A method for preparing CO product by catalytic cracking

Abstract

The present application discloses a method for preparing CO products by 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 coke-loaded spent catalyst, and feeding the reaction oil gas into a subsequent separation system; subjecting the spent catalyst to steam stripping and then feeding it into a regenerator, making the spent catalyst contact countercurrently with an oxygen-containing gas in the regenerator in the regenerator to regenerate the spent catalyst, and transporting the obtained regenerated catalyst to the catalytic cracking reactor; leading out the flue gas from the top of the regenerator and separating it to obtain CO products; wherein, at least one orifice plate is arranged in the first regeneration zone of the regenerator, and the inclination angle of the orifice plate is 0 to 50°. The method of the present invention can greatly reduce CO2 emissions, produce CO, and also reduce the excess heat in the catalytic regeneration process, and solve the problem of afterburning at the tail of the regenerator.

Description

Technical Field

[0001] The present invention relates to catalytic cracking of petroleum hydrocarbons, and more particularly to a method for producing carbon monoxide by utilizing a 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 regeneration gas is used to regenerate the carbonized catalyst, and regeneration flue gas is generated at the same time. During the regeneration process of the catalyst, the combustion of coke produces a large amount of CO2 gas, making the catalytic cracking unit the largest source of CO2 emissions in the refinery. CO2 in the catalytic cracking flue gas accounts for 15% to 50% of the total emissions of the refinery. The catalytic cracking unit emits 211.7kgCO2 for processing each ton of raw materials. There are about 190 catalytic cracking units in China, with a total processing capacity of about 210 million tons / year, and at least 40 million tons of CO2 emissions.

[0003] During the regeneration process of the catalyst, a large amount of heat is generated, which makes the catalytic device have excess heat. An external heat extraction device is required to convert the heat generated by the catalyst regeneration into steam energy and recover the energy of the high-temperature flue gas, but this is all low-quality energy utilization. In addition, the regenerated flue gas contains carbon monoxide, which often causes tail combustion, causing local overheating of the regenerator and aggravated catalyst deactivation. Tail combustion can be reduced by controlling the oxygen content in the flue gas, but it will reduce the burning rate and burning intensity. At the same time, there is a problem of tail gas emissions, resulting in the loss of chemical energy in carbon monoxide. Refineries often use carbon monoxide combustion aids or flue gas boilers to reduce carbon monoxide in flue gas and recover energy, but the problem of carbon monoxide in flue gas has never been properly solved.

[0004] CN1400159A discloses a method for producing hydrogen using catalytic cracking regeneration flue gas, which can make reasonable use of CO in the regeneration flue gas and alleviate the problem of excess heat in the FCC device. However, the CO content obtained by this method is low, only reaching about 14% by volume.

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

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

[0007] However, the existing technology produces hydrogen through incomplete regeneration of flue gas. Although coke is used, carbon is still mainly emitted in the form of carbon dioxide, and the CO content is relatively low; and the method of directly contacting the regenerated catalyst with water vapor to produce synthesis gas will accelerate the deactivation of the catalyst. Summary of the invention

[0008] The present application provides a method for preparing a CO product by catalytic cracking, comprising:

[0009] The hydrocarbon oil feedstock is brought into contact with the catalytic cracking catalyst in the catalytic cracking reactor to carry out a catalytic cracking reaction, and the reaction oil gas and the spent catalyst with carbon deposition are separated, and the reaction oil gas is sent to a subsequent separation system;

[0010] The catalyst to be regenerated is sent into a regenerator after stripping, and the regenerator comprises a first regeneration zone and a second regeneration zone from top to bottom, and the catalyst to be regenerated enters the first regeneration zone of the regenerator from the upper part of the regenerator;

[0011] Allowing the regenerator oxygen-containing gas to enter the second regeneration zone of the regenerator from the lower part of the regenerator;

[0012] The catalyst to be regenerated is contacted with the oxygen-containing gas in the regenerator in countercurrent in the regenerator to regenerate the catalyst to be regenerated, and the obtained regenerated catalyst is transported to the catalytic cracking reactor;

[0013] Flue gas is drawn out from the top of the regenerator and separated to obtain CO product;

[0014] Wherein, the first regeneration zone of the regenerator is provided with at least one orifice plate, and the inclination angle of the orifice plate is 0 to 50 degrees.

