Method for Reducing Carbon Dioxide Emissions in Catalytic Cracking

Abstract

The present application provides a method for reducing carbon dioxide emissions in catalytic cracking, which includes: contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a catalytic cracking reactor to carry out a catalytic cracking reaction, separating the reaction oil gas and the coked spent catalyst, and feeding the reaction oil gas into a subsequent separation system; subjecting the spent catalyst to stripping and then regenerating it, the regeneration being carried out in a regeneration device, and transporting the obtained regenerated catalyst to the catalytic cracking reactor. This method can significantly reduce CO2 emissions and produce CO without affecting the catalyst carbon burning effect.

Description

Technical Field

[0001] The present invention relates to the catalytic cracking of petroleum hydrocarbons, and more specifically, to a method for producing carbon monoxide during the catalytic cracking regeneration process to reduce carbon dioxide emissions. Background Art

[0002] The catalytic cracking of petroleum raw materials is an important petroleum refining process. The catalytic cracking unit mainly includes a catalytic cracking reactor and a catalyst regenerator. In the catalyst regenerator, the coked catalyst is regenerated using a regeneration gas, and at the same time, regeneration flue gas is generated. During the regeneration process of the catalyst, a large amount of CO2 gas is generated by the combustion of coke, making the catalytic cracking unit the largest CO2 emission source in the refinery. CO2 in the catalytic cracking flue gas accounts for 15% - 50% of the total refinery emissions. For each ton of raw material processed, the catalytic cracking unit emits 211.7 kg of CO2. There are about 190 catalytic cracking units in China, with a total processing capacity of about 210 million tons / year, and there is at least 40 million tons of CO2 emissions.

[0003] During the regeneration process of the catalyst, the large amount of heat generated causes heat surplus in the catalytic unit. An external heat extraction device is required to convert the heat generated during catalyst regeneration into steam energy and recover the energy of the high-temperature flue gas, but these all belong to low-quality energy utilization. Moreover, the regeneration flue gas contains carbon monoxide, and this part of carbon monoxide often causes tail burning, resulting in local overheating of the regenerator and increased deactivation of the catalyst. By controlling the oxygen content in the flue gas, tail burning can be reduced, but the coking rate and coking intensity will be decreased, and there is also the problem of tail gas emissions, resulting in the loss of chemical energy in carbon monoxide. Refineries often use carbon monoxide combustion promoters or flue gas boilers to reduce carbon monoxide in the flue gas and recover energy, but the problem of carbon monoxide in the flue gas has never been properly solved.

[0004] CN1400159A discloses a method for producing hydrogen using catalytic cracking regeneration flue gas. This method can reasonably utilize the CO in the regeneration flue gas and alleviate the problem of heat surplus in the FCC unit. However, the CO content obtained by this method is low, only reaching about 14 v%.

[0005] CN102698817A discloses a pure oxygen regeneration process and a hydrogen production method for fluid catalytic cracking catalysts, which can significantly improve the energy utilization quality and efficiency, reduce the energy consumption and pollutant emissions of the FCC regeneration system, and at the same time produce hydrogen by the water-gas shift reaction of the generated CO.

[0006] CN101457152A discloses a method for hydrocarbon oil conversion. During the regeneration process, the spent catalyst contacts with steam and oxygen-containing gas in a gasifier to obtain synthesis gas and semi-regenerated catalyst. This method can increase the production of carbon monoxide and hydrogen. Carbon monoxide can also be converted into hydrogen during subsequent processing, thereby obtaining a higher hydrogen yield.

