet, so that the mixture of atomizing medium and combustion oil comes into contact with the catalyst in the coking unit, and a coking reaction occurs, resulting in a catalyst with coke and reaction oil gas.

[0086] After the catalyst containing coke and the reaction oil and gas are separated by the gas-solid separation and collection equipment, the reaction oil and gas are transported to the product separation system, and the catalyst containing coke enters the stripping section. After stripping, it is introduced into the regeneration system, where a complete combustion reaction occurs, releasing heat and yielding a regenerated catalyst.

[0087] In one embodiment, the reaction zone of the coking device is a bubbling fluidized bed or a turbulent fluidized bed.

[0088] In one embodiment, the linear velocity of the reaction zone of the coking unit is 0.2 m / s to 1.2 m / s, and the catalyst particle density is 300 kg / m³ to 700 kg / m³.

[0089] In one embodiment, the pre-lift gas is selected from water vapor, nitrogen, dry gas, rich gas, or C4 fraction or a mixture thereof, and the mass ratio of the pre-lift gas to fuel oil is 0.01:1 to 0.05:1.

[0090] In one embodiment, the fuel oil comprises straight-run distillate or secondary-processed distillate. Preferably, the secondary-processed distillate may be selected from one or more blends of catalytic cracking diesel, coking gasoline, coking diesel, and coking wax oil.

[0091] In one embodiment, the atomizing medium of the fuel oil may be selected from water vapor, nitrogen, or a mixture thereof, and the mass ratio of the atomizing medium to the fuel oil is 0.01:1 to 0.5:1.

[0092] In one embodiment, the outlet temperature of the coking device is 460-560°C.

[0093] like Figure 2 As shown, the regenerator 500 is used to regenerate the catalyst to be regenerated. It is provided with an oxygen gas inlet 501, a catalyst to be regenerated inlet 505 and two catalyst regeneration outlets 506 and 508 at the bottom, a cyclone separator 503 inside, and a flue gas outlet 504 at the top.

[0094] Within the regenerator 500, oxygen-containing gas from the oxygen-containing gas inlet 501 enters the regenerator after passing through the gas distributor 502, where it comes into contact with the coke-bearing catalyst and undergoes a complete combustion reaction, releasing heat completely. Part of the regenerated catalyst is returned to the catalytic cracking reactor (not shown in the figure) via the regenerated catalyst circulation outlet 508 for recycling, while another part of the catalyst is sent to the catalytic cracking coke generator 300 for recycling via the regenerated catalyst outlet 506 and the regenerated catalyst inlet 303. The regenerated flue gas is used to recover the entrained catalyst via the cyclone separator 503 and is then sent to the subsequent energy recovery system via the flue outlet 504.

[0095] The catalytic cracking coke generator of this application can be connected to one or more catalytic cracking reactors, allowing the coke-laden catalyst from the coke generator and the spent catalyst from the catalytic cracking reactor to be regenerated together in a regenerator, releasing heat. The regenerated catalyst carrying the heat is then recycled back to the catalytic cracking reactor to provide heat for the reaction. The catalytic cracking coke generator of this application is suitable for catalytic cracking reaction-regeneration systems with various feedstocks and insufficient coke production, such as reactions involving the catalytic cracking of petroleum hydrocarbons and oxygenated hydrocarbons to produce propylene or fuel oil, or reactions involving the catalytic cracking to produce low-carbon olefins. The catalytic cracking coke generator and regeneration system of this application need to be used in conjunction with a catalytic cracking reactor to form a catalytic cracking reaction-regeneration system. It should be noted that although fuel oil is also injected into the catalytic cracking coke generator of this application, the purpose of this fuel oil is not as feedstock for catalytic cracking, but rather to replenish coke on the catalyst, which is beneficial for the thermal balance of the catalytic cracking reaction.

[0096] In this application, the coke generated on the catalyst in the coking unit can be combined with the coke generated on the catalyst in the catalytic cracking reactor. In the regeneration system, under the action of high temperature and oxygen-enriched gas, the coke is fully burned and released heat to supply the heat required for the reaction without damaging the properties of the catalyst.