[0015] In one embodiment, the opening rate of the orifice plate is 1% to 90%, and the opening diameter is 1 to 30 cm.

[0016] In one embodiment, an overflow weir is arranged on the orifice plate.

[0017] In one embodiment, the second regeneration zone of the regenerator is a dense phase bed with a bed density of 100-700 kg / m3.

[0018] In one embodiment, the volume ratio of the second regeneration zone of the regenerator to the first regeneration zone of the regenerator is 1:1-1:10.

[0019] In one embodiment, in the regenerator, the reaction temperature is 400-600° C., the gas superficial velocity is 0.3-5 m / s, and the average residence time of the catalyst to be regenerated is 0.6-10 minutes.

[0020] In one embodiment, the oxygen content in the regenerator oxygen-containing gas is greater than 10% based on the total volume of the regenerator oxygen-containing gas.

[0021] In one embodiment, the regenerator oxygen-containing gas is selected from oxygen, air, a mixed gas of oxygen and nitrogen with an oxygen content of 10-30%, and a mixed gas of oxygen and CO2 with an oxygen content of 10-30%.

[0022] In one embodiment, the catalytic cracking reactor is a riser reactor, a fluidized bed reactor, or a combination thereof.

[0023] In one embodiment, the catalytic cracking reaction conditions of the hydrocarbon oil feedstock include: a reaction temperature of 450-700°C, a time of 1-10 seconds, a catalyst-oil ratio of 1-50:1, and a space velocity of 0.5-20 h -1 .

[0024] 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 wax oil, atmospheric wax oil, coker wax oil, deasphalted oil, vacuum residue oil, atmospheric residue oil, extracted oil and inferior recycled oil, and the other mineral oils are selected from one or more of coal liquefaction oil, oil sand oil and shale oil.

[0025] In the present invention, the combustion of coke in the catalyst regeneration process is controlled so that incomplete combustion occurs to generate CO, and part of the energy is stored in CO as chemical energy, which can reduce excess heat in the catalytic regeneration process, solve the problem of tail combustion in the regenerator, and greatly reduce CO2 emissions without affecting the catalyst regeneration effect. Part of the CO2 in the first oxygen-containing gas can also react with coke to further generate CO. The generated CO can be a raw material for subsequent chemical industry, metallurgy, etc., saving raw materials such as coal and methane for the production of CO, saving resources and energy consumption, and further reducing emissions. Therefore, under the background of carbon neutrality and carbon peak goals, the production of CO using the catalytic cracking regeneration process can achieve waste recycling and energy conservation and emission reduction, which has huge economic and social benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present invention but do not constitute a limitation of the present invention. In the accompanying drawings:

[0027] Figure 1It is a schematic diagram of the process according to the present invention.

[0028] Figure 2 Schematic diagram of the catalytic cracking process with single-stage regeneration. DETAILED DESCRIPTION

[0029] The present application is further described in detail below through the accompanying drawings and embodiments. Through these descriptions, the characteristics and advantages of the present application will become clearer and more specific.

[0030] The word "exemplary" is used exclusively herein to mean "serving as an example, embodiment, or illustration." Any embodiment described herein as "exemplary" is not necessarily to be construed as preferred or advantageous over other embodiments. Although various aspects of the embodiments are shown in the drawings, the drawings are not necessarily drawn to scale unless otherwise noted.

[0031] 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.

