Carbon capture and utilization system for olefin cracking process

Abstract

The carbon capture and utilization system comprises an olefin cracking device, a combustion heat supply device, a heat exchanger, an oxygen supply device and a CO2 pretreatment device which are in fluid communication, and is characterized by comprising a first hydrogen pretreatment device, a second hydrogen pretreatment device and a third hydrogen pretreatment device, the first hydrogen pretreatment device is used for separating hydrogen from byproducts of the olefin cracking device and increasing hydrogen pressure, and an inlet of the first hydrogen pretreatment device is communicated with an outlet of the olefin cracking device; the CO2 hydrogenation reactor is used for receiving pretreated CO2 and hydrogen, the CO2 hydrogenation reactor is provided with a CO2 inlet and a first hydrogen inlet, the CO2 inlet is communicated with an outlet of the CO2 pretreatment device, and the first hydrogen inlet is communicated with an outlet of the first hydrogen pretreatment device.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of carbon capture and utilization. Specifically, the present application relates to a carbon capture and utilization system for an olefin cracking process. BACKGROUND

[0002] The information provided in this section is for the purpose of generally presenting the context of the disclosure. To the extent that specific experiments, aspects, examples or the like that are described in this section are already prior art as of the filing date of this disclosure and are included in the background of the disclosure for purposes of enabling the present disclosure, it should not be assumed that the same is appreciated in such art prior to the filing date of this disclosure.

[0003] Existing olefin cracking processes face many challenges in achieving emission reduction and zero carbon targets. Although CO2 emissions are reduced to some extent by carbon capture technology, current processes mainly focus on the capture and absorption of CO2 and the carbon capture facility investment is huge due to large amount of flue gas and low CO2 concentration, and the actual utilization rate of captured CO2 is low, which is difficult to effectively convert into valuable products. At the same time, since the all-electric operation process is not realistic under the current conditions, the cracking process relying on fossil fuel heating is still the main mode, which results in limited emission reduction effect.

[0004] In addition, the products of the olefin cracking process usually need to go through a dehydrogenation step, but a large amount of waste hydrogen gas produced by dehydrogenation is not fully recovered and utilized, and is often discharged as waste gas, further increasing resource waste. The existing process fails to effectively combine captured CO2 with cracking by-product waste hydrogen to produce high value-added chemicals through hydrogenation reaction, and fails to form a comprehensive zero carbon emission olefin cracking process system. SUMMARY

[0005] The present application provides a carbon capture and utilization system for an olefin cracking process to solve one or more of the above problems and other aspects, or to provide an alternative technical solution to the prior art.

[0006] According to one aspect of the present application, a carbon capture and utilization system for an olefin cracking process is provided, which comprises an olefin cracking device, a combustion heat supply device, a heat exchanger, an oxygen supply device and a CO2 pretreatment device in fluid communication, the heat exchanger is provided with a first inlet, a second inlet, a first outlet and a second outlet, the first inlet is in communication with the outlet of the combustion heat supply device, the second inlet is in communication with the oxygen outlet of the oxygen supply device, the first outlet is in communication with the reflux inlet of the combustion heat supply device, and the second outlet is in communication with the inlet of the CO2 pretreatment device, the carbon capture and utilization system comprises:

[0007] a first hydrogen pretreatment device for separating hydrogen from byproducts of the olefin cracking device and increasing hydrogen pressure, an inlet of the first hydrogen pretreatment device being in communication with an outlet of the olefin cracking device; and

[0008] a CO2 hydrogenation reactor for receiving the pretreated CO2 and hydrogen, the CO2 hydrogenation reactor being provided with a CO2 inlet and a first hydrogen inlet, the CO2 inlet being in communication with an outlet of the CO2 pretreatment device, and the first hydrogen inlet being in communication with an outlet of the first hydrogen pretreatment device.

