Recovery system and method

Abstract

In order to recover carbon dioxide in a short time without reducing the operation rate of a moving body, this recovery system comprises: a packed bed attached to the moving body and containing an adsorbent that adsorbs carbon dioxide; and an attachment / detachment part provided on the moving body and to / from which the packed bed can be attached / detached.

Description

Recovery system and method

[0001] This disclosure relates to a recovery system and method.

[0002] Conventionally, recovery devices that are mounted on mobile vehicles to recover and separate carbon dioxide are known (for example, Patent Document 1).

[0003] Japanese Patent Publication No. 2023-147631

[0004] However, mounting a separation device to separate the captured carbon dioxide onto a mobile vehicle would increase the size of the device. On the other hand, if carbon dioxide is separated and recovered from the device mounted on the mobile vehicle at a recovery station, the recovery process may take a long time. As a result, the operational efficiency of the mobile vehicle may decrease. Therefore, there is a need for a recovery system that can recover carbon dioxide in a short time without reducing the operational efficiency of the mobile vehicle.

[0005] The recovery system comprises a packed bed attached to a mobile body and having an adsorbent material for adsorbing carbon dioxide, and a detachable part provided on the mobile body that allows the packed bed to be attached to and detached.

[0006] The recovery method includes sorbing carbon dioxide onto an adsorbent material in a packed bed attached to a mobile vehicle, and recovering carbon dioxide from the packed bed removed from the mobile vehicle in a stand-side system installed at a recovery stand.

[0007] According to this disclosure, carbon dioxide can be captured without reducing the operating rate of the mobile device.

[0008] The effects described above are merely illustrative for the sake of explanation and are not limiting. In addition to, or in lieu of, any other effects described herein or that would be obvious to those skilled in the art may be achieved.

[0009] This is a diagram showing an overview of the mobile system. This is a diagram showing an overview of the mobile system with the packed bed removed. This is a diagram showing an example of the stand system. This is a block diagram showing an example of the configuration of the processing device. This is a diagram illustrating the flow for recovering carbon dioxide. This is a diagram illustrating the flow for recovering carbon dioxide. This is a diagram illustrating the flow for recovering carbon dioxide. This is a diagram showing an overview of the mobile system according to another embodiment. This is a diagram showing an example of a recovery system equipped with a gas supply unit sweep gas supply unit.

[0010] Hereinafter, embodiments of the recovery system of this disclosure will be described with reference to the drawings. Common components in the drawings are denoted by the same reference numerals.

[0011] In this disclosure, "sorbition" is synonymous with "absorption" and "adsorption," and means the chemical or physical attachment of carbon dioxide, moisture, vapor, etc., to the material itself. For this reason, "sorbition" is primarily used, but "absorption" or "adsorption" may be used for explanatory purposes, but the meaning of the reaction is not different. Similarly, "release" is synonymous with "desorption," "desorption," and "dissipation," and means the separation of carbon dioxide, moisture, vapor, etc., from the material itself. For this reason, "release" is primarily used, but "desorption," "desorption," and "dissipation" may be used for explanatory purposes, but the meaning of the reaction is not different. Furthermore, "separation" means separating some of the components contained in the gas, and includes cases where separation occurs via the above-mentioned sorbition and release, and cases where separation occurs through the permeation of only the components without going through sorbition. Furthermore, in this disclosure, the gas discharged from the mobile body and taken into the recovery system is referred to as "gas" or "supply gas."

[0012] A recovery system is a system for capturing carbon dioxide. The recovery system implements at least one of a carbon dioxide capture method and a carbon dioxide utilization method. The carbon dioxide captured by the recovery system may be at least carbon dioxide contained in the gas emitted from the heat engine of a mobile vehicle. The carbon dioxide captured by the recovery system may also be carbon dioxide in the atmosphere or carbon dioxide contained in the air inside the cabin of the mobile vehicle. A mobile vehicle is an object capable of moving from a first point to a second point different from the first point using a heat engine. A heat engine is a prime mover that converts thermal energy into mechanical work. Examples of heat engines include gasoline engines, diesel engines, jet engines, and engines that use high-pressure gases such as heavy oil, liquefied natural gas, city gas, and propane gas as fuel. Examples of mobile vehicles include automobiles, motorcycles, trains, ships, aircraft, railcars, and construction machinery. Automobiles include trucks, buses, and garbage trucks.

[0013] Part of the recovery system is mounted on a mobile vehicle, while other parts are installed, for example, at a carbon dioxide recovery stand. Hereafter, the recovery system mounted on the mobile vehicle may be referred to as the mobile vehicle system, and the other parts installed at the recovery stand may be referred to as the stand system. In other words, the recovery system includes both the mobile vehicle system and the stand system.

[0014] The collection station is, for example, located next to a waste treatment plant. For instance, if the mobile unit is a garbage truck, the packed bed is removed from the mobile unit's system while the garbage truck is collecting waste at the waste treatment plant. The removed packed bed is then installed in the station's system, where carbon dioxide is recovered. The recovered carbon dioxide is then used to produce, for example, dry ice or methane gas.

[0015] Recycling stations may be located next to gas stations, bus and taxi stations, or delivery vehicle collection points, or they may be located in the parking lots of commercial facilities, businesses, factories, or shopping malls. To conserve energy during the recycling process, it is desirable to install the recycling station next to a heat source such as a factory, power plant, or boiler, so that the heat necessary for generating the steam required for recycling can be supplied to the recycling system. It is even more desirable to be able to use waste heat, low-temperature waste heat, solar heat, renewable energy, or non-fossil fuel electricity to generate the steam required for recycling, as this will lead to energy conservation and a reduction in carbon dioxide emissions.

[0016] Figure 1 shows an overview of the recovery system (mobile body side system) mounted on the mobile body. Figure 2 shows an overview of the mobile body side system in a state where the packed bed has been removed. The mobile body side system 100 includes, for example, a bypass 20, an inlet passage 30, a first cooling unit 40, a second cooling unit 50, a detachable unit 60, a packed bed 3, an outlet passage 70, an inlet passage valve 80, and an outlet passage valve 90.

[0017] The bypass 20 is a passage for taking in gas discharged from the exhaust pipe E of the mobile unit. The bypass 20 is connected to the exhaust pipe E, for example, via a connector C. This allows the bypass 20 to take in gas discharged from the mobile unit.

[0018] The inlet of the detour 20 that takes in exhaust gas and the outlet of the mobile unit's exhaust pipe E do not necessarily have to be physically connected. In other words, the inlet of the detour 20 and the outlet of the mobile unit's exhaust pipe E may be far apart. In this case, the detour 20 takes in air from the atmosphere along with the gas discharged from the mobile unit. The inlet of the detour 20 and the outlet of the mobile unit's exhaust pipe E may be, for example, several centimeters apart.

[0019] The detour 20 is a passage that guides the gas discharged from the heat engine of the mobile unit and the gas that has passed through the packed bed 3 into the atmosphere. In other words, the detour 20 is equipped with a passage that guides the taken-in gas into the atmosphere without guiding it to the packed bed 3. Equipment used for purposes other than carbon dioxide recovery, such as a muffler, may be attached to the detour 20. The detour 20 is, for example, made up of cylindrical pipe members with a circular cross-section.

[0020] The detour 20 includes a branching section 21 at a predetermined location and a merging section 22 located on the exit side of the predetermined location. In other words, the branching section 21 is located closer to the entrance than the merging section 22.