[0007] However, in the prior art, hydrogen is produced by incomplete regeneration flue gas. Although coke is utilized, carbon is still mainly emitted in the form of carbon dioxide, and the CO content is relatively low. Moreover, the method of directly contacting the spent catalyst with steam to produce synthesis gas will accelerate the deactivation of the catalyst. Summary of the Invention

[0008] This application provides a method for reducing carbon dioxide emissions in catalytic cracking, including:

[0009] Contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a catalytic cracking reactor to carry out a catalytic cracking reaction, separating the reaction oil gas and the coke-loaded spent catalyst, and sending the reaction oil gas to a subsequent separation system;

[0010] Subjecting the spent catalyst to stripping and then regenerating it in a regeneration device, and transporting the obtained regenerated catalyst to the catalytic cracking reactor;

[0011] Wherein, the regeneration device includes a first regenerator and a second regenerator, and the regeneration includes:

[0012] Contacting the spent catalyst with a first oxygen-containing gas in the first regenerator to carry out a first regeneration reaction to obtain a semi-regenerated catalyst, leading out a first flue gas from the first regenerator, and separating to obtain a CO product;

[0013] Contacting the semi-regenerated catalyst with a second oxygen-containing gas in the second regenerator to carry out a second regeneration to obtain a regenerated catalyst and generate a second flue gas;

[0014] Wherein, part or all of the first oxygen-containing gas is the second flue gas; wherein, the first regeneration reaction conditions in the first regenerator include: the reaction temperature is 400-600 °C, and the average residence time of the spent catalyst is 2-10 minutes.

[0015] In one embodiment, the first regeneration reaction conditions in the first regenerator include: the reaction temperature is 500-550 °C, the apparent gas linear velocity is 0.3-5 m / s, and the average residence time of the spent catalyst is 5-10 minutes.

[0016] In one embodiment, the first regenerator is a downflow bed reactor, and both the first oxygen-containing gas and the spent catalyst enter the first regenerator from the top of the first regenerator.

[0017] In one embodiment, the regeneration device further includes a gas-solid separator for separating the first flue gas generated by the first regenerator from the semi-regenerated catalyst.

[0018] In one embodiment, the second regeneration reaction conditions in the second regenerator include: a reaction temperature of 600 to 750 °C, a gas superficial linear velocity of 0.3 to 5 m / s, and an average residence time of the spent catalyst of 0.6 to 5 minutes.

[0019] In one embodiment, the second oxygen-containing gas is selected from oxygen, air, a mixed gas of oxygen and nitrogen with an oxygen content of 10 to 30%, and a mixed gas of oxygen and CO2 with an oxygen content of 10 to 30%.

[0020] In one embodiment, the catalytic cracking reactor is a riser reactor, a fluidized bed reactor, or a combination thereof.

[0021] In one embodiment, the catalytic cracking reaction conditions of the hydrocarbon oil feedstock include: a reaction temperature of 450 to 700 °C, a time of 1 to 10 seconds, a catalyst-to-oil ratio of 1 to 50:1, and a space velocity of 0.5 to 20 h -1 。

[0022] In one embodiment, the hydrocarbon oil feedstock includes petroleum hydrocarbons and / or other mineral oils. The petroleum hydrocarbons are selected from one or more of gasoline, diesel, vacuum gas oil, atmospheric gas oil, coker gas oil, deasphalted oil, vacuum residue, atmospheric residue, extracted oil, and poor recycle oil. The other mineral oils are selected from one or more of coal liquefied oil, oil sand oil, and shale oil.

[0023] In the present invention, the combustion of coke in the catalyst regeneration process is controlled to cause incomplete combustion to generate CO. By controlling the regeneration conditions, the CO2 emissions of the catalytic device can be greatly reduced. At the same time, the CO2 in the first oxygen-containing gas can react with coke to generate CO, further reducing CO2 emissions and significantly increasing the content of CO in the flue gas. The generated CO can be used as a raw material for subsequent chemical industry, metallurgy, etc., saving raw materials such as coal and methane for producing CO, saving resources and energy consumption, and further reducing emissions. Therefore, in the context of the goals of carbon neutrality and carbon peak, using the catalytic cracking regeneration process to produce CO can turn waste into treasure and save energy and reduce emissions, with great economic and social benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] The drawings are used to provide a further understanding of the present invention and constitute a part of the specification. They are used together with the following specific embodiments to explain the present invention, but do not limit the present invention. In the drawings:

[0025] Figure 1 is a schematic flow diagram according to an embodiment of the present invention.