[0009] In the carbon capture and utilization system according to the present application, preferably, the oxygen supply device comprises a water electrolysis device for supplying hydrogen to the CO2 hydrogenation reactor, the water electrolysis device being further provided with a hydrogen outlet and the CO2 hydrogenation reactor being provided with a second hydrogen inlet, the hydrogen outlet of the water electrolysis device being in communication with the second hydrogen inlet of the CO2 hydrogenation reactor via a portion of a second hydrogen pretreatment device.

[0010] In the carbon capture and utilization system according to the present application, preferably, renewable energy is used to supply electric energy to the water electrolysis device.

[0011] In the carbon capture and utilization system according to the present application, preferably, the oxygen supply device comprises an air separation device for receiving air and separating oxygen therefrom.

[0012] In the carbon capture and utilization system according to the present application, preferably, the air separation device is further provided with a nitrogen outlet, the nitrogen outlet being in communication with an ammonia production system.

[0013] In the carbon capture and utilization system according to the present application, preferably, an outlet of the CO2 hydrogenation reactor is in communication with a CO2 hydrogenation product preparation process system.

[0014] The technical solution provided by the present application realizes significantly reduced total flue gas emission and nitrogen oxide generation by using oxygen-enriched combustion technology, and reduces the cost and energy consumption of CO2 capture. On this basis, the byproduct waste hydrogen in the olefin cracking process is efficiently separated, and high value-added products are generated by hydrogenation reaction with CO2, reducing the demand for external hydrogen and optimizing energy consumption. In addition, combined with the water electrolysis process driven by green electricity, oxygen and hydrogen are provided simultaneously, further reducing carbon emissions and improving energy utilization efficiency, realizing the zero carbon emission goal of the entire process, and significantly improving the comprehensive utilization rate of resources and economic benefits. BRIEF DESCRIPTION OF DRAWINGS

[0015] The disclosure of the present application will become more apparent from the following description in conjunction with the accompanying drawings. As will be readily appreciated by one skilled in the art, the present application is susceptible to capricious variations without departing from the scope of the application. Accordingly, the drawings of the application are schematic and illustrative of preferred embodiments of the present application. In these drawings, like reference numerals indicate like parts:

[0016] Figure 1 A system for carbon capture for an olefin cracking process in the prior art is exemplarily shown.

[0017] Figure 2 A system for carbon capture and utilization for an olefin cracking process according to the present application is exemplarily shown. DETAILED DESCRIPTION

[0018] In order that the foregoing and other objects, features and advantages of the present application can be readily understood, a more particular description of the carbon capture and utilization system for an olefin cracking process according to the present application can be had by reference to the following detailed description when considered in connection with the drawings. It is to be understood that all descriptions are illustrative and are not intended to limit the scope of the present application. For the avoidance of doubt, the present application still allows any combination or deletion of technical features (or their equivalents) described or implied in each embodiment mentioned herein, or any single technical feature shown or implied in each drawing, to continue without any technical obstacles, so that more embodiments according to the present application should be considered to be included in the scope of the description herein.

[0019] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. If there is an inconsistency between the definitions provided in this application and the commonly understood meanings, the definitions provided in this application control.

[0020] In the present application, unless specifically stated otherwise, the terms "first", "second", and so on are used only for the purpose of distinguishing different objects and are not intended to indicate relative importance or order of sequence and the like.

[0021] In the present application, unless specifically stated otherwise, the term "communication (or connection, connection, etc.)" includes communication (or connection, connection, etc.) in a direct or indirect manner.

[0022] In the present application, unless otherwise defined, the numerical ranges listed herein are intended to include the endpoints of the range, and all numerical values and all sub-ranges within the range.

[0023] In the present application, unless otherwise specified, in the specification and claims of the present application, all numbers representing quantities, percentages, and the like are understood to be modified by the term "about".

[0024] The present application provides a system for carbon capture and utilization for an olefin cracking process, comprising: Figure 2The carbon capture and utilization system for olefin cracking process shown in the figure is provided by setting at least an oxygen supply device, a combustion heat supply device, an olefin cracking device, a heat exchanger, a CO2 pretreatment device (not shown), a hydrogen pretreatment device including a hydrogen separation device and a pressure increasing device (not shown), and a CO2 hydrogenation reaction device, by allowing oxygen-enriched combustion to increase the concentration of CO2 in the flue gas, which is conducive to the capture of CO2 by miniaturized devices; at the same time, it enables efficient recovery of byproduct waste hydrogen in the olefin cracking reaction, and allows the captured CO2 to be converted into CO2 hydrogenation products with high added value.