[0032] The present application provides a method for preparing a CO product by catalytic cracking, comprising:

[0033] The hydrocarbon oil feedstock is brought into contact with the catalytic cracking catalyst in the catalytic cracking reactor to carry out a catalytic cracking reaction, and the reaction oil gas and the spent catalyst with carbon deposition are separated, and the reaction oil gas is sent to a subsequent separation system;

[0034] The catalyst to be regenerated is sent into a regenerator after stripping, and the regenerator comprises a first regeneration zone and a second regeneration zone from top to bottom, and the catalyst to be regenerated enters the first regeneration zone of the regenerator from the upper part of the regenerator;

[0035] Allowing the regenerator oxygen-containing gas to enter the second regeneration zone of the regenerator from the lower part of the regenerator;

[0036] The catalyst to be regenerated is contacted with the oxygen-containing gas in the regenerator in countercurrent in the regenerator to regenerate the catalyst to be regenerated, and the obtained regenerated catalyst is transported to the catalytic cracking reactor;

[0037] Flue gas is drawn out from the top of the regenerator and separated to obtain CO product;

[0038] Wherein, the first regeneration zone of the regenerator is provided with at least one orifice plate, and the inclination angle of the orifice plate is 0 to 50 degrees.

[0039] The process flow of the method provided by the present invention is described in detail below with reference to the accompanying drawings:

[0040] As attached Figure 1As shown, the catalytic cracking feedstock 1 enters from the bottom of the riser reactor 2, contacts with the regenerated catalyst for reaction, the reaction oil gas and catalyst move upward to the settler 3 for gas-solid separation, the separated reaction oil gas 4 goes to the subsequent absorption stabilization system, the catalyst to be regenerated enters the first regeneration zone 9 of the regenerator 6 through the slide valve 5 to be regenerated, contacts with the first oxygen-containing gas from the second regeneration zone 8 for the first regeneration, and obtains a semi-regenerated catalyst; the semi-regenerated catalyst moves downward along the orifice plate of the first regeneration zone into the second regeneration zone 8, contacts with the second oxygen-containing gas 7 for the second regeneration, and obtains a regenerated catalyst; the regenerated catalyst returns to the bottom of the riser reactor 2 through the regeneration slide valve to contact with the feedstock 1 for reaction. After gas-solid separation, the regenerated flue gas 10 is led out of the regenerator 6 to the subsequent energy recovery and separation system 11 to obtain carbon monoxide 12 and other flue gas components 13.

[0041] In one embodiment, the catalyst to be spent comes from a catalytic cracking reactor 2 of hydrocarbon oil feedstock, and the regenerated catalyst is also transported to the catalytic cracking reactor 2 .

[0042] According to the present invention, after catalytic cracking, the spent catalyst and the reaction oil and gas are separated, and the reaction oil and gas are separated into dry gas, liquefied gas, stabilized gasoline, catalytic diesel and other fractions through a subsequent separation system. This is a conventional technical method in the art, and the present invention is not limited to this and will not be described in detail herein.

[0043] According to the present invention, the catalytic cracking reactor can be a conventional catalytic cracking riser reactor, a fluidized bed reactor or a combination thereof known to those skilled in the art, for example, a catalytic cracking riser reactor 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, preferably an equal diameter riser. The fluidized bed reactor is located downstream of the riser reactor and is connected to the outlet of the riser reactor. The riser reactor includes a pre-lifting section and at least one reaction zone from bottom to top. In order to allow the crude oil to react fully and according to different quality requirements of the target product, the reaction zones can be 2 to 8, preferably 1 to 3.

[0044] According to the present invention, the catalytic cracking reaction conditions include: reaction temperature of 450-700°C, preferably 500-650°C, more preferably 550-600°C; reaction time of 1-10 seconds, preferably 2-5 seconds; catalyst-oil ratio (weight ratio of catalyst to hydrocarbon oil feedstock) of 1-50:1, preferably 5-30:1; space velocity of 0.5-20h -1 , preferably 2 to 10 hours -1 .

[0045] In the present invention, water vapor may be injected into the catalytic cracking reactor. The water vapor is preferably injected in the form of atomized steam. The weight ratio of the injected water vapor to the light hydrocarbon oil feedstock may be 0.01 to 1:1, preferably 0.05 to 0.5:1.

