Transport vehicle, carbon dioxide capture method, and carbon dioxide transport method

Abstract

To provide a conveying vehicle, a carbon dioxide recovery method and a carbon dioxide conveying method which can suppress a facility for recovering carbon dioxide included in exhaust gas exhausted from a burning apparatus from being enlarged in size and complicated.SOLUTION: A conveying vehicle, which conveys liquid carbon dioxide, is provided with a refrigeration machine for liquefying carbon dioxide and a storage tank that stores liquid carbon dioxide. The refrigeration machine includes: a compressor that compresses a first heat medium; a heat exchanger that cools the first heat medium compressed by the compressor; an expanding machine that expands the first heat medium cooled by the heat exchanger; a separator that separates carbon dioxide gas from absorbing liquid or an adsorbing material, by heat energy of the first heat medium compressed by the compressor; and a liquefier that liquefies the carbon dioxide gas separated from the absorbing liquid or the adsorbing material by the separator, by cold energy of the first heat medium expanded by the expander.SELECTED DRAWING: Figure 2

Description

Technical Field

[0001] The present disclosure relates to a transport vehicle, a carbon dioxide recovery method, and a carbon dioxide transport method for recovering and transporting carbon dioxide contained in exhaust gas discharged from a combustion device.

Background Art

[0002] Carbon dioxide contained in exhaust gas discharged from a combustion device is separated from the exhaust gas by absorbing it in a liquid absorbent such as an amine or adsorbing it on an adsorbent (see, for example, Patent Document 1). Since the recovered carbon dioxide is in a gaseous state, liquefaction and densification of carbon dioxide are required to efficiently transport carbon dioxide to a remote storage site.

Prior Art Documents

Patent Documents

[0003]

Patent Document 1

Summary of the Invention

Problems to be Solved by the Invention

[0004] In order to recover and liquefy carbon dioxide from exhaust gas, both equipment for supplying a heat source for separating carbon dioxide gas from the exhaust gas and equipment for supplying a cold heat source for liquefying carbon dioxide are required. Introducing both pieces of equipment is likely to be too burdensome for small and medium-sized enterprises. In order to reduce the above burden, it is desired to suppress the enlargement and complication of the equipment for recovering carbon dioxide contained in the exhaust gas.

[0005] In view of the above circumstances, at least one embodiment of the present invention aims to provide a transport vehicle, a carbon dioxide recovery method, and a carbon dioxide transport method that can suppress the enlargement and complication of equipment for recovering carbon dioxide contained in exhaust gas discharged from a combustion device. [Means for solving the problem]

[0006] A transport vehicle according to at least one embodiment of the present invention is A transport vehicle for transporting liquid carbon dioxide, A refrigerator for liquefying carbon dioxide gas, A storage tank configured for storing liquid carbon dioxide, The aforementioned refrigerator is A compressor configured to compress a first heat transfer medium, A heat exchanger configured to cool the first heat transfer medium compressed in the compressor, An expander configured to expand the first heat transfer medium cooled in the heat exchanger, A separator configured to separate carbon dioxide gas from an absorbent liquid that has absorbed carbon dioxide or an adsorbent material that has adsorbed carbon dioxide, using the thermal energy of the first heat transfer medium compressed in the compressor, The system includes a liquefaction unit configured to liquefy the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separator using the cold energy of the first heat transfer medium expanded in the expander.

[0007] The carbon dioxide recovery method according to at least one embodiment of the present invention is: A carbon dioxide capture method for recovering carbon dioxide contained in exhaust gas emitted from a combustion device, A carbon dioxide extraction step in which carbon dioxide contained in the exhaust gas is absorbed into an absorbent liquid, or carbon dioxide is adsorbed onto an adsorbent, A compression step in which the first heat transfer medium is compressed by a compressor of a refrigerator mounted on a transport vehicle for transporting liquid carbon dioxide, A cooling step in which the first heat transfer medium compressed in the compressor is cooled by the heat exchanger of the refrigerator, An expansion step in which the first heat transfer medium cooled in the heat exchanger is expanded by the expander of the refrigerator, A separation step in which carbon dioxide gas is separated from the absorbent liquid that has absorbed the carbon dioxide or the adsorbent that has adsorbed the carbon dioxide by the thermal energy of the first heat transfer medium compressed in the compressor, The system includes a liquefaction step in which the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separation step is liquefied by the cold energy of the first heat transfer medium expanded in the expansion machine.

[0008] The carbon dioxide transport method according to at least one embodiment of the present invention is A method for transporting carbon dioxide, A first transfer step involves transferring the liquid carbon dioxide recovered in equipment for recovering carbon dioxide contained in exhaust gas discharged from a combustion device from the equipment to a first tank installed at a remote location, The system includes a second transfer step of transferring the liquid carbon dioxide from the first tank to the second tank via a first pipeline connecting the first tank and the second tank located remotely from the first tank, The first transfer step is, The process includes a transport vehicle step of storing the liquid carbon dioxide in a storage tank mounted on a transport vehicle, and transporting the liquid carbon dioxide stored in the storage tank to the first tank using the transport vehicle. [Effects of the Invention]

[0009] According to at least one embodiment of the present invention, a transport vehicle, a carbon dioxide capture method, and a carbon dioxide transport method are provided that can suppress the increasing size and complexity of equipment for capturing carbon dioxide contained in exhaust gas discharged from a combustion device. [Brief explanation of the drawing]

[0010] [Figure 1] This is an explanatory diagram illustrating a carbon dioxide recovery method according to one embodiment of the present disclosure. [Figure 2] This figure schematically shows a transport vehicle and a carbon dioxide capture device according to one embodiment of the present disclosure. [Figure 3] It is an explanatory diagram for explaining a carbon dioxide recovery method according to an embodiment of the present disclosure. [Figure 4] It is a diagram schematically showing a regeneration tower, a separator, and a heat exchanger on the drive device side according to an embodiment of the present disclosure. [Figure 5] It is a diagram schematically showing a regeneration tower, a separator, and a heat exchanger on the drive device side according to an embodiment of the present disclosure. [Figure 6] It is an explanatory diagram for explaining a carbon dioxide recovery method according to an embodiment of the present disclosure. [Figure 7] It is a diagram schematically showing a transport vehicle according to an embodiment of the present disclosure. [Figure 8] It is an explanatory diagram for explaining an example of the arrangement of equipment, a first tank, and a second tank in a carbon dioxide transport method according to an embodiment of the present disclosure. [Figure 9] It is an explanatory diagram for explaining a carbon dioxide transport method according to an embodiment of the present disclosure. [Figure 10] It is an explanatory diagram for explaining a carbon dioxide transport method according to an embodiment of the present disclosure. [Figure 11] It is an explanatory diagram for explaining a carbon dioxide transport method according to an embodiment of the present disclosure.

Mode for Carrying Out the Invention

[0011] Hereinafter, some embodiments of the present invention will be described with reference to the accompanying drawings. However, the dimensions, materials, shapes, relative arrangements, etc. of the components described as embodiments or shown in the drawings are not intended to limit the scope of the present invention, but are merely illustrative examples.

[0012] (Method for Recovering Carbon Dioxide) Figures 1, 3, and 6 are explanatory diagrams illustrating a carbon dioxide recovery method according to one embodiment of the present disclosure. Figure 2 is a schematic diagram showing a transport vehicle 2 and a carbon dioxide recovery device 1 according to one embodiment of the present disclosure. Several embodiments of the carbon dioxide recovery method are methods for recovering carbon dioxide contained in exhaust gas emitted from a combustion device 11 such as an engine. The carbon dioxide recovery method comprises a carbon dioxide extraction step, a compression step, a cooling step, an expansion step, a separation step, and a liquefaction step.

[0013] In the illustrated embodiment, the carbon dioxide extraction step is performed by the carbon dioxide recovery device 1. The compression step, cooling step, expansion step, separation step, and liquefaction step are performed by a refrigerator 3 mounted on the transport vehicle 2. Some steps in the carbon dioxide recovery method may be performed by the equipment constituting the carbon dioxide recovery device 1 or the equipment constituting the transport vehicle 2, or by equipment not constituting the carbon dioxide recovery device 1 or transport vehicle 2, or by manual means.

[0014] (Carbon dioxide capture device) In the carbon dioxide extraction step described above, carbon dioxide contained in the exhaust gas is absorbed by an absorbent liquid, or the carbon dioxide is adsorbed onto an adsorbent. The carbon dioxide recovery device 1 is installed in a facility (for example, a plant) 10 equipped with a combustion device 11. The carbon dioxide recovery device 1 is configured to absorb carbon dioxide contained in the exhaust gas discharged from the combustion device 11 into an absorbent liquid, or to adsorb the carbon dioxide contained in the exhaust gas onto an adsorbent.

[0015] In some embodiments, the carbon dioxide recovery device 1 is configured to absorb carbon dioxide contained in the exhaust gas discharged from the combustion device 11 into a liquid absorbent. In the illustrated embodiment, the carbon dioxide recovery device 1 includes an absorption tower 12 configured to bring the exhaust gas discharged from the combustion device 11 and the absorbent into gas-liquid contact. In the absorption tower 12, the exhaust gas introduced into the absorption tower 12 and the absorbent sprayed inside the absorption tower 12 are brought into gas-liquid contact, thereby absorbing the carbon dioxide contained in the exhaust gas into the absorbent. Examples of the absorbent include liquid amines. However, the absorbent is not limited to liquid amines and can be any liquid capable of absorbing carbon dioxide.

[0016] In the illustrated embodiment, the carbon dioxide recovery device 1 further includes a cooling tower 13 and a regeneration tower 14. The cooling tower 13 is provided with a cooling water circulation line 131 for drawing cooling water stored inside the cooling tower 13 out of the cooling tower 13 and spraying it inside the cooling tower 13, and a cooling water cooler 132 for cooling the cooling water flowing through the cooling water circulation line 131 with a cooling medium (for example, industrial water at a lower temperature than the cooling water). Exhaust gas discharged from the combustion device 11 is introduced into the cooling tower 13. In the cooling tower 13, the exhaust gas introduced into the cooling tower 13 and the cooling water sprayed inside the cooling tower 13 via the cooling water circulation line 131 are brought into gas-liquid contact to cool the exhaust gas to approximately room temperature. The exhaust gas cooled in the cooling tower 13 is introduced into the absorption tower 12. The absorbent liquid that absorbed carbon dioxide in the absorption tower 12 is introduced into the regeneration tower 14 and stored inside the regeneration tower 14.