[0021] The branching section 21 is the part where the detour 20 and the inlet passage 30 are connected. That is, the detour 20 is connected to the inlet passage 30 at the branching section 21. The passage through which the gas taken in from the inlet of the detour 20 passes branches at the branching section 21. The merging section 22 is the part where the detour 20 and the outlet passage 70 are connected. That is, the detour 20 is connected to the outlet passage 70 at the merging section 22. Furthermore, the cross-sectional area d of the detour 20 at the merging section 22 may be configured to be smaller than the cross-sectional area D of the detour 20 at the branching section 21.

[0022] To effectively guide gas containing carbon dioxide from the branching section 21 to the packed bed 3, it is effective to design the system so that the pressure loss when a certain amount of gas is passed from the branching section 21 through the packed bed 3 to the confluence section 22 is smaller than the pressure loss when the same amount of gas is passed from the branching section 21 through the bypass 20 to the confluence section 22. To reduce pressure loss, it is effective to minimize bends in the piping from the branching section 21 through the packed bed 3 to the confluence section 22, including the branching section 21 and the confluence section 22, and to avoid reducing the diameter of the valve orifice or the piping. It is also effective to design the bypass 20 to include bends and orifices as needed, thereby increasing the relative pressure loss of the bypass 20.

[0023] The inlet passage 30 is a passage that guides the gas discharged from the heat engine of the mobile unit to the packed bed 3. In other words, the inlet passage 30 is a passage that guides the gas taken in by the bypass 20 to the packed bed 3. One end of the inlet passage 30 is connected to the bypass 20 at the branching section 21. The other end of the inlet passage 30 is connected to the second cooling section 50. The inlet passage 30 is, for example, made up of a cylindrical pipe member with a circular cross-section.

[0024] The first cooling unit 40 is a part that cools the gas passing through it. The first cooling unit 40 is installed, for example, in a position above the inlet passage 30. The first cooling unit 40 is, for example, a radiator. That is, when outside air hits the first cooling unit 40, the first cooling unit 40 dissipates heat and cools the gas passing through it. The first cooling unit 40 may cool the gas using cooling water used to cool a heat engine. The first cooling unit 40 may also cool the gas introduced to the packed bed 3 by utilizing the exhaust cooling heat generated in the mobile body. When, for example, high-pressure gas is used as fuel for the mobile body, the exhaust cooling heat is generated when the fuel expands. For example, when the mobile body uses compressed natural gas, liquefied natural gas, city gas, propane gas, etc. as fuel, the fuel is depressurized in the regulator (not shown). At this time, the fuel expands, causing the fuel temperature to drop. The resulting exhaust cooling heat is guided to the first cooling unit 40, thereby cooling the gas passing through the first cooling unit 40.

[0025] The second cooling section 50 is a part that cools the gas discharged from the heat engine of the mobile body by bringing it into contact with a liquid. One end of the second cooling section 50 is connected to the other end of the inlet passage 30 and takes in the gas passing through the inlet passage 30. A detachable section 60 is attached to the other end of the second cooling section 50. As will be described later, a connecting section (not shown) of the packed bed 3 is detachably connected to the detachable section 60. Therefore, the gas that has passed through the second cooling section 50 is taken into the packed bed 3 via the detachable section 60.

[0026] The second cooling unit 50 includes, for example, a storage unit for storing liquid, and brings the gas taken in from one end of the second cooling unit 50 into contact with the liquid stored in the storage unit. When a gas with a vapor pressure below the saturated vapor pressure of the liquid is passed through the liquid stored in the storage unit, the liquid evaporates. The gas is cooled by the heat of vaporization generated at this time. The second cooling unit 50 cools the gas passing through it to a temperature in the range of 0°C to 100°C. Preferably, the second cooling unit 50 cools the gas passing through it to a temperature in the range of 10°C to 70°C. In other words, the second cooling unit 50 cools the gas passing through it to a temperature near room temperature. More preferably, the second cooling unit 50 may cool the gas passing through it to a temperature in the range of 20°C to 60°C.

[0027] Furthermore, the humidity of the gas is adjusted as it passes through the liquid in the storage section. For example, the relative humidity of the gas is adjusted to 80% or higher as it passes through the liquid stored in the storage section.

[0028] The detachable section 60 is the part to which the packed bed 3 is detachably attached. The detachable section 60 is composed of, for example, a convex joint. An operator can, for example, attach the packed bed 3 to the detachable section 60 and remove the packed bed 3 from the detachable section 60 with a single touch. The second cooling section 50 and the packed bed 3 may be provided as a single unit. In this case, the detachable section 60 may be provided between the inlet passage 30 and the second cooling section 50. By integrating the second cooling section 50 and the packed bed 3, when the packed bed 3 is removed from the mobile system, adjustments can be made in the stand system, such as adding water to the second cooling section 50 or draining water from the second cooling section 50. For example, when the outside temperature is low, moisture from exhaust gases after combustion may accumulate in the second cooling section 50, increasing the amount of water. In this case, water is drained from the second cooling section 50 in the stand system. On the other hand, when the outside temperature is high, the water in the second cooling unit 50 may evaporate, potentially causing the amount of water to become too low. In this case, water is added to the second cooling unit 50 in the stand-side system.

[0029] The packed bed 3 is attached to the mobile body and has an adsorbent 33 that adsorbs carbon dioxide contained in the gas discharged from the heat engine of the mobile body. The adsorbent 33 effectively adsorbs gases with high carbon dioxide concentration and high humidity. The adsorbent 33 can adsorb carbon dioxide at least near atmospheric pressure. That is, the adsorbent 33 can adsorb carbon dioxide at least under an environment of 1 atmosphere or the exhaust pressure of the mobile body. Furthermore, the adsorbent 33 can adsorb carbon dioxide at least at room temperature. For example, the adsorbent 33 can adsorb carbon dioxide at temperatures in the range of at least -30° to 100°. The adsorbent 33 may also be able to adsorb carbon dioxide at temperatures in the range of at least 0° to 80°. Alternatively, the adsorbent 33 may be able to adsorb carbon dioxide at temperatures in the range of 10° to 60°. Preferably, the adsorbent 33 can adsorb carbon dioxide at temperatures in the range of 20° to 30°.

[0030] The packed bed 3 is a modular device composed of, for example, a substantially cylindrical housing 31 and an sorbent material 33 filled in the internal space 32 of the housing 31. That is, the packed bed 3 may consist of at least the housing 31. In the packed bed 3, the sorbent material 33 is used as a carbon dioxide separator. Multiple such configurations may be installed in parallel or in series. The packed bed 3 according to one embodiment can perform carbon dioxide sorbent and release under high humidity conditions. High humidity is, for example, a relative humidity of 60% or more. High humidity may be a relative humidity of 70% or more. Preferably, high humidity is a relative humidity of 80% or more. Thus, the packed bed 3 is configured to operate to separate carbon dioxide under high humidity conditions. Here, high humidity conditions further include, for example, a state in which the water vapor pressure of the supply gas at the inlet of the packed bed 3 or the steam supplied by the steam supply unit 4 described later is 80% or more of the saturated water vapor pressure. Alternatively, a high humidity state includes, for example, a state in which the water vapor pressure of the vapor is equal to or equal to the saturation water vapor pressure inside at least a part of the packed bed 3, or a state in which this may occur.

[0031] The housing 31 is made of a general synthetic resin, metal, or ceramic. In particular, when the housing 31 is made of synthetic resin, the weight of the packed layer 3 can be reduced. That is, since the sorbent material 33 according to this disclosure can sorb carbon dioxide at or near room temperature and near atmospheric pressure, there is no need to make the housing 31 out of heat-resistant or pressure-resistant material. As a result it is lightweight, and concerns about deterioration of the fuel efficiency of the mobile body due to an increase in the weight of the housing 31 are limited. The housing 31 is provided with connecting parts at both ends that can be connected to the detachable parts 60. For example, concave joints may be provided at both ends of the housing 31 as connecting parts. In this case, as described above, the detachable parts 60 are made out of convex joints into which the concave joints of the housing 31 are fitted.