[0097] This application has a simple structure. With only adaptive modifications, the regenerator can still use existing technology, making it easy to implement and highly applicable. In particular, it can be used in catalytic cracking units with low-carbon olefins and other chemical raw materials as the main target products. It can not only fundamentally solve the problem of heat balance, but also reduce the damage to the catalyst and regeneration system caused by the traditional method of injecting combustion oil. This saves catalyst costs and improves the economic efficiency of the refinery.

[0098] This application also provides a catalytic cracking coke-forming system, which includes the catalytic cracking coke-forming device of this application. Furthermore, the catalytic cracking coke-forming system also includes an oil-to-chemicals separation device, a stripper, and optional reaction product separation equipment. In the catalytic cracking coke-forming system provided by this application, the oil-to-chemicals separation device, stripper, etc., can all be equipment well known to those skilled in the art, and the connection methods between these devices can also be carried out in accordance with methods known in the art. For example, the oil-to-chemicals separation device may include a cyclone separator and an outlet rapid separator. In some specific embodiments, the oil-to-chemicals separation and collection equipment includes a settling device arranged coaxially or parallel at different heights with the catalytic cracking reactor.

[0099] Figure 3An embodiment of a catalytic cracking reaction-regeneration system incorporating the regeneration system of this application is shown. This reaction-regeneration system includes a catalytic cracking reactor 100, a coking unit 300, a gas-solid separation and collection device 200, a regenerator 500, and a product separation system (not shown), etc. The coking unit 300, the gas-solid separation and collection device 200, and the regenerator 500, and their connections, are as described above and will not be repeated here. Figure 3 As shown, the coking unit 300 and the gas-solid separation and collection device 200 are coaxially arranged; while the catalytic cracking reactor 100 is located outside the gas-solid separation and collection device 200, with its outlet end 104 in fluid communication with the gas-solid separation and collection device 200, allowing the oil from the catalytic cracking reactor 100 to enter the gas-solid separation and collection device 200 for separation and collection. Figure 3 As shown, the outlet 104 of the catalytic cracking reactor 100 is connected to the inlet of the gas-solid separation device 201. The catalytic cracking reactor 100 can be any commonly used catalytic cracking reactor, such as a riser reactor or a fluidized bed reactor. The catalytic cracking reactor 100 is provided with a regenerated catalyst inlet 103, which can be connected to the regenerated catalyst circulation outlet 508, allowing the regenerated catalyst to be recycled back to the catalytic cracking reactor 100. The catalytic cracking reactor 100 is also provided with a feed inlet 102 and a riser gas inlet 101.

[0100] The present application will be further described below with reference to the preferred embodiments shown in the accompanying drawings, but this does not limit the present application.

[0101] Figure 1 A preferred embodiment of the catalytic cracking coke generator 300 of this application is provided, wherein the catalytic cracking coke generator 300 includes, from bottom to top, a pre-lifting zone I, a reaction zone II, and an outlet zone III. A pre-lifting gas inlet 301 and a regeneration catalyst inlet 303 are provided at the lower part of the pre-lifting zone I of the coke generator 300. One or more, for example, one, two, or more fuel oil inlets 302 are provided on the lower sidewall of the reaction zone II of the coke generator 300.

