Production device of liquid carbon dioxide and production method of carbon dioxide

Abstract

The invention provides a production device of liquid carbon dioxide and a production method of the liquid carbon dioxide. The production device of the liquid carbon dioxide comprises desulfurization process equipment, dealkylation process equipment, purification process equipment, liquefaction purification equipment and compression process equipment, the compression process equipment comprises a first compression assembly, a second compression assembly, a third compression assembly and a fourth compression assembly; the desulfurization process equipment comprises a raw material gas inlet pipeline, a deep freezer and a desulfurization tower, the two ends of the first compression assembly are communicated with the raw material gas inlet pipeline and the deep freezer, and the desulfurization tower is communicated with the deep freezer; two ends of the second compression assembly are communicated with the desulfurization tower and dealkylation process equipment; two ends of the third compression assembly are communicated with the dealkylation process equipment and the purification process equipment; two ends of the fourth compression assembly are communicated with the purification process equipment and the liquefaction purification equipment. The compression procedure is matched with the working conditions of the desulfurization procedure, the dealkylation procedure, the purification procedure and the liquefaction and purification procedure, so that the impurity removal efficiency and the liquefaction efficiency of carbon dioxide production are improved.

Description

Technical Field

[0001] The present disclosure relates to the technical field of carbon dioxide production, and particularly to a production device for liquid carbon dioxide and a production method thereof for carbon dioxide. Background Art

[0002] Liquid carbon dioxide is produced through a desulfurization process, a dehydrocarbonization process, a purification process, and a liquefaction and purification process to obtain liquid carbon dioxide. The temperature of the carbon dioxide feed gas entering the desulfurization process is at room temperature, and the pressure is 10 Kpa - 100 Kpa. During the production process of liquid carbon dioxide, the pressure of the carbon dioxide feed gas is first increased to 0.9 MPa - 1.2 MPa through a compression process, and then successively introduced into the desulfurization process, the dehydrocarbonization process, and the purification process. Then, the purified carbon dioxide gas is compressed to 2.8 Mpa - 3.3 MPa through a compression process and then sent to the liquefaction process and the distillation and purification process.

[0003] In the carbon dioxide desulfurization process, when the temperature of the carbon dioxide feed gas entering the desulfurization tower is relatively high and the pressure is too high, the adsorption capacity of the adsorbent in the desulfurization tower is relatively small, which is not conducive to the adsorption of the desulfurization adsorbent; the change in pressure will change the specific surface area and structure of the catalyst. The pressure of the carbon dioxide feed gas entering the dehydrocarbonization process is relatively high, resulting in a relatively low activity of the dehydrocarbonization catalyst, thus affecting the efficiency of the carbon dioxide gas in the dehydrocarbonization process.

[0004] For example, a method for reducing carbon dioxide emissions in the production of a food-grade liquid carbon dioxide product disclosed in the comparative document CN201210583434.X includes the following steps: a denitrification process; a first compression process; a desulfurization process; a dehydrocarbonization process; a purification process; a second compression process; a liquefaction process; a distillation and purification process. By adopting this method, the carbon dioxide emissions can be greatly reduced. However, in this solution, after passing through the compression process, the temperature of the carbon dioxide feed gas entering the desulfurization tower is relatively high and the pressure is too high, which is not conducive to the adsorption of the desulfurization adsorbent. The pressure of the carbon dioxide feed gas entering the dehydrocarbonization process is relatively high, resulting in a relatively low activity of the catalyst in the dehydrocarbonization process, thus affecting the efficiency of liquid carbon dioxide production. Summary of the Invention

[0005] The purpose of the present disclosure is to overcome the deficiencies in the prior art and provide a production device for liquid carbon dioxide and a production method thereof for carbon dioxide that improve the efficiency of removing impurities and the liquefaction efficiency through a four-stage compression process to match the working conditions.

[0006] The purpose of the present disclosure is achieved through the following technical solutions:

[0007] A production device for liquid carbon dioxide includes a desulfurization process device, a dehydrocarbonization process device, a purification process device, a liquefaction and purification device, and a compression process device;

[0008] The equipment for the compression process includes a first compression assembly, a second compression assembly, a third compression assembly, and a fourth compression assembly;

[0009] The equipment for the desulfurization process includes a raw material inlet pipeline, a cryogenic cooler, and a desulfurization tower. The raw material inlet pipeline is connected to the inlet end of the first compression assembly, the inlet end of the cryogenic cooler is connected to the outlet end of the first compression assembly, and the desulfurization tower is connected to the outlet end of the cryogenic cooler;

[0010] The inlet end of the second compression assembly is connected to the outlet end of the desulfurization tower, and the inlet end of the dehydrocarbonization process equipment is connected to the outlet end of the second compression assembly; the inlet end of the third compression assembly is connected to the outlet end of the dehydrocarbonization process equipment, the outlet end of the third compression assembly is connected to the inlet end of the purification process equipment, and the purification process equipment is connected to the outlet end of the third compression assembly; the inlet end of the fourth compression assembly is connected to the outlet end of the purification process equipment, the inlet end of the liquefaction and purification equipment is connected to the purification process equipment, and the outlet end of the liquefaction and purification equipment is used to connect to a storage tank.

[0011] In one embodiment, the equipment for the desulfurization process further includes a first normal-temperature cooler. One end of the first normal-temperature cooler is connected to the outlet end of the first compression assembly, and the other end of the first normal-temperature cooler is connected to the inlet end of the cryogenic cooler.

[0012] In one embodiment, the equipment for the dehydrocarbonization process includes a dehydrocarbonization heat exchanger, a dehydrocarbonization heater, and a dehydrocarbonization reactor. The inlet end of the dehydrocarbonization heat exchanger is connected to the outlet end of the second compression assembly, the dehydrocarbonization heat exchanger, the dehydrocarbonization heater, and the dehydrocarbonization reactor are connected in sequence, and the outlet end of the dehydrocarbonization reactor is further connected to the inlet end of the third compression assembly.

[0013] In one embodiment, the equipment for the dehydrocarbonization process further includes a second normal-temperature cooler. One end of the second normal-temperature cooler is connected to the outlet end of the second compression assembly, and the other end of the second normal-temperature cooler is connected to the inlet end of the dehydrocarbonization heat exchanger.

[0014] In one embodiment, the equipment for the purification process includes a purification tower, a regeneration preheater, and a purification heat exchanger. The inlet end of the purification tower is connected to the outlet end of the third compression assembly, the regeneration preheater is connected to the purification tower, the regeneration preheater is used to backflush and regenerate the purification tower, the purification heat exchanger is connected to the regeneration preheater, and the outlet end of the purification tower is connected to the inlet end of the fourth compression assembly.

[0015] In one embodiment, the purification process equipment further includes a third normal-temperature cooler. One end of the third normal-temperature cooler is connected to the gas outlet end of the third compression assembly, and the other end of the third normal-temperature cooler is connected to the gas inlet end of the purification tower.

[0016] In one embodiment, the liquefaction and purification equipment includes a liquid nitrogen freezing pipe, an evaporation condenser, and a purification tower. The liquid nitrogen freezing pipe is connected to the cooling channel opened in the evaporation condenser. The evaporation condenser is connected to the gas outlet end of the fourth compression assembly. The liquid inlet end of the purification tower is connected to the gas outlet end of the evaporation condenser, and the liquid outlet end of the purification tower is used to connect to a storage tank.

[0017] In one embodiment, the liquefaction and purification equipment further includes a fourth normal-temperature cooler. One end of the fourth normal-temperature cooler is connected to the gas outlet end of the fourth compression assembly, and the other end of the fourth normal-temperature cooler is connected to the gas inlet end of the evaporation condenser.

[0018] A method for producing carbon dioxide, which is produced by using the production device of liquid carbon dioxide described in any one of the above embodiments, includes the following steps:

[0019] Introduce the carbon dioxide raw material gas into the first compression assembly for the first compression, introduce the carbon dioxide gas after the first compression into the deep cooler for deep cooling, and then introduce the deep-cooled carbon dioxide gas into the desulfurization tower for desulfurization;

[0020] Introduce the carbon dioxide gas after desulfurization in the desulfurization tower into the second compression assembly for the second compression, and introduce the desulfurized carbon dioxide gas after the second compression into the dehydrocarbonization process equipment for dehydrocarbonization;

[0021] Introduce the carbon dioxide gas after dehydrocarbonization in the dehydrocarbonization process equipment into the third compression assembly for the third compression, and introduce the carbon dioxide gas after the third compression into the purification process equipment for adsorption purification;

[0022] Introduce the carbon dioxide gas purified by the purification process equipment into the fourth compression assembly for the fourth compression, and introduce the carbon dioxide gas after the fourth compression into the liquefaction and purification equipment for liquefaction and purification;

[0023] Introduce the liquefied and purified carbon dioxide into a storage tank for storage.

[0024] In one embodiment, the pressure of the carbon dioxide gas in the first compression is 0.3 Mpa - 0.4 Mpa; the pressure of the carbon dioxide gas in the second compression is 0.7 Mpa - 0.8 Mpa; the pressure of the carbon dioxide gas in the third compression is 1.4 Mpa - 1.5 Mpa; the pressure of the carbon dioxide gas in the fourth compression is 2.3 Mpa - 2.4 Mpa.

[0025] Compared with the prior art, the present disclosure has at least the following advantages:

[0026] For the above liquid carbon dioxide production device and carbon dioxide production method, the carbon dioxide raw gas is cooled by a cryogenic cooler, so that the temperature of the carbon dioxide raw gas entering the desulfurization tower is reduced, thereby increasing the adsorption amount of the adsorbent in the desulfurization tower for the carbon dioxide raw gas; the pressure of the desulfurized carbon dioxide gas entering the dehydrocarbonization process equipment is relatively low, so that the catalyst activity of the dehydrocarbonization process equipment is relatively high, thereby improving the efficiency of removing hydrocarbon gas impurities from the carbon dioxide gas; the carbon dioxide gas after dehydrocarbonization enters the purification process equipment after being pressurized, so that the efficiency of the purification process equipment for adsorbing moisture and oxygen-containing organic matter impurities is improved; the carbon dioxide gas after purification enters the liquefaction and purification equipment after being pressurized again, so that the liquefaction efficiency of the liquefaction and purification equipment is improved;

[0027] By adapting the first compression component, the second compression component, the third compression component and the fourth compression component of the compression process to the working conditions of the desulfurization process, the dehydrocarbonization process, the purification process and the liquefaction and purification process, the efficiency of removing impurities in the production of liquefied carbon dioxide gas is improved, and the liquefaction efficiency of carbon dioxide is increased, thereby improving the production efficiency and quality of liquefied carbon dioxide gas.

[0028] By independently controlling the corresponding desulfurization process, dehydrocarbonization process, purification process and liquefaction and purification process among the first compression component, the second compression component, the third compression component and the fourth compression component, the interference between each process is reduced, and the stability and sustainability of carbon dioxide liquefaction production are improved. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] In order to more clearly illustrate the technical solutions of the embodiments of the present disclosure, the following will briefly introduce the drawings required to be used in the embodiments. It should be understood that the following drawings only show some embodiments of the present disclosure, and therefore should not be regarded as limiting the scope. For those of ordinary skill in the art, other related drawings can be obtained based on these drawings without creative efforts.

[0030] Figure 1 It is a schematic structural diagram of a liquid carbon dioxide production device according to an embodiment;

[0031] Figure 2 For Figure 1Schematic structural diagram of the desulfurization process equipment shown;

[0032] Figure 3 is Figure 1 Schematic structural diagram of the dehydrocarbonization process equipment shown;

[0033] Figure 4 is Figure 1 Schematic structural diagram of the purification process equipment shown;

[0034] Figure 5 is Figure 1 Schematic structural diagram of the liquefaction and purification equipment shown;

[0035] Figure 6 is a step flowchart of a production method of carbon dioxide according to an embodiment. Detailed implementation manners

[0036] To facilitate the understanding of the present disclosure, the present disclosure will be described more comprehensively below with reference to the relevant drawings. Preferred embodiments of the present disclosure are shown in the drawings. However, the present disclosure can be implemented in many different forms and is not limited to the embodiments described herein. On the contrary, these embodiments are provided to make the understanding of the disclosure content of the present disclosure more thorough and comprehensive.

[0037] It should be noted that when an element is referred to as being "fixed to" another element, it can be directly on the other element or there may also be an intermediate element. When an element is considered to be "connected" to another element, it can be directly connected to the other element or there may be an intermediate element at the same time. The terms "vertical", "horizontal", "left", "right" and similar expressions used herein are for illustrative purposes only and do not represent the only embodiments.

[0038] Unless otherwise defined, all technical and scientific terms used herein have the same meaning as commonly understood by those of ordinary skill in the technical field to which the present disclosure belongs. The terms used herein in the specification of the present disclosure are only for the purpose of describing specific embodiments and are not intended to limit the present disclosure. The term "and / or" used herein includes any and all combinations of one or more of the related listed items.

[0039] To better understand the technical solutions and beneficial effects of the present disclosure, the present disclosure will be further described in detail below with reference to specific embodiments:

[0040] As Figures 1 to 5 shown, a production device 10 for liquid carbon dioxide according to an embodiment of the present disclosure includes a desulfurization process equipment 100, a dehydrocarbonization process equipment 200, a purification process equipment 300, a liquefaction and purification equipment 400, and a compression process equipment 500;

[0041] The equipment 500 for the compression process includes a first compression component 510, a second compression component 520, a third compression component 530, and a fourth compression component 540;

[0042] The equipment 100 for the desulfurization process includes a raw material inlet pipeline 110, a cryogenic cooler 120, and a desulfurization tower 130. The raw material inlet pipeline 110 is connected to the inlet end of the first compression component 510. The inlet end of the cryogenic cooler 120 is connected to the outlet end of the first compression component 510. The desulfurization tower 130 is connected to the outlet end of the cryogenic cooler 120. The inlet end of the second compression component 520 is connected to the outlet end of the desulfurization tower 130. The inlet end of the dehydrocarbonization process equipment 200 is connected to the outlet end of the second compression component 520. The inlet end of the third compression component 530 is connected to the outlet end of the dehydrocarbonization process equipment 200. The outlet end of the third compression component 530 is connected to the inlet end of the purification process equipment 300. The purification process equipment 300 is connected to the outlet end of the third compression component 530. The inlet end of the fourth compression component 540 is connected to the outlet end of the purification process equipment 300. The inlet end of the liquefaction and purification equipment 400 is connected to the purification process equipment 300. The outlet end of the liquefaction and purification equipment 400 is used to connect to a storage tank.

[0043] In this embodiment, the carbon dioxide raw material gas first enters the first compression component 510 through the raw material inlet pipeline 110 for compression and pressure increase. The pressure of the carbon dioxide raw material gas after the first pressure increase is about 0.4 MPa. The pressurized carbon dioxide raw material gas enters the cryogenic cooler 120 for cooling. Chilled water is introduced into the cryogenic cooler 120. The temperature of the carbon dioxide raw material gas rapidly drops below 10°C after passing through the cryogenic cooler. The pressurized and low-temperature carbon dioxide raw material gas enters the desulfurization tower 130 for the desulfurization process. The desulfurized carbon dioxide gas enters the second compression component 520 for the second pressure increase. The pressure after the second pressure increase is about 0.8 Mpa. The pressurized and desulfurized carbon dioxide gas enters the dehydrocarbonization equipment. The hydrocarbon gas in the desulfurized carbon dioxide gas reacts with oxygen in the catalyst of the dehydrocarbonization process equipment 200 for the dehydrocarbonization process. The dehydrocarbonized carbon dioxide gas enters the third compression component 530 for the third pressure increase. The pressure after the third pressure increase is about 1.5 Mpa. The pressurized and dehydrocarbonized carbon dioxide gas enters the purification equipment for purification to remove moisture and oxygen-containing organic compounds in the raw material gas. The purified carbon dioxide gas enters the fourth compression component 540 for pressure increase. The pressure after the fourth pressure increase is about 2.4 Mpa. The pressurized and purified carbon dioxide gas enters the liquefaction and purification equipment 400 for liquefaction. The liquefied carbon dioxide liquid is sent into the storage tank.

[0044] The above-mentioned liquid carbon dioxide production device 10 cools the carbon dioxide raw gas through the cryogenic cooler 120, reducing the temperature of the carbon dioxide raw gas entering the desulfurization tower 130, thereby increasing the adsorption capacity of the adsorbent in the desulfurization tower 130 for the carbon dioxide raw gas; the pressure of the desulfurized carbon dioxide gas entering the dehydrocarbonization process equipment 200 is relatively low, making the catalyst activity of the dehydrocarbonization process equipment 200 relatively high, thus improving the efficiency of removing hydrocarbon gas impurities from the carbon dioxide gas; the carbon dioxide gas after dehydrocarbonization is pressurized and then enters the purification process equipment 300, increasing the efficiency of the purification process equipment 300 in adsorbing moisture and oxygen-containing organic compound impurities; the carbon dioxide gas after purification is pressurized again and then enters the liquefaction and purification equipment 400, increasing the liquefaction efficiency of the liquefaction and purification equipment 400; the first compression component 510, the second compression component 520, the third compression component 530, and the fourth compression component 540 in the compression process are adapted to the working conditions of the desulfurization process, the dehydrocarbonization process, the purification process, and the liquefaction and purification process, improving the efficiency of removing impurities in the production of liquefied carbon dioxide gas and increasing the efficiency of carbon dioxide liquefaction, thereby improving the production efficiency and quality of liquefied carbon dioxide gas.

[0045] As Figure 2 shown, in one embodiment, the desulfurization process equipment 100 further includes a first normal-temperature cooler 140. One end of the first normal-temperature cooler 140 is connected to the outlet end of the first compression component 510, and the other end of the first normal-temperature cooler 140 is connected to the inlet end of the cryogenic cooler 120. In this embodiment, the temperature of the carbon dioxide raw gas is relatively high. When the carbon dioxide raw gas passes through the first normal-temperature cooler 140, the first normal-temperature cooler 140 reduces the temperature of the carbon dioxide raw gas through heat exchange, reducing the cooling difficulty of the cryogenic cooler 120 for the carbon dioxide raw gas and improving the cooling efficiency of the cryogenic cooler 120 for the carbon dioxide raw gas.

[0046] As Figure 3 shown, in one embodiment, the dehydrocarbonization process equipment 200 includes a dehydrocarbonization heat exchanger 210, a dehydrocarbonization heater 220, and a dehydrocarbonization reactor 230. The inlet end of the dehydrocarbonization heat exchanger 210 is connected to the outlet end of the second compression component 520. The dehydrocarbonization heat exchanger 210, the dehydrocarbonization heater 220, and the dehydrocarbonization reactor 230 are connected in sequence. The outlet end of the dehydrocarbonization reactor 230 is also connected to the inlet end of the third compression component 530. In this embodiment, through the dehydrocarbonization heat exchanger 210, the hydrocarbon compounds with low boiling points in the carbon dioxide gas are condensed and removed. Through the dehydrocarbonization heater 220, the temperature of the carbon dioxide gas is increased, and then it enters the dehydrocarbonization reactor 230, which is beneficial for the reaction of oxygen-containing organic compound impurities and other substances in the heated carbon dioxide gas with the catalyst to generate water and carbon dioxide.

[0047] AsFigure 3 As shown, in one embodiment, the dehydrocarbonization process equipment 200 further includes a second normal temperature cooler 240. One end of the second normal temperature cooler 240 communicates with the gas outlet end of the second compression assembly 520, and the other end of the second normal temperature cooler 240 communicates with the gas inlet end of the dehydrocarbonization heat exchanger 210. In this embodiment, after the carbon dioxide is desulfurized and passes through the second compression assembly 520, the pressure increases and the temperature of the carbon dioxide gas rises. Heat exchange is carried out through the second normal temperature cooler 240 to reduce the temperature of the carbon dioxide gas. After the carbon dioxide gas with reduced temperature flows into the dehydrocarbonization heat exchanger 210, it is beneficial for the carbon dioxide gas in the dehydrocarbonization heat exchanger 210 to carry out heat exchange condensation to remove low-boiling hydrocarbon compounds.

[0048] As Figure 3 Shown, in one embodiment, the dehydrocarbonization process equipment 200 further includes a dehydrocarbonization cooler 250 and a water separator 260. The gas inlet end of the dehydrocarbonization cooler 250 communicates with the gas outlet end of the dehydrocarbonization reactor 230. The gas inlet end of the water separator 260 communicates with the gas outlet end of the dehydrocarbonization cooler 250, and the gas outlet end of the water separator 260 communicates with the gas inlet end of the third compression assembly 530. In this embodiment, the dehydrocarbonization cooler 250 is used to cool the moisture in the dehydrocarbonized carbon dioxide gas, and then the moisture is separated by the water separator 260, so that the moisture content of the dehydrocarbonized carbon dioxide gas passing through the dehydrocarbonization cooler 250 and the water separator 260 is reduced.

[0049] As Figure 4 Shown, in one embodiment, the purification process equipment 300 includes a purification tower 310, a regeneration preheater 320 and a purification heat exchanger 330. The gas inlet end of the purification tower 310 communicates with the gas outlet end of the third compression assembly 530. The purification tower 310 and the regeneration preheater 320 are connected to the purification tower 310. The regeneration preheater 320 is used to blow and regenerate the purification tower 310 in reverse. The purification heat exchanger 330 is connected to the regeneration preheater 320. The gas outlet end of the purification tower 310 communicates with the gas inlet end of the fourth compression assembly 540. In this embodiment, the purification tower 310 performs pressure swing adsorption through an adsorbent to remove moisture in the carbon dioxide gas and trace oxygen-containing organic substances remaining from the dehydrocarbonization process. When the adsorbent in the purification tower 310 is saturated, high-temperature gas can be introduced through the regeneration preheater 320 to perform hot blowing regeneration on the adsorbent in the purification tower 310. The purification heat exchanger 330 is used to exchange heat with the gas released from the flash steam of the evaporation condenser 420 and then introduce it into the regeneration preheater 320 for utilization.

[0050] As Figure 4As shown, in one embodiment, the purification process equipment 300 further includes a third normal temperature cooler 340. One end of the third normal temperature cooler 340 communicates with the gas outlet end of the third compression assembly 530, and the other end of the third normal temperature cooler 340 communicates with the gas inlet end of the purification tower 310. In this embodiment, after the hydrocarbon-removed carbon dioxide gas passes through the third compression assembly 530, the temperature of the pressurized hydrocarbon-removed carbon dioxide gas increases. By passing through the third normal temperature cooler 340, the temperature of the purified carbon dioxide gas can be reduced, so that the normal temperature hydrocarbon-removed carbon dioxide gas enters the purification process equipment 300 for purification. Low temperature is beneficial to the adsorption of the adsorbent in the purification process equipment 300, thereby improving the purification effect of the purification process equipment 300 on the hydrocarbon-removed carbon dioxide gas.

[0051] As Figure 5 shown, in one embodiment, the liquefaction and purification equipment 400 includes a liquid nitrogen freezing tube 410, an evaporation condenser 420 and a purification tower 430. The liquid nitrogen freezing tube 410 communicates with the cooling channel opened in the evaporation condenser. The evaporation condenser 420 communicates with the gas outlet end of the fourth compression assembly 540. The liquid inlet end of the purification tower 430 communicates with the gas outlet end of the evaporation condenser 420, and the liquid outlet end of the purification tower 430 is used to communicate with a storage tank. In this embodiment, after being compressed by the fourth compression assembly 540, the pressure of the purified carbon dioxide gas increases. The purified carbon dioxide gas with a higher pressure flows into the evaporation condenser 420. After liquid nitrogen is introduced into the liquid nitrogen freezing tube 410 and communicates with the cooling channel of the evaporation condenser 420, the carbon dioxide gas in the evaporation condenser 420 is liquefied. Both cooling and pressurization will cause the carbon dioxide gas to liquefy. The liquefied carbon dioxide and the uncondensed carbon dioxide gas are sent into the purification tower 430. The purification tower 430 is purified by distillation, so that other gas impurities that are not adsorbed and removed and the uncondensed ones are released by distillation, and purified carbon dioxide liquid is obtained at the bottom of the purification tower 430.

[0052] As Figure 5 shown, in one embodiment, the liquefaction and purification equipment 400 further includes a fourth normal temperature cooler 440. One end of the fourth normal temperature cooler 440 communicates with the gas outlet end of the fourth compression assembly 540, and the other end of the fourth normal temperature cooler 440 communicates with the gas inlet end of the evaporation condenser 420. In this embodiment, the temperature of the purified carbon dioxide after passing through the fourth compression assembly 540 increases. After the temperature of the carbon dioxide gas passing through the fourth normal temperature cooler 440 is reduced, it flows into the liquefaction and purification equipment 400, so that the heat absorbed by the liquefaction of the carbon dioxide gas is reduced, thereby improving the liquefaction efficiency of the carbon dioxide.

[0053] As Figure 5As shown, in one embodiment, the liquefaction and purification device 400 further includes a subcooler 450. A subcooling channel communicating with the liquid nitrogen freezing tube 410 is provided in the subcooler 450. The intake end of the subcooler 450 communicates with the liquid outlet end of the purification tower 430, and the outlet end of the subcooler 450 is used to communicate with a storage tank. In this embodiment, the subcooling channel of the subcooler 450 communicates with the liquid nitrogen freezing tube 410. After the liquid carbon dioxide passes through the subcooler 450, the temperature of the liquid carbon dioxide is further reduced to the subcooled state, so as to maintain the stability of the liquid state of the liquid carbon dioxide, thereby ensuring the quality of the liquid carbon dioxide flowing into the storage tank.

[0054] The present disclosure also provides a production method of carbon dioxide. The production is carried out by using the production device of liquid carbon dioxide described in any one of the above embodiments, and includes the following steps: introducing the carbon dioxide raw material gas into the first compression assembly for the first compression, introducing the carbon dioxide raw material gas after the first compression into the deep cooler for deep cooling, and then introducing the deep-cooled carbon dioxide gas into the desulfurization tower for desulfurization; introducing the carbon dioxide gas after desulfurization in the desulfurization tower into the second compression assembly for the second compression, and introducing the desulfurized carbon dioxide gas after the second compression into the dehydrocarbonization process equipment for dehydrocarbonization; introducing the carbon dioxide gas after dehydrocarbonization in the dehydrocarbonization process equipment into the third compression assembly for the third compression, and introducing the carbon dioxide gas after the third compression into the purification process equipment for adsorption purification; introducing the carbon dioxide gas after purification in the purification process equipment into the fourth compression assembly for the fourth compression, introducing the carbon dioxide gas after the fourth compression into the liquefaction and purification equipment for liquefaction and purification, and introducing the liquefied and purified carbon dioxide into a storage tank for storage.

[0055] As Figure 6 shown, it is a production method of carbon dioxide according to an embodiment of the present invention. The production is carried out by using the production device of liquid carbon dioxide described in any one of the above embodiments, and includes the following steps:

[0056] S101 Feed the carbon dioxide feed gas into the first compression assembly for the first compression, feed the carbon dioxide feed gas after the first compression into the deep cooler for deep cooling, and then feed the deep-cooled carbon dioxide gas into the desulfurization tower for desulfurization. In this embodiment, there is a close relationship between the adsorption capacity of the adsorbent in the desulfurization tower and the temperature. Adsorption is an exothermic process. An increase in temperature will reduce the adsorption amount of the adsorbent for substances. At high temperatures, the thermal motion of molecules is enhanced, making it easier for adsorbate molecules to detach from the surface of the adsorbent, resulting in a decrease in adsorption efficiency. An increase in temperature will also affect the physical and chemical properties of the adsorbent and reduce the adsorption sites on the surface of the adsorbent, further reducing its adsorption capacity. By deeply cooling the compressed carbon dioxide feed gas, the temperature of the carbon dioxide gas is reduced to below 10°C, which is conducive to the adsorbent in the desulfurization tower adsorbing sulfur dioxide impurities in the carbon dioxide gas.

[0057] S103 Feed the carbon dioxide gas after desulfurization in the desulfurization tower into the second compression assembly for the second compression, and feed the desulfurized carbon dioxide gas after the second compression into the dehydrocarbonization process equipment for dehydrocarbonization. In this embodiment, during the dehydrocarbonization reaction, the catalyst and pressure have a significant impact on the reaction. It can increase the reaction rate and lower the reaction activation energy, making the reaction more efficient; gaseous impurities of oxygen-containing organic compounds such as methane react with oxygen at a lower temperature to form carbon dioxide and water under the action of the catalyst. When the pressure increases from 0.1 MPa to 1.1 MPa, the specific surface area of the catalyst will be reduced by half, changing the catalyst structure and thus affecting the reaction rate and efficiency of the reaction between the impurities of oxygen-containing organic compounds and oxygen; therefore, the second compression is carried out in the second compression assembly to make the pressure of the carbon dioxide gas in the dehydrocarbonization process equipment appropriate, which is conducive to protecting the activity of the catalyst and improving the efficiency of removing impurities of oxygen-containing organic compounds in the dehydrocarbonization process.

[0058] S105 Feed the carbon dioxide gas after dehydrocarbonization in the dehydrocarbonization process equipment into the third compression assembly for the third compression, and feed the carbon dioxide gas after the third compression into the purification process equipment for adsorption purification. In this embodiment, under high pressure, the adsorbent in the purification process equipment adsorbs a large number of gas molecules. Under low pressure, the gas molecules on the adsorbent in the purification process equipment will be desorbed, realizing gas separation and purification. The adsorption effect of the adsorbent is closely related to the pressure. The higher the pressure of the carbon dioxide gas, the greater the adsorption amount of water and impurity gas by the adsorbent; by compressing the carbon dioxide gas for the third time, the pressure of the carbon dioxide gas entering the purification process equipment increases, so that the adsorbent in the purification process equipment maintains a strong adsorption capacity under the condition of higher pressure, thereby improving the adsorption efficiency of the adsorbent in the purification process equipment.

[0059] S107 Introduce the purified carbon dioxide gas from the purification process equipment into the fourth compression component for the fourth compression, and introduce the carbon dioxide gas after the fourth compression into the liquefaction and purification equipment for liquefaction and purification. In this embodiment, an increase in pressure will reduce the distance between gas molecules, making it easier to reach the liquefied state. Cooling is achieved by lowering the temperature of the gas to its liquefaction point, while pressurization is achieved by increasing the pressure of the gas to liquefy it. Therefore, both cooling and pressurization can liquefy the gas. Through the fourth compression, the pressure of the carbon dioxide gas is further increased to the liquefaction pressure of the carbon dioxide gas, thereby enabling the carbon dioxide gas to liquefy rapidly.

[0060] S109 Introduce the liquefied and purified carbon dioxide into a storage tank for storage. In this embodiment, the purity of the liquid carbon dioxide obtained through the liquefaction and purification process is relatively high, and it can be transported to the storage tank for storage and subsequent filling processes.

[0061] For the above-mentioned carbon dioxide production method, by cryogenic cooling the compressed carbon dioxide raw material gas, the temperature of the carbon dioxide gas is reduced, which is beneficial for the adsorbent in the desulfurization tower to adsorb sulfur dioxide impurities in the carbon dioxide gas. Through the sequential boosting of the first compression component, the second compression component, the third compression component, and the fourth compression component, the pressure of the carbon dioxide meets the different pressure requirements of the desulfurization process, the dehydrocarbonization process, the purification process, and the liquefaction and purification process, and improves the efficiency of separating impurities and liquefying the carbon dioxide gas. By independently controlling the corresponding desulfurization process, dehydrocarbonization process, purification process, and liquefaction and purification process between the first compression component, the second compression component, the third compression component, and the fourth compression component, the interference between the processes is reduced, and the stability and sustainability of carbon dioxide liquefaction production are improved.

[0062] It can be understood that in one of the embodiments, after introducing the carbon dioxide raw material gas into the first compression component for the first compression, before introducing the carbon dioxide gas after the first compression into the cryogenic cooler for cryogenic cooling, the following steps are further included:

[0063] Introduce the carbon dioxide gas after the first compression into the first normal-temperature cooler for temperature reduction. In this embodiment, the cryogenic cooler uses chilled water for water cooling. When the temperature of the carbon dioxide gas changes significantly, the cryogenic cooler needs to first adjust the temperature of the chilled water, resulting in a slower impact on the cooling temperature of the carbon dioxide gas. After the carbon dioxide gas is compressed by the first compression component, its temperature rises. After temperature reduction through the first normal-temperature cooler, the temperature of the carbon dioxide gas after the first compression is close to that of the air, enabling the continuously input of the carbon dioxide gas with a stable temperature into the cryogenic cooler, reducing the adjustment requirements of the cryogenic cooler for the temperature of the chilled water, and improving the efficiency of the cryogenic cooler in cooling the carbon dioxide gas.

[0064] Further, in one embodiment, the adsorbent of the desulfurization tower includes an activated carbon substrate and a special adsorbent material. The special adsorbent material is added to the activated carbon substrate and mixed. The special adsorbent material includes at least one of silica gel, zeolite, and molecular sieve. In this embodiment, silica gel is an organic material with high activity and high adsorbability. After combining with activated carbon, it can further improve the adsorption performance. Zeolite is an adsorbent material with a hydrophilic and polar surface. Zeolite has the ability of molecular sieving. The pores of activated carbon are smaller than those of zeolite, and activated carbon is an adsorbent material with a hydrophobic and non-polar surface, and has a poor removal effect on polar short-chain organic compounds and their precursors. Zeolite can make up for the deficiencies of activated carbon and has a better removal effect on polar substances. Molecular sieve is a crystalline silicate or aluminosilicate with the characteristic of screening molecules. It has a nano-scale pore and cavity system with uniform pore diameter inside, and can selectively adsorb molecules through the pore diameter. Molecular sieve has higher selectivity and separation ability. By adding the special adsorbent material, the adsorption capacity for impurities such as sulfur dioxide is increased, and the increase in adsorption capacity reduces the influence of temperature rise on the adsorption amount, thereby maintaining the adsorption efficiency of the desulfurization tower for sulfur dioxide.

[0065] It can be understood that, in one embodiment, after the carbon dioxide gas desulfurized by the desulfurization tower is introduced into the second compression assembly for secondary compression, before the secondary compressed desulfurized carbon dioxide gas is introduced into the dehydrocarbonization process equipment for dehydrocarbonization, the following steps are further included:

[0066] The secondary compressed carbon dioxide gas is introduced into a second normal temperature cooler for temperature reduction. In this embodiment, in the dehydrocarbonization process equipment, it is necessary to first condense the low-boiling hydrocarbon compounds in the carbon dioxide gas through a dehydrocarbonization heat exchanger, so as to remove the low-boiling hydrocarbon compounds in the carbon dioxide gas through the dehydrocarbonization heat exchanger. After the carbon dioxide gas is compressed by the second compression assembly, its temperature rises. After being cooled by the second normal temperature cooler, the carbon dioxide gas entering the dehydrocarbonization heat exchanger is easier to cool down, thereby improving the efficiency of the dehydrocarbonization heat exchanger in condensing the low-boiling hydrocarbon compounds in the carbon dioxide gas, and further effectively removing the low-boiling hydrocarbon compounds in the carbon dioxide gas.

[0067] It can be understood that, in one embodiment, after the carbon dioxide gas dehydrocarbonized by the dehydrocarbonization process equipment is introduced into the third compression assembly for tertiary compression, before the tertiary compressed carbon dioxide gas is introduced into the purification process equipment for adsorption purification, the following steps are further included:

[0068] The carbon dioxide gas after the third compression is introduced into a third normal-temperature cooler for temperature reduction. In this embodiment, the purification process equipment performs pressure swing adsorption through a purification tower to remove moisture in the carbon dioxide gas and trace oxygen-containing organic compounds remaining from the dehydrocarbonization process. During pressure swing adsorption, the adsorbent adsorbs a large number of gas molecules under high pressure and is prone to desorption under low pressure and high temperature. After the carbon dioxide gas is compressed by the third compression assembly and its temperature rises, after being cooled by the third normal-temperature cooler, the carbon dioxide gas with a reduced temperature is conducive to the adsorbent in the purification tower adsorbing moisture and trace oxygen-containing organic compounds remaining from the dehydrocarbonization process, thereby improving the efficiency of purifying moisture and trace oxygen-containing organic compounds remaining from the dehydrocarbonization process in the carbon dioxide gas.

[0069] It can be understood that in one of the embodiments, after introducing the carbon dioxide gas purified by the purification process equipment into the fourth compression assembly for the fourth compression, before introducing the carbon dioxide gas after the fourth compression into the liquefaction and purification equipment for liquefaction and purification, the following steps are further included:

[0070] The carbon dioxide gas after the fourth compression is introduced into a fourth normal-temperature cooler for temperature reduction. In this embodiment, after the carbon dioxide gas is compressed by the fourth compression assembly and its temperature rises, it is heat-exchanged and cooled by the fourth normal-temperature cooler, so that the temperature of the evaporative condenser into which the carbon dioxide gas enters the liquefaction and purification equipment is relatively low, reducing the temperature difference for the evaporative condenser to cool the carbon dioxide gas, thereby improving the efficiency of liquefying the carbon dioxide gas.

[0071] In one embodiment, the pressure of the carbon dioxide gas in the first compression is 0.3 Mpa - 0.4 Mpa; the pressure of the carbon dioxide gas in the second compression is 0.7 Mpa - 0.8 Mpa; the pressure of the carbon dioxide gas in the third compression is 1.4 Mpa - 1.5 Mpa; the pressure of the carbon dioxide gas in the fourth compression is 2.3 Mpa - 2.4 Mpa. In this embodiment, the pressure of the carbon dioxide gas in the first compression is 0.3 Mpa - 0.4 Mpa. The increase in the pressure of the carbon dioxide gas passing through the first compression component increases the flow rate of the carbon dioxide gas and increases the contact between the carbon dioxide gas and the adsorbent in the desulfurization tower, enabling the carbon dioxide gas to maintain good desulfurization efficiency in the desulfurization tower; the pressure of the carbon dioxide gas in the second compression is 0.7 Mpa - 0.8 Mpa, which reduces the pressure of the carbon dioxide gas entering the dehydrocarbonization process equipment compared to the traditional process pressure, resulting in a relatively high specific surface area of the catalyst in the dehydrocarbonization process equipment, thereby improving the dehydrocarbonization efficiency of the gas impurities of the oxygen-containing organic compounds in the carbon dioxide gas to generate carbon dioxide and water; the pressure of the carbon dioxide gas in the third compression is 1.4 Mpa - 1.5 Mpa, which increases the pressure of the carbon dioxide gas entering the purification tower in the purification process equipment, thereby enabling the adsorbent in the purification tower to maintain the effect of removing moisture and trace oxygen-containing organic compounds remaining from the dehydrocarbonization process from the carbon dioxide gas; the pressure of the carbon dioxide gas in the fourth compression is 2.3 Mpa - 2.4 Mpa, and the relatively high pressure causes the carbon dioxide gas to quickly liquefy into liquid carbon dioxide; through the sequential increase by the first compression component, the second compression component, the third compression component, and the fourth compression component, the pressure of the carbon dioxide meets the different pressure requirements of the desulfurization process, the dehydrocarbonization process, the purification process, and the liquefaction and purification process, and improves the efficiency of separating impurities and liquefying the carbon dioxide gas.

[0072] Further, in one embodiment, when the pressure passing through the first compression component is abnormal, the cooling effect of the cryogenic cooler can be controlled. Therefore, after the carbon dioxide raw material gas is introduced into the first compression component for the first compression, before the first-compressed carbon dioxide gas is introduced into the cryogenic cooler for deep cooling, the following steps are further included:

[0073] Detect the pressure of the carbon dioxide gas at the outlet end of the first compression component;

[0074] If the pressure of the carbon dioxide gas is greater than the first preset pressure, for every 0.02 Mpa increase in the pressure of the carbon dioxide gas, the temperature of the cryogenic cooler decreases by 1 °C from the preset temperature;

[0075] If the pressure of the carbon dioxide gas is less than the first preset pressure, for every 0.02 Mpa decrease in the pressure of the carbon dioxide gas, the temperature of the cryogenic cooler increases by 1 °C from the preset temperature.

[0076] In this embodiment, the first preset pressure is 0.3 Mpa - 0.4 Mpa, the preset temperature is 10 °C. When the pressure of the carbon dioxide gas increases, the flow rate of the carbon dioxide gas passing through the desulfurization tower increases, so that the adsorption amount of sulfur dioxide impurities in the carbon dioxide gas that the desulfurization tower needs to adsorb increases. By cooling the pressure of the carbon dioxide gas, the detachment of adsorbed molecules from the adsorbent surface is reduced, so that the adsorption amount of sulfur dioxide by the adsorbent in the desulfurization tower increases; when the pressure of the carbon dioxide gas decreases, the flow rate of the carbon dioxide gas decreases, and the cooling temperature of the cryogenic cooler increases, so that the temperature of the carbon dioxide gas after cryogenic cooling increases, thereby increasing the movement speed of the carbon dioxide gas, and further increasing the desulfurization efficiency of the desulfurization tower for the carbon dioxide gas.

[0077] Further, in one embodiment, when the pressure of the second compression component is abnormal, the pressure of the third compression component can be controlled to control the effect on the trace oxygen-containing organic substances remaining in the dehydrocarbonization process. Therefore, after the carbon dioxide gas desulfurized by the desulfurization tower is introduced into the second compression component for secondary compression, and the desulfurized carbon dioxide gas after secondary compression is introduced into the dehydrocarbonization process equipment for dehydrocarbonization, before the carbon dioxide gas after dehydrocarbonization in the dehydrocarbonization process equipment is introduced into the third compression component for tertiary compression and then the carbon dioxide gas after tertiary compression is introduced into the purification process equipment for adsorption purification, the following steps are further included:

[0078] Detect the pressure of the carbon dioxide gas at the outlet end of the second compression component;

[0079] When the pressure of the carbon dioxide gas is greater than the second preset pressure, for every 0.01 Mpa increase in the pressure of the carbon dioxide gas, the third preset pressure of the third compression component for the carbon dioxide gas increases by 0.02 Mpa;

[0080] The third preset pressure of the third compression component for the carbon dioxide gas remains unchanged.

[0081] In this embodiment, the second preset pressure of the second compression assembly is 0.7 Mpa - 0.8 Mpa, and the preset pressure of the third compression assembly is 1.4 Mpa - 1.5 Mpa. The dehydrocarbonization process is used to remove oxygen-containing organic impurities, and the purification process is used to remove the remaining oxygen-containing organic impurities and moisture in the dehydrocarbonization process. When the pressure of the second compression assembly is greater than the second preset pressure, the amount of carbon dioxide gas passing through the dehydrocarbonization process is relatively large, resulting in a decrease in the removal effect of the oxygen-containing organic impurities in the carbon dioxide gas by the dehydrocarbonization process. By pressurizing with the third preset pressure of the third compression assembly, the pressure of the carbon dioxide gas entering the purification process increases, thereby improving the effect of removing the remaining oxygen-containing organic impurities. When the pressure of the second compression assembly is less than the second preset pressure, the amount of carbon dioxide gas entering the third compression assembly from the dehydrocarbonization process is relatively small. By maintaining the pressure of the carbon dioxide entering the purification process through the third compression assembly, the purification effect of the purification process on carbon dioxide is kept stable, thereby improving the stability of the carbon dioxide production process.

[0082] Compared with the prior art, the present disclosure has at least the following advantages:

[0083] For the above-mentioned liquid carbon dioxide production device 10 and the carbon dioxide production method, the carbon dioxide raw material gas is cooled by the cryogenic cooler 120, so that the temperature of the carbon dioxide raw material gas entering the desulfurization tower 130 is reduced, thereby increasing the adsorption amount of the adsorbent in the desulfurization tower 130 for the carbon dioxide raw material gas; the pressure of the desulfurized carbon dioxide gas entering the dehydrocarbonization process equipment 200 is relatively low, making the catalyst activity of the dehydrocarbonization process equipment 200 relatively high, thereby improving the efficiency of removing hydrocarbon gas impurities from the carbon dioxide gas; the carbon dioxide gas after dehydrocarbonization enters the purification process equipment 300 after being pressurized, so that the efficiency of the purification process equipment 300 in adsorbing moisture and oxygen-containing organic impurities is improved; the carbon dioxide gas after purification enters the liquefaction and purification equipment 400 after being pressurized again, so that the liquefaction efficiency of the liquefaction and purification equipment 400 is improved;

[0084] By adapting the first compression assembly 510, the second compression assembly 520, the third compression assembly 530 and the fourth compression assembly 540 in the compression process to the working conditions of the desulfurization process, the dehydrocarbonization process, the purification process and the liquefaction and purification process, the efficiency of removing impurities in the production of liquefied carbon dioxide gas is improved, and the liquefaction efficiency of carbon dioxide is increased, thereby improving the production efficiency and quality of liquefied carbon dioxide gas.

[0085] By independently controlling the corresponding desulfurization process, dehydrocarbonization process, purification process and liquefaction and purification process between the first compression assembly, the second compression assembly, the third compression assembly and the fourth compression assembly, the interference between each process is reduced, and the stability and sustainability of the liquefied carbon dioxide production are improved.

[0086] The above-described embodiments merely represent several implementation manners of the present disclosure. The description thereof is relatively specific and detailed, but it should not be construed as a limitation to the scope of the disclosed patent. It should be noted that for those of ordinary skill in the art, without departing from the concept of the present disclosure, several modifications and improvements can still be made, and these all fall within the protection scope of the present disclosure. Therefore, the protection scope of the present disclosure patent shall be subject to the appended claims.

Claims

1. A liquid carbon dioxide production device, characterized in that: Including desulfurization process equipment, dehydrogenation process equipment, purification process equipment, liquefaction purification equipment and compression process equipment; The compression process equipment includes a first compression assembly, a second compression assembly, a third compression assembly and a fourth compression assembly; The desulfurization process equipment includes a raw material air inlet pipeline, a cryogenic cooler and a desulfurization tower, wherein the raw material air inlet pipeline is connected to the air inlet end of the first compression assembly, the air inlet end of the cryogenic cooler is connected to the air outlet end of the first compression assembly, and the desulfurization tower is connected to the air outlet end of the cryogenic cooler; The air inlet end of the second compression assembly is connected to the air outlet end of the desulfurization tower, and the air inlet end of the dehydrocarbon process equipment is connected to the air outlet end of the second compression assembly; the air inlet end of the third compression assembly is connected to the air outlet end of the dehydrocarbon process equipment, and the air outlet end of the third compression assembly is connected to the air inlet end of the purification process equipment, and the purification process equipment is connected to the air outlet end of the third compression assembly; the air inlet end of the fourth compression assembly is connected to the air outlet end of the purification process equipment, the air inlet end of the liquefaction and purification equipment is connected to the purification process equipment, and the air outlet end of the liquefaction and purification equipment is used to connect to the storage tank.

2. The liquid carbon dioxide production device according to claim 1, characterized in that: The desulfurization process equipment also includes a first normal temperature cooler, one end of which is connected to the air outlet end of the first compression component, and the other end of which is connected to the air inlet end of the deep freezer.

3. The liquid carbon dioxide production device according to claim 1, characterized in that: The dehydrocarbonization process equipment includes a dehydrocarbonization heat exchanger, a dehydrocarbonization heater and a dehydrocarbonization reactor. The air inlet end of the dehydrocarbonization heat exchanger is connected to the air outlet end of the second compression component. The dehydrocarbonization heat exchanger, the dehydrocarbonization heater and the dehydrocarbonization reactor are connected in sequence, and the air outlet end of the dehydrocarbonization reactor is also connected to the air inlet end of the third compression component.

4. The liquid carbon dioxide production device according to claim 3, characterized in that: The dehydrocarbon process equipment also includes a second normal temperature cooler, one end of which is connected to the air outlet end of the second compression assembly, and the other end of which is connected to the air inlet end of the dehydrocarbon heat exchanger.

5. The liquid carbon dioxide production device according to claim 1, characterized in that: The purification process equipment includes a purification tower, a regeneration preheater and a purification heat exchanger. The air inlet end of the purification tower is connected to the air outlet end of the third compression component. The regeneration preheater is connected to the purification tower. The regeneration preheater is used for back-blowing and regenerating the purification tower. The purification heat exchanger is connected to the regeneration preheater. The air outlet end of the purification tower is connected to the air inlet end of the fourth compression component.

6. The liquid carbon dioxide production device according to claim 5, characterized in that: The purification process equipment also includes a third normal temperature cooler, one end of the third normal temperature cooler is connected to the air outlet end of the third compression assembly, and the other end of the third normal temperature cooler is connected to the air inlet end of the purification tower.

7. The liquid carbon dioxide production device according to claim 1, characterized in that: The liquefaction and purification equipment includes a liquid nitrogen freezing tube, an evaporative condenser and a purification tower. The liquid nitrogen freezing tube is connected to the cooling channel opened in the evaporative condenser, the evaporative condenser is connected to the gas outlet end of the fourth compression component, the liquid inlet end of the purification tower is connected to the gas outlet end of the evaporative condenser, and the liquid outlet end of the purification tower is used to connect to a storage tank.

8. The liquid carbon dioxide production device according to claim 7, characterized in that: The liquefaction and purification equipment also includes a fourth normal temperature cooler, one end of the fourth normal temperature cooler is connected to the air outlet end of the fourth compression assembly, and the other end of the fourth normal temperature cooler is connected to the air inlet end of the evaporative condenser.

9. A method for producing carbon dioxide, characterized in that: The production of liquid carbon dioxide using the production device of any one of claims 1 to 8 comprises the following steps: Passing the carbon dioxide raw gas into the first compression assembly for first compression, passing the carbon dioxide gas after the first compression into the deep cooler for deep cooling, and then passing the deep cooled carbon dioxide gas into the desulfurization tower for desulfurization; Passing the carbon dioxide gas desulfurized by the desulfurization tower into the second compression assembly for a second compression, and passing the desulfurized carbon dioxide gas compressed for the second time into the dehydrogenation process equipment for dehydrogenation; Passing the carbon dioxide gas after dehydrogenation in the dehydrogenation process equipment into the third compression assembly for third compression, and passing the carbon dioxide gas compressed for the third time into the purification process equipment for adsorption purification; Passing the carbon dioxide gas purified by the purification process equipment into the fourth compression assembly for fourth compression, and passing the fourth compressed carbon dioxide gas into the liquefaction and purification equipment for liquefaction and purification; The liquefied and purified carbon dioxide is passed into a storage tank for storage.

10. The method for producing carbon dioxide according to claim 9, characterized in that: The pressure of the carbon dioxide gas compressed for the first time is 0.3Mpa-0.4Mpa; the pressure of the carbon dioxide gas compressed for the second time is 0.7Mpa-0.8Mpa; the pressure of the carbon dioxide gas compressed for the third time is 1.4Mpa-1.5Mpa; the pressure of the carbon dioxide gas compressed for the fourth time is 2.3Mpa-2.4Mpa.

Images