[0032] The connecting parts provided at both ends of the housing 31 may be equipped with mechanical automatic on / off valves. For example, the automatic on / off valve opens when the housing 31 is attached to the attachment part 60 and closes when the housing 31 is removed from the attachment part 60. This prevents carbon dioxide adsorbed on the adsorbent material 33 from leaking out of the housing 31 when the housing 31 is removed from the attachment part 60.

[0033] The sorbent material 33 is a material that can sorb carbon dioxide under predetermined sorbent conditions and release carbon dioxide under predetermined release conditions. Here, the predetermined sorbent conditions are, for example, a relative humidity of 80% or more and a partial pressure of carbon dioxide gas of 0.04 kPa to 100 kPa. On the other hand, the predetermined release conditions may be set so that the partial pressure of carbon dioxide is lower than that of the sorbent conditions, or only the temperature is set higher than that of the sorbent conditions, or furthermore, the partial pressure may be set lower than that of the sorbent conditions while the temperature is set higher than that of the sorbent conditions.

[0034] More specifically, the sorbent 33 has a reversible gas absorption capacity that absorbs carbon dioxide from a supply gas containing a predetermined amount of moisture, and then releases the carbon dioxide due to a change in temperature or gas partial pressure. In particular, if the sorbent 33 can absorb carbon dioxide in a wet state, it is possible to efficiently utilize the phase transition heat of water vapor or water. Furthermore, the sorbent 33 may also have a reversible moisture absorption capacity that allows for the reversible absorption and release of moisture. To have these characteristics, for example, the sorbent 33 may be made by crushing a bulk gel made of a predetermined polymer material, or by using a gel formed from a gel particle solution containing the polymer material.Alternatively, the sorbent 33 may be an ion exchange resin such as an anion exchange resin, a polymer containing an amino group or ammonium group or quaternary ammonium group such as polyethyleneimine or polyvinylamine, or a medium-sized molecule such as oligoethyleneimine or ethanolamine, including ethanolamine, 2-(dimethylamino)ethanol (DMAE), isopropylaminoethanol (IPAE), 2-(2-aminoethylaminoethanol) (AEAE), diethylenetriamine (DETA), tris(2-aminoethyl)amine (TAEA), triethylenetetraamine (TAEA), tetraethylenepentamine (TEPA), N-butyldiethanolamine (NBDEA), 1-(2-hydroxyethyl)pyrrolidine (1-2HE-PRLD), It may also be low molecular weight amines such as 1-(2-aminoethyl)piperazine (AEPz), 1-(2-hydroxyethyl)piperidine (1-2HE-PP, TM-1), tetramethylene-1,4-diaminobutane (TM-1,4-DAB), N,N,N',N'-tetramethyl-1,6-hexanediamine (TMHAD), 4-amino-2,2,6,6-tetramethylpiperidine (TMPD), 3-(1-piperazinyl)-1,2-propanediol (PzPD), pentamethyldiethylenetriamine (PMDETA), oligoethyleneimine, etc. It may also be a porous material, such as activated carbon, porous silica, fumed silica, zeolite, MOF (Metal-Organic Framework), etc., and may contain alkalis such as calcium hydroxide and lithium hydroxide.

[0035] The specified polymer material includes, for example, (A) a polymer having a polymer chain containing structural units derived from a monofunctional monomer and a crosslinked structure derived from a polyfunctional monomer, and an amine derived from an amine-containing treatment solution, and (B) a polymer having a polymer chain containing structural units derived from a monofunctional monomer having an amino group and a crosslinked structure derived from a polyfunctional monomer, but without containing any components derived from an amine-containing treatment solution. The monofunctional monomer in embodiment (A) and the polyfunctional monomer in embodiment (B) may or may not have an amino group.

[0036] The specified polymer material selectively absorbs carbon dioxide by containing an amino group in at least one of the polymer's constituent units and the impregnated amine. Furthermore, heating causes a phase transition, such as a decrease in pKa and an increase in hydrophobic interactions between hydrophobic groups, which releases the absorbed acidic gas. In other words, the specified polymer material has reversible gas absorption capacity, selectively and reversibly absorbing carbon dioxide. In addition, the specified polymer material has low water content and swelling properties. Therefore, when the specified polymer material is used as a gas absorbent or gas separator, a sufficiently large volume packing density can be achieved. By using the specified polymer material, a sufficient gas flow path can be secured in the packed bed 3, and the amount of heat required for the heating process for gas release can be kept low.

[0037] Furthermore, even when liquid water is added to the absorbent material, the gaps between the water-containing polymers are maintained, ensuring a sufficient water flow path. Additionally, the subsequent gas flow allows for easy discharge of the water and introduction of gas into the gaps. Therefore, a given polymer material can be effectively used as a gas absorbent material for reversibly absorbing carbon dioxide, and this gas absorbent material can be effectively used as a gas separation material for separating acidic gases from a mixed gas.

[0038] The following describes the average molecular weight of the polymer contained in a given polymer material, the amount of each group if the polymer has amino groups or hydrophobic groups, the physical properties of the polymer, and the amine content if the polymer material contains amines.

[0039] The proportion of monomers having amino groups in all monomers can be, for example, 5 mol% to 100 mol%, or 30 mol% to 100 mol%, or 50 mol% to 90 mol%. When the polymer has a hydrophobic group, the amount of the hydrophobic group can be, for example, 0 mol% to 95 mol%, or 5 mol% to 70 mol%, or 10 mol% to 43 mol%. The degree of crosslinking of the polymer can be, for example, 0 mol% to 50 mol%, or 5 mol% to 40 mol%, or 10 mol% to 30 mol%. When the polymer material contains an amine, the content can be, for example, 1 to 30 mmol / g, or 2 to 20 mmol / g, or 3 to 10 mmol / g per dry weight of the polymer. Here, a monomer containing a quaternary ammonium group of an amino group may be used, or the amine grade may be increased by an alkylation reaction of the amine after synthesizing a polymer having an amino group.

[0040] The degree of swelling of the polymer contained in a predetermined polymer material can be evaluated, for example, by the water content when impregnated with water for a long time.

[0041] The polymer contained in a predetermined polymer material can have a water content, for example, of 4 grams / gram polymer or less, or 3 grams / gram polymer or less, or 2 grams / gram polymer or less when swollen with an excessive amount of water. Here, the "water content" of the polymer refers to the value obtained by the following formula (1) when the weight of the wet polymer after removing moisture by filtration using filter paper or a metal mesh after pulverizing the polymer added with an excessive amount of water and left standing overnight at room temperature is M1, and the weight of the polymer when the polymer is dried by freeze-drying or natural drying is M0. Water content = (M1 - M0) / M0...(1)

[0042] The polymer material can have a reversible carbon dioxide absorption amount of, for example, 15 mL / g or more, or 30 mL / g or more, or 60 mL / g or more per dry polymer weight. Thereby, for example, when the polymer material is applied to the recovery system 1 for recovering carbon dioxide from exhaust gas, carbon dioxide contained in the exhaust gas can be efficiently absorbed and recovered.

[0043] Further, in addition to the polymer material, the adsorbent 33 may contain, as other components, for example, moisture, pKa adjuster, absorption accelerator, diffusion accelerator, moisture absorbent, antioxidant, thermoplastic resin, filler, or the like.