[0102] Figure 2A preferred embodiment of the catalytic cracking regeneration system including the catalytic cracking coke generator of this application is provided. Pre-lift gas enters the pre-lifting zone I of the coke generator 300 from the bottom through pre-lift gas inlet 301. The pre-lift gas can be nitrogen, water vapor, dry gas, rich gas, or C4 fraction or a mixture thereof. High-temperature regeneration catalyst from the regenerator 500 enters the lower part of the coke generator 300 through regeneration catalyst inlet 303, mixes with the pre-lift gas, moves upward, and comes into contact with fuel oil from fuel oil inlet 302, entering the reaction zone II of the coke generator to undergo a coking reaction. The catalyst with coke and the reaction-generated oil and gas flow upward, enter the gas-solid separation device 201 of the gas-solid separation and collection equipment 200 through outlet zone III, and the separated reaction oil and gas enter the gas collection chamber 202 and is introduced into the product separation system through the oil and gas pipeline 203. The separated coke-containing catalyst enters the settling tank 210 and is stripped in the stripper 205 at the bottom of the settling tank 210. After stripping, the gas enters the regenerator 500 through the standpipe 206 and the catalyst inlet 505. The oxygen-containing gas from the oxygen-containing gas inlet 501 enters the regenerator through the gas distributor 502, where it comes into contact with the coke-bearing catalyst and undergoes a complete combustion reaction, releasing heat completely. Part of the regenerated catalyst is returned to the catalytic cracking reactor (not shown in the figure) through the regenerated catalyst circulation outlet 508 for recycling, and part of the catalyst is sent to the coke generator for recycling through the regenerated catalyst outlet 506 and the regenerated catalyst inlet 303. The regenerated flue gas recovers the entrained catalyst through the cyclone separator 503 and is sent to the subsequent energy recovery system through the flue outlet 504.

[0103] Example

[0104] The following examples will further illustrate this application, but do not limit the scope of this application. The catalyst used in the experiment was an industrial catalyst, commercially known as SHMP-4; the fuel oil was catalytic cracking slurry oil taken from the Anqing Petrochemical catalytic cracking unit, and its properties are shown in Table 1.

[0105] Example 1

[0106] according to Figure 2 Experiments were conducted to test the coking-regeneration reaction of catalytic oil slurry in the regeneration system.

[0107] The coking unit 300 used includes:

[0108] The pre-lifting zone I has a length of 1 meter and an inner diameter of 0.2 meters;

[0109] Coke reaction zone II is a turbulent bed reactor with a length of 3 meters and an inner diameter of 0.4 meters;

[0110] Export area III is 2 meters long and has an inner diameter of 0.2 meters.

[0111] The coking unit is provided with a pre-lift gas inlet 301, a regeneration catalyst inlet 303, and a fuel oil inlet 302 from bottom to top, all of which are located at the bottom of the coking unit 300.

[0112] The distance from the fuel oil inlet 302 to the bottom of the coker is independently 10% of the height of the coker.

[0113] The following is an experiment to test the coke-regeneration reaction:

[0114] Nitrogen gas, the pre-lifting medium, enters the lower part of the coking unit and mixes with the regenerated catalyst before flowing upward. The mixture of Anqing oil slurry (coking fuel oil) and atomizing medium (steam) enters the coking unit through the fuel oil inlet, comes into contact with the hot regenerated catalyst, and undergoes a coking reaction. The reaction products and the catalyst to be regenerated enter the cyclone separator 201 from the coking unit outlet (outlet area), where the reaction products and the catalyst to be regenerated are rapidly separated, and the reaction products are collected after cooling.

[0115] The spent catalyst enters the stripping section of the settling tank under gravity, where water vapor strips the hydrocarbon products adsorbed on the catalyst. The stripped catalyst then enters regenerator 500, where it is regenerated by contacting oxygen-rich air. A portion of the regenerated catalyst is returned to the coking unit for recycling. Operating conditions and product distribution are listed in Table 2.

[0116] As can be seen from the results in Table 2, the oil slurry conversion rate was 59.36%, and the coke yield was 21.93%.

[0117] As can be seen from the results of the above embodiments, the coking device and coking regeneration system of this application can achieve highly selective coking of the oil slurry, provide a heat source for the regenerator from the perspective of the reaction system, have no impact on the regeneration system, and help maintain the physical and chemical properties of the catalyst.