[0017] In some other embodiments, the carbon dioxide recovery device 1 may be configured to adsorb carbon dioxide contained in the exhaust gas emitted from the combustion device 11 onto a solid adsorbent. Examples of adsorbents include solid adsorbents such as zeolites. The adsorbent is not limited to zeolites and can be any solid capable of adsorbing carbon dioxide.

[0018] The adsorbent material is designed to adsorb carbon dioxide contained in exhaust gas and to separate the adsorbed carbon dioxide using either thermal swing adsorption (TSA) or pressure swing adsorption (PSA). In thermal swing adsorption (TSA), a temperature difference is used as a means of separating carbon dioxide from exhaust gas. Specifically, in thermal swing adsorption (TSA), carbon dioxide gas is separated from the adsorbent by heating the adsorbent, which has adsorbed carbon dioxide, to a second predetermined temperature that is higher than the first predetermined temperature at which carbon dioxide is adsorbed onto the adsorbent. In pressure swing adsorption (PSA), a pressure difference is used as a means of separating carbon dioxide from exhaust gas. Specifically, in pressure swing adsorption (PSA), carbon dioxide gas is separated from the adsorbent by reducing the pressure of the adsorbent, which has adsorbed carbon dioxide, to a second predetermined pressure that is lower than the first predetermined pressure at which carbon dioxide is adsorbed onto the adsorbent.

[0019] (Transport vehicle) The transport vehicle 2 is a vehicle for transporting liquid carbon dioxide (liquid carbon dioxide). As shown in Figures 1, 3, and 6, the transport vehicle 2 comprises a chiller 3 for liquefying carbon dioxide gas and a storage tank 4 configured to store liquid carbon dioxide. In the illustrated embodiment, the transport vehicle 2 comprises a drive unit 20 and a cargo bed 21 for driving the transport vehicle 2, and the chiller 3 and storage tank 4 are mounted on the cargo bed 21 of the transport vehicle 2. The cargo bed 21 is located above the drive unit 20 of the transport vehicle 2.

[0020] (Refrigeration unit) As shown in Figure 2, the refrigerator 3 includes a compressor 5, a heat exchanger 6, an expander 7, a separator 8, and a liquefaction unit 9. The refrigerator 3 further includes a circulation line 31 configured to circulate a first heat transfer medium. The compressor 5, heat exchanger 6, and expander 7 are each located in the circulation line 31. The compressor 5, heat exchanger 6, expander 7, and circulation line 31 constitute a refrigeration cycle. The first heat transfer medium can be, for example, air. However, the first heat transfer medium may be a heat transfer medium other than air.

[0021] The circulation line 31 includes an expansion gas line 31A for guiding the first heat medium expanded in the expander 7 to the compressor 5, and a compressed gas line 31B for guiding the first heat medium compressed in the compressor 5 to the expander 7. Each of the expansion gas line 31A and the compressed gas line 31B forms a flow path for the circulation of the first heat medium, and is formed, for example, by piping. Note that each pipe forming the circulation line 31 may have multiple piping sections connected via flanges or the like.

[0022] (Compressor) The compressor 5 is configured to compress the first heat transfer medium. In the compression step described above, the first heat transfer medium is compressed by the compressor 5. By driving the compressor 5, the gaseous first heat transfer medium drawn into the compressor 5 from upstream of the compressor 5 in the circulation line 31 is compressed. The first heat transfer medium compressed in the compressor 5 is heated and pressurized higher than before it was introduced into the compressor 5, becoming a high-temperature, high-pressure gas.

[0023] (heat exchanger) The heat exchanger 6 is configured to cool the first heat transfer medium compressed in the compressor 5. In the cooling step described above, the heat exchanger 6 cools the first heat transfer medium compressed in the compressor 5. The heat exchanger 6 is configured to perform heat exchange between the first heat transfer medium flowing through the expansion gas line 31A and the first heat transfer medium flowing through the compressed gas line 31B. The first heat transfer medium flowing through the compressed gas line 31B is at a higher temperature than the first heat transfer medium flowing through the expansion gas line 31A because it has been compressed in the compressor 5.

[0024] Through heat exchange in the heat exchanger 6, the first heat transfer medium flowing through the compressed gas line 31B is cooled, while the first heat transfer medium flowing through the expanding gas line 31A is heated. In other words, the heat exchanger 6 includes a low-temperature side heat exchange section 61 through which the first heat transfer medium flows, located in the expanding gas line 31A, and a high-temperature side heat exchange section 62 through which the first heat transfer medium flows, located in the compressed gas line 31B, and heat is transferred from the first heat transfer medium flowing through the high-temperature side heat exchange section 62 to the first heat transfer medium flowing through the low-temperature side heat exchange section 61.

[0025] (Pre-cooler) The refrigerator 3 may further include a pre-cooler 63 provided between the compressor 5 and the heat exchanger 6 (high-temperature side heat exchange section 62) of the compressed gas line 31B (circulation line 31), as shown in Figure 2. The pre-cooler 63 is provided upstream of the high-temperature side heat exchange section 62 of the compressed gas line 31B and is configured to perform heat exchange between a first heat transfer medium flowing through the compressed gas line 31B (pre-cooler 63) and a coolant at a lower temperature than the first heat transfer medium (for example, water such as industrial water). The coolant is introduced into the pre-cooler 63 by a pump. Through heat exchange in the pre-cooler 63, the first heat transfer medium flowing through the compressed gas line 31B toward the high-temperature side heat exchange section 62 is cooled by the coolant. The first heat transfer medium cooled in the pre-cooler 63 is introduced into the high-temperature side heat exchange section 62 through the compressed gas line 31B.

[0026] (Inflator) The expander 7 is configured to expand the first heat transfer medium that has been cooled in the heat exchanger 6 (high-temperature side heat exchange section 62). In the expansion step, the expander 7 expands the first heat transfer medium that has been cooled in the heat exchanger 6. The gaseous first heat transfer medium that has expanded in the expander 7 is cooled and depressurized to a lower temperature and pressure than before it was introduced into the expander 7, becoming a low-temperature, low-pressure gas.

[0027] In some embodiments, the expander 7 may be connected to the compressor 5 via a rotating shaft 51. In the illustrated embodiment, the refrigerator 3 further includes an electric motor 52 configured to generate a driving force to drive the compressor 5. The electric motor 52 is configured to have a variable output. The compressor 5 includes an electric compressor configured to be driven by the electric motor 52 to compress the circulating gas. The compressor 5 and the expander 7 are arranged coaxially with each other and connected to the rotating shaft 51, which is the output shaft of the electric motor 52 for driving the compressor 5. The electric motor 52 is supplied with current from a power source (such as a generator) not shown, and is driven by the current supplied from the power source to drive the rotating shaft 51, the compressor 5, and the expander 7. In the expander 7, a portion of the expansion energy generated when the gas expands is recovered, and the recovered expansion energy assists in driving the compressor 5. The power source for the electric motor 52 is preferably mounted on the transport vehicle 2.

[0028] (Separator) In the separation step described above, carbon dioxide gas is separated from the absorbent liquid that has absorbed carbon dioxide or the adsorbent material that has adsorbed carbon dioxide, using the thermal energy of the first heat transfer medium compressed in the compressor 5. In the illustrated embodiment, the separation step is performed by a separator 8. The separator 8 is configured to separate carbon dioxide gas from the absorbent liquid that has absorbed carbon dioxide or the adsorbent material that has adsorbed carbon dioxide, using the thermal energy of the first heat transfer medium compressed in the compressor 5.

[0029] In the illustrated embodiment, the absorbent liquid that has absorbed carbon dioxide stored inside the regeneration tower 14 is heated by the thermal energy of the first heat transfer medium compressed in the compressor 5, thereby separating the carbon dioxide gas from the absorbent liquid. By heating the absorbent liquid to a predetermined temperature (for example, 140°C) or higher, the carbon dioxide gas absorbed by the absorbent liquid is separated. The carbon dioxide absorption performance of the absorbent liquid is restored by the separation of the carbon dioxide gas in the separator 8.

[0030] (liquefier) In the liquefaction step described above, the cold energy of the first heat transfer medium expanded in the expander 7 is used to liquefy the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separation step described above. In the illustrated embodiment, the liquefaction step is performed by a liquefier 9. The liquefier 9 is configured to liquefy the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separator 8 using the cold energy of the first heat transfer medium expanded in the expander 7.

[0031] In the illustrated embodiment, the liquefier 9 includes a cooler 91 configured to perform heat exchange between a first heat transfer medium flowing through the expansion gas line 31A and carbon dioxide gas separated from the absorbent liquid in the separator 8. Through heat exchange in the cooler 91, the first heat transfer medium flowing through the expansion gas line 31A is heated, and the carbon dioxide gas is cooled and liquefied. The cooler 91 is provided between the expander 7 and the low-temperature side heat exchange section 61 (heat exchanger 6) of the expansion gas line 31A and includes a first heat transfer medium side heat exchange section 92 through which the first heat transfer medium expanded in the expander 7 flows, and a carbon dioxide gas side heat exchange section 93 through which carbon dioxide gas separated from the absorbent liquid in the separator 8 is introduced via the gas line 94 and through which the carbon dioxide gas flows. Heat is transferred from the carbon dioxide gas flowing through the carbon dioxide gas side heat exchange section 93 to the first heat transfer medium flowing through the first heat transfer medium side heat exchange section 92. A compressor 941 configured to increase the pressure of the carbon dioxide gas flowing through the gas line 94 may be installed in the gas line 94. The compressor 941 may be an electric compressor connected to and driven by an electric motor 942. The carbon dioxide gas pressurized by the compressor 941 flows downstream (towards the carbon dioxide gas side heat exchange section 93) through the gas line 94.