[0026] Figure 2 It is a process flow diagram of a preferred embodiment according to the present invention.

[0027] Figure 3 It is a process flow diagram of catalytic cracking in a single-stage regeneration mode. Specific embodiments

[0028] The present application will be further described in detail below with reference to the accompanying drawings and embodiments. Through these descriptions, the features and advantages of the present application will become clearer and more definite.

[0029] The special term "exemplary" here means "serving as an example, embodiment or illustration". Any embodiment described as "exemplary" here does not have to be construed as superior or better than other embodiments. Although various aspects of the embodiments are shown in the drawings, the drawings do not have to be drawn to scale unless otherwise specified.

[0030] In addition, the technical features involved in different embodiments of the present application described below can be combined with each other as long as they do not conflict with each other.

[0031] The present application provides a method for reducing carbon dioxide emissions in catalytic cracking, including:

[0032] Contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a catalytic cracking reactor and performing a catalytic cracking reaction, separating the reaction oil gas and the spent catalyst with coke, and feeding the reaction oil gas into a subsequent separation system;

[0033] Subjecting the spent catalyst to stripping and then regeneration, the regeneration being carried out in a regeneration device, and feeding the obtained regenerated catalyst to the catalytic cracking reactor;

[0034] Wherein, the regeneration device includes a first regenerator and a second regenerator, and the regeneration includes:

[0035] Contacting the spent catalyst with a first oxygen-containing gas in the first regenerator to carry out a first regeneration reaction to obtain a semi-regenerated catalyst, leading out a first flue gas from the first regenerator, and separating to obtain a CO product;

[0036] Contacting the semi-regenerated catalyst with a second oxygen-containing gas in the second regenerator to carry out a second regeneration to obtain a regenerated catalyst, and generating a second flue gas;

[0037] Wherein, part or all of the first oxygen-containing gas is the second flue gas.

[0038] In the catalytic cracking method according to the present invention, separating the spent catalyst and the reaction oil gas, and separating fractions such as dry gas, liquefied gas, stabilized gasoline, and catalytic diesel from the reaction oil gas through subsequent separation systems can adopt conventional technical methods in the art. The present invention has no limitation in this regard and will not be described in detail herein.

[0039] According to the present invention, the catalytic cracking reactor can be a conventional catalytic cracking riser reactor, fluidized bed reactor, or a combination thereof known to those skilled in the art. For example, a catalytic cracking riser reactor is connected in series with a fluidized bed reactor. The riser reactor can be selected from an equal-diameter riser reactor and / or an equal-linear velocity riser reactor, and an equal-diameter riser is preferably used. The fluidized bed reactor is located downstream of the riser reactor and is connected to the outlet of the riser reactor. The riser reactor sequentially includes a pre-lift section and at least one reaction zone from bottom to top. In order to enable the feedstock oil to fully react and according to the quality requirements of different target products, the number of reaction zones can be 2 to 8, preferably 1 to 3.

[0040] According to the present invention, the catalytic cracking reaction conditions include: the reaction temperature is 450 to 700 °C, preferably 500 to 650 °C, more preferably 550 to 600 °C; the time is 1 to 10 seconds, preferably 2 to 5 seconds, the catalyst-to-oil ratio (i.e., the weight ratio of the catalyst to the hydrocarbon oil feedstock) is 1 to 50:1, preferably 5 to 30:1; the space velocity is 0.5 to 20 h -1 , preferably 2 to 10 h -1 .

[0041] In the method provided by the present invention, steam can also be injected into the reactor. The steam is preferably injected in the form of atomizing steam, and the weight ratio of the injected steam to the light hydrocarbon oil feedstock can be 0.01 to 1:1, preferably 0.05 to 0.5:1.

[0042] In the catalytic cracking method according to the present invention, preferably, the method of the present invention further includes: before contacting the feedstock oil with the catalytic cracking catalyst, preheating the feedstock oil to 100 to 450 °C and then introducing it into the reactor to contact the catalytic cracking catalyst, preferably preheating to 150 to 300 °C.