[0046] According to the present invention, the catalyst used for the catalytic cracking reaction can be a conventional choice in the art. For the present invention, preferably, based on the total weight of the catalyst, the catalytic cracking catalyst comprises 15 to 65% by weight of natural minerals, 10 to 30% by weight of inorganic oxides, and 25 to 75% by weight of zeolite.

[0047] According to the present invention, the zeolite as the active component is preferably one or a mixture of Y zeolite, mordenite, β zeolite, zeolite with MFI structure (such as ZSM series zeolite and / or ZRP zeolite).

[0048] According to the present invention, the natural mineral is selected from one or more of kaolin, halloysite, montmorillonite, diatomaceous earth, attapulgite, sepiolite, halloysite, hydrotalcite, bentonite and rectorite.

[0049] The inorganic oxide is selected from one or more of silicon oxide, aluminum oxide, zirconium oxide, titanium oxide and amorphous silicon aluminum.

[0050] According to the present invention, the raw materials used for catalytic cracking include petroleum hydrocarbons and / or other mineral oils, wherein the petroleum hydrocarbons are selected from one or more of gasoline, diesel, vacuum wax oil, atmospheric wax oil, coker wax oil, deasphalted oil, vacuum residue oil, atmospheric residue oil, extracted oil and inferior recycled oil, and the other mineral oils are selected from one or more of coal liquefaction oil, oil sand oil and shale oil.

[0051] The regenerator 6 used in the present invention includes two regeneration areas, a first regeneration zone 9 and a second regeneration zone 8. The first regeneration zone 9 is located at the upper part of the regenerator 6, and the second regeneration zone 8 is located at the lower part of the regenerator 6. In one embodiment, at least one orifice plate is provided in the first regeneration zone 9 of the regenerator 6, and the orifice plate has an inclination angle of 0 to 50°. In one embodiment, the orifice plate opening rate is 1% to 90%, preferably 5% to 80%, and more preferably 20% to 70%; the opening diameter is 1 to 30 cm, preferably 5 to 20 cm, and more preferably 10 to 15 cm. The number of orifice plates and their distribution in the first regeneration zone 9 can be set as needed. For example, the number of orifice plates can be 2 to 10, preferably 4 to 8, and can be distributed in the first regeneration zone 9 in a roughly uniform manner.

[0052] In one embodiment, the orifice plate inclination angle (the angle between the orifice plate and the horizontal line) is 0 to 50°, preferably 5 to 45°, and more preferably 15 to 30°. The orifice plate is arranged with a certain inclination angle, which is conducive to the semi-regenerated catalyst moving downward along the orifice plate of the first regeneration zone into the second regeneration zone 8. In one embodiment, an overflow weir is arranged on the orifice plate.

[0053] By setting the perforated plate as above, the following effects can be achieved: under the premise of ensuring the fluidized state of the catalyst, the ratio of coke to oxygen-containing gas can be increased, the catalyst residence time can be increased, and more coke can be promoted to be incompletely burned to produce CO, thereby reducing the combustion of coke to produce CO2 in the second regeneration zone.

[0054] In one embodiment, the second regeneration zone 8 of the regenerator is a dense bed with a bed density of 100-700 kg / m3. In one embodiment, the bed density is 100-700 kg / m3, preferably 150-600 kg / m3, and more preferably 250-500 kg / m3.

[0055] In one embodiment, the volume ratio of the second regeneration zone 8 of the regenerator to the first regeneration zone 9 of the regenerator is 1:1-1:10, preferably 1:2-1:5. Such a ratio is beneficial to prolong the residence time of the catalyst to be regenerated in the second regeneration zone, so that more coke is burned to generate CO and the carbon content on the semi-regenerated catalyst is reduced.