[0044] The moisture can be intentionally added to the gas absorption material, for example, by using water or water vapor. When adding water, for example, carbon dioxide gas or bicarbonate ions can also be added.

[0045] The pKa adjuster can be added, for example, for the purpose of adjusting the pKa of the polymer after polymerization by adding it during polymerization. Thereby, the type of gas absorbed by the polymer, the types of gas and liquid selectively permeated by the gas absorption material, the permeation flux, the selectivity of the target gas for absorption relative to other gases, etc. can be controlled. As the pKa adjuster, for example, those capable of protonating or deprotonating the amino group of the polymer can be used, and acids such as hydrochloric acid or bases such as sodium hydroxide can be used with appropriately adjusted concentrations according to the desired pKa. Also, since the local environment such as the polymer density around the amine in the polymer, the distance between amines, and the polarity can be adjusted by the crosslinking rate with the polyfunctional monomer to control the pKa of the amine, the above polyfunctional monomer may be used also as the pKa adjuster. Further, since the local environment such as the polymer density around the amine, the distance between amines, and the polarity can be adjusted by adding hydrophobic monomers, alcohols, or hydrophilic polymers during polymerization to control the pKa of the amine, these may be used also as the pKa adjuster.

[0046] The absorption accelerator is a compound that has the function of promoting the absorption of acidic gas into the polymer of one embodiment. The release accelerator is a compound that has the function of promoting the release of acidic gas from the polymer. In one embodiment, an absorption-release accelerator having both the functions of an absorption accelerator and a release accelerator may be used. These absorption accelerators, release accelerators, and absorption-release accelerators may also function as stabilizers that stabilize the gas-absorbing material. The total content of the absorption accelerator, release accelerator, and absorption-release accelerator in the gas-absorbing material of one embodiment can be, for example, 0.05 mL or more, or 0.1 mL or more, per gram of solids. Furthermore, the content of the absorption accelerator in the gas-absorbing material can be, for example, 0.1 to 12 N, 1 to 10 N, or 3 to 9 N in terms of amine concentration.

[0047] Low molecular weight amines can be used as absorption enhancers, release enhancers, or absorption-release enhancers. The molecular weight of the low molecular weight amine may be, for example, 61 to 10,000, 75 to 1,000, or 90 to 500. The boiling point of the low molecular weight amine may be, for example, 80°C or higher, 120°C or higher, or 150°C or higher, as this is practical for long-term use. To raise the boiling point, an amine-containing compound that has a site that forms a salt with a counterion like an ionic liquid and is liquid may be used.

[0048] Low molecular weight amines may contain any of the following: primary amino groups, secondary amino groups, tertiary amino groups, primary ammonium groups, secondary ammonium groups, tertiary ammonium groups, quaternary ammonium groups, imidazolium groups, guanidium groups, piperidium groups, or 2,2,6,6-tetramethylpiperidium groups. Multiple amino groups, ammonium groups, imidazolium groups, and guanidium groups may be present, for example, one to three. Secondary and tertiary amino groups may also be cyclic amino groups. Furthermore, low molecular weight amines may contain functional groups other than amino groups, ammonium groups, imidazolium groups, and guanidium groups, such as hydroxyl groups. Low molecular weight amines may also be oligomers of ethyleneimine. Low molecular weight amines may contain zero to two hydroxyl groups. Examples of low molecular weight amines include amines having an amino group and a hydroxyl group, or amines having three amino groups; for example, amines having a secondary amino group and a hydroxyl group. In the high-concentration range, the amount of acidic gas released can be dramatically increased, and it is suitable for repeated use. For example, an amine having a secondary amino group and a hydroxyl group with a boiling point of 150°C or higher may be selected.

[0049] Examples of low molecular weight amines include ETA (Ethanol Amine), DMAE (2-(Dimethylamino)ethanol), and IPAE (Isopropyl amine). DMAEA (2-(Dimethylamino)ethylamine), TMEDA (Tetramethy TM-1,4-DAB (Tetramethylenediamine), TM HAD ('N,N,N',N'-Tetramethyl-1,6-hexanediamine), DEOA (Diethanol amine), MDEOA (N-Methyldiethanolamine), DAMDPA (Diamino-N-methyl dipropyl amine), 1-2HE-PRLD (1-2 Hydroxy ethylene pyrrolidine), 1-2HE-PP (1-2 Hydroxyethylepiperidine), Bis(2DMAE)ER(Bis(2-dimethylaminoethyl) ether), e(PMDETA)(Pentamethyldiethylenetriamine), AEAE(2-(2-Aminoethylamino)e thanol), TAEA (Tris(2-aminoethyl)amine), DETA (diethylenetriamine), tetraethylene Pentamine or TETA (Triethylene Tetramine) are available. In particular, DMAE, IPAE, Bis(2DMAE)ER, 1-2HE-PRLD, 1-2HE-PP, TM-1,4-DAB, TMHAD, and PMDETA may be selected because they can release a large amount of acidic gas. Among these, IPAE, Bis(2DMAE)ER, 1-2HE-PP, TM-1,4-DAB, TMHAD, and PMDETA may be selected because they have relatively high boiling points and do not evaporate easily. IPAE, TM-1,4-DAB, TMHAD, and PMDETA may also be selected because their concentration can be significantly increased to release acidic gas. IPAE, TMHAD, and PMDETA may also be selected because they are readily available.

[0050] The desiccant that can be used as an additive is, for example, one that, when prepared as a saturated aqueous solution, has a relative humidity of 80% or less at 25°C. Examples of such desiccant ions include bromide ions, chloride ions, acetate ions, carbonate ions, bicarbonate ions, lithium ions, potassium ions, calcium ions, magnesium ions, and sodium ions. Salts such as lithium bromide, lithium chloride, calcium chloride, potassium acetate, magnesium chloride, potassium carbonate, and sodium carbonate can also be used as desiccant ions. When adding a desiccant, the amount added can be, for example, 0.01 to 10% by mass of the total amount of gas absorbent material.

[0051] Antioxidants that can be used as additives are those that can suppress or prevent oxidation when added. Examples of such antioxidants include vitamin C (ascorbic acid), vitamin E (tocopherol), BHT (dibutylhydroxytoluene), BHA (butylhydroxyanisole), sodium erythorbate, propyl gallate, sodium sulfite, sulfur dioxide, hydroquinone, and its derivatives. When adding antioxidants, the amount added can be, for example, 0.01 to 10% by mass of the total amount of gas absorbent material.

[0052] The gas-absorbing material may contain a thermoplastic resin. This allows the thermoplastic resin to be kneaded with the polymer of one embodiment and other components added as needed to form pellets or films. Known thermoplastic resins can be used. For example, polyolefins such as polyethylene, polypropylene, and ethylene-vinyl acetate copolymers, modified polyolefins, polyamides, thermoplastic polyimides, liquid crystal polymers such as aromatic polyesters, polyphenylene oxide, polyphenylene sulfide, polycarbonate, polymethyl methacrylate, polyethers, polyetheretherketones, polyetherimides, polyacetals, styrene-based, polyolefin-based, polyvinyl chloride-based, polyurethane-based, polyester-based such as polyethyl polylactic acid, polyamide-based, polybutadiene-based, trans-polyisoprene-based, fluororubber-based, polyvinyl chloride, polyvinylidene chloride-based chlorinated polyethylene-based, and various thermoplastic elastomers, or copolymers, blends, polymer alloys mainly composed of these, and polyolefin resins such as polyethylene can be selected. When a thermoplastic resin is included in the gas-absorbing material, the amount of thermoplastic resin can be, for example, 10 to 40% by mass relative to the total amount of the gas-absorbing material.