[0118] Example 2

[0119] Figure 3 The catalytic cracking reaction system shown includes Figure 2 The regeneration system and riser reactor are shown. According to... Figure 3 The process was tested: A cracking reaction experiment of Daqing wax oil was conducted on a riser reactor. Preheated feedstock oil was introduced from the bottom of the cracking reactor, contacting with the regenerated catalyst from the regenerator, and undergoing a catalytic cracking reaction from bottom to top. This yielded an oil-catalyst mixture of reaction products and the regenerated catalyst. The oil-catalyst mixture entered a cyclone separator from the reactor outlet, where the reaction products and the regenerated catalyst were rapidly separated. The reaction products were then collected after cooling. The properties of the Daqing wax oil used are shown in Table 3.

[0120] The coking and regeneration of Anqing oil slurry was carried out in accordance with the method of Example 1. Anqing oil slurry (coking fuel oil) enters the coking unit, contacts the hot regeneration catalyst and undergoes a coking reaction to obtain a mixture of reaction products and oil with carbonized catalyst. The oil mixture enters a cyclone separator from the outlet of the coking unit, where the reaction products and the catalyst to be regenerated are rapidly separated. The reaction products are collected after cooling.

[0121] The spent catalyst and the carbonized catalyst enter the stripping section of the settling tank under gravity. Hydrocarbon products adsorbed on the spent catalyst are stripped by steam. The stripped spent catalyst then enters the regenerator for regeneration through contact with air. The regenerated catalyst is then returned to the reactor and the coking unit for recycling. The weight ratio of regenerated catalyst recycled back to the catalytic cracking reactor to that recycled back to the coking unit is 5:1. Operating conditions and product distribution are listed in Table 4.

[0122] As can be seen from the results in Table 4, the methane yield was 1.90%, the ethylene yield was 5.34 wt%, the propylene yield was 21.74 wt%, and the coke yield was 8.39%.

[0123] Comparative Example 1

[0124] according to Figure 3 The process was carried out in Comparative Example 1, with the exception of Example 2, where the coking unit was not turned on. Catalyst regeneration was performed as follows:

[0125] The spent catalyst enters the stripping section of the settling tank under gravity, where water vapor strips the hydrocarbon products adsorbed on the catalyst. The stripped catalyst then enters the regenerator for regeneration through contact with air. Simultaneously, oil slurry is introduced into the regenerator bed as fuel oil for combustion to replenish the regenerator's heat. The regenerated catalyst is then returned to the reactor for recycling. Operating conditions and product distribution are listed in Table 4.

[0126] As can be seen from the results in Table 4, the methane yield was 2.35%, the ethylene yield was 5.04 wt%, the propylene yield was 19.81 wt%, and the coke yield was 4.33%.

[0127] As can be seen from the results of Example 2 and Comparative Example 1 above, adding the coking unit of this application to the catalytic cracking reaction system can not only reduce the methane yield and increase ethylene and propylene yields, but also provide the coke source required for the regeneration process.

[0128] 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.

[0129] 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.

[0130] 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.

[0131] Table 1 Properties of Anqing Petrochemical Oil Slurry

[0132] numerical values <![CDATA[Density at 20 °C, kg / m 3 > 1068.6 70℃ refractive index 1.6361 <![CDATA[Viscosity at 100°C, millimeters 2 / second]]> 11.5 Residual char, % (by weight) 4.79 Carbon content, % (by weight) 91.22 Hydrogen content, % (by weight) 8.06 Sulfur content, % (by weight) 0.331 Nitrogen content, % (by weight) 0.21 Basic nitrogen, mg / kg 86 Distillation range, °C 5% (by volume) 364.5 10% (by volume) 373.2 30% (by volume) 400.6 50% (by volume) 425.6 70% (by volume) 464.8

[0133] Table 2 Operating conditions and results of Example 1

[0134] Example 1 Coking unit outlet temperature, °C 540 Coking unit inlet temperature, ℃ 557 Catalyst to fuel oil feed weight ratio 7：1 Reaction time, seconds 5.0 Water vapor to fuel oil feed weight ratio 0.16 nitrogen to fuel oil feed weight ratio 0.05 Temperature inside the regenerator, °C 720 Product yield, by weight % dry air 3.67 Liquefied gas 10.07 <![CDATA[C5 + Gasoline 8.35 diesel fuel 15.34 heavy oil 40.64 coke 21.93 total 100.00

