Carbon dioxide hydrogenation conversion apparatus and method

Abstract

This invention provides a carbon dioxide hydrogenation conversion apparatus and method, relating to the field of coal chemical technology. The apparatus includes: a first reactor storing a first catalyst, used to separate a portion of the hydrogen from a first mixed gas (hydrogen and carbon dioxide) entering the first reactor to form a second mixed gas, and to utilize the separated hydrogen to react with carbon monoxide under the action of the first catalyst to generate hydrocarbons which are then discharged; a second reactor storing a second catalyst, connected to the first reactor via a pipeline, used to utilize the second mixed gas under the action of the second catalyst to undergo a counter-current water-gas reaction to generate a third mixed gas (carbon monoxide and water vapor), the second reactor being used to separate water vapor and carbon monoxide from the third mixed gas, and the separated carbon monoxide being transported to the first reactor. The carbon dioxide hydrogenation conversion apparatus and method provided by this invention solve the problem of low carbon dioxide hydrogenation conversion efficiency in the prior art.

Description

Technical Field

[0001] This invention relates to the field of coal chemical technology, specifically to a carbon dioxide hydrogenation conversion device and a carbon dioxide hydrogenation conversion method. Background Technology

[0002] Carbon dioxide hydrogenation conversion technology is a key core technology in CCUS (carbon dioxide capture, conversion, and storage). The reaction unit is its key core component. The carbon dioxide hydrogenation reaction can convert carbon dioxide into high-value-added chemicals, thereby achieving the effective utilization of carbon resources.

[0003] In existing carbon dioxide hydrogenation reactors, the structure is mainly based on radial or axial reactors, each with its own advantages and disadvantages. Axial reactors are easy to manufacture, install, and maintain, and have a simple structure and low cost. They can rationally utilize the heat of reaction to meet the required reaction temperature, and have a large pressure drop, making them suitable for hydrogenation processes. They can maintain a high flow rate, which is beneficial for the diffusion of the material to the catalyst surface, thus improving the reaction efficiency. However, they suffer from unstable bed temperature distribution. In radial reactors, the linear velocity and contact time of the gas are constantly changing, and the catalyst performance is not fully utilized. Furthermore, the pressure drop in radial reactors is much smaller than in axial reactors, which is beneficial for meeting the requirements of reforming reactions under low pressure, increasing reaction intensity, and reducing energy consumption. However, due to the different pressure differences, the material distribution in radial reactors is uneven when passing through the upper and lower beds, easily causing short circuits in the material flow and forming catalyst dead zones, thus affecting the catalyst contact efficiency.

[0004] Therefore, there is an urgent need for a device that can solve at least one of the above problems. Summary of the Invention

[0005] The purpose of this invention is to provide a carbon dioxide hydrogenation conversion apparatus and method to solve the problem of low carbon dioxide hydrogenation conversion efficiency in the prior art.

[0006] To achieve the above objectives, the present invention provides a carbon dioxide hydrogenation conversion apparatus, the carbon dioxide hydrogenation conversion apparatus comprising:

[0007] The first reactor stores a first catalyst. The first reactor is used to separate a portion of the hydrogen from a first mixture of hydrogen and carbon dioxide entering the first reactor to form a second mixture. The separated portion of hydrogen reacts with carbon monoxide under the action of the first catalyst to generate hydrocarbons, which are then discharged from the first reactor.

[0008] The second reactor, which stores the second catalyst, is connected to the first reactor via a pipeline. The second reactor uses the second mixed gas to perform a reverse water-gas reaction under the action of the second catalyst to generate a third mixed gas composed of carbon monoxide and water vapor. The second reactor is used to separate the water vapor and carbon monoxide in the third mixed gas, and the separated carbon monoxide is transported to the first reactor.

[0009] Specifically, the carbon dioxide hydrogenation conversion device further includes a temperature controller connected to the second reactor, wherein the temperature controller controls the temperature in the second reactor within a set temperature range by absorbing heat from the third mixed gas.

[0010] Specifically, the temperature controller is configured to store a liquid medium, and the temperature controller absorbs heat from the third mixture by exchanging heat with the third mixture through the liquid medium.

[0011] Specifically, the carbon dioxide hydrogenation conversion device further includes a preheater connected to the first reactor, wherein the preheater utilizes the waste heat of hydrocarbons discharged from the first reactor to preheat the first mixed gas entering the first reactor.