[0043] In the catalytic cracking method according to the present invention, the catalytic cracking catalyst can be a conventional selection in the art. For the present invention, preferably based on the total weight of the catalyst, the catalytic cracking catalyst includes 15 to 65% by weight of natural minerals, 10 to 30% by weight of inorganic oxides, and 25 to 75% by weight of zeolite.

[0044] According to the present invention, as the active component, the zeolite is preferably one or more mixtures of Y zeolite, mordenite, β zeolite, and zeolites with an MFI structure (such as ZSM series zeolites and / or ZRP zeolites).

[0045] According to the present invention, the natural mineral is selected from one or more of kaolin, halloysite, montmorillonite, diatomite, attapulgite, sepiolite, halloysite, hydrotalcite, bentonite, and rectorite.

[0046] The inorganic oxide is selected from one or more of silica, alumina, zirconia, titania, and amorphous silica-alumina.

[0047] According to the fluid catalytic cracking method of the present invention, at least a part of the fluid catalytic cracking catalyst is a regenerated catalyst, and preferably all are regenerated catalysts.

[0048] According to the present invention, the feedstock includes petroleum hydrocarbons and / or other mineral oils. The petroleum hydrocarbons are selected from one or more of gasoline, diesel, vacuum gas oil, atmospheric gas oil, coker gas oil, deasphalted oil, vacuum residue, atmospheric residue, extracted oil, and poor recycle oil. The other mineral oils are selected from one or more of coal liquefied oil, oil sand oil, and shale oil.

[0049] According to the present invention, the reaction temperature of the first regenerator is 400 - 600 °C, preferably 450 - 580 °C, more preferably 500 - 550 °C; the superficial gas velocity is 0.3 - 5 m / s, preferably 0.9 - 3 m / s, more preferably 1 - 2.5 m / s; the average residence time of the spent catalyst is 2 - 10 minutes, preferably 4 - 8 minutes, more preferably 5 - 7 minutes. Moreover, the inventors of the present application also found that selecting the reaction temperature of the first regenerator and the average residence time of the spent catalyst is very important for controlling the proportion of CO in the regenerated flue gas: under the condition of controlling the carbon-oxygen ratio, reducing the reaction temperature of the first regenerator and increasing the residence time of the spent catalyst in the first regenerator are beneficial to increasing the proportion of CO in the flue gas. The inventors of the present application found that when the reaction temperature of the first regenerator is 500 - 550 °C and the average residence time of the spent catalyst is 5 - 7 minutes, a high proportion of CO in the flue gas can be achieved, which can reach about 80%, or even exceed 90% (using oxygen as the second oxygen-containing gas), which is unexpected to those skilled in the art.

[0050] According to the present invention, the reaction temperature of the second regenerator is 600 - 750 °C, preferably 630 - 720 °C, more preferably 670 - 700 °C; the superficial gas velocity is 0.3 - 5 m / s, preferably 0.9 - 3 m / s, more preferably 1 - 2.5 m / s; the average residence time of the spent catalyst is 0.6 - 5 minutes, preferably 2 - 4 minutes, more preferably 2.5 - 3.5 minutes.

[0051] According to the present invention, during the regeneration process, the catalyst and the oxygen-containing gas can be in countercurrent contact or cocurrent contact, and the catalyst can move upward or downward.