[0135] Table 3 Feedstock for Pyrolysis Reaction

[0136] Daqing wax oil Anqing Oil Slurry <![CDATA[Density at 20 °C, kg / m 3 > 864.0 1068.6 70℃ refractive index 1.4624 1.6361 <![CDATA[Viscosity at 100°C, millimeters 2 / second]]> 4.648 11.5 Residual char, % (by weight) 0.04 4.79 Carbon content, % (by weight) 86.40 91.22 Hydrogen content, % (by weight) 13.44 8.06 Sulfur content, % (by weight) 0.12 0.331 Nitrogen content, % (by weight) 0.0657 0.21 Basic nitrogen, mg / kg / 86 Distillation range, °C 5% (by volume) 331 364.5 10% (by volume) 354 373.2 30% (by volume) 402 400.6 50% (by volume) 435 425.6 70% (by volume) 467 464.8

[0137] Table 4. Operating conditions and results of Example 2 and Comparative Example 1

[0138] Example 2 Comparative Example 1 Pyrolysis reactor conditions Pyrolysis reactor outlet temperature, °C 560 560 Catalyst to feedstock weight ratio 10：1 10：1 Reaction time, seconds 2.5 2.5 Water vapor to feed weight ratio 0.25 0.25 Coking equipment conditions Coking unit outlet temperature, °C 540 Catalyst to raw coke fuel oil feed weight ratio 7 Reaction time, seconds 5 Water vapor to raw coke fuel oil feed weight ratio 0.16 nitrogen to raw coke fuel oil feed weight ratio 0.05 The percentage of raw coke fuel oil in the cracking reactor feed, %. 30 Regenerator conditions Temperature inside the regenerator, °C 720 720 The percentage of oil slurry feed in the regenerator relative to the feed to the pyrolysis reactor. 30 Product yield, by weight % dry air 8.79 8.91 Methane 1.90 2.35 ethylene 5.34 5.04 Liquefied gas 47.49 48.32 Among them, propylene 21.74 19.81 <![CDATA[C5 + Gasoline 21.97 24.44 diesel fuel 10.36 10.49 heavy oil 3.00 3.51 coke 8.39 4.33 total 100.00 100.00

Claims

1. A catalytic cracking coke generator, characterized in that, The forking unit, from bottom to top, comprises: Pre-upgrade area The coking reaction zone, wherein the coking reaction zone is a bubbling fluidized bed or a turbulent fluidized bed, and Export area The top of the pre-lifting zone is connected to the coking reaction zone, and the top of the coking reaction zone is connected to the outlet zone. The bottom end of the pre-lifting zone and / or the bottom end of the coking reaction zone are configured to be connected to the regenerator for conveying the catalyst of the regenerator to the coking reactor. At least one fuel oil inlet is provided in the middle and upper reaches of the coking reaction zone; The coking unit is provided with a pre-lift gas inlet, a catalyst inlet, and one or more fuel oil inlets from bottom to top. Pre-lift gas is injected into the pre-lift zone through the pre-lift gas inlet. The one or more fuel oil inlets are each independently located at the outlet end of the pre-lifting zone, or located at the bottom or side wall of the coking reaction zone; The pre-lifting gas is selected from water vapor, nitrogen, dry gas, rich gas, C4 fraction or a combination thereof, and the mass ratio of the pre-lifting gas to fuel oil is 0.01:1 to 0.05:1; The linear velocity of the coking reaction zone in the coking unit is 0.3 m / s to 1.2 m / s, and the catalyst particle density is 300 kg / m³ to 700 kg / m³.

2. The catalytic cracking coke generator according to claim 1, characterized in that, The distance from each of the one or more fuel oil inlets to the bottom of the coker is independently 5% to 15% of the coker height.

3. The catalytic cracking coke generator according to claim 1, characterized in that, One or more coking reaction zones are hollow cylinders with a length-to-diameter ratio of 20:1 to 2:

1.