[0053] The gas-absorbing material may contain a filler. This allows for the formation of voids in the gas-absorbing material, promoting the diffusion of gas into the material and improving the reversible absorption rate and amount of gas. Furthermore, by using a filler with gas adsorption capacity, it is possible to enable gas adsorption by the adsorbent in addition to the gas absorption of the absorbent material. Since gas adsorbents are known to exhibit high reversible gas adsorption capacity at low humidity and gas-absorbing materials exhibit high gas absorption performance at high humidity, using a gas adsorbent as a filler makes it possible to realize a material with high reversible gas adsorption capacity over a wide range of humidity conditions. As a filler with gas adsorption capacity, for example, materials with a large pore area such as various activated carbons and zeolites may be used. In particular, an adsorbent with high carbon dioxide gas adsorption capacity may be selected and used. In addition, if the polymer material constituting the gas-absorbing material is gelled with water or is a pulverized gelled polymer (polymer pulverized material), adding a filler reduces the bulk and increases the packing amount, thereby improving the reversible gas absorption capacity. Fine particles with a primary particle diameter of 1000 nm or less, as described later, can preferably be used as the filler. Furthermore, grinding the polymer pulverized material and the gas-absorbing material containing the filler can further improve its reversible gas absorption capacity. This grinding of the polymer pulverized material and the gas-absorbing material containing the filler can be carried out using a planetary ball mill device such as a bead mill.

[0054] To promote gas diffusion into the absorbent material, the filler may be selected in powder form. Alternatively, the primary particle diameter may be, for example, 1000 nm or less. The primary particle diameter can be measured by transmission electron microscopy. The fine particles with a primary particle diameter of 1000 nm or less used in one embodiment may consist only of fine particles with a primary particle diameter of 1000 nm or less. The particle size can be 0.1 nm to 1000 nm, or 0.3 nm to 500 nm, or 0.5 nm to 300 nm, or 1 nm to 200 nm, or 1.5 nm to 100 nm, or 2 nm to 50 nm, or 2.5 nm to 25 nm in average primary particle diameter. This tends to lead to a more reliable formation of the gas diffusion phase in the molded body of the gas absorbent material, and a greater improvement in the gas absorption rate and emission rate. The fine particles may be aggregated primary particles. The aggregates are preferably 100 nm to 200 μm in size, more preferably 500 nm to 100 μm, and most preferably 2.5 μm to 50 μm. In addition, fillers with a water contact angle of, for example, 70° or more may be used. The water contact angle may be 80° or more, or 100° or more, or 110° or more, or 120° or more, or 130° or more, or 140° or more.

[0055] In the following, we will specifically describe fine particles with a primary particle diameter of 1000 nm or less that can be used as fillers. Fine particles with a primary particle diameter of 1000 nm or less may be composed of inorganic materials, organic materials, or a combination of organic and inorganic materials. Furthermore, the fine particles may be hydrophobic or hydrophilic, but hydrophobic fine particles are preferred. By being hydrophobic, the voids formed by the fine particles are prevented from being blocked by the moisture contained in the gas-absorbing material, and these voids function effectively as a gas diffusion phase.

[0056] Here, "water-repellent microparticles" refers to microparticles with a primary particle diameter of 1000 nm or less and a water contact angle of 70° or more. The "water contact angle" of microparticles refers to the contact angle with water measured on the surface of a microparticle deposition film formed by these microparticles. The water contact angle of the surface of the microparticle deposition film can be measured by measuring the static contact angle with water.

[0057] The water contact angle of the water-repellent fine particles is preferably 80° or more, more preferably 100° or more, even more preferably 110° or more, even more preferably 120° or more, particularly preferably 130° or more, and most preferably 140° or more.

[0058] Water-repellent fine particles with a primary particle diameter of 1000 nm or less may be fine particles that are water-repellent themselves, or they may be fine particles in which water repellency has been imparted to the surface of a base particle (base particle). Examples of fine particles in which water repellency has been imparted to the surface of a base particle include coated fine particles in which a water-repellent film has been formed on the surface of the base particle, and surface-modified fine particles in which surface modification has been applied to impart water repellency to the base particle.

[0059] First, carbon black can be cited as a fine particle that is itself water-repellent. Examples of carbon black include acetylene black, furnace black, channel black, thermal black, lamp black, and Ketjen black, among which acetylene black is preferred.

[0060] Other water-repellent microparticles include those made of Knobel® (porous carbon, manufactured by Toyo Tanso Co., Ltd.), titanium dioxide, mesoporous silica, etc. Furthermore, microparticles formed from water-repellent organic materials can also be used as microparticles that themselves possess water-repellent properties. Examples of water-repellent organic materials that can be used to form particles include -(CA １ A ２ -CA ３ A ４ Examples of fluororesins include those containing constituent units represented by ) (however, A １ ~A ４A represents a hydrogen atom, a fluorine atom, a chlorine atom, or a perfluoroalkyl group. １ ~A ４ (At least one of them is a fluorine atom.) Specific examples of fluororesins include polytetrafluoroethylene (PTFE), copolymers of tetrafluoroethylene and other monomers, polychlorotrifluoroethylene (PCTFE), copolymers of chlorotrifluoroethylene and other monomers, polyvinylidene fluoride (PVDF), polyvinyl fluoride (PVF), and polytetrafluoropropylene (PTFP). Examples of copolymers of tetrafluoroethylene and other monomers include perfluoroalkoxyalkane (PFA: copolymer of tetrafluoroethylene and perfluoroalkyl vinyl ether), perfluoroethylenepropene copolymer (FEP: copolymer of tetrafluoroethylene and hexafluoropropylene), ethylene-tetrafluoroethylene copolymer (ETFE), and tetrafluoroethylene-perfluorodioxole copolymer (TFE / PDD). An example of a copolymer of chlorotrifluoroethylene and other monomers is ethylene-chlorotrifluoroethylene copolymer (ECTFE). These water-repellent organic materials may be used individually or in combination of two or more types.

[0061] The base particles of the coated fine particles and surface-modified fine particles may be inorganic or organic particles, but inorganic particles are preferred. Furthermore, if fine particles that are themselves water-repellent are used as the base particles, and a water-repellent coating or surface modification that imparts water repellency is applied to these fine particles, the gas absorption rate and emission rate, as well as the amount of gas absorbed and emitted, can be improved.

[0062] As inorganic particles, known materials can be used, including carbon blacks such as acetylene black, furnace black, channel black, thermal black, lamp black, and Ketjen black; particles made of inorganic compounds such as oxides, hydroxides, nitrides, halides, carbonates, sulfates, acetates, and phosphates of metallic or metalloid elements; and natural mineral particles. Examples of inorganic compounds of metallic or metalloid elements include lithium fluoride, calcium carbonate, calcium phosphate, calcium sulfate, calcium fluoride, barium sulfate, titanium dioxide (titania), zirconium dioxide (zirconia), aluminum oxide (alumina), aluminosilicates (alumina silicate, kaolin, kaolinite), and silicon dioxide (silica, silica gel). Examples of natural minerals include talc and clay. Among these, particles made of carbon black and silicon dioxide are preferred.

[0063] Known organic particles can be used, including particles made of styrene-based, acrylic-based, melamine-based, benzoguanamine-based, and silicone-based polymers. Fillers may also be used in combination; for example, activated carbon and zeolite can be preferably used as fillers.