[0032] During the compression, cooling, expansion, separation, and liquefaction steps, the transport vehicle 2 is positioned at a location within the premises of the plant 10 where the carbon dioxide recovery device 1 is installed, allowing for the connection of piping between the transport vehicle and the carbon dioxide recovery device 1. The gas line 94 is a line for guiding carbon dioxide gas from the regeneration tower 14 to the carbon dioxide gas-side heat exchange section 93. The gas line 94 is connected before the compression, cooling, expansion, separation, and liquefaction steps are performed, and after the transport vehicle 2 has moved to the plant 10. The gas line 94, compressor 941, and electric motor 942 may be provided by the carbon dioxide recovery device 1 or by the transport vehicle 2.

[0033] The carbon dioxide recovery method may further include a transport step of transporting the liquefied carbon dioxide from the liquefaction step to a destination 100 (supply destination or storage destination) for the liquid carbon dioxide. The carbon dioxide liquefied in the cooler 91 (liquefaction unit 9) is stored in the storage tank 4. The liquid carbon dioxide stored in the storage tank 4 is transported by the transport vehicle 2 to the destination 100 for the liquid carbon dioxide.

[0034] In some embodiments, the transport vehicle 2, as shown in Figure 2, comprises the above-described chiller 3, which includes a compressor 5, a heat exchanger 6, an expander 7, a separator 8, and a liquefaction unit 9, and the above-described storage tank 4. In addition, the carbon dioxide recovery method in some embodiments comprises the above-described carbon dioxide extraction step, compression step, cooling step, expansion step, separation step, and liquefaction step.

[0035] According to the above configuration (method), in the liquefaction step, the cold energy of the first heat transfer medium expanded in the expander 7 of the refrigerator 3 is used as a cold source, thereby liquefying the carbon dioxide gas separated from the absorbent liquid or adsorbent. Furthermore, in the separator 8 (separation step), the heat energy of the first heat transfer medium compressed in the compressor 5, which is the waste heat of the refrigerator 3, is used as a heat source, thereby separating the carbon dioxide gas from the absorbent liquid or adsorbent. In this case, since the waste heat of the refrigerator 3 is used, the load on the boiler equipment that supplies the heat source to the absorbent liquid or adsorbent can be reduced, or the boiler equipment can be made unnecessary. According to the above configuration (method), since both the heat source and the cold source can be supplied from the refrigerator 3, it is possible to suppress the enlargement and complexity of the equipment (plant) 10 for recovering carbon dioxide contained in the exhaust gas.

[0036] Furthermore, according to the above configuration (method), even without installing a refrigerator in the carbon dioxide recovery equipment described above, a heat source can be supplied to the absorbent liquid or adsorbent from the refrigerator 3 mounted on the transport vehicle 2, and a cooling source can be supplied to the carbon dioxide gas. Therefore, according to the above configuration (method), it is not necessary to install a refrigerator in the carbon dioxide recovery equipment (plant) 10 described above, thus suppressing the increase in size and complexity of the equipment.

[0037] Figure 4 is a schematic diagram showing a regeneration tower 14, a separator 8, and a drive unit side heat exchanger 22A according to one embodiment of the present disclosure. In some embodiments, as shown in Figure 4, the separator 8 described above includes a heater 81A configured to perform heat exchange between the absorbent liquid or adsorbent and the first heat transfer medium to heat the absorbent liquid or adsorbent. The liquefier 9 described above includes a cooler 91 configured to perform heat exchange between the first heat transfer medium and carbon dioxide gas to cool the carbon dioxide gas, as shown in Figure 2.

[0038] In the illustrated embodiment, the regeneration tower 14 is provided with an absorbent liquid circulation line 141 that returns the absorbent liquid stored inside the regeneration tower 14 to the regeneration tower 14 after it has been withdrawn from the regeneration tower 14. The heater 81A (separator 8) is installed between the compressor 5 and the precooler 63 of the compressed gas line 31B (circulation line 31). Heat exchange in the heater 81A cools the first heat transfer medium flowing through the compressed gas line 31B and heats the absorbent liquid flowing through the absorbent liquid circulation line 141.

[0039] The heater 81A includes a first heat medium side heat exchange section 82A through which a first heat medium flows, located between the compressor 5 and the precooler 63 of the compressed gas line 31B, and an absorbent liquid side heat exchange section 83A through which absorbent liquid flows, located in the absorbent liquid circulation line 141. Heat is transferred from the first heat medium flowing through the first heat medium side heat exchange section 82A to the absorbent liquid flowing through the absorbent liquid side heat exchange section 83A. The absorbent liquid heated in the heater 81A is guided to the regeneration tower 14 via the absorbent liquid circulation line 141, thereby heating the absorbent liquid inside the regeneration tower 14 and separating the carbon dioxide gas absorbed by the absorbent liquid.

[0040] In the illustrated embodiment, the cooler 91 (liquefier 9) is installed between the expander 7 and the low-temperature side heat exchange section 61 (heat exchanger 6) of the expansion gas line 31A (circulation line 31). Through heat exchange in the cooler 91, the first heat transfer medium flowing through the expansion gas line 31A is heated, and the carbon dioxide gas is cooled and liquefied.

[0041] The cooler 91 is provided between the expander 7 and the low-temperature side heat exchange section 61 of the expansion gas line 31A and includes a first heat medium side heat exchange section 92 through which the first heat medium expanded in the expander 7 flows, and a carbon dioxide gas side heat exchange section 93 through which carbon dioxide gas separated from the adsorbent in the separator 8 is introduced via the gas line 94 and the carbon dioxide gas flows. Heat is transferred from the carbon dioxide gas flowing through the carbon dioxide gas side heat exchange section 93 to the first heat medium flowing through the first heat medium side heat exchange section 92.

[0042] In the above configuration, heat exchange occurs directly between the absorbent liquid or adsorbent and the first heat transfer medium in the heater 81A. Heat exchange occurs directly between the first heat transfer medium and carbon dioxide gas in the cooler 91. In this case, by reducing the number of heat exchangers that make up the refrigerator 3, it is possible to suppress the increase in size, complexity, and cost of the refrigerator 3.

[0043] In some embodiments, as shown in Figure 4, the refrigerator 3 described above may further include a drive unit-side heat exchanger 22A configured to heat the absorbent liquid or adsorbent using the thermal energy of the drive unit 20 (see Figure 3) for driving the transport vehicle 2.

[0044] The drive unit 20 includes a drive force generating unit configured to generate driving force for the transport vehicle 2, such as an engine or fuel cell, and a drive force transmission unit configured to transmit the driving force generated by the drive force generating unit, such as a drive shaft, to the wheels. The refrigerator 3 may further include an exhaust gas introduction passage 201 for guiding exhaust gas generated in at least one of the drive force generating unit or the drive force transmission unit of the drive unit 20 to the drive unit side heat exchanger 22A.

[0045] The drive unit-side heat exchanger 22A is located upstream of the absorbent liquid-side heat exchange section 83A of the absorbent liquid circulation line 141. Heat exchange in the drive unit-side heat exchanger 22A heats the absorbent liquid flowing through the absorbent liquid circulation line 141.

[0046] The drive unit side heat exchanger 22A includes an exhaust gas side heat exchange section 221 through which exhaust gas introduced from the drive unit 20 to the drive unit side heat exchanger 22A via an exhaust gas introduction passage 201 flows, and an absorbent liquid side heat exchange section 222 through which absorbent liquid flows, which is located upstream of the absorbent liquid side heat exchange section 83A of the absorbent liquid circulation line 141. Heat is transferred from the exhaust gas flowing through the exhaust gas side heat exchange section 221 to the absorbent liquid flowing through the absorbent liquid side heat exchange section 222.

[0047] According to the above configuration, the heat exchanger 22A on the drive unit side can use the waste heat (thermal energy) from the drive unit 20 of the transport vehicle 2 as a heat source to heat the absorbent liquid or adsorbent. In this case, the thermal energy supplied from the refrigerator 3 to the absorbent liquid or adsorbent as a heat source can be reduced, thereby increasing the energy efficiency of the refrigerator 3 and reducing the running costs of the refrigerator 3.

[0048] Figure 5 is a schematic diagram showing a regeneration tower 14, a separator 8, and a drive unit side heat exchanger 22B according to one embodiment of the present disclosure. In some embodiments, as shown in Figures 2 and 5, the separator 8 described above includes a heater 81B configured to perform heat exchange between a second heat medium and a first heat medium, to which thermal energy is transferred to an absorbent liquid or adsorbent, thereby heating the second heat medium. The liquefier 9 described above includes a cooler 91 configured to perform heat exchange between a first heat medium and carbon dioxide gas, thereby cooling the carbon dioxide gas, as shown in Figure 2.

[0049] In the illustrated embodiment, the regeneration tower 14 is provided with an absorbent liquid circulation line 141 that returns the absorbent liquid stored inside the regeneration tower 14 to the regeneration tower 14 after it has been withdrawn from the regeneration tower 14. The chiller 3 further includes a second heat medium side circulation line 84 configured to circulate the second heat medium. The second heat medium side circulation line 84 is provided with a pump 85 for pressurizing the second heat medium. The second heat medium side circulation line 84 may also be provided with a buffer tank 86 for storing the second heat medium. The heater 81B (separator 8) is provided between the compressor 5 and the precooler 63 of the compressed gas line 31B (circulation line 31). Heat exchange in the heater 81B cools the first heat medium flowing through the compressed gas line 31B and heats the second heat medium flowing through the second heat medium side circulation line 84.

[0050] The heater 81B includes a first heat medium side heat exchange section 82B through which a first heat medium flows, located between the compressor 5 and the precooler 63 of the compressed gas line 31B, and a second heat medium side heat exchange section 83B through which a second heat medium flows, located in the second heat medium side circulation line 84. Heat is transferred from the first heat medium flowing through the first heat medium side heat exchange section 82A to the second heat medium flowing through the second heat medium side heat exchange section 83B.