4. The catalytic cracking coke generator according to claim 3, characterized in that, The pre-lifting zone is a hollow cylinder with a length-to-diameter ratio of 10:1 to 2:

1. The export area is a hollow cylinder with a length-to-diameter ratio of 30:1 to 5:

1.

5. The catalytic cracking coke generator according to claim 4, characterized in that, The ratio of the inner diameters of the pre-lifting zone, the coking reaction zone, and the outlet zone is 1:2:1 to 1:10:

2.

6. The catalytic cracking coke generator according to claim 1, characterized in that, The outlet area of ​​the coking unit is configured to be in fluid communication with a gas-solid separation and collection device, wherein the gas-solid separation and collection device is connected to the product separation system and the regenerator respectively, so that the reaction oil and gas and the coke-containing catalyst generated by the coking unit are separated by the gas-solid separation and collection device and then introduced into the product separation system and the regenerator respectively.

7. A catalytic cracking regeneration system, comprising: The catalytic cracking coke generator according to any one of claims 1-6; Gas-solid separation and collection equipment, and Regenerator, The bottom end of the pre-lifting zone and / or the bottom end of the coking reaction zone are configured to be connected to the regenerator for conveying the catalyst of the regenerator to the coking reactor. The outlet area of ​​the catalytic cracking coke generator is in fluid communication with the gas-solid separation and collection device, so that the material from the coke generator is separated into oil and gas and coke-containing catalyst by the gas-solid separation and collection device. The gas-solid separation and collection device is connected to the regenerator, so that the coke-bearing catalyst is transported to the regenerator.

8. The catalytic cracking regeneration system according to claim 7, wherein, The gas-solid separation and collection device includes: A gas-solid separation device is connected to the outlet area of ​​the catalytic cracking coke generator, so that the material from the coke generator is separated into oil and gas and coke-containing catalyst by the gas-solid separation device. A settling device configured to collect the coke-bearing catalyst; the settling device is connected to the regenerator, such that the coke-bearing catalyst is transported to the regenerator.

9. The catalytic cracking regeneration system according to claim 8, wherein, The gas-solid separation device is housed inside the settler. The settling device includes a stripping section located at the lower part of the settling device, the stripping section being configured for stripping and collecting coke-laden catalyst; and the regenerator is connected to the stripping section such that the stripped coke-laden catalyst is conveyed to the regenerator.

10. A method for regenerating a catalytic cracking catalyst, carried out in the catalytic cracking regeneration system according to any one of claims 7-9, comprising the following steps: Pre-lift gas is injected into the pre-lift zone of the coking unit through the pre-lift gas inlet, and comes into contact with the regenerated catalyst from the regenerator; A mixture of atomizing medium and fuel oil is injected into the coking unit through the fuel oil inlet, so that the mixture of atomizing medium and fuel oil comes into contact with the catalyst in the coking unit, and a coking reaction occurs, yielding a catalyst with coke and reaction oil gas. The coke-coated catalyst and the reaction oil and gas are separated by a gas-solid separation and collection device. The separated coke-coated catalyst is introduced into a regenerator to regenerate the catalyst for recycling.

11. The regeneration method according to claim 10, wherein, It also includes stripping the coke-coated catalyst and introducing the stripped catalyst into the regenerator.

12. The regeneration method according to claim 10, wherein, The atomizing medium is nitrogen, and the mass ratio of the atomizing medium to fuel oil is 0.01:1 to 0.5:

1.

13. The regeneration method according to claim 10, wherein, The fuel oil is selected from straight-run distillate or secondary-processed distillate.

14. The regeneration method according to claim 13, wherein, Secondary processed distillate oils are selected from one or more of catalytic cracking diesel, catalytic cracking slurry oil, coking gasoline, coking diesel, and coking wax oil.

15. The regeneration method according to claim 10, wherein, The outlet temperature of the coking unit is 460-560℃.

16. A catalytic cracking coking system comprising the coking unit of any one of claims 1-6.

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