[0064] For the water-repellent coating formed on the base particles, in addition to the water-repellent organic materials exemplified as water-repellent materials that can be used to form fine particles, coatings of organopolysiloxanes and organohydrogenpolysiloxanes can be used. Examples of organopolysiloxanes include dialkylpolysiloxanes and alkylphenylpolysiloxanes, and examples of organohydrogenpolysiloxanes include alkylhydrogenpolysiloxanes. The alkyl groups in dialkylpolysiloxanes, alkylphenylpolysiloxanes, and alkylhydrogenpolysiloxanes may be linear, branched, or cyclic, but linear is preferred. The number of carbon atoms in the alkyl group is preferably 1 to 20, more preferably 1 to 10, and even more preferably 1 to 6. Here, the two alkyl groups bonded to the silicon atom may be the same or different. Specific examples of organopolysiloxanes include dimethylpolysiloxane and methylphenylpolysiloxane, while specific examples of organohydrogenpolysiloxanes include methylhydrogenpolysiloxane.

[0065] Surface modification methods for substrate particles include introducing water-repellent groups such as alkyl groups and alkyl fluoride groups onto the surface of the substrate particles. The alkyl groups and alkyl fluoride groups introduced into the substrate particles may be linear, branched, or cyclic, but linear is preferred. The number of carbon atoms in the alkyl groups and alkyl fluoride groups is preferably 1 to 20, more preferably 1 to 15, and even more preferably 1 to 10. Furthermore, the alkyl fluoride groups may be alkyl fluoride groups in which some of the hydrogen atoms of the alkyl group are replaced with fluorine atoms, or perfluoroalkyl groups in which all of the hydrogen atoms are replaced with fluorine atoms.

[0066] Surface modification to introduce these water-repellent groups into substrate particles can be carried out using silane coupling agents or silane compounds such as silazanes. Examples of silane coupling agents include compounds represented by the following general formula (2): R1nSiX(4-n)...(2) In general formula (2), X represents a hydrolyzable group that generates a silanol group by hydrolysis, and R1 represents a group containing a water-repellent group. n is an integer from 1 to 3. The silane coupling agent represented by general formula (2) introduces water-repellent groups into the substrate particles by the reaction of silanol groups or silyl groups generated by the hydrolysis of X with functional groups on the surface of the substrate particles.

[0067] In general formula (2), the "hydrolysis group that generates a silanol group" represented by X can be an alkoxy group such as a methoxy group or an ethoxy group, or a halogen group. Examples of hydrophobic groups in R1 can be an alkyl group, an alkyl fluoride group, or a dimethylsiloxane. For a description of alkyl groups and alkyl fluoride groups and their preferred ranges, refer to the description of hydrophobic groups that can be introduced onto the surface of the substrate particles and their preferred ranges. The hydrophobic group may be directly bonded to Si or bonded via a linking group.

[0068] n is an integer between 1 and 3, preferably 1 or 2. When n is 2 or greater, multiple R1s may be the same or different from each other. When n is 2 or less, multiple Xs may be the same or different from each other.

[0069] Examples of silane coupling agents represented by general formula (2) include triethoxyalkylsilane, diethoxydialkylsilane, ethoxytrialkylsilane, trimethoxyalkylsilane, dimethoxydialkylsilane, methoxytrialkylsilane, and trichloroalkylsilane. Specific examples of silane coupling agents include triethoxycaprylylsilane (triethoxy-n-octylsilane) and octadecyltrichlorosilane.

[0070] The formation of the water-repellent film on the above base material particles and the surface modification treatment can be carried out according to conventional methods. Examples of commercially available water-repellent fine particles include Microdispers-200 (manufactured by Technochemical Co., Ltd.), AEROSIL RY200, AEROSIL RY300, AEROSIL R805 (all manufactured by Evonik Industries AG), Ketjenblack (manufactured by Lion Specialty Chemicals Co., Ltd.), and the like. The above water-repellent fine particles may be used alone or in combination of two or more kinds.

[0071] The fine particles having a primary particle diameter of 1000 nm or less that can be used as a filler are not limited to water-repellent fine particles, and may be fine particles other than water-repellent fine particles, that is, fine particles having a water contact angle of less than 70°. Also, water-repellent fine particles and fine particles having a water contact angle of less than 70° may be used in combination. The fine particles having a water contact angle of less than 70° may have a water contact angle of 50° or less, 30° or less, or 10° or less. The lower limit value of the water contact angle of the fine particles is 0°.

[0072] Examples of the base material particles of the coated fine particles and the surface-modified fine particles as the fine particles other than the water-repellent fine particles are assumed, and particles composed of inorganic compounds of metal elements and metalloid elements and organic particles can be mentioned, and it is preferable to use silicon oxide particles. Further, these inorganic particles and organic particles may have an organic compound film formed on their surfaces or may have an organic functional group introduced. As a commercially available product of fine particles other than water-repellent fine particles, AEROSIL 200 (manufactured by Evonik Industries AG) can be mentioned.

[0073] The specific surface area of the fine particles is preferably 1 to 3000 m ２ / g, more preferably 2.5 to 2750 m ２ / g, and even more preferably 5 to 2500 m ２ / g. Thereby, a gas diffusion phase is more reliably formed in the molded body of the gas absorption material, and the gas absorption rate and the dissipation rate tend to be further improved. The specific surface area of the fine particles can be measured by the BET method.

[0074] The mixing ratio of polymer material to fine particles by weight of solid content (polymer material:fine particles) is preferably 95:5 to 5:95, more preferably 90:10 to 30:70, and even more preferably 80:20 to 50:50. Furthermore, the content of polymer material in the gas absorbent material is preferably greater than the content of water-repellent fine particles in terms of solid content. In addition, when the polymer material is gelled with water or is a pulverized gelled polymer, adding a filler to the gas absorbent material reduces the bulk, increases the filling capacity, and improves the reversible gas absorption capacity. To effectively obtain such effects, the volume ratio of gelled polymer or its pulverized material to fine particles (gelled polymer or its pulverized material:fine particles) is preferably 99.9:0.1 to 98:2, more preferably 99.75:0.25 to 98.5:1.5, and even more preferably 99.5:0.5 to 99:1. By setting the ratio of polymer material to fine particles within the above range, the gas absorption rate and emission rate tend to increase. However, the gas absorbing material of one embodiment is not limited to containing fine particles with a primary particle diameter of 1000 nm or less. In other words, the gas absorbing material of one embodiment does not need to contain fine particles with a primary particle diameter of 1000 nm or less.

[0075] In one embodiment, the gas-absorbing material can use known fillers in addition to the fine particles exemplified above. For example, activated carbon, zeolite, silica, fumed silica, hydrophobic silica, hydrophobic fumed silica, hydrophobic silica, alumina, hydrophobic alumina, hydrophobic alumina, boehmite, diatomaceous earth, oxides such as titanium dioxide, iron oxide, zinc oxide, magnesium oxide, and metal ferrite, hydroxides such as aluminum hydroxide and magnesium hydroxide, carbonates such as calcium carbonate (light and heavy), magnesium carbonate, dolomite, and dawsonite, sulfates or sulfites such as calcium sulfate, barium sulfate, ammonium sulfate, and calcium sulfite, talc, mica, clay, and glass fibers. Examples of fillers include silicates such as calcium silicate, montmorillonite, and bentonite; borates such as zinc borate, barium metaborate, aluminum borate, calcium borate, and sodium borate; carbon such as carbon black, hydrophobic carbon black, water-repellent carbon black, graphite, and carbon fibers; and other materials such as iron powder, copper powder, aluminum powder, zinc oxide, molybdenum sulfide, boron fibers, potassium titanate, lead zirconate titanate, fluorinated resin powder, and Teflon® powder. Hydrophobic substances can be selected and used to suppress the condensation of water vapor. Materials made of carbon, such as carbon black, can also be selected and used. These fillers may have a primary particle size of 1000 nm or less, or greater than 1000 nm. Furthermore, the gas-absorbing material of one embodiment may contain particles made of the same material as those exemplified as fine particles with a primary particle size of 1000 nm or less, and may also contain particles with a primary particle size greater than 1000 nm. When a filler is included in the gas absorbent material, the filler content can be, for example, 0.1 to 60% by mass relative to the total amount of the gas absorbent material.