[0051] The regeneration tower 14 or refrigerator 3 includes an absorbent side heater 142 configured to perform heat exchange between the absorbent liquid and the second heat transfer medium, thereby heating the absorbent liquid. The absorbent side heater 142 performs heat exchange between the second heat transfer medium, which is heated in the second heat transfer medium side heat exchange section 83B flowing through the second heat transfer medium side circulation line 84, and the absorbent liquid flowing through the absorbent liquid circulation line 141, thereby heating the absorbent liquid flowing through the absorbent liquid circulation line 141 with the thermal energy of the second heat transfer medium. The absorbent liquid heated in the absorbent side heater 142 is then guided to the regeneration tower 14 via the absorbent liquid circulation line 141, thereby heating the absorbent liquid inside the regeneration tower 14 and separating the carbon dioxide gas absorbed by the absorbent liquid.

[0052] According to the above configuration, in the heater 81B, heat exchange occurs between the second heat transfer medium, which transfers thermal energy to the absorbent liquid or adsorbent, and the first heat transfer medium. In other words, heat exchange occurs indirectly between the absorbent liquid or adsorbent and the first heat transfer medium via the second heat transfer medium (intermediate heat transfer medium). In this case, the robustness of the first heat transfer medium against fluctuations in thermal energy can be improved, and the refrigerator 3 can be operated stably.

[0053] In some embodiments, as shown in Figure 5, the chiller 3 described above may further include a drive unit-side heat exchanger 22B configured to heat a second heat transfer medium with the thermal energy of a drive unit 20 (see Figure 3) for driving a transport vehicle 2. The chiller 3 may further include an exhaust gas introduction channel 202 for guiding exhaust gas generated in at least one of the drive force generating section or drive force transmission section of the drive unit 20 to the drive unit-side heat exchanger 22B.

[0054] The drive unit-side heat exchanger 22B is located downstream of the absorbent liquid-side heater 142 in the second heat medium-side circulation line 84, and upstream of the second heat medium-side heat exchange section 83B. Heat exchange in the drive unit-side heat exchanger 22B heats the absorbent liquid flowing through the second heat medium-side circulation line 84.

[0055] The drive unit side heat exchanger 22B includes an exhaust gas side heat exchange section 223 through which exhaust gas introduced from the drive unit 20 to the drive unit side heat exchanger 22B via an exhaust gas introduction passage 202 flows, and a second heat medium side heat exchange section 224 through which a second heat medium flows, located downstream of the absorbent liquid side heater 142 and upstream of the second heat medium side heat exchange section 83B in the second heat medium side circulation line 84. Heat is transferred from the exhaust gas flowing through the exhaust gas side heat exchange section 223 to the second heat medium flowing through the second heat medium side heat exchange section 224.

[0056] According to the above configuration, the drive unit-side heat exchanger 22B can use the waste heat (thermal energy) from the drive unit 20 of the transport vehicle 2 as a heat source to heat the second heat transfer medium. In this case, the thermal energy supplied from the refrigerator 3 to the absorbent liquid or adsorbent as a heat source can be reduced, thereby increasing the energy efficiency of the refrigerator 3 and reducing the running costs of the refrigerator 3.

[0057] (Liquid carbon dioxide introduction line) In some embodiments, as shown in Figure 2, the chiller 3 described above further includes a liquid carbon dioxide introduction line 95 for guiding the liquid carbon dioxide liquefied in the liquefier 9 to the storage tank 4.

[0058] With the above configuration, the liquid carbon dioxide liquefied in the liquefier 9 can be directly guided to the storage tank 4 via the liquid carbon dioxide introduction line 95, thereby suppressing the need to increase the size and complexity of the chiller 3. The liquid carbon dioxide introduction line 95 may also be equipped with a pump for pressurizing the liquid carbon dioxide. Furthermore, the gas line 94 may be equipped with a compressor or blower for pressurizing the carbon dioxide gas.

[0059] (Absorbent liquid storage tank) In some embodiments, the transport vehicle 2 described above further comprises an absorbent liquid side storage tank 23 configured to store the absorbent liquid, as shown in Figure 6. In the illustrated embodiment, the absorbent liquid side storage tank 23 is mounted on the cargo bed 21 of the transport vehicle 2. The transport vehicle 2 is configured to move to the plant 10 with the absorbent liquid that has not absorbed carbon dioxide stored in the absorbent liquid side storage tank 23.

[0060] According to the above configuration, once the absorbent liquid absorbs a certain amount of carbon dioxide, it becomes unable to absorb any more carbon dioxide. By exchanging the absorbent liquid stored in the absorbent liquid-side storage tank 23, which has not absorbed carbon dioxide, with the absorbent liquid stored in the carbon dioxide recovery equipment (plant) 10, the time required to restore the carbon dioxide absorption capacity of the absorbent liquid can be shortened compared to the separation of carbon dioxide gas by heating in the separator 8. This makes it possible to increase the amount of carbon dioxide recovered by the absorbent liquid in the above equipment.

[0061] (Reliquefaction equipment) Figure 7 is a schematic diagram showing a transport vehicle 2 according to one embodiment of the present disclosure. In some embodiments, the transport vehicle 2 described above further includes a reliquefaction device 24 configured to reliquefy the vaporized carbon dioxide gas in the storage tank 4 using the cold energy of the first heat transfer medium expanded in the expander 7, as shown in Figure 7.

[0062] According to the above configuration, when liquid carbon dioxide is transported by the transport vehicle 2, the liquid carbon dioxide inside the storage tank 4 is vaporized by heat input from outside the storage tank 4, generating boil-off gas (carbon dioxide gas vaporized in the storage tank 4), and the pressure inside the storage tank 4 increases. The reliquefaction device 24 can suppress the pressure increase inside the storage tank 4 by reliquefying the boil-off gas.

[0063] In some embodiments, the reliquefaction apparatus 24 described above includes a reliquefaction unit 241 that performs heat exchange between the first heat transfer medium expanded in the expander 7 and the carbon dioxide gas vaporized in the storage tank 4, as shown in Figure 7.

[0064] In the illustrated embodiment, the storage tank 4 has a reliquefaction line 242 that guides the boil-off gas from the storage tank 4 to the reliquefied gas reliquidator 241, and the liquid carbon dioxide liquefied from the boil-off gas in the reliquefied gas reliquidator 241 back to the storage tank 4. In the illustrated embodiment, the reliquefied gas reliquidator 241 is located between the expander 7 and the low-temperature side heat exchange section 61 (heat exchanger 6) of the expansion gas line 31A (circulation line 31). Heat exchange in the reliquefied gas reliquidator 241 heats the first heat transfer medium flowing through the expansion gas line 31A, and cools and liquefies the boil-off gas. The reliquefied gas reliquidator 241 may be located either upstream or downstream of the cooler 91 in the expansion gas line 31A, or it may be located in a bypass line that bypasses the cooler 91 in the expansion gas line 31A.

[0065] The reliquefied unit 241 is installed between the expander 7 and the low-temperature side heat exchange unit 61 of the expansion gas line 31A. It includes a first heat medium side heat exchange unit 241A through which the first heat medium expanded in the expander 7 flows, and a carbon dioxide gas side heat exchange unit 241B through which carbon dioxide gas (boil-off gas) introduced from the storage tank 4 via the reliquefied line 242 flows. Heat is transferred from the carbon dioxide gas flowing through the carbon dioxide gas side heat exchange unit 241B to the first heat medium flowing through the first heat medium side heat exchange unit 241A.

[0066] According to the above configuration, the reliquefied unit 241 can liquefy boil-off gas (carbon dioxide gas vaporized in the storage tank 4) by utilizing the cold energy of the first heat transfer medium expanded in the expander 7 of the refrigerator 3 as a cold source. In this case, the transport vehicle 2 does not need dedicated equipment for liquefying boil-off gas. According to the above configuration, the transport vehicle 2 can be made larger and less complex.

[0067] In some embodiments, the compressor 5 described above includes an electric compressor configured to be driven by an electric motor 52 with variable output. The reliquefaction device 24 described above further includes a pressure acquisition unit (e.g., a pressure sensor) 243 configured to acquire the pressure inside the storage tank 4, as shown in Figure 7, and a control device 244 configured to adjust the output of the electric motor 52 according to the pressure inside the storage tank 4 acquired by the pressure acquisition unit 243. The control device 244 consists of a control unit for controlling the output of the electric motor 52. The control device 244 adjusts the output of the electric motor 52 in steps or continuously according to the pressure inside the storage tank 4 acquired by the pressure acquisition unit 243.

[0068] According to the above configuration, when boil-off gas (carbon dioxide gas vaporized in the storage tank 4) is generated, the pressure inside the storage tank 4 increases in proportion to the amount of boil-off gas generated. Here, the amount of boil-off gas generated fluctuates depending on the ambient temperature, etc. The pressure acquisition unit 243 monitors the pressure inside the storage tank 4, and the control device 244 increases the output of the electric motor 52 according to the gradient (degree of increase) of the pressure rise inside the storage tank 4, thereby increasing the cooling energy in the re-liquefier 241. In this case, by adjusting the output of the electric motor 52 with the control device 244, the boil-off gas can be efficiently re-liquefied in the re-liquefier 241 in accordance with the amount of boil-off gas generated.

[0069] Figure 8 is an explanatory diagram illustrating an example of the arrangement of equipment, a first tank 101 and a second tank 102 in a carbon dioxide transport method according to one embodiment of the present disclosure. Figures 9 to 11 are each explanatory diagram illustrating a carbon dioxide transport method according to one embodiment of the present disclosure. A carbon dioxide recovery method according to some embodiments is a carbon dioxide transport method for transporting carbon dioxide, comprising a first transport step and a second transport step.