[0052] Figure 1 An embodiment of the present application is shown, which shows the countercurrent contact between the catalyst and the oxygen-containing gas. As Figure 1 shown, the catalytic cracking feedstock 1 enters from the bottom of the riser reactor 2 and contacts with the regenerated catalyst for reaction. The reaction oil gas and the catalyst move upward to the settler 3 for gas-solid separation. The separated reaction oil gas 4 goes to the subsequent separation system (not shown) for separation to obtain various products; the spent catalyst separated by the settler 3 enters the first regenerator 6 through the spent catalyst slide valve 5 and undergoes the first regeneration in the presence of the first oxygen-containing gas, generating the first flue gas 7 and the semi-regenerated catalyst; the regenerated first flue gas 7 goes to the subsequent energy recovery and separation system 8 to obtain carbon monoxide 9 and other flue gas components 16. The semi-regenerated catalyst enters the second regenerator 13 under the transportation of the gas 11, contacts with the second oxygen-containing gas 12 for the second regeneration, and obtains the regenerated catalyst and the second flue gas 10; the regenerated catalyst is degassed by the degassing tank 14 and then returns to the bottom of the riser reactor 2 through the regenerated catalyst slide valve 15 to contact with the feedstock 1 for reaction; the second flue gas 10 is all returned to the first regenerator 6 as the first oxygen-containing gas.

[0053] Figure 2 Another embodiment of the present application is shown, which shows the co-current contact between the catalyst and the oxygen-containing gas. As Figure 2 shown, the catalytic cracking feedstock 21 enters from the bottom of the riser reactor 22 and contacts with the regenerated catalyst for reaction. The reaction oil gas and the catalyst move upward to the settler 23 for gas-solid separation. The separated reaction oil gas 24 goes to the subsequent separation system (not shown) for separation. The obtained spent catalyst enters the top of the first regenerator 27 through the spent catalyst slide valve 25, contacts with the first oxygen-containing gas 26 and moves downward together for the first regeneration, and then enters the gas-solid separator 210. The separated first flue gas 14 goes to the subsequent energy recovery and separation system 215 to obtain carbon monoxide 216 and other flue gas components 217; the separated semi-regenerated catalyst enters the second regenerator 28 and contacts with the second oxygen-containing gas 212 for the second regeneration and moves upward together, and enters the cyclone separator 29 for gas-solid separation. The separated second flue gas 26 all enters the first regenerator 27, and the separated regenerated catalyst is degassed by the degassing section 213 and then returns to the bottom of the riser reactor 22 through the regenerated catalyst slide valve 211 to contact with the feedstock 21 for reaction.

[0054] In Figure 2 the shown embodiment, the first regenerator 26 may be a downflow bed reactor, and both the first oxygen-containing gas and the spent catalyst enter the first regenerator 26 from the top of the first regenerator 26. Using this form of downflow bed reactor as the first regenerator can achieve a large C / O ratio (carbon / oxygen atomic ratio), thereby increasing the content of CO in the first flue gas.

[0055] According to the present invention, the second oxygen-containing gas may be oxygen, air, a mixed gas of oxygen and nitrogen with an oxygen content of 10-30%, and / or a mixed gas of oxygen and CO2 with an oxygen content of 10-30%. Oxygen is preferred, and a mixed gas of oxygen and CO2 with an oxygen content of 10-30% is more preferred. According to the present invention, the CO2 in the mixed gas of oxygen and CO2 with an oxygen content of 10-30% may come from the CO2 in the regenerated flue gas.

[0056] According to the fluid catalytic cracking method of the present invention, preferably, the method of the present invention further includes stripping (generally with steam stripping) the regenerated catalyst obtained from the second regeneration to remove impurities such as gases.

[0057] According to the present invention, the separation of CO can adopt methods such as caustic scrubbing, membrane separation, pressure swing adsorption, cryogenic separation, COSORB method or other separation and purification methods well-known to those skilled in the art. The caustic scrubbing method is preferably adopted. According to the present invention, before separating CO, the flue gas can be purified to remove impurities such as sulfur oxides and nitrogen oxides.

[0058] The method provided by the present invention produces carbon monoxide by changing the mode of regenerative burning. The catalyst does not come into contact with high-temperature steam, does not accelerate the deactivation of the catalyst, and can effectively reduce afterburning and slow down the catalyst deactivation rate.

[0059] The method provided by the present invention reduces the heat release during combustion through incomplete combustion, alleviating the problem of excessive heat in the catalytic unit. The method provided by the present invention enables the spent catalyst to be completely regenerated in the second regenerator without affecting the catalytic cracking reaction activity.