[0076] The gas-absorbing material may include a dispersion medium for suspending the polymer material and additives of one embodiment. The other components that can be used in the gas-absorbing material described above may be used individually or in combination of two or more types.

[0077] The sorbent 33 is not limited to the specified polymer material described above. For example, basic polymers, basic polymer gels (fine particles), or ion exchange resins can also be used. These materials also satisfy the requirements of reversible sorbent and release of carbon dioxide, reversible sorbent and release depending on temperature and pressure, and reversible sorbent and release of water.

[0078] By increasing the packing density of the sorbent material 33 in the internal space 32 of the housing 31, the amount of carbon dioxide sorbed per unit volume of the housing 31 can be improved, and the size and weight of the packed bed 3 can be reduced. By reducing the size and weight, the decrease in fuel consumption of the mobile body due to the weight of the housing 31 of the packed bed 3 can be suppressed. Increasing the packing density of the sorbent material 33 can also reduce the amount of retained gas. Reducing the amount of retained gas makes it easier to concentrate carbon dioxide during recovery. Also, when using a retained gas recovery unit 7 (see Figure 3, etc., described later), the dimensions of the retained gas recovery unit 7 can be reduced. Furthermore, even when the operation to expel retained gas from the packed bed 3 is performed by supplying a portion of the recovered carbon dioxide to the packed bed 3, the amount of carbon dioxide supplied can be reduced, minimizing carbon dioxide loss. On the other hand, if the packing density is too high, it will lead to an increase in pressure loss and further to the disappearance of the gas diffusion phase. For this reason, the packing density is preferably 10% to 95% by volume, and more preferably 20% to 80%. In the case of an adsorbent 33 that expands or contracts due to the adsorption and release of carbon dioxide and moisture, the packing density and pressure resistance can be adjusted by adjusting the amount of moisture and carbon dioxide adsorbed at the time of packing. For example, by packing with less moisture than required for use and then adsorbing moisture, the packing density can be increased, while conversely, by packing with more moisture than required for use and then releasing it, the packing density can be decreased.

[0079] It is also possible to introduce interconnected flow channels into the housing 31 that allow gas to flow linearly using hollow fibers, porous sheets, or honeycomb-shaped porous materials made of porous material. The interconnected linear flow channels reduce pressure loss and allow for easy introduction of large amounts of gas. Alternatively, gas-absorbing material can be introduced at high density on the outside of tubular gas flow channels made of hollow fibers or corrugated porous material. The cross-sectional area of ​​the gas flow channels may be from 0.1 millimeters to several millimeters in diameter. The distance between gas flow channels in the space filled with gas-absorbing material may be from 0.1 to 50 millimeters or from 1 to 10 millimeters. Increasing this distance can increase the amount of material to be filled. Conversely, shortening this distance can increase the absorption rate of carbon dioxide. Furthermore, gas flow channels can also be introduced into the material by mixing porous fine particles with gas-absorbing material. If there is a sufficiently large amount of porous material mixed, interconnected flow channels are formed, significantly reducing pressure resistance. Even if there is not enough porous material, pressure resistance can be reduced according to the amount of porous material.

[0080] When a large amount of gas absorbent material is filled, the gas absorbent material may expand as it absorbs carbon dioxide and moisture. However, by selecting materials and structures that do not deform or become blocked by external pressure as flow channels such as hollow fibers, gas flow can be maintained. The porous material used here can be nonwoven fabric or fiber paper, as long as the pores are small enough that the gas absorbent material cannot permeate through them. The porous material, nonwoven fabric, or fiber paper only needs to have a pore size small enough to suppress the scattering of the gas absorbent material along with the circulating gas, and it is desirable to have the largest possible pore size to allow gas to permeate at high speed. Furthermore, the porous material, nonwoven fabric, or fiber paper only needs to be dense enough to suppress gas scattering and not deform or become blocked by external pressure, and from the standpoint of gas permeability, it is preferable to be as sparse as possible. Examples of porous materials include fluororesin porous materials such as polytetrafluoroethylene (PTFE), porous ceramics, polyethersulfone (PES) and polysulfone (PS), porous materials, and sintered metals.

[0081] Now, let's return to the explanation of Figures 1 and 2. The outlet passage 70 is a passage that guides the gas that has passed through the packed bed 3 into the atmosphere. Specifically, one end of the outlet passage 70 is connected to the outlet of the packed bed 3 via the attachment / detachment part 60. The other end of the outlet passage 70 is connected to the junction part 22 of the bypass 20. In other words, the outlet passage 70 and the bypass 20 merge at the junction part 22. The outlet passage 70 also guides the gas that has passed through the packed bed 3 into the atmosphere via the bypass 20. The outlet passage 70 is, for example, made up of a cylindrical pipe member with a circular cross-section.

[0082] The inlet passage valve 80 is installed in the middle of the inlet passage 30 and is a valve that opens and closes the inlet passage 30. When the heat engine stops, the inlet passage valve 80 closes the inlet passage 30. That is, when the heat engine stops and gas intake from the bypass 20 stops, the inlet passage valve 80 closes the inlet passage 30 to prevent carbon dioxide from being released to the outside from the packed bed 3. The inlet passage valve 80 may also close the inlet passage 30 when the movement of the moving body stops, even if the heat engine is not stopped. The inlet passage valve 80 may also close the inlet passage 30 when sufficient carbon dioxide has been adsorbed onto the gas absorbent material, even if the heat engine is not stopped. The amount of carbon dioxide adsorbed may be estimated by the gas intake time, by the amount of gas taken in, or by installing a carbon dioxide sensor downstream of the housing 31 and measuring the carbon dioxide concentration.

[0083] The outlet passage valve 90 closes the outlet passage 70 when the heat engine stops. That is, when the heat engine stops and gas intake from the bypass 20 stops, the outlet passage valve 90 closes the outlet passage 70 to prevent carbon dioxide from being released to the outside from the packed bed 3. The outlet passage valve 90 may also close the outlet passage 70 when the movement of the moving body stops, even if the heat engine is not stopped. The outlet passage valve 90 may also close the outlet passage 70 when sufficient carbon dioxide has been adsorbed onto the gas absorbent material, even if the heat engine is not stopped. The amount of carbon dioxide adsorbed may be estimated by the gas intake time, by the amount of gas taken in, or by installing a carbon dioxide sensor downstream of the housing 31 and measuring the carbon dioxide concentration.

[0084] Next, we will explain the process from when the mobile system 100 mounted on the mobile body takes in the gas emitted from the mobile body, until the carbon dioxide is recovered at the recovery station. First, when the heat engine of the mobile body starts up, gas is discharged from the exhaust pipe E of the mobile body. After the heat engine of the mobile body starts up, the mobile body begins to move.

[0085] In a typical embodiment, the exhaust pipe E and the inlet of the bypass 20 are in communication, and when gas is discharged from the exhaust pipe E of the mobile unit, the discharged exhaust gas is taken into the bypass 20 from its inlet. The gas taken into the bypass 20 flows through the bypass 20 and is discharged from its outlet. Here, the gas taken into the bypass 20 includes the exhaust gas discharged from the mobile unit.