[0070] Liquid carbon dioxide is recovered in a facility (e.g., a plant) 10 for recovering carbon dioxide contained in the exhaust gas emitted from the combustion device 11. In the first transfer step described above, as shown in Figures 8 to 11, the liquid carbon dioxide recovered in the facility 10 is transferred from the facility 10 to a first tank (relay tank) 101 located at a remote location. The first tank 101 stores liquid carbon dioxide recovered from multiple facilities 10. The location of the first tank 101 is outside the premises of the facility 10.

[0071] The first transfer step described above includes a transport vehicle transport step in which liquid carbon dioxide is stored in a storage tank 4 mounted on the transport vehicle 2 described above, and the liquid carbon dioxide stored in the storage tank 4 is transported by the transport vehicle 2 to the first tank 101. At facility 10, the liquid carbon dioxide recovered at facility 10 is transferred to the storage tank 4 mounted on the transport vehicle 2. The transport vehicle 2 transports the liquid carbon dioxide stored in the storage tank 4 to the first tank 101. Specifically, the transport vehicle 2 is driven from facility 10 to the installation site of the first tank 101, and at the installation site of the first tank 101, liquid carbon dioxide is transferred from the storage tank 4 to the first tank 101. By repeatedly transporting liquid carbon dioxide by the transport vehicle 2, liquid carbon dioxide is collected in the first tank 101 from multiple facilities 10.

[0072] In the transport vehicle step, liquid carbon dioxide may be recovered from the carbon dioxide recovery device 1 of the facility 10 which does not have a refrigerator 3 using a transport vehicle 2 equipped with a refrigerator 3 and a storage tank 4, or liquid carbon dioxide may be recovered from the carbon dioxide recovery device 1 of the facility 10 which has a refrigerator 3 using a transport vehicle 2A which does not have a refrigerator 3 but has a storage tank 4.

[0073] The first tank 101 is designed to store liquid carbon dioxide recovered from multiple facilities 10 by multiple transport vehicles 2 and 2A. The first tank 101 is equipped with a reliquefaction device 111 configured to reliquefy the boil-off gas formed by the vaporization of liquid carbon dioxide inside the first tank 101. The first tank 101 is installed in a location that reduces the time required for transporting liquid carbon dioxide from the facilities 10 by transport vehicles 2 and 2A compared to the second tank 102, which will be described later.

[0074] In the second transfer step described above, as shown in Figures 8 to 11, liquid carbon dioxide is transferred from the first tank 101 to the second tank (port tank) 102 via a first pipeline 103 connecting the first tank 101 to the second tank 102, which is located at a remote location from the first tank 101. The second tank 102 is capable of storing the liquid carbon dioxide transferred via the pipeline 103 from each of the multiple first tanks 101 located at various locations. In the illustrated embodiment, each of the multiple first tanks 101 is located at a distance of 10 km or more in a straight line from the second tank 102. Each of the multiple first tanks 101 is located closer to the facility 10 in a straight line than the second tank 102.

[0075] As shown in Figure 8, the multiple first pipelines 103 connecting each of the multiple first tanks 101 to the second tank 102 may have junctions P1 and P2 with other first pipelines 103, and the piping between the junctions P1 and P2 and the second tank 102 may be shared with other first pipelines 103. Furthermore, the multiple first pipelines 103 connecting each of the multiple first tanks 101 to the second tank 102 may be configured to include a relay line 103A connecting one of the multiple first tanks 101 to another first tank 101.

[0076] The second tank 102 is equipped with a reliquefaction device 112 configured to reliquefy the boil-off gas formed by the vaporization of liquid carbon dioxide inside the second tank 102. The second tank 102 is installed in a location suitable for transporting the liquid carbon dioxide stored in the second tank 102. In the illustrated embodiment, the second tank 102 is installed in a bay area. The bay area is defined as an area within 50 km in a straight line from a mooring place where the ship 110 can dock. It is preferable that the second tank 102 be installed near a mooring place, and in one embodiment, it is installed within 10 km in a straight line from a mooring place. In this case, by installing the second tank 102 in a bay area, the liquid carbon dioxide stored in the second tank 102 can be easily transferred to the ship 110. The ship 110 can then transport the liquid carbon dioxide to various destinations. In some other embodiments, the liquid carbon dioxide stored in the second tank 102 may be transported by railcar. In this case, the second tank 102 is preferably located within 50 km (preferably within 10 km) in a straight line from a station where railcars can be parked.

[0077] A carbon dioxide recovery method according to several embodiments comprises a first transfer step including the transport vehicle step described above, and a second transfer step described above. According to the above method, by including the first transfer step, the liquid carbon dioxide recovered in the facility 10 can be collected in the first tank 101 by the transport vehicle 2 or the like. Then, by including the second transfer step, the liquid carbon dioxide collected in the first tank 101 can be transferred to the second tank 102 via the first pipeline 103. In this case, by temporarily collecting the liquid carbon dioxide recovered in the facility 10 in the first tank 101, it becomes possible to recover liquid carbon dioxide more efficiently than when the liquid carbon dioxide is directly transferred from the facility 10 to the second tank 102. For example, it becomes unnecessary to transport the liquid carbon dioxide from the facility 10 to the second tank 102 by the transport vehicle 2.

[0078] In some embodiments, as shown in Figure 8, the first transfer step described above may further include a pipeline transfer step in addition to the transport vehicle transfer step described above. In the pipeline transfer step, liquid carbon dioxide is transported from the large-scale equipment 10B, 10C to the first tank 101 via second pipelines 103B, 103C that connect the large-scale equipment 10B, 10C, which recover carbon dioxide contained in the exhaust gas discharged from the combustion device 11 that discharges a predetermined amount or more of exhaust gas, to the first tank 101.

[0079] For small-scale facilities 10 (10A) where the exhaust gas emissions from the combustion device 11 are less than a predetermined amount, for example, less than 300 tpd (tons per day), transporting liquid carbon dioxide from the first tank 101 is preferable to be done by transport vehicles 2 and 2A in terms of transport costs. For large-scale facilities 10 (10B, 10C) where the exhaust gas emissions from the combustion device 11 are greater than or equal to a predetermined amount, for example, 300 tpd (tons per day) or more, transporting liquid carbon dioxide from the first tank 101 is preferable to be done by second pipelines 103B and 103C in terms of transport costs compared to transport vehicles 2 and 2A.

[0080] Examples of large-scale facilities 10 (10B, 10C) include a cement plant 10B and a steel mill 10C. The second pipelines 103B and 103C include pipeline 103B connecting the first tank 101 to the cement plant 10B and pipeline 103C connecting the first tank 101 to the steel mill 10C. The second pipelines 103B and 103C may also be configured to merge with the first pipeline 103.

[0081] According to the above method, in the large-scale facilities 10B and 10C, a large amount of liquid carbon dioxide is recovered in proportion to the large amount of exhaust gas discharged from the combustion device 11. When transporting large amounts of carbon dioxide, transport via the second pipelines 103B and 103C is preferable in terms of transport costs than transport by transport vehicles 2 and 2A.

[0082] In some embodiments, as shown in Figure 8, at least one of the first tanks 101 is installed, corresponding to each of the multiple recovery areas A1 to A7 that have been pre-divided into administrative districts. In the first transfer step described above, liquid carbon dioxide is transferred from the equipment 10 located in each of the multiple recovery areas A1 to A7 (e.g., A1) to the first tank 101 corresponding to the recovery area where the equipment 10 is located (e.g., A1). Preferably, the first tanks 101 corresponding to each of the multiple recovery areas A1 to A7 are installed in the corresponding recovery areas.

[0083] According to the method described above, in each administrative district (recovery areas A1 to A7), the liquid carbon dioxide recovered by the equipment 10 located in the recovery area (for example, A1) can be collected in the first tank 101 corresponding to that recovery area (for example, A1). By collecting liquid carbon dioxide for each administrative district (recovery areas A1 to A7), the administrative body responsible for recovering liquid carbon dioxide from each equipment 10 becomes clear, and the recovery of liquid carbon dioxide can be carried out efficiently.

[0084] As shown in Figure 8, the multiple collection areas A1 to A7, which are divided by administrative district, may also be divided by prefecture. In this case, by collecting liquid carbon dioxide in the corresponding first tank 101 for each prefecture, it becomes possible to efficiently recover liquid carbon dioxide.

[0085] In some embodiments, as shown in Figures 9 and 10, the second transfer step described above includes a pipeline-side vaporization step in which a pipeline-side vaporizer 104 vaporizes the liquid carbon dioxide flowing through the first pipeline 103, and a pipeline-side liquefaction step in which a pipeline-side liquefaction device 105 liquefies the carbon dioxide gas vaporized in the pipeline-side vaporization step.

[0086] The pipeline-side vaporizer 104 is installed on the first tank 101 side (near the first tank 101) of the first pipeline 103. The pipeline-side vaporizer 104 may be, for example, a compressor configured to pressurize and vaporize the liquid carbon dioxide flowing through the first pipeline 103. The pipeline-side liquefier 105 is installed on the second tank 102 side (near the second tank 102) of the first pipeline 103. The piping between the pipeline-side vaporizer 104 and the pipeline-side liquefier 105 of the first pipeline 103 is configured to carry carbon dioxide gas, which is the result of the liquid carbon dioxide vaporizing in the pipeline-side vaporizer 104. The pipeline-side liquefier 105 may be, for example, a refrigerator configured to cool and liquefy the carbon dioxide gas.

[0087] Furthermore, in order to promote the liquefaction of carbon dioxide gas in the pipeline-side liquefier 105, a pipeline-side pressure reducer 106 (106A, 106B) configured to reduce the pressure of carbon dioxide gas may be installed between the pipeline-side vaporizer 104 and the pipeline-side liquefier 105 of the first pipeline 103. The pipeline-side pressure reducer 106 may be, for example, a pressure reducing valve 106A as shown in Figure 8. In this case, the carbon dioxide gas reduced in pressure by the pipeline-side pressure reducer 106 is introduced into the pipeline-side liquefier 105.