[0056] In one embodiment, in the regenerator, the reaction temperature is 400-600°C, the gas superficial linear velocity is 0.3-5 m / s, and the average residence time of the catalyst to be regenerated is 0.6-10 minutes. In one embodiment, the reaction conditions of the regenerator include: the reaction temperature is 400-600°C, preferably 450-580°C, and more preferably 500-550°C; the gas superficial linear velocity is 0.3-5 m / s, preferably 0.5-3.5 m / s, and more preferably 0.8-2 m / s; the average residence time of the catalyst to be regenerated is 0.6-10 minutes, preferably 2-8 minutes, and more preferably 3-6 minutes.

[0057] In one embodiment, the oxygen content in the regenerator oxygen-containing gas 7 (i.e., the second regenerator oxygen-containing gas) is more than 10%, based on the total volume of the regenerator oxygen-containing gas. In one embodiment, the regenerator oxygen-containing gas can be 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%. In one embodiment, the second oxygen-containing gas can be oxygen, air, a mixed gas of oxygen and nitrogen with an oxygen content of 10 to 30%, and / or a mixed gas of oxygen and CO2 with an oxygen content of 10 to 30%, preferably oxygen, more preferably a mixed gas of oxygen and CO2 with an oxygen content of 10 to 30%. In one embodiment, the regenerator oxygen-containing gas 7 (i.e., the second regenerator oxygen-containing gas) is preferably oxygen, more preferably a mixed gas of oxygen and CO2 with an oxygen content of 10 to 30%.

[0058] According to the present invention, the CO2 in the mixed gas of oxygen and CO2 with an oxygen content of 10-30% can come from the CO2 in the regeneration flue gas, thereby further reducing the CO2 gas emission of the catalytic cracking unit.

[0059] According to the present invention, the first oxygen-containing gas used in the first regeneration reaction zone is the gas obtained by the reaction of the regenerator oxygen-containing gas 7 (ie, the second regenerator oxygen-containing gas) with the semi-regenerated catalyst.

[0060] According to the present invention, at least a portion of the catalytic cracking catalyst is a regenerated catalyst, and preferably all of the catalytic cracking catalyst is a regenerated catalyst.

[0061] According to the present invention, preferably, the method of the present invention further comprises stripping (generally with steam) the regenerated catalyst obtained from the second regeneration to remove gas and other impurities.

[0062] According to the present invention, an internal heat exchanger or an external heat exchanger may be provided in the regenerator, and the type, connection and operation of the heat exchanger are well known to those skilled in the art.

[0063] According to the present invention, the flue gas obtained from the regenerator is separated to obtain a CO product. The CO product can be separated by alkali washing, membrane separation, pressure swing adsorption, cryogenics, COSORB or other separation and purification methods well known to those skilled in the art, preferably alkali washing.

[0064] According to the present invention, before separating CO, the flue gas can be purified to remove impurities such as sulfur oxides and nitrogen oxides.

[0065] The method provided by the present invention converts the coke on the catalytic cracking catalyst to be regenerated into carbon monoxide, which greatly reduces the emission of CO2. By changing the regeneration and burning method to produce carbon monoxide, the catalyst does not come into contact with high-temperature water vapor, which will not accelerate the deactivation of the catalyst. At the same time, it can effectively reduce tail combustion and slow down the catalyst deactivation rate.

[0066] The method provided by the present invention reduces combustion heat release through incomplete combustion, thereby alleviating the problem of excess heat in the catalytic device; and enables the catalyst to be regenerated to be completely regenerated in the second regeneration zone without affecting the activity of the catalytic cracking reaction.

[0067] When the method provided by the present invention uses oxygen as the oxygen source for burning, nitrogen is not introduced, and a relatively simple method can be adopted to separate and obtain a CO product with a higher purity. When a mixed gas of oxygen and CO2 is used as the oxygen source, part of the CO2 can be converted into CO, and at the same time, it plays a role in enriching CO2, which is beneficial to carbon capture and utilization. By adopting the method of the present invention, the CO content in the flue gas can reach a very high level, which is beneficial to the subsequent further purification and application of CO. When pure oxygen is used as the oxygen-containing gas of the regenerator, the volume ratio of CO in the flue gas can reach more than 76%; when air is used as the oxygen-containing gas of the regenerator, the volume ratio of CO in the flue gas can reach more than 26%; and, a mixed gas of oxygen and CO2 gas can also be used as the oxygen-containing gas of the regenerator, and the volume ratio of CO in the flue gas can reach more than 80%.