[0086] The flow of gas into the detour 20 can be effectively facilitated by utilizing the Venturi effect. For example, as described above, the cross-sectional area of ​​the branch section 21 of the detour 20 is larger than the cross-sectional area of ​​the confluence section 22 of the detour 20. Therefore, the flow velocity of the gas flowing near the confluence section 22 within the detour 20 is faster than the flow velocity of the gas flowing near the branch section 21. As a result, the pressure near the branch section 21 becomes higher than the pressure near the confluence section 22, and some of the gas taken into the detour 20 is guided to the inlet passage 30. In other words, the gas taken into the packed bed 3 is part of the gas discharged from the heat engine of the mobile body.

[0087] The gas introduced into the entrance passage 30 is cooled as it passes through the first cooling section 40. The first cooling section 40 is exposed to air from the atmosphere as, for example, a moving body moves. As a result, heat from the first cooling section 40 is released into the air. Consequently, the gas passing through the first cooling section 40 is cooled. Alternatively, the first cooling section 40 may use the waste cooling heat generated by the moving body to cool the gas passing through it.

[0088] The gas that has passed through the first cooling section 40 flows through the inlet passage 30 and is guided to the second cooling section 50. The gas guided to the second cooling section 50 is cooled by contact with the liquid stored in the storage section of the second cooling section 50. Furthermore, the humidity of the gas guided to the second cooling section 50 is adjusted by contact with the liquid stored in the storage section of the second cooling section 50. If necessary, a filter may be provided somewhere between the inlet passage 30 and the sorbent material 33. The filter may capture solids such as particulate matter, or it may react with impurities physically or chemically to prevent the inflow of impurities into the sorbent material 33. For example, an air filter such as a HEPA filter can be used to prevent the inflow of particulate matter. Alternatively, an adsorbent that reacts with strong acid gases or an ion exchange resin can be used to remove strong acid gases.

[0089] The gas that has passed through the second cooling section 50 is led to the packed bed 3. Of the gas led to the packed bed 3, carbon dioxide is adsorbed onto the adsorbent material 33. The gas that is not adsorbed onto the adsorbent material 33 is led to the outlet passage 70. The gas led to the outlet passage 70 merges with the bypass 20 at the confluence section 22. After that, the gas that has passed through the bypass 20 and the gas that has passed through the outlet passage 70 is led to the outlet of the bypass 20 and released into the atmosphere. In this way, the packed bed 3 is filled with carbon dioxide. The adsorbent material 33 may contain water. The water evaporates, suppressing the heat generated when carbon dioxide is adsorbed, and allowing carbon dioxide to be adsorbed effectively. The water may be supplied from water contained in the exhaust gas, as water vapor from the recovery piping, or as liquid water from the recovery piping.

[0090] With the packed bed 3 filled with carbon dioxide, the packed bed 3 is removed from the mobile system 100 (see Figure 2). At this time, the automatic opening and closing valves of the connecting parts attached to both ends of the housing 31 are closed.

[0091] The packed bed 3, removed from the mobile system 100, is installed at the mounting position for the packed bed 3 on the stand system 200. Once the packed bed 3 is installed at the mounting position, the stand system 200 starts operating and recovers carbon dioxide from the packed bed 3. In other words, at least a part of the carbon dioxide recovery method is realized in the recovery system 1.

[0092] Meanwhile, a new packed bed 3 is installed on the mobile system 100 from which the packed bed 3 has been removed, after the carbon dioxide has been released. This allows the recovery system 1 to recover the carbon dioxide emitted as the mobile body starts moving again.

[0093] Figure 3 shows an example of the stand-side system 200. When explaining with reference to the drawing, upstream refers to the side where gas etc. is input (supplied), and downstream refers to the side where gas etc. is output (discharged). First, the overall configuration of the stand-side system 200 will be explained with reference to Figure 3.

[0094] As shown in Figure 3, the stand-side system 200 installed at the recovery stand is broadly composed of a packed bed 3, a steam supply unit 4, a carbon dioxide recovery unit 5, a retained gas recovery unit 7, and a processing unit 8. The recovery system 1 is also provided with multiple pipes and valves between each part, which will be described later. In this embodiment, carbon dioxide adsorbed on the adsorbent material 33 is released when steam is supplied to the packed bed 3, causing a decrease in partial pressure, and carbon dioxide is separated from the supply gas. The concentrated carbon dioxide is then recovered in the carbon dioxide recovery unit 5. The recovered carbon dioxide can be used as appropriate in the vicinity of the recovery system 1 or at a different facility. The operation of each part when carbon dioxide is recovered will be described in detail later.

[0095] As shown in Figure 3, the other end (downstream side) of the packed bed 3 installed at the mounting position is connected to one end (upstream side) of the carbon dioxide recovery unit 5 via the recovery piping P2 and valve V3. The other end (downstream side) of the packed bed 3 may be connected to the stagnant gas recovery unit 7. The stagnant gas recovery unit 7 branches off from the connection point (branching point) T3 of the piping P51 (piping from valve V3 to the carbon dioxide recovery unit 5) that connects the packed bed 3 and the carbon dioxide recovery unit 5. In other words, the carbon dioxide recovery unit 5 and the stagnant gas recovery unit 7 are connected at connection point T3 and are commonly connected to valve V3.

[0096] The other end (downstream side) of the carbon dioxide recovery unit 5 may be connected to the other end (upstream side) of the steam supply unit 4 via a valve V5. This allows the recovered carbon dioxide to be circulated within the carbon dioxide recovery unit 5, the steam supply unit 4, and the packed bed 3. In other words, the carbon dioxide recovery unit 5, the steam supply unit 4, and the packed bed 3 are connected to form a carbon dioxide circulation path. However, a configuration without such a circulation path is also possible.

[0097] Furthermore, as shown in Figure 3, a processing device 8 is electrically connected to each component to control the operation of the packed bed 3, steam supply unit 4, carbon dioxide recovery unit 5, and retained gas recovery unit 7 by transmitting control signals to each component.

[0098] Next, the detailed configuration of each part will be described with reference to Figures 3 and 4. Figure 4 is a block diagram showing an example of the configuration of a processing apparatus 8 according to one embodiment of the present disclosure. Note that the configuration of the packed bed 3 is as described above, so a detailed explanation is omitted here.

[0099] The steam supply unit 4 can generate and supply steam upstream of the packed bed 3 in order to lower the partial pressure of carbon dioxide in the packed bed 3. The steam supply unit 4 may also be operated to adsorb or condense steam (moisture) onto the sorbent material 33. When operating under condensation conditions, the steam supply unit 4 adjusts the state of the steam so that when the generated steam reaches the packed bed 3, the pressure of the steam becomes equal to or greater than the saturated water vapor pressure at the temperature of the sorbent material 33 within at least a portion of the packed bed 3. Here, adjusting the state means adjusting the temperature, adjusting the humidity, adjusting the pressure, or adjusting at least one of these. For example, a temperature sensor may be introduced inside the packed bed 3, and the steam supply unit 4 may adjust the pressure of the supplied steam so that the supplied steam becomes saturated steam at that temperature in a portion of the inside of the packed bed 3. Alternatively, the supplied steam itself may be saturated steam. When the pressure exceeds the saturated vapor pressure, the water vapor condenses into liquid water at that location and simultaneously releases the latent heat of vaporization of water. This heat can be used as reaction heat to release carbon dioxide from the sorbent 33, thereby reducing the temperature drop of the sorbent 33 during carbon dioxide release and accelerating the release of carbon dioxide. Furthermore, although the temperature rises during carbon dioxide sorption due to the supply of reaction heat associated with carbon dioxide sorption, the temperature rise can be reduced by the condensed