[0088] According to the above method, gaseous carbon dioxide, which has been vaporized from liquid carbon dioxide, can be transferred in the first pipeline 103. Specifically, in the first pipeline 103, the gaseous carbon dioxide vaporized in the pipeline-side vaporizer 104 can be sent toward the second tank 102. Then, in the first pipeline 103, the carbon dioxide gas flowing through the first pipeline 103 can be liquefied by the pipeline-side liquefier 105 before being introduced into the second tank 102. In this case, compared to the case where liquid carbon dioxide is transferred in liquid form in the first pipeline 103, the influence of heat input from outside the first pipeline 103 is smaller, and therefore, insulation treatment for the first pipeline 103 can be omitted.

[0089] In some embodiments, as shown in Figure 9, the second transfer step described above further includes a pipeline-side depressurization step in which the carbon dioxide gas vaporized in the pipeline-side vaporization step is depressurized by a pipeline-side expander 106B to which a generator 107 is connected. That is, the pipeline-side depressurizer 106 described above may be a pipeline-side expander 106B.

[0090] According to the method described above, by using a pipeline-side expander 106B connected to a generator 107 to reduce the pressure of carbon dioxide gas flowing through the first pipeline 103, electricity can be recovered by the generator 107. By supplying the electricity recovered by the generator 107 to the reliquefaction device 111 of the first tank 101, the reliquefaction device 112 of the second tank 102, or the pipeline-side liquefier 105, the power required to drive these devices and equipment can be reduced.

[0091] In some embodiments, as shown in Figure 10, the second transfer step described above involves transferring liquid carbon dioxide in liquid form from the first tank 101 to the second tank 102. That is, liquid carbon dioxide flows through the first pipeline 103. To suppress heat input from outside the first pipeline 103 to the liquid carbon dioxide flowing through the first pipeline 103, it is preferable that an insulating material 108 covering the outer surface of the first pipeline 103 is attached to the outer surface.

[0092] According to the method described above, liquid carbon dioxide can be transported in liquid form in the first pipeline 103, so the diameter of the piping constituting the first pipeline 103 can be reduced compared to when carbon dioxide gas is transported in the first pipeline 103. The second pipelines 103B and 103C may be configured to transport liquid carbon dioxide in liquid form, similar to the first pipeline 103, or they may be configured to transport vaporized carbon dioxide gas.

[0093] In this specification, expressions describing relative or absolute arrangements such as "in a certain direction," "along a certain direction," "parallel," "orthogonal," "center," "concentric," or "coaxial" shall not only describe such arrangements strictly, but also describe states of relative displacement with tolerances or angles or distances that allow for the same function to be achieved. For example, expressions such as "identical," "equal," and "homogeneous" that describe things being in an equal state not only describe a state of being strictly equal, but also describe a state in which there is a tolerance or a difference that is sufficient to achieve the same function. Furthermore, in this specification, expressions describing shapes such as quadrilaterals and cylindrical shapes shall not only represent geometrically precise quadrilaterals and cylindrical shapes, but also shapes that include uneven surfaces, chamfered surfaces, etc., to the extent that the same effect can be achieved. Furthermore, in this specification, the expressions “equipment,” “includes,” or “possess” of a component are not exclusive expressions that exclude the existence of other components.

[0094] This disclosure is not limited to the embodiments described above, but also includes modified forms of the embodiments described above, as well as forms that combine these forms as appropriate.

[0095] The contents described in some of the embodiments above can be understood, for example, as follows:

[0096] 1) A transport vehicle (2) according to at least one embodiment of the present disclosure is A transport vehicle (2) for transporting liquid carbon dioxide, A refrigerator (3) for liquefying carbon dioxide gas, A storage tank (4) configured for storing liquid carbon dioxide is provided, The aforementioned refrigerator (3) is A compressor (5) configured to compress a first heat transfer medium, A heat exchanger (6) configured to cool the first heat transfer medium compressed in the compressor (5), An expander (7) configured to expand the first heat transfer medium cooled in the heat exchanger (6), A separator (8) is configured to separate carbon dioxide gas from an absorbent liquid that has absorbed carbon dioxide or an adsorbent that has adsorbed carbon dioxide, using the thermal energy of the first heat transfer medium compressed in the compressor (5), The system includes a liquefaction unit (9) configured to liquefy the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separator (8) using the cold energy of the first heat transfer medium expanded in the expander (7).

[0097] According to the configuration described in 1) above, the liquefier (9) can liquefy carbon dioxide gas separated from the absorbent liquid or adsorbent by utilizing the cold energy of the first heat transfer medium expanded in the expander (7) of the refrigerator (3) as a cold source. In addition, the separator (8) can separate carbon dioxide gas from the absorbent liquid or adsorbent by utilizing the thermal energy of the first heat transfer medium compressed in the compressor (5), which is the waste heat of the refrigerator (3), as a heat source. In this case, since the waste heat of the refrigerator (3) is used, the load on the boiler equipment that supplies the heat source to the absorbent liquid or adsorbent can be reduced, or the boiler equipment can be made unnecessary. According to the configuration described in 1) above, since both the heat source and the cold source can be supplied from the refrigerator (3), it is possible to suppress the enlargement and complexity of the equipment (10) for recovering carbon dioxide contained in the exhaust gas.

[0098] Furthermore, according to the configuration in 1) above, even without installing a refrigerator in the carbon dioxide recovery equipment described above, a heat source can be supplied to the absorbent liquid or adsorbent from the refrigerator (3) mounted on the transport vehicle (2), and a cooling source can be supplied to the carbon dioxide gas. Therefore, according to the configuration in 1) above, it is not necessary to install the refrigerator in the carbon dioxide recovery equipment described above, thus preventing the equipment from becoming larger or more complex.

[0099] 2) In some embodiments, the transport vehicle is as described in 1) above, The separator (8) includes a heater (81A) configured to perform heat exchange between the absorbent liquid or adsorbent and the first heat transfer medium, thereby heating the absorbent liquid or adsorbent. The liquefier (9) includes a cooler (91) configured to perform heat exchange between the first heat transfer medium and the carbon dioxide gas to cool the carbon dioxide gas.

[0100] According to the configuration described in 2) above, heat exchange occurs directly between the absorbent liquid or adsorbent and the first heat transfer medium in the heater (81A). Heat exchange occurs directly between the first heat transfer medium and carbon dioxide gas in the cooler (91). In this case, by reducing the number of heat exchangers that make up the refrigerator (3), it is possible to suppress the increase in size, complexity, and cost of the refrigerator (3).

[0101] 3) In some embodiments, the transport vehicle is as described in 1) above, The separator (8) includes a heater (81B) configured to perform heat exchange between a second heat transfer medium and a first heat transfer medium, thereby heating the second heat transfer medium, to which thermal energy is transferred to the absorbent liquid or the adsorbent. The liquefier (9) includes a cooler (91) configured to perform heat exchange between the first heat transfer medium and the carbon dioxide gas to cool the carbon dioxide gas.

[0102] According to the configuration described in 3) above, heat exchange occurs in the heater (81B) between the second heat transfer medium, which transfers thermal energy to the absorbent liquid or adsorbent, and the first heat transfer medium. In other words, heat exchange occurs indirectly between the absorbent liquid or adsorbent and the first heat transfer medium via the second heat transfer medium (intermediate heat transfer medium). In this case, the robustness of the first heat transfer medium against fluctuations in thermal energy can be improved, and the operation of the refrigerator (3) can be made stable.

[0103] 4) In some embodiments, the transport vehicle (2) described in 2) above, The refrigerator (3) further includes a drive unit-side heat exchanger (22A) configured to heat the absorbent liquid or adsorbent material using the thermal energy of the drive unit (20) for driving the transport vehicle (2).

[0104] According to the configuration described in 4) above, the heat exchanger (22A) on the drive unit side can use the waste heat (thermal energy) from the drive unit (20) of the transport vehicle (2) as a heat source to heat the absorbent liquid or adsorbent. In this case, the thermal energy supplied from the refrigerator (3) to the absorbent liquid or adsorbent as a heat source can be reduced, thereby increasing the energy efficiency of the refrigerator (3) and reducing the running costs of the refrigerator (3).

[0105] 5) In some embodiments, the transport vehicle (2) described in 3) above, The refrigerator (3) further includes a drive unit-side heat exchanger (22B) configured to heat the second heat transfer medium with the thermal energy of the drive unit (20) for driving the transport vehicle (2).

[0106] According to the configuration in 5) above, the heat exchanger (22B) on the drive unit side can use the waste heat (thermal energy) from the drive unit (20) of the transport vehicle (2) as a heat source to heat the second heat transfer medium. In this case, the thermal energy supplied from the refrigerator (3) to the absorbent liquid or adsorbent as a heat source can be reduced, thereby increasing the energy efficiency of the refrigerator (3) and reducing the running costs of the refrigerator (3).

[0107] 6) In some embodiments, the transport vehicle (2) is as described in any of 1) to 5) above, The refrigerator (3) further includes a liquid carbon dioxide introduction line (95) for guiding the liquid carbon dioxide liquefied in the liquefier (9) to the storage tank (4).

[0108] According to the configuration described in 6) above, the liquid carbon dioxide liquefied in the liquefier (9) can be directly guided to the storage tank (4) via the liquid carbon dioxide introduction line (95), thereby suppressing the need to increase the size and complexity of the chiller (3).

[0109] 7) In some embodiments, the transport vehicle (2) is as described in any of 1) to 6) above, The system further includes an absorbent liquid side storage tank (23) configured to store the absorbent liquid.

[0110] According to the configuration described in 7) above, once the absorbent liquid has absorbed a certain amount of carbon dioxide, it becomes unable to absorb any more carbon dioxide. By exchanging the absorbent liquid stored in the absorbent liquid-side storage tank (23) that has not absorbed carbon dioxide with the absorbent liquid stored in the carbon dioxide recovery equipment (10), the time required to restore the carbon dioxide absorption capacity of the absorbent liquid can be shortened compared to the separation of carbon dioxide gas by heating in the separator (8). This makes it possible to increase the amount of carbon dioxide recovered by the absorbent liquid in the above equipment.