[0060] When the method provided by the present invention uses oxygen as the oxygen source for burning, no nitrogen is introduced, and a relatively simple method can be adopted to obtain a CO product with a relatively high purity. When a mixed gas of oxygen and CO2 is used as the oxygen source, part of the CO2 can be converted into CO, while playing a role in enriching CO2, which is beneficial to carbon capture and utilization. When pure oxygen is used as the oxygen-containing regenerated gas, the volume ratio of CO in the flue gas can reach more than 76%; when air is used as the oxygen-containing regenerated gas, the volume ratio of CO in the flue gas can reach more than 24%; and a mixed gas of oxygen and CO2 gas can also be used as the oxygen-containing regenerated gas, and the volume ratio of CO in the flue gas can reach more than 80%.

[0061] The method provided by the present invention has a low regeneration temperature and can achieve a large catalyst-to-oil ratio operation for catalytic cracking reactions.

[0062] The method provided by the present invention not only reduces the carbon dioxide emissions of the catalytic device, but also can generate carbon monoxide with a high content as the raw material for subsequent chemical processes, realizing the transformation of waste into treasure and the full utilization of resources, saving fossil resources such as coal, oil and methane used to produce carbon monoxide, reducing energy consumption and investment, reducing pollution, and improving the economic and social benefits of the petrochemical industry.

[0063] The following examples will further illustrate the method, but do not limit the present invention thereby.

[0064] The feedstock oil used in the examples and comparative examples is Anqing wax oil, and its properties are shown in Table 1.

[0065] The fluid catalytic cracking catalyst used in the examples and comparative examples has a commercial brand number of CDOS (Changling Branch of Sinopec Catalyst Co., Ltd.).

[0066] Examples 1-5

[0067] Carry out the test according to the process attached Figure 2 , and the relevant operating conditions and products are listed in Table 2.

[0068] Example 6

[0069] Carry out the test according to the process attached Figure 1 , and the relevant operating conditions and products are listed in Table 2

[0070] Comparative Examples 1-2

[0071] Carry out the test according to the process attached Figure 1 , and the relevant operating conditions and products are listed in Table 3.

[0072] Comparative Examples 3-4

[0073] Carry out the test according to the process attached Figure 2 , and the relevant operating conditions and products are listed in Table 3.

[0074] Comparative Examples 5-6

[0075] Carry out the test according to the process attached Figure 3 , the fluid catalytic cracking feedstock oil 31 enters from the bottom of the riser reactor 32, contacts with the regenerated catalyst for reaction, the reaction oil gas and the catalyst move upward to the settler 33 for gas-solid separation, the separated reaction oil gas 34 goes to the subsequent absorption and stabilization system, the spent catalyst enters the regenerator 36 through the spent catalyst slide valve 35 to contact with the oxygen-containing gas for regeneration, the regenerated flue gas 37 is led out of the regenerator 36 to the subsequent energy recovery system, and the regenerated catalyst returns to the bottom of the riser reactor 32 through the regenerated catalyst slide valve 39 to contact with the feedstock oil 31 for reaction. The relevant operating conditions and products are listed in Table 3.

[0076] As can be seen from the results of the embodiments, the method of the present invention has the advantages of significantly reducing carbon dioxide emissions and producing carbon monoxide.

[0077] The above description of the present application is combined with preferred embodiments. However, these embodiments are only exemplary and only serve an illustrative purpose. On this basis, various substitutions and improvements can be made to the present application, and all of these fall within the protection scope of the present application.