[0068] The method provided by the present invention has a low regeneration temperature and can realize a large catalyst-to-oil ratio operation of the catalytic cracking reaction. The method provided by the present invention not only reduces the carbon dioxide emission of the catalytic device, but also uses carbon monoxide as a raw material for subsequent chemical processes, realizes the transformation of waste into treasure and the full utilization of resources, saves fossil resources such as coal, oil and methane used to produce carbon monoxide, reduces energy consumption and investment, reduces pollution, and improves the economic and social benefits of the petrochemical industry.

[0069] The following examples will further illustrate the method, but are not intended to limit the present invention.

[0070] The raw material oil used in the embodiments and comparative examples is Anqing wax oil, and its properties are shown in Table 1.

[0071] The catalytic cracking catalyst used in the examples and comparative examples has a trade name of CDOS (Sinopec Catalyst Co., Ltd. Changling Branch).

[0072] As attached Figure 1As shown, the catalytic cracking feedstock 1 enters from the bottom of the riser reactor 2, contacts with the regenerated catalyst for reaction, the reaction oil gas and catalyst move upward to the settler 3 for gas-solid separation, the separated reaction oil gas 4 goes to the subsequent absorption stabilization system, the catalyst to be regenerated enters the first regeneration zone 9 of the regenerator 6 through the slide valve 5 to be regenerated, contacts with the first oxygen-containing gas from the second regeneration zone 8 for the first regeneration, and obtains a semi-regenerated catalyst; the semi-regenerated catalyst moves downward along the orifice plate of the first regeneration zone into the second regeneration zone 8, contacts with the second oxygen-containing gas 7 for the second regeneration, and obtains a regenerated catalyst; the regenerated catalyst returns to the bottom of the riser reactor 2 through the regeneration slide valve to contact with the feedstock 1 for reaction. After gas-solid separation, the regenerated flue gas 10 is led out of the regenerator 6 to the subsequent energy recovery and separation system 11 to obtain carbon monoxide 12 and other flue gas components 13.

[0073] Figure 1 The regenerator 6 used has the following structure:

[0074] The regenerator 6 includes a first regeneration zone 9 and a second regeneration zone 8, wherein four orifice plates are arranged in the first regeneration zone 9, the opening rate of the orifice plates is 50%, and the inclination angle of the orifice plates is 20°; the volume ratio of the first regeneration zone 9 to the second regeneration zone 8 is 4:1.

[0075] Comparative Example 1

[0076] According to the attached Figure 1 The relevant operating conditions and products are listed in Table 3.

[0077] Comparative Examples 2-3

[0078] According to the attached Figure 2 The process was tested, the catalytic cracking feedstock 21 entered from the bottom of the riser reactor 22, contacted with the regenerated catalyst for reaction, the reaction oil gas and catalyst moved upward to the settler 23 for gas-solid separation, the separated reaction oil gas 24 went to the subsequent separation system, the catalyst to be regenerated entered the regenerator 26 through the regeneration slide valve 25 and contacted with the oxygen-containing gas for regeneration, the regenerated flue gas 27 was led out of the regenerator 26 to the subsequent energy recovery system, and the regenerated catalyst returned to the bottom of the riser reactor 22 through the regeneration slide valve 29 to contact with the feedstock 21 for reaction. The relevant operating conditions and products are listed in Table 3.

[0079] Examples 1-6

[0080] According to the attached Figure 1 The relevant operating conditions and products are listed in Table 2.

[0081] Comparative Example 4

[0082] According to the attached Figure 2 The relevant operating conditions and products are listed in Table 3.

[0083] It can be seen from the results of the examples that the method of the present invention has the advantages of significantly reducing carbon dioxide emissions and producing carbon monoxide.