[0111] 8) In some embodiments, the transport vehicle (2) is as described in any of 1) to 7) above, The system further includes a reliquefaction device (24) configured to reliquefy the vaporized carbon dioxide gas in the storage tank (4) using the cold energy of the first heat transfer medium expanded in the expander (7).

[0112] According to the configuration described in 8) above, when liquid carbon dioxide is transported by the transport vehicle (2), the liquid carbon dioxide inside the storage tank (4) is vaporized by heat input from outside the storage tank (4), generating boil-off gas (carbon dioxide gas vaporized in the storage tank 4), and causing the pressure inside the storage tank (4) to rise. The boil-off gas is reliquefied by the reliquefaction device (24), thereby suppressing the rise in pressure inside the storage tank (4).

[0113] 9) In some embodiments, the transport vehicle (2) described in 8) above, The reliquefaction apparatus (24) includes a reliquefier (241) that performs heat exchange between the first heat transfer medium expanded in the expander (7) and the carbon dioxide gas vaporized in the storage tank (4).

[0114] According to the configuration in 9) above, the reliquefied gas (241) can liquefy the boil-off gas (carbon dioxide gas vaporized in the storage tank 4) by utilizing the cold energy of the first heat transfer medium expanded in the expander (7) of the refrigerator (3) as a cold source. In this case, the transport vehicle (2) does not need dedicated equipment for liquefying the boil-off gas. According to the configuration in 9) above, the transport vehicle (2) can be made larger and less complex.

[0115] 10) In some embodiments, the transport vehicle (2) described in 9) above, The compressor (5) includes an electric compressor configured to be driven by an electric motor (52) with a variable output, The aforementioned reliquefaction device (24) A pressure acquisition unit (243) is configured to acquire the internal pressure of the storage tank (4), The system further includes a control device (244) configured to adjust the output of the electric motor (52) according to the pressure inside the storage tank (4) acquired by the pressure acquisition unit (243).

[0116] According to the configuration described in 10) above, when boil-off gas (carbon dioxide gas vaporized in the storage tank 4) is generated, the pressure inside the storage tank (4) rises in proportion to the amount of boil-off gas generated. Here, the amount of boil-off gas generated fluctuates depending on the ambient temperature, etc. The pressure acquisition unit (243) monitors the pressure inside the storage tank (4), and the control device (244) increases the output of the electric motor (52) according to the gradient (degree of increase) of the pressure rise inside the storage tank (4), thereby increasing the cooling energy in the re-liquefier (241). In this case, by adjusting the output of the electric motor (52) with the control device (244), the boil-off gas can be efficiently re-liquefied in the re-liquefier (241) in accordance with the amount of boil-off gas generated.

[0117] 11) A carbon dioxide recovery method according to at least one embodiment of the present disclosure is A carbon dioxide recovery method for recovering carbon dioxide contained in exhaust gas emitted from a combustion device (11), A carbon dioxide extraction step in which carbon dioxide contained in the exhaust gas is absorbed into an absorbent liquid, or carbon dioxide is adsorbed onto an adsorbent, A compression step in which the first heat transfer medium is compressed by the compressor (5) of a refrigerator (3) mounted on a transport vehicle (2) for transporting liquid carbon dioxide, A cooling step in which the first heat transfer medium compressed in the compressor is cooled by the heat exchanger (6) of the refrigerator (3), An expansion step in which the first heat transfer medium cooled in the heat exchanger is expanded by the expander (7) of the refrigerator (3), A separation step in which carbon dioxide gas is separated from the absorbent liquid that has absorbed the carbon dioxide or the adsorbent that has adsorbed the carbon dioxide by the thermal energy of the first heat transfer medium compressed in the compressor (5), The system includes a liquefaction step in which the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separation step is liquefied by the cold energy of the first heat transfer medium expanded in the expander (7).

[0118] According to the method described in 11) above, in the liquefaction step, the cold energy of the first heat transfer medium expanded in the expander (7) of the refrigerator (3) is used as a cold energy source, thereby liquefying the carbon dioxide gas separated from the absorbent liquid or adsorbent. Furthermore, in the separation step, the thermal energy of the first heat transfer medium compressed in the compressor (5), which is the waste heat of the refrigerator (3), is used as a heat source, thereby separating the carbon dioxide gas from the absorbent liquid or adsorbent. In this case, since the waste heat of the refrigerator (3) is used, the load on the boiler equipment supplying the heat source can be reduced, or the boiler equipment can be made unnecessary. According to the method described in 11) above, since both the heat source and the cold energy source can be supplied from the refrigerator (3), it is possible to suppress the need for equipment to recover carbon dioxide contained in the exhaust gas, which can be enlarged and made more complex.

[0119] Furthermore, according to the method described in 11) above, even without installing a refrigerator in the carbon dioxide recovery equipment described above, a heat source can be supplied to the absorbent liquid or adsorbent from the refrigerator (3) mounted on the transport vehicle (2), and a cooling source can be supplied to the carbon dioxide gas. Therefore, according to the method described in 11) above, it is not necessary to install the refrigerator in the carbon dioxide recovery equipment described above, thus preventing the equipment from becoming larger or more complex.

[0120] 12) A carbon dioxide recovery method according to at least one embodiment of the present disclosure is A method for transporting carbon dioxide, A first transfer step involves transferring the liquid carbon dioxide recovered in equipment (10) for recovering carbon dioxide contained in exhaust gas discharged from a combustion device (11) to a first tank (101) installed at a remote location, The system includes a second transfer step of transferring the liquid carbon dioxide from the first tank (101) to the second tank (102) via a first pipeline (103) connecting the first tank (101) and the second tank (102) located remotely from the first tank (101), The first transfer step is, The process includes a transport vehicle step in which the liquid carbon dioxide is stored in a storage tank (4) mounted on a transport vehicle (2), and the liquid carbon dioxide stored in the storage tank (4) is transported by the transport vehicle (2) to the first tank (101).

[0121] According to the method described in 12) above, by including a first transfer step, the liquid carbon dioxide recovered in the equipment (10) can be collected in a first tank (101) by a transport vehicle (2), etc. Then, by including a second transfer step, the liquid carbon dioxide collected in the first tank (101) can be transferred to a second tank (102) via a first pipeline (103). In this case, by temporarily collecting the liquid carbon dioxide recovered in the equipment (10) in the first tank (101), it becomes possible to recover liquid carbon dioxide more efficiently than when the liquid carbon dioxide is directly transferred from the equipment (10) to the second tank (102).

[0122] 13) In some embodiments, the carbon dioxide transport method described in 12) above, The second transfer step is: A pipeline-side vaporization step is performed by vaporizing the liquid carbon dioxide flowing through the first pipeline (103) using a pipeline-side vaporizer (104), The system includes a pipeline-side liquefaction step in which a pipeline-side liquefaction unit (105) liquefies the carbon dioxide gas vaporized in the pipeline-side vaporization step.

[0123] According to the method described in 13) above, gaseous carbon dioxide, which has been vaporized from liquid carbon dioxide, can be transported in the first pipeline (103). Specifically, in the first pipeline (103), gaseous carbon dioxide, vaporized in the pipeline-side vaporizer (104), can be sent toward the second tank (102). Then, in the first pipeline (103), the carbon dioxide gas flowing through the first pipeline (103) can be liquefied by the pipeline-side liquefier (105) and then introduced into the second tank (102). In this case, compared to the case where liquid carbon dioxide is transported in liquid form in the first pipeline (103), the influence of heat input from outside the first pipeline (103) is smaller, so insulation treatment for the first pipeline (103) can be omitted.

[0124] 14) In some embodiments, the carbon dioxide transport method described in 13) above, The second transfer step is: The pipeline-side depressurization step further includes depressurizing the carbon dioxide gas vaporized in the pipeline-side vaporization step using a pipeline-side expander (106B) connected to a generator (107).

[0125] According to the method described in 14) above, by using a pipeline-side expander (106B) connected to a generator (107) to reduce the pressure of carbon dioxide gas flowing through the first pipeline (103), electricity can be recovered by the generator (107). By supplying the electricity recovered by the generator (107) to the reliquefaction device (111) of the first tank (101), the reliquefaction device (112) of the second tank (102), or the pipeline-side liquefier (105), the power required to drive these devices and equipment can be reduced.

[0126] 15) In some embodiments, the carbon dioxide transport method described in 12) above, In the second transfer step described above, The liquid carbon dioxide is transferred in liquid form from the first tank (101) to the second tank (102).

[0127] According to the method described in 15) above, liquid carbon dioxide can be transported in liquid form in the first pipeline (103), so the diameter of the piping constituting the first pipeline (103) can be reduced compared to the case where carbon dioxide gas is transported in the first pipeline (103).

[0128] 16) In some embodiments, the carbon dioxide transport method described in any of 12) to 15) above, The first transfer step is, The present invention further includes a pipeline transport step of transporting the liquid carbon dioxide from the large-scale equipment (10B, 10C) to the first tank (101) via a second pipeline (103B, 103C) that connects the large-scale equipment (10B, 10C) for recovering carbon dioxide contained in the exhaust gas discharged from the combustion device (11) which discharges an amount greater than a predetermined amount of exhaust gas to the first tank (101).

[0129] According to the method described in 16) above, in large-scale facilities (10B, 10C), a large amount of liquid carbon dioxide is recovered in proportion to the large amount of exhaust gas discharged from the combustion device (11). When transporting large amounts of carbon dioxide, transport via the second pipeline (103B, 103C) is preferable to transport by transport vehicles (2, 2A) in terms of transport costs.

[0130] 17) In some embodiments, a carbon dioxide transport method according to any one of 12) to 16) above, At least one of the first tanks (101) is installed in each of the multiple collection areas (A1 to A7) that have been pre-divided into administrative districts. In the first transfer step, the liquid carbon dioxide is transferred from the equipment (10) for recovering carbon dioxide located in each of the plurality of recovery areas (A1 to A7) (for example, A1) to the first tank (101) corresponding to the recovery area (A1) where the equipment (10) is located.