[0078] Table 1

[0079]

[0080] Table 2

[0081]

[0082] Table 3

[0083] Item Comparative Example 1 Comparative Example 2 Comparative Example 3 Comparative Example 4 Comparative Example 5 Comparative Example 6 Reaction Conditions Reaction Temperature / °C 550 550 550 550 550 550 Ratio of Reagent to Oil 8 8 8 8 8 8 Reaction Time / s 3 3 3 3 3 3 First Regenerator Conditions Regeneration Temperature / °C 650 650 650 650 650 650 Catalyst Residence Time / min 5 5 2 5 5 5 Gas Velocity (m / s) 1.1 1.1 1 0.8 1.1 1.1 Second Regenerator Conditions Regeneration Temperature / °C 650 650 650 650 - - Catalyst Residence Time / min 3 3 3 3 - - Gas Velocity (m / s) 1.2 1.2 1.2 1.2 Composition of Second Oxygen-Containing Gas <![CDATA[CO2]]> - - - - - - <![CDATA[O2]]> 100.00 21.00 100.00 100.00 21.00 100.00 <![CDATA[N2]]> - 79.00 - - 79.00 - Composition of Flue Gas from First Regeneration CO 70.99 11.50 62.4 68.37 11.56 45.83 <![CDATA[CO2]]> 28.71 11.78 37.22 31.29 13.64 53.84 <![CDATA[O2]]> 0.02 2.26 0.17 0.09 0.21 0.08 <![CDATA[N2]]> 0.28 74.46 0.21 0.25 74.59 0.25

Claims

1. A method for reducing carbon dioxide emissions in catalytic cracking, comprising: contacting a hydrocarbon oil feedstock with a catalytic cracking catalyst in a catalytic cracking reactor to carry out a catalytic cracking reaction, separating the reaction oil gas and the spent catalyst with coke, and feeding the reaction oil gas into a subsequent separation system; subjecting the spent catalyst to stripping and then regeneration, the regeneration being carried out in a regeneration device, and feeding the obtained regenerated catalyst to the catalytic cracking reactor; wherein the regeneration device comprises a first regenerator and a second regenerator, and the regeneration comprises: contacting the spent catalyst with a first oxygen-containing gas in the first regenerator to carry out a first regeneration reaction to obtain a semi-regenerated catalyst, leading out first flue gas from the first regenerator, and separating to obtain a CO product; contacting the semi-regenerated catalyst with a second oxygen-containing gas in the second regenerator to carry out a second regeneration to obtain a regenerated catalyst and generate second flue gas; wherein part or all of the first oxygen-containing gas is the second flue gas; wherein the first regeneration reaction conditions in the first regenerator include: the reaction temperature is 500-550 °C, the gas superficial linear velocity is 0.3-5 m / s, and the average residence time of the spent catalyst is 5-10 minutes; the second oxygen-containing gas is selected from oxygen, air, a mixed gas of oxygen and nitrogen with an oxygen content of 10-30%, or a mixed gas of oxygen and CO2 with an oxygen content of 10-30%.

2. The method according to claim 1, wherein The first regenerator is a downflow bed reactor, and both the first oxygen-containing gas and the spent catalyst enter the first regenerator from the top of the first regenerator.

3. The method according to claim 2, wherein The regeneration device further comprises a gas-solid separator for separating the first flue gas generated by the first regenerator from the semi-regenerated catalyst.

4. The method according to claim 1, wherein, The second regeneration reaction conditions in the second regenerator include: the reaction temperature is 600-750 °C, the gas superficial linear velocity is 0.3-5 m / s, and the average residence time of the semi-regenerated catalyst is 0.6-5 minutes.

5. The method according to claim 1, wherein The catalytic cracking reactor is a riser reactor, a fluidized bed reactor or a combination thereof.

6. The method according to claim 1, wherein, The catalytic cracking reaction conditions of the hydrocarbon oil feedstock include: the reaction temperature is 450-700 °C, the time is 1-10 seconds, the catalyst-oil ratio by weight of the catalyst to the hydrocarbon oil feedstock is 1-50:1, and the space velocity is 0.5-20 h -1 .

7. The method according to claim 1, wherein The hydrocarbon oil feedstock is selected from one or more of gasoline, diesel, vacuum gas oil, atmospheric gas oil, coker gas oil, deasphalted oil, vacuum residue, atmospheric residue, extracted oil, poor recycle oil, coal liquefaction oil, oil sand oil and shale oil.

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