[0012] Specifically, the first reactor further includes a hydrogen separation membrane disposed within the first reactor for separating a portion of the hydrogen from a first mixed gas formed by the mixing of hydrogen and carbon dioxide entering the first reactor.

[0013] Specifically, the second reactor further includes a water-selective permeation membrane disposed within the second reactor for separating water vapor from the third mixed gas.

[0014] Specifically, the carbon dioxide hydrogenation conversion device further includes a nitrogen supply component for supplying nitrogen to the second reactor, thereby increasing the separation rate of water vapor in the third mixed gas by supplying nitrogen to the second reactor.

[0015] Another aspect of the present invention provides a carbon dioxide hydrogenation conversion method, implemented based on the carbon dioxide hydrogenation conversion apparatus described above, the carbon dioxide hydrogenation conversion method comprising:

[0016] S1) Separate a portion of the hydrogen from the first mixture of hydrogen and carbon dioxide to form a second mixture. Use the separated hydrogen to react with carbon monoxide under the action of the first catalyst to generate hydrocarbons.

[0017] S2) The second mixed gas undergoes a reverse water-gas reaction under the action of the second catalyst to generate a third mixed gas composed of carbon monoxide and water vapor. The water vapor and carbon monoxide in the third mixed gas are separated, and the separated carbon monoxide is transported to step S1) to react with a portion of the separated hydrogen under the action of the first catalyst to generate hydrocarbons.

[0018] Specifically, the carbon dioxide hydrogenation conversion method further includes: using a liquid medium to exchange heat with the third mixed gas to absorb the heat of the third mixed gas.

[0019] Specifically, the carbon dioxide hydrogenation conversion method further includes: preheating the first mixed gas using the waste heat of the hydrocarbon.

[0020] The carbon dioxide hydrogenation conversion apparatus provided by this invention first separates a portion of the hydrogen from a first mixed gas (hydrogen and carbon dioxide) in a first reactor. This separated hydrogen then reacts with carbon monoxide entering the first reactor under the action of a first catalyst to produce hydrocarbons, which are then discharged. The first mixed gas, having lost some hydrogen, becomes a second mixed gas and enters a second reactor. Under the action of a second catalyst, the second mixed gas undergoes a counter-current water-gas reaction in the second reactor to produce a third mixed gas (carbon monoxide and water vapor). The second reactor separates the water vapor and carbon monoxide from the third mixed gas, and the separated carbon monoxide is then transported back to the first reactor to react with a portion of the hydrogen. The carbon dioxide hydrogenation conversion apparatus and method provided by this invention control the feedstock ratio for the final hydrocarbon production through the first and second reactors, i.e., precisely metering the hydrogen-to-carbon ratio of the feedstock. This improves the conversion rate of carbon dioxide and the yield of products such as alcohols and hydrocarbons, solving the problem of low carbon dioxide hydrogenation conversion efficiency in existing technologies.

[0021] Other features and advantages of the embodiments of the present invention will be described in detail in the following detailed description section. Attached Figure Description

[0022] The accompanying drawings are provided to further illustrate embodiments of the present invention and form part of the specification. They are used together with the following detailed description to explain the embodiments of the present invention, but do not constitute a limitation thereof. In the drawings:

[0023] Figure 1 This is a schematic diagram of the carbon dioxide hydrogenation conversion device provided by the present invention;

[0024] Figure 2 This is a graph showing the gas phase component temperature versus reactor axial length for the carbon dioxide hydrogenation conversion device provided by this invention and a conventional reactor.

[0025] Figure 3This is a graph showing the CO2 mole fraction versus reactor axial height for the carbon dioxide hydrogenation conversion device provided by this invention and a conventional reactor.

[0026] Explanation of reference numerals in the attached figures

[0027] 1-First reactor; 2-Second reactor; 3-Temperature controller; 4-Preheater; 11-Hydrogen separation membrane; 21-Water selective permeation membrane; 31-Inlet section; 32-Return section. Detailed Implementation

[0028] The specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit the scope of the present invention.

[0029] like Figures 1-3 As shown, the present invention provides a carbon dioxide hydrogenation conversion apparatus, the carbon dioxide hydrogenation conversion apparatus comprising:

[0030] The first reactor 1 stores a first catalyst. The first reactor 1 is used to separate a portion of the hydrogen from a first mixture of hydrogen and carbon dioxide that enters the first reactor 1 to form a second mixture. The separated portion of hydrogen reacts with carbon monoxide under the action of the first catalyst to generate hydrocarbons which are discharged from the first reactor 1.

[0031] The second reactor 2 stores the second catalyst and is connected to the first reactor 1 through a pipeline. The second reactor 2 uses the second mixed gas to carry out a counter-current water gas reaction under the action of the second catalyst to generate a third mixed gas composed of carbon monoxide and water vapor. The second reactor 2 is used to separate the water vapor and carbon monoxide in the third mixed gas, and the separated carbon monoxide is transported to the first reactor 1.

[0032] The carbon dioxide hydrogenation conversion apparatus provided by this invention uses a first mixed gas of hydrogen and carbon dioxide as feed gas, which enters the first reactor 1 from the top. A portion of the hydrogen in the first mixed gas is separated in the first reactor 1. This separated hydrogen reacts with carbon monoxide entering from the bottom of the first reactor 1 under the action of a first catalyst to generate hydrocarbons. The generated hydrocarbons are discharged from the first reactor 1. The first mixed gas, having lost some hydrogen, becomes a second mixed gas and enters the second reactor 2. Under the action of a second catalyst, the second mixed gas undergoes a counter-current water-gas reaction in the second reactor 2 to generate a third mixed gas of carbon monoxide and water vapor. The water vapor and carbon monoxide in the third mixed gas are separated in the second reactor 2. The separated carbon monoxide is transported back to the first reactor 1 to react with a portion of the hydrogen. Thus, by controlling the amount of hydrogen participating in the hydrocarbon generation reaction in the first reactor 1 and controlling the amount of carbon monoxide participating in the hydrocarbon generation reaction in the second reactor 2, the conversion rate of carbon dioxide and the yield of products such as alcohols and hydrocarbons are improved, solving the problem of low carbon dioxide hydrogenation conversion efficiency in existing technologies.

[0033] In order to provide a suitable reaction temperature for the second mixed gas in the second reactor 2, the carbon dioxide hydrogenation conversion device further includes a temperature controller 3 connected to the second reactor 2. The temperature controller 3 controls the temperature in the second reactor 2 within a set temperature range by absorbing the heat of the third mixed gas.

[0034] The temperature controller 3 is configured to store a liquid medium, and the temperature controller 3 absorbs heat from the third mixture by exchanging heat with the third mixture through the liquid medium.

[0035] The second mixed gas enters the second reactor 2 and undergoes a counter-current gas-water reaction under the action of the second catalyst to produce a third mixed gas of carbon monoxide and water vapor. This conversion reaction is exothermic; therefore, the temperature inside the second reactor 2 will rise after the counter-current gas-water reaction. To avoid the temperature inside the second reactor 2 becoming too high and affecting the reaction effect, as follows... Figure 1As shown, a temperature controller 3 is installed, which is a steam drum. The liquid medium is saturated water. The temperature controller 3 is connected to the second reactor 2 through a control pipe. The control pipe includes an inlet section 31, a return section 32, and a heat exchange section located inside the second reactor 2. The inlet section 31 and the return section 32 are exposed outside the second reactor 2, while the heat exchange section is located inside the second reactor 2. After the liquid medium in the temperature controller 3 flows through the inlet section 31, it enters the heat exchange section to exchange heat with the third mixed gas to remove the heat of the third mixed gas, thereby reducing the temperature inside the second reactor 2 and preventing the temperature from becoming too high due to the reverse water-gas reaction inside the second reactor 2. After the liquid medium exchanges heat with the third mixed gas, it vaporizes into water vapor. The water vapor returns to the temperature controller 3 through the return section 32. In this way, not only can the temperature inside the second reactor 2 be controlled to remain within the set temperature range, but the heat inside the second reactor 2 can also be recovered through the temperature controller 3, avoiding energy waste.

[0036] like Figure 1 As shown, some hydrogen and carbon monoxide react in the first reactor 1 under the action of a first catalyst to produce hydrocarbons. Since the hydrocarbons are at a high temperature, to fully utilize the waste heat from the hydrocarbons, the carbon dioxide hydrogenation conversion device further includes a preheater 4 connected to the first reactor 1. The preheater 4 utilizes the waste heat from the hydrocarbons discharged from the first reactor 1 to preheat the first mixed gas entering the first reactor 1. After being discharged from the first reactor 1, the hydrocarbons flow through the preheater 4. The first mixed gas entering the first reactor 1 also flows through the preheater 4, allowing the first mixed gas and hydrocarbons to exchange heat within the preheater 4 to absorb the waste heat from the hydrocarbons. This not only increases the temperature of the first mixed gas, thereby improving the efficiency of subsequent reactions, but also fully utilizes the waste heat from the hydrocarbons, avoiding energy waste.

[0037] To separate a portion of the hydrogen from the first mixed gas, the first reactor 1 further includes a hydrogen separation membrane 11, disposed within the first reactor 1, for separating a portion of the hydrogen from the first mixed gas formed by the mixture of hydrogen and carbon dioxide entering the first reactor 1. Figure 1 As shown, a hydrogen separation membrane 11 is installed in the first reactor 1, which is a fluidized bed. The first catalyst is disposed between the hydrogen separation membrane 11 and the inner wall of the first reactor 11. When the first mixed gas flows from the top to the bottom of the first reactor 1, the hydrogen separation membrane 11 separates some of the hydrogen in the first mixed gas. In order to improve the reaction efficiency of generating hydrocarbons, a carbon monoxide inlet is provided at the bottom of the first reactor 1. The carbon monoxide inlet is located between the hydrogen separation membrane 11 and the inner wall of the first reactor 1, so that carbon monoxide enters the first reactor 1 directly through the carbon monoxide inlet and immediately comes into contact with the first catalyst. Under the action of the first catalyst, it reacts with carbon monoxide and some hydrogen.

[0038] To separate carbon monoxide from the third gas mixture, the second reactor 2 further includes a water-selective permeation membrane 21, disposed within the second reactor 2, for separating water vapor from the third gas mixture. Figure 1 As shown, the second reactor 2 is a fixed bed, and the second catalyst is placed between the water selective permeation membrane 21 and the inner wall of the second reactor 2. The water selective permeation membrane 21 separates carbon monoxide and water vapor in the third mixed gas.

[0039] To accelerate the reaction process within the second reactor 2, the carbon dioxide hydrogenation conversion device further includes a nitrogen supply component for supplying nitrogen to the second reactor 2, thereby accelerating the separation of water vapor in the third mixed gas. The second mixed gas enters the second reactor 2 from the top, and the nitrogen supply component similarly supplies nitrogen from the top of the second reactor 2. The nitrogen supplied to the second reactor 2 agitates the movement of the second mixed gas within the reactor 2, thus accelerating the reaction process. Simultaneously, it also agitates the movement of the generated third mixed gas within the reactor 2, accelerating the separation speed of the water-selective permeation membrane 21. After the temperature controller 3 maintains the temperature in the second reactor 2 within a set temperature range, a portion of the separated water vapor liquefies into liquid water. Nitrogen enters from the top of the second reactor 2 and exits from the bottom. As the nitrogen exits from the bottom of the second reactor 2, it carries the separated water vapor and the liquefied liquid water out together from the bottom of the second reactor 2.

[0040] In one embodiment, such as Figure 1As shown, a raw material gas inlet is provided at the top of the first reactor 1, and the raw material gas inlet is connected to a raw material gas supply device via an inlet pipe. The raw material supply device consists of a carbon dioxide supply device and a hydrogen supply device. A mixed gas outlet and a carbon monoxide inlet are provided at the bottom of the first reactor 1. A mixed gas inlet and a nitrogen inlet are provided at the top of the second reactor 2, and a carbon monoxide outlet and a nitrogen outlet are provided at the bottom of the second reactor 2. The mixed gas outlet of the first reactor 1 and the mixed gas inlet of the second reactor 2 are connected by an intermediate pipe. A nitrogen supply component is connected to a nitrogen inlet via a nitrogen pipe. The carbon monoxide outlet of the second reactor 2 is connected to the carbon monoxide inlet of the first reactor 1 via a carbon monoxide delivery pipe. A first mixed gas, composed of hydrogen and carbon dioxide, enters the first reactor 1 as raw material gas through the inlet pipe. After the first reactor 1 separates some hydrogen from the first mixed gas, the first mixed gas loses some hydrogen and becomes a second mixed gas. The second mixed gas flows out from the mixed gas outlet of the first reactor 1 and then passes through an intermediate pipe. The mixed gas enters the second reactor 2 through a pipeline and a mixed gas inlet. The second mixed gas undergoes a counter-current reaction with water gas in the second reactor 2 to generate a third mixed gas. Carbon monoxide is separated from the third mixed gas and discharged from the carbon monoxide outlet at the bottom of the second reactor 2. It then enters the first reactor 1 through a carbon monoxide conveying pipeline and a carbon monoxide inlet. During the downward flow of the first mixed gas from the top of the first reactor 1, some hydrogen is separated, and the first mixed gas becomes the second mixed gas. The second mixed gas moves towards the bottom of the first reactor 1 and is eventually discharged from the mixed gas outlet. Carbon monoxide flows upward from the bottom of the first reactor 1. The second mixed gas and carbon monoxide flow in a counter-current mode. The heat generated by the reaction of some hydrogen and carbon monoxide under the action of the first catalyst is carried away by the second mixed gas and enters the second reactor 2. A temperature controller 3 is connected to the second reactor 2 to control the temperature inside the second reactor 2, maintaining it within a suitable set temperature range to ensure the smooth progress of the reaction within the second reactor 2.

[0041] Another aspect of the present invention provides a carbon dioxide hydrogenation conversion method, implemented based on the carbon dioxide hydrogenation conversion apparatus described above, the carbon dioxide hydrogenation conversion method comprising:

[0042] S1) Separate a portion of the hydrogen from the first mixture of hydrogen and carbon dioxide to form a second mixture. Use the separated hydrogen to react with carbon monoxide under the action of the first catalyst to generate hydrocarbons.

[0043] S2) The second mixed gas undergoes a reverse water-gas reaction under the action of the second catalyst to generate a third mixed gas composed of carbon monoxide and water vapor. The water vapor and carbon monoxide in the third mixed gas are separated, and the separated carbon monoxide is transported to step S1) to react with a portion of the separated hydrogen under the action of the first catalyst to generate hydrocarbons.

[0044] The carbon dioxide hydrogenation conversion method further includes: using a liquid medium to exchange heat with the third mixed gas to absorb the heat of the third mixed gas.

[0045] The carbon dioxide hydrogenation conversion method further includes: preheating the first mixed gas using the waste heat of the hydrocarbon.

[0046] The carbon dioxide hydrogenation conversion method provided by this invention separates a portion of the hydrogen from a first mixture of hydrogen and carbon dioxide. The first mixture, having lost some hydrogen, becomes a second mixture. Under the action of a second catalyst, the second mixture undergoes a counter-current water gas reaction to produce a third mixture. The third mixture includes carbon monoxide and water vapor. The carbon monoxide separated from the third mixture reacts with a portion of the hydrogen under the action of the first catalyst to generate hydrocarbons, which are then discharged. To ensure that the second mixture can undergo the counter-current water gas reaction within a suitable temperature range, a liquid medium exchanges heat with the third mixture generated by the counter-current water gas reaction to absorb the temperature of the third mixture, thereby controlling the reaction temperature of the second mixture. To improve energy utilization, the hydrocarbons exchange heat with the first mixture to preheat it, thereby improving the efficiency of subsequent reactions.

[0047] The carbon dioxide hydrogenation conversion apparatus provided by this invention first separates a portion of the hydrogen from a first mixed gas (hydrogen and carbon dioxide) in a first reactor. This separated hydrogen then reacts with carbon monoxide entering the first reactor under the action of a first catalyst to produce hydrocarbons, which are then discharged. The first mixed gas, having lost some hydrogen, becomes a second mixed gas and enters a second reactor. Under the action of a second catalyst, the second mixed gas undergoes a counter-current water-gas reaction in the second reactor to produce a third mixed gas (carbon monoxide and water vapor). The second reactor separates the water vapor and carbon monoxide from the third mixed gas, and the separated carbon monoxide is then transported back to the first reactor to react with a portion of the hydrogen. The carbon dioxide hydrogenation conversion apparatus and method provided by this invention control the feedstock ratio for the final hydrocarbon production through the first and second reactors, i.e., precisely metering the hydrogen-to-carbon ratio of the feedstock. This improves the conversion rate of carbon dioxide and the yield of products such as alcohols and hydrocarbons, solving the problem of low carbon dioxide hydrogenation conversion efficiency in existing technologies.

[0048] The optional embodiments of the present invention have been described in detail above with reference to the accompanying drawings. However, the embodiments of the present invention are not limited to the specific details in the above embodiments. Within the scope of the technical concept of the embodiments of the present invention, various simple modifications can be made to the technical solutions of the embodiments of the present invention, and these simple modifications all fall within the protection scope of the embodiments of the present invention.

[0049] It should also be noted that the various specific technical features described in the above embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the embodiments of the present invention will not describe the various possible combinations separately.

[0050] Furthermore, various different implementations of the present invention can be combined arbitrarily, as long as they do not violate the spirit of the present invention, they should also be regarded as the content disclosed in the present invention.

Claims

1. A carbon dioxide hydroconversion apparatus, characterized by, The carbon dioxide hydrogenation conversion unit includes: The first reactor (1) stores a first catalyst. The first reactor (1) is used to separate a portion of the hydrogen in the first mixed gas formed by the mixture of hydrogen and carbon dioxide entering the first reactor (1) to form a second mixed gas. The separated portion of hydrogen reacts with carbon monoxide under the action of the first catalyst to generate hydrocarbons, which are discharged from the first reactor (1). The first reactor (1) also includes a hydrogen separation membrane (11) disposed in the first reactor (1) for separating a portion of the hydrogen in the first mixed gas formed by the mixture of hydrogen and carbon dioxide entering the first reactor (1). The second reactor (2) stores a second catalyst and is connected to the first reactor (1) through a pipeline. The second reactor (2) uses the second mixed gas to perform a reverse water-gas reaction under the action of the second catalyst to generate a third mixed gas composed of carbon monoxide and water vapor. The second reactor (2) is used to separate water vapor and carbon monoxide in the third mixed gas. The separated carbon monoxide is transported to the first reactor (1). The second reactor (2) also includes a water selective permeation membrane (21) which is installed in the second reactor (2) and is used to separate water vapor in the third mixed gas. The carbon dioxide hydrogenation conversion device further includes a temperature controller (3), which is connected to the second reactor (2). The temperature controller (3) controls the temperature in the second reactor (2) within a set temperature range by absorbing the heat of the third mixed gas. The carbon dioxide hydrogenation conversion device further includes a nitrogen supply component for supplying nitrogen to the second reactor (2) to increase the separation rate of water vapor in the third mixed gas by supplying nitrogen to the second reactor (2).

2. The carbon dioxide hydroconversion apparatus of claim 1, wherein, The temperature controller (3) is configured to store a liquid medium, and the temperature controller (3) absorbs heat from the third mixture by exchanging heat with the third mixture through the liquid medium.

3. The carbon dioxide hydroconversion apparatus of claim 1, wherein, The carbon dioxide hydrogenation conversion device further includes a preheater (4) connected to the first reactor (1), wherein the preheater (4) uses the residual heat of the hydrocarbons discharged from the first reactor (1) to preheat the first mixed gas entering the first reactor (1).

4. A method for carbon dioxide hydrogenation conversion, implemented based on the carbon dioxide hydrogenation conversion apparatus according to any one of claims 1-3, characterized in that, The carbon dioxide hydrogenation conversion method includes: S1) Separate a portion of the hydrogen from the first mixture of hydrogen and carbon dioxide to form a second mixture. Use the separated hydrogen to react with carbon monoxide under the action of the first catalyst to generate hydrocarbons. S2) The second mixed gas undergoes a reverse water-gas reaction under the action of the second catalyst to generate a third mixed gas composed of carbon monoxide and water vapor. The water vapor and carbon monoxide in the third mixed gas are separated, and the separated carbon monoxide is transported to step S1) to react with a portion of the separated hydrogen under the action of the first catalyst to generate hydrocarbons.

5. The carbon dioxide hydrogenation conversion method according to claim 4, characterized in that, The carbon dioxide hydrogenation conversion method further includes: using a liquid medium to exchange heat with the third mixed gas to absorb the heat of the third mixed gas.

6. The carbon dioxide hydrogenation conversion method according to claim 4, characterized in that, The carbon dioxide hydrogenation conversion method further includes: preheating the first mixed gas using the waste heat of the hydrocarbon.

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