[0084] The present application has been described above in conjunction with preferred embodiments, but these embodiments are only exemplary and serve only as an illustration. On this basis, various replacements and improvements may be made to the present application, all of which fall within the scope of protection of the present application.

[0085] Table 1

[0086]

[0087] Table 2

[0088]

[0089] Table 3

[0090] project Comparative Example 1 Comparative Example 2 Comparative Example 3 Comparative Example 4 Reaction conditions Reaction temperature / ℃ 550 550 550 550 Agent-oil ratio 8 8 8 8 Reaction time / s 3 3 3 3 Regeneration conditions Regeneration temperature / ℃ 650 650 650 550 Catalyst residence time / min 2 5 5 5 Gas speed (m / s) 0.9 1.2 1.2 1.2 Oxygen-containing gas composition / volume % <![CDATA[CO2]]> - - - - <![CDATA[O2]]> 100.00 100.00 21.00 100.00 <![CDATA[N2]]> - - 79 - Flue gas composition / volume % CO 40.13 45.83 11.56 60.75 <![CDATA[CO2]]> 59.49 53.84 13.64 37.66 <![CDATA[O2]]> 0.12 0.08 0.21 1.38 <![CDATA[N2]]> 0.26 0.25 74.59 0.21

Claims

1. A method for preparing a CO product by catalytic cracking, comprising: The hydrocarbon oil feedstock is brought into contact with the catalytic cracking catalyst in the catalytic cracking reactor to carry out a catalytic cracking reaction, and the reaction oil gas and the spent catalyst with carbon deposition are separated, and the reaction oil gas is sent to a subsequent separation system; The catalyst to be regenerated is sent into a regenerator after stripping, and the regenerator comprises a first regeneration zone and a second regeneration zone from top to bottom, and the catalyst to be regenerated enters the first regeneration zone of the regenerator from the upper part of the regenerator; Allowing the regenerator oxygen-containing gas to enter the second regeneration zone of the regenerator from the lower part of the regenerator; The catalyst to be regenerated is contacted with the oxygen-containing gas in the regenerator in countercurrent in the regenerator to regenerate the catalyst to be regenerated, and the obtained regenerated catalyst is transported to the catalytic cracking reactor; Flue gas is drawn out from the top of the regenerator and separated to obtain CO product; Wherein, the first regeneration zone of the regenerator is provided with at least one orifice plate, and the orifice plate has an inclination angle of 5 to 50°; In the regenerator, the reaction temperature is 400-600°C, the gas superficial velocity is 0.3-5 m / s, and the average residence time of the catalyst to be regenerated is 0.6-10 minutes; The oxygen-containing gas of the regenerator is selected from oxygen, air, a mixed gas of oxygen and nitrogen with an oxygen content of 10-30%, and a mixed gas of oxygen and CO2 with an oxygen content of 10-30%.

2. The method according to claim 1, wherein: The opening rate of the orifice plate is 1% to 90%, and the opening diameter is 1 to 30 cm.

3. The method according to claim 1, wherein: An overflow weir is arranged on the orifice plate.

4. The method according to claim 1, wherein: The second regeneration zone of the regenerator is a dense phase bed with a bed density of 100-700 kg / m3.

5. The method according to claim 1, wherein: The volume ratio of the second regeneration zone of the regenerator to the first regeneration zone of the regenerator is 1:1-1:

10.

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

7. The method according to claim 1, wherein: The catalytic cracking reaction conditions of hydrocarbon oil raw materials include: reaction temperature of 450-700°C, time of 1-10 seconds, catalyst-oil ratio of 1-50:1, space velocity of 0.5-20h -1 .

8. The method according to claim 1, wherein: The hydrocarbon oil raw material includes petroleum hydrocarbons and / or other mineral oils, the petroleum hydrocarbons are selected from one or more of gasoline, diesel, vacuum wax oil, atmospheric wax oil, coker wax oil, deasphalted oil, vacuum residue oil, atmospheric residue oil, extracted oil and inferior recycled oil, and the other mineral oils are selected from one or more of coal liquefaction oil, oil sand oil and shale oil.

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