[0025] The carbon capture and utilization system for olefin cracking process according to the present application can include an oxygen supply device, a combustion heat supply device, an olefin cracking device, a first hydrogen pretreatment device, a heat exchanger, a CO2 pretreatment device, and a CO2 hydrogenation reactor, wherein the heat exchanger can be provided with a first inlet, a second inlet, a first outlet, and a second outlet.

[0026] In the carbon capture and utilization system according to the present application as shown in Figure 2 , the combustion heat supply device can include a burner for fuel gas combustion and a plurality of heaters for heating the olefin cracking device by means of the heat-conducting fluid generated by combustion with a suitably high temperature, wherein the outlet provided on the burner can be in communication with the first inlet of the heat exchanger, and the outlet provided on the heater can be in communication with the inlet of the olefin cracking device.

[0027] In the carbon capture and utilization system according to the present application, the person skilled in the art can select the burner and the heater suitable for withstanding and conducting the required high temperature according to the temperature required by the olefin cracking reaction, and configure the combustion heat supply device as needed. For example, for the burner whose temperature needs to be maintained in the range of 700℃ to 1200℃, the burner can take the form of a radiant tube burner or a direct flame burner, the heater can take the form of a radiant heater or a convection heater, and be configured in the form of a tube, a disc, or a plate.

[0028] In the carbon capture and utilization system according to the present application, referring to Figure 2 , the second inlet of the heat exchanger can be in communication with the oxygen supply device, and the first outlet of the heat exchanger can be in communication with the backflow inlet of the combustion heat supply device. In use, the oxygen generated by the oxygen supply device flows into the burner through the heat exchanger for oxygen-enriched combustion, and the high-temperature gas stream generated by combustion is used to heat the olefin cracking device through the heater; the flue gas generated by oxygen-enriched combustion in the burner flows into the heat exchanger for cooling, part of which flows back to the burner to cool the burner, and the other part continues to flow into the CO2 pretreatment device (not shown in Figure 2 ).

[0029] In the carbon capture and utilization system according to the present application, the CO2preprocessing device can include a CO2gas pressurization device and a purification device known in the art. The CO2passing through the CO2preprocessing device is pressurized and purified to a pressure suitable for use in the CO2hydrogenation reactor.

[0030] For example, the CO2gas purification device according to the present application includes, but is not limited to, an adsorption type CO2purification device, a membrane separation CO2purification device, and a chemical absorption CO2device, and the like, and the operation method for purifying CO2using the above-mentioned CO2gas purification device is known in the art.

[0031] In the carbon capture and utilization system according to the present application, for the olefin cracking device, any reaction device conventionally used for an olefin cracking reaction and an optional main by-product separation device can be selected as needed. The configuration of the reaction device and the main by-product separation device is known in the art. The olefin cracking device can be provided with a main product outlet for outputting a main product generated by the cracking reaction, and a by-product outlet for outputting a by-product, the by-product outlet being in communication with the inlet of the first hydrogen preprocessing device.

[0032] In the carbon capture and utilization system according to the present application, the first hydrogen preprocessing device can include a hydrogen pressure increasing device and a hydrogen separation device in fluid communication, so that the by-product from the olefin cracking device is pressurized to an appropriate pressure and then enters the hydrogen separation device for hydrogen separation. In some embodiments, especially in the case where there is another source of hydrogen in addition to the hydrogen separation device, the system can further include, as needed, another hydrogen pressure increasing device and a hydrogen purification device in fluid communication as a second hydrogen preprocessing device, to further increase the purity of hydrogen before it enters the CO2hydrogenation reactor.

[0033] For example, the hydrogen separation device according to the present application can employ, including but not limited to, pressure swing adsorption technology, membrane separation technology, and any technology suitable for separating hydrogen and light hydrocarbons in the by-product and achieving a hydrogen recovery rate of 90% or more, the operation process of which is known in the art. The hydrogen pressure increasing device according to the present application can employ a gas pressurization device that is conventional in the art and has appropriate parameters.

[0034] In the carbon capture and utilization system according to the present application, the CO2hydrogenation reactor can thus have a CO2inlet for receiving the combustion product from the heat exchanger and a first hydrogen inlet for receiving hydrogen from the first hydrogen preprocessing device. The CO2hydrogenation reactor can be configured to have conditions and parameters that allow CO2and hydrogen to undergo the desired hydrogenation reaction and facilitate the reaction.

[0035] For example, the types of CO2 hydrogenation reactors according to the present application include, but are not limited to, fixed bed reactors, fluidized bed reactors, slurry bed reactors, circulating bed reactors, multi-stage tube reactors, loop reactors, and column reactors. One skilled in the art can select an appropriate reactor type based on factors such as flow rate, catalyst regeneration cycle, and the like, and use a suitable reactor type.

[0036] In some embodiments, in the carbon capture and utilization system according to the present application, the oxygen supply device can comprise a water electrolysis device. In use, oxygen gas produced by water electrolysis is supplied from an oxygen gas outlet to the heat exchanger as described above.

[0037] In some embodiments, in the carbon capture and utilization system according to the present application, the water electrolysis device can be further provided with a hydrogen gas outlet and the CO2 hydrogenation reactor is provided with a second hydrogen gas inlet, the hydrogen gas outlet of the water electrolysis device can be in communication with the additional hydrogen gas pressure increasing device and the hydrogen gas purification device in the hydrogen gas pretreatment device described above, and the additional hydrogen gas purification device can be in communication with the second hydrogen gas inlet of the CO2 hydrogenation reactor, so that the water electrolysis device can further supply hydrogen gas to the CO2 hydrogenation reactor as a supplement to the hydrogen gas source other than the hydrogen gas from the olefin cracking device.

[0038] In some embodiments, in the carbon capture and utilization system according to the present application, the water electrolysis device can include, but is not limited to, alkaline water electrolysis cells and proton exchange membrane electrolysis cells and other water electrolysis devices with appropriate energy consumption.

[0039] In some embodiments, in the carbon capture and utilization system according to the present application, renewable energy can be used to supply electrical energy to the water electrolysis device. The form of the renewable energy can be selected from wind energy, photovoltaic energy, hybrid energy, and other suitable energy forms applicable to the application.

[0040] In some embodiments, in the carbon capture and utilization system according to the present application, the oxygen supply device can comprise an air separation device for receiving air and separating oxygen gas therefrom. In use, air enters the air separation device, and the resulting oxygen gas is supplied from an oxygen gas outlet to the heat exchanger as described above.

[0041] In some embodiments, in the carbon capture and utilization system according to the present application, the air separation device can separate air based on, for example, cryogenic rectification, pressure swing adsorption, membrane separation, cryogenic separation, and other separation methods suitable for the present application, as a supplement to the additional oxygen gas source other than the oxygen gas from the water electrolysis device.

[0042] In some embodiments, in the carbon capture and utilization system according to the present application, the air separation device can be further provided with a nitrogen gas outlet, which is in communication with an ammonia production system, for supplying the separated nitrogen gas to the ammonia production system. The ammonia production system is a system commonly used in the art for preparing ammonia gas.

[0043] In some embodiments, when the carbon capture and utilization system according to the present application is used on an industrial scale, the outlet of the CO2 hydrogenation reactor can be communicated to a CO2 hydrogenation product preparation process system, so as to supply the CO2 hydrogenation product to a further processing device and convert it into a downstream product required by industrial applications.

[0044] In some embodiments, in the carbon capture and utilization system according to the present application, the CO2 hydrogenation product can be methanol. The product preparation process system can include a methanol-to-olefin (MTO) preparation process system and a methanol-to-jet fuel (MTJ) preparation process system.

[0045] In practice, after the olefin cracking device has been operated for a period of time, a decoking process is usually carried out in the gap of the olefin cracking process, in order to solve the problems of device life shortening and yield reduction caused by coking of the olefin cracking device. Continuing to refer to Figure 2 At this time, the olefin cracking device should be considered as a device to be decoked, and no feed for the olefin cracking process is carried out. The oxygen supply device, the combustion heat supply device, the device to be decoked, the heat exchanger and the CO2 pretreatment device (not shown) according to the present application can be used to capture the CO2 generated in the decoking process.

[0046] Compared with the prior art, the carbon capture and utilization system according to the present application applies the oxygen-enriched combustion carbon capture device to the combustion heat supply device for the olefin process, and recovers the byproduct waste hydrogen gas in the cracking process through the hydrogen separation device for reaction with CO2, achieving efficient utilization of CO2 while reducing the dependence on external hydrogen gas and optimizing energy consumption. In addition, the carbon capture and utilization system according to the present application combines a green electricity-driven water electrolysis device, achieving simultaneous supply of oxygen and hydrogen, thereby enhancing the synergistic cooperation between the devices and further improving the overall energy utilization efficiency and environmental benefits.

[0047] Example

[0048] The concept, specific structure and technical effects of the present application will be further described in conjunction with the embodiments below, so as to enable those skilled in the art to fully understand the purposes, features and effects of the present application. Those skilled in the art will understand that the embodiments herein are only for illustrative purposes and are not intended to limit the scope of the present application.

[0049] Example 1

[0050] Example 1 relates to the laboratory scale capture and utilization of by-product hydrogen and CO2 generated in a propane dehydrogenation process. Referring to Figure 2 , an alkaline electrolyzer powered by renewable energy is used as an oxygen supply device, which obtains oxygen with a purity of about 99% through a water electrolysis reaction, and supplies the oxygen to a heat exchanger at a flow rate of about 9 Nm 3 / h.

[0051] As a supplement to the above-mentioned electrolyzer oxygen supply, an air separator based on vacuum swing adsorption technology is used to separate oxygen from nitrogen in air. The generated oxygen with a purity of about 93% is supplied to the heat exchanger at a flow rate of about 6 Nm 3 / h. Oxygen from both sources of electrolyzer and air separator is collected in the heat exchanger and further supplied to the combustion heating device at a flow rate of about 15 Nm 3 / h.

[0052] The core part of the combustion heating device used in the embodiments of the present application includes a propane dehydrogenation heating furnace and a UOP Kettle propane dehydrogenation oxygen-rich burner. The heating furnace is used to heat the raw gas of the propane dehydrogenation process to the required reaction temperature, and the furnace temperature is set to 800°C and the pressure is set to -100 PaG. The fuel gas used in the embodiments of the present application is selected as natural gas, which enters the burner through the fuel inlet arranged on the burner at a flow rate of 6 Nm 3 / h, and the furnace chamber temperature is controlled by adjusting the flow rate of natural gas. The above-mentioned oxygen from the heat exchanger is mixed with the fuel gas and about 20% of the circulating flue gas and then undergoes oxygen-rich combustion in the burner, and the oxygen content in the furnace chamber of the heating furnace is controlled at about 3% by adjusting the flow rate of the combustion-supporting oxygen. The amount of flue gas generated by combustion is about 25 Nm 3 / h.

[0053] Propane as a raw material enters the heating furnace at a flow rate of 112.5 kg / h, and after being heated to a reaction temperature of 600°C to 650°C, it enters the cracking reactor which includes 4 moving bed reactors in series. The inlet pressure of the cracking reactor is set to 0.23 MPaG, and the outlet pressure of the reactor is set to 3.5 kPaG. Under the above conditions, the raw gas undergoes a cracking reaction in the presence of a Pt / Al2O3 catalyst to produce propylene and hydrogen, and then propylene is obtained after cooling, separation and purification. The yield of propylene is about 88%.

[0054] After the above-mentioned cracking reaction, the tail gas from the cracking reactor containing about 92.5% by volume of hydrogen is introduced into the UOP Polybed TMPressure Swing Adsorption. The device mainly consists of an adsorption column filled with UOP H102 adsorbent and related valve set and controller. At room temperature, the tail gas is first pressurized to 2.5 MPaG, then passed through the pressure swing adsorption device to produce hydrogen gas with purity >99.9% and hydrogen recovery of about 91%.

[0055] The high temperature flue gas of the combustion products from the oxygen enriched combustion is further flowed from the heater to the heat exchanger to remove water vapor and cool the combustion products to room temperature and obtain a mixed gas containing >95 vol% of CO2 and balance of impurities based on the total volume of the cooled gas. The flow of oxygen and CO2 in the mixed gas flowed through the heat exchanger is adjusted so that the mixed gas contains only about 5 vol% to 20 vol% of oxygen based on the total volume of the mixed gas and the mixed gas is sent back to the combustor to reduce the oxygen concentration in the mixed gas in the combustor and the heater to suppress the combustion temperature from being too high and to minimize the formation of nitrogen oxides (a small amount of N2 is inevitably present in the heater due to air leakage). The remaining portion of CO2 is pressurized to 3.5 MPaG and introduced to a CO2 purification device to remove impurities such as SO2 and the like to increase the purity of CO2 to >99%.

[0056] To meet the hydrogen demand for the CO2 hydrogenation reaction, additional hydrogen is provided by the above-mentioned alkaline electrolyzer through water electrolysis reaction. The hydrogen produced is first pressurized to 2.4 MPaG together with the hydrogen from the pressure swing adsorption device and then passed through another hydrogen purification device to further remove impurities. The >99.9% pure hydrogen obtained is introduced into the CO2 hydrogenation reactor at a flow rate of 3.9 kg / h and mixed with the CO2 from the above-mentioned CO2 purification device in the CO2 hydrogenation reactor. The hydrogenation reactor is filled with Cu-Zn based catalyst and is set at a reaction temperature of 267°C and a pressure of 5.5 MPa, and a gas hourly space velocity (GHSV) of 10000 ml.gcat -1 ·h -1 so that the CO2 and hydrogen mainly undergo hydrogenation reaction on the surface of the catalyst to form methanol.

[0057] After the flashing and rectification steps, a refined methanol product is obtained. In the CO2 hydrogenation reaction, the hydrogen conversion is about 91.5%, the selectivity is about 91.2%, and the methanol yield is about 83.1%.

[0058] After the completion of the CO2 hydrogenation to methanol process, the methanol produced is introduced into a downstream process system. The downstream process system involves a methanol to olefin (MTO) production process system and a methanol to jet fuel (MTJ) production process system, which are existing mature processes.

[0059] Comparative Example 1

[0060] Comparative Example 1 involves a propane dehydrogenation process using conventional air combustion technology. Reference is made to Figure 1 Air (containing about 21% oxygen by volume based on the total volume of air) was introduced into the combustion heating device at a flow rate of about 72 Nm 3 / h. The combustion heating device used was similar to that used in Example 1, and the core part of the combustion heating device used included a propane dehydrogenation heating furnace and a UOP Kellogg CUBL-LFM propane dehydrogenation burner. The furnace was used to heat the feed gas of the propane dehydrogenation process to the required reaction temperature, and the furnace temperature was set to 800°C and the pressure was set to -100 PaG. The fuel gas selected was natural gas, and the flow rate was 6 Nm 3 / h. The oxygen content of the heating furnace hearth was controlled to about 3% by adjusting the flow rate of the combustion air.

[0061] Propane was used as the raw material and passed through the heating furnace at a flow rate of 112.5 kg / h, and after being heated to a reaction temperature of 600°C to 650°C, entered the 4 moving bed reactors in series. The reactor inlet pressure was set to 0.23 MPaG, and the reactor outlet pressure was set to 3.5 kPaG. Under the above conditions, the feed gas underwent a cracking reaction in the presence of a Pt / Al2O3 catalyst to produce propylene and hydrogen, and then after cooling, separation and purification, propylene was obtained. The propylene yield was about 88%.

[0062] The flow rate of the high-temperature flue gas generated after air combustion was 78 Nm 3 / h. Relative to the total volume of the air combustion product, the air combustion product contained about 10% CO2 by volume, about 18% water by volume, about 70% N2 by volume and other small amounts of impurity gases, including <50 ppm of nitrogen oxides.

[0063] Compared with the comparative example using conventional air combustion technology, according to the example of the present application, by using oxygen-enriched combustion technology, the CO2 concentration in the flue gas was significantly increased by about 7 times, and the amount of flue gas after combustion was reduced to about 32% of the comparative example, thereby greatly reducing the difficulty and energy consumption of carbon capture. At the same time, the combustion efficiency according to the example of the present application was not reduced, and the propylene yield of the propane dehydrogenation reaction remained stable and was not affected by the oxygen supply. In addition, according to the example of the present application, the byproduct hydrogen in the olefin cracking process was recovered by pressure swing adsorption technology, with a recovery rate of about 91%, greatly reducing the demand for external hydrogen, further improving resource utilization and reducing environmental impact.

Claims

1. A carbon capture and utilization system for an olefin cracking process, comprising an olefin cracking device, a combustion heat supply device, a heat exchanger, an oxygen supply device and a CO2 pretreatment device in fluid communication, the heat exchanger being provided with a first inlet, a second inlet, a first outlet and a second outlet, the first inlet being in communication with an outlet of the combustion heat supply device, the second inlet being in communication with an oxygen outlet of the oxygen supply device, the first outlet being in communication with a return inlet of the combustion heat supply device, the second outlet being in communication with an inlet of the CO2 pretreatment device, characterized in that, The carbon capture and utilization system comprises: a first hydrogen pretreatment device for separating hydrogen from by-products of the olefin cracking device and increasing hydrogen pressure, an inlet of the first hydrogen pretreatment device being communicated with an outlet of the olefin cracking device; and a CO2 hydrogenation reactor for receiving the pretreated CO2 and hydrogen, the CO2 hydrogenation reactor being provided with a CO2 inlet and a first hydrogen inlet, the CO2 inlet being communicated with an outlet of the CO2 pretreatment device, the first hydrogen inlet being communicated with an outlet of the first hydrogen pretreatment device.

2. The carbon capture and utilization system of claim 1, wherein, The oxygen supply device comprises a water electrolysis device for supplying hydrogen to the CO2 hydrogenation reactor, the water electrolysis device being further provided with a hydrogen outlet and the CO2 hydrogenation reactor being provided with a second hydrogen inlet, the hydrogen outlet of the water electrolysis device being communicated with the second hydrogen inlet of the CO2 hydrogenation reactor through a second hydrogen pretreatment device.

3. The carbon capture and utilization system of claim 2, wherein, Electric energy is supplied to the water electrolysis device using renewable energy.

4. The carbon capture and utilization system of claim 1, wherein, The oxygen supply device comprises an air separation device for receiving air and separating oxygen therefrom.

5. The carbon capture and utilization system of claim 2 or 3, wherein, The oxygen supply device comprises an air separation device for receiving air and separating oxygen therefrom.

6. The carbon capture and utilization system of claim 4, wherein, The air separation device is further provided with a nitrogen outlet, the nitrogen outlet being communicated with an ammonia production system.

7. The carbon capture and utilization system of claim 5, wherein, The air separation device is further provided with a nitrogen outlet, the nitrogen outlet being communicated with an ammonia production system.

8. The carbon capture and utilization system of claim 1, wherein, An outlet of the CO2 hydrogenation reactor is communicated to a CO2 hydrogenation product preparation process system.

9. The carbon capture and utilization system of claim 2 or 3, wherein, An outlet of the CO2 hydrogenation reactor is communicated to a CO2 hydrogenation product preparation process system.

10. The carbon capture and utilization system of claim 4, wherein, An outlet of the CO2 hydrogenation reactor is communicated to a CO2 hydrogenation product preparation process system.

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