[0131] According to the method described in 17) above, in each administrative district (recovery areas A1 to A7), the liquid carbon dioxide recovered at the equipment (10) located in the recovery area (for example, A1) can be collected in the first tank (101) corresponding to that recovery area (for example, A1). By collecting liquid carbon dioxide for each administrative district (recovery areas A1 to A7), the administrative body responsible for recovering liquid carbon dioxide from each piece of equipment becomes clear, and the recovery of liquid carbon dioxide becomes more efficient.

[0132] 18) In some embodiments, the carbon dioxide transport method described in 17) above, The aforementioned collection areas are divided by prefecture.

[0133] According to the method described in 18) above, liquid carbon dioxide can be collected in the corresponding first tank (101) for each prefecture, making it possible to efficiently recover liquid carbon dioxide.

[0134] 19) In some embodiments, the carbon dioxide transport method described in any of 12) to 18) above, The aforementioned second tank (102) was installed in the bay area.

[0135] According to the method described in 19) above, by installing the second tank (102) in the bay area, the liquid carbon dioxide stored in the second tank (102) can be easily transferred to the ship (110). The ship (110) can then transport the liquid carbon dioxide to various destinations. [Explanation of symbols]

[0136] 1. Carbon dioxide capture device 2,2A Transport Vehicle 3. Refrigeration unit 4 Storage tanks 5. Compressor 6 Heat exchanger 7. Inflator 8 Separator 9 Liquefier 10 Equipment 11 Combustion device 12 Absorption Towers 13 Cooling Tower 14 Regeneration Tower 20 Drive unit 21 Cargo bed 22A, 22B Drive unit side heat exchanger 23 Absorbent liquid side storage tank 24,111,112 Reliquefaction equipment 31 Circulation Line 31A Expansion gas line 31B Compressed Gas Line 51 Rotating shaft 52 Electric motor 61 Low-temperature side heat exchange section 62 High temperature side heat exchange section 63 Pre-cooler 81A,81B Heater 82A, 82B, 92, 241A 1st heat medium side heat exchange section 83A,222 Absorbent liquid side heat exchange section 83B,224 2nd heat medium side heat exchange section 84 Second heat transfer fluid side circulation line 85 pumps 86 Buffer Tank 91 Cooler 93,241B Carbon dioxide gas side heat exchange section 94 Gas Line 95 Liquid carbon dioxide introduction line 100 destinations 101 Tank No. 1 102 Tank No. 2 103 Pipelines 104 Pipeline-side vaporizer 105 Pipeline-side liquefier 106 Pipeline-side pressure reducer 106A Pressure Reducing Valve 106B Pipeline-side expander 107 Generator 108 Insulation 110 Ships 131 Cooling water circulation line 132 Cooling water cooler 141 Absorbent fluid circulation line 142 Absorbent liquid side heater 201,202 Exhaust gas introduction path 221,223 Exhaust gas side heat exchange section 241 Reliquefier 242 Reliquefaction Line 243 Pressure acquisition unit 244 Control device

Claims

1. A transport vehicle for transporting liquefied carbon dioxide, which supplies a heat source for separating carbon dioxide gas and a cooling source for liquefying the separated carbon dioxide gas to an external facility where a carbon dioxide recovery device is installed, having an absorbent liquid or an adsorbent material for adsorbing carbon dioxide contained in exhaust gas discharged from a combustion device, A refrigerator for liquefying the aforementioned carbon dioxide gas, A storage tank configured to store the aforementioned liquid carbon dioxide, The aforementioned refrigerator is A compressor configured to compress a first heat transfer medium, A heat exchanger configured to cool the first heat transfer medium compressed in the compressor, An expander configured to expand the first heat transfer medium cooled in the heat exchanger, A separator configured to separate carbon dioxide gas from the absorbent liquid or adsorbent of the carbon dioxide recovery device by the thermal energy of the first heat transfer medium compressed in the compressor, The liquefaction includes a liquefaction unit configured to liquefy the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separator using the cold energy of the first heat transfer medium expanded in the expander, Transport vehicle.

2. The separator includes a heater configured to perform heat exchange between the absorbent liquid or adsorbent and the first heat transfer medium, thereby heating the absorbent liquid or adsorbent. The liquefaction includes a cooler configured to perform heat exchange between the first heat transfer medium and the carbon dioxide gas and to cool the carbon dioxide gas. The transport vehicle according to claim 1.

3. The separator includes a heater configured to perform heat exchange between a second heat transfer medium, which transfers thermal energy to the absorbent liquid or the adsorbent, and the first heat transfer medium, thereby heating the second heat transfer medium. The liquefaction includes a cooler configured to perform heat exchange between the first heat transfer medium and the carbon dioxide gas and to cool the carbon dioxide gas. The transport vehicle according to claim 1.

4. The refrigerator further includes a drive unit-side heat exchanger configured to heat the absorbent liquid or adsorbent material using the thermal energy of the drive unit for driving the transport vehicle. The transport vehicle according to claim 2.

5. The refrigerator further includes a drive unit-side heat exchanger configured to heat the second heat transfer medium using the thermal energy of the drive unit for driving the transport vehicle. The transport vehicle according to claim 3.

6. The refrigerator further includes a liquid carbon dioxide introduction line for guiding the liquid carbon dioxide liquefied in the liquefier to the storage tank. A transport vehicle according to any one of claims 1 to 5.

7. The system further comprises an absorbent liquid side storage tank configured to store the absorbent liquid. A transport vehicle according to any one of claims 1 to 5.

8. The device further comprises a reliquefaction apparatus configured to reliquefy the vaporized carbon dioxide gas in the storage tank using the cold energy of the first heat transfer medium expanded in the expansion machine. A transport vehicle according to any one of claims 1 to 5.

9. The reliquefaction apparatus includes a reliquefaction unit that performs heat exchange between the first heat transfer medium expanded in the expander and the carbon dioxide gas vaporized in the storage tank. The transport vehicle according to claim 8.

10. The compressor includes an electric compressor configured to be driven by an electric motor with a variable output, The aforementioned reliquefaction apparatus is A pressure acquisition unit configured to acquire the internal pressure of the storage tank, The control device further includes a control device configured to adjust the output of the electric motor according to the pressure inside the storage tank acquired by the pressure acquisition unit, The transport vehicle according to claim 9.

11. A carbon dioxide recovery method for recovering liquefied liquid carbon dioxide, comprising supplying a heat source for separating carbon dioxide gas and a cold source for liquefying the separated carbon dioxide gas to an external facility equipped with a carbon dioxide recovery device having an absorbent liquid for absorbing carbon dioxide contained in exhaust gas discharged from a combustion device, or an adsorbent material for adsorbing carbon dioxide, the method comprising: A carbon dioxide extraction step in which the carbon dioxide contained in the exhaust gas is absorbed by the absorbent liquid, or the carbon dioxide is adsorbed by the adsorbent, A compression step in which the first heat transfer medium is compressed by a compressor of a refrigerator mounted on a transport vehicle for transporting the aforementioned liquid carbon dioxide, A cooling step in which the first heat transfer medium compressed in the compressor is cooled by the heat exchanger of the refrigerator, An expansion step in which the first heat transfer medium cooled in the heat exchanger is expanded by the expander of the refrigerator, A separation step in which the thermal energy of the first heat transfer medium compressed in the compressor is used to separate the carbon dioxide gas from the absorbent liquid or adsorbent in the carbon dioxide recovery device, The system comprises a liquefaction step in which the carbon dioxide gas separated from the absorbent liquid or adsorbent in the separation step is liquefied by the cold energy of the first heat transfer medium expanded in the expansion machine, Methods for capturing carbon dioxide.

12. A method for transporting carbon dioxide, A first transfer step involves transferring the liquid carbon dioxide recovered in equipment for recovering carbon dioxide contained in exhaust gas discharged from a combustion device from the equipment to a first tank installed at a remote location, The system includes a second transfer step of transferring the liquid carbon dioxide from the first tank to the second tank via a first pipeline connecting the first tank and the second tank located at a remote location from the first tank, The first transfer step is, The transport vehicle includes a transport step of supplying the heating source and the cooling source to the equipment using the transport vehicle described in claim 1 to recover the liquid carbon dioxide, storing the liquid carbon dioxide in a storage tank mounted on the transport vehicle, and transporting the liquid carbon dioxide stored in the storage tank to the first tank using the transport vehicle. Methods for transporting carbon dioxide.

13. The second transfer step described above is: A pipeline-side vaporization step involves vaporizing the liquid carbon dioxide flowing through the first pipeline using a pipeline-side vaporizer, A pipeline-side liquefaction step includes liquefying the carbon dioxide gas vaporized in the pipeline-side vaporization step using a pipeline-side liquefaction device. The carbon dioxide transport method according to claim 12.

14. The second transfer step described above is: The pipeline-side depressurization step further includes depressurizing the carbon dioxide gas vaporized in the pipeline-side vaporization step using a pipeline-side expander connected to a generator. The carbon dioxide transport method according to claim 13.

15. In the second transfer step described above, The liquid carbon dioxide is transferred in liquid form from the first tank to the second tank. The carbon dioxide transport method according to claim 12.

16. The first transfer step is, The present invention further includes a pipeline transport step of transporting the liquid carbon dioxide from a large-scale facility to a first tank via a second pipeline connecting the large-scale facility to the first tank, which is used to recover carbon dioxide contained in exhaust gas emitted from a combustion device that emits an amount of exhaust gas exceeding a predetermined amount. The carbon dioxide transport method according to claim 12.

17. At least one of the aforementioned first tanks is installed in each of the multiple collection areas that have been pre-divided into administrative districts. In the first transfer step, the liquid carbon dioxide is transferred from the equipment for recovering carbon dioxide present in each of the plurality of recovery areas to the first tank corresponding to the recovery area where the equipment is located. A method for transporting carbon dioxide according to any one of claims 12 to 15.

18. The aforementioned collection areas are divided by prefecture. The carbon dioxide transport method according to claim 17.

19. The aforementioned second tank is installed in the bay area, A method for transporting carbon dioxide according to any one of claims 12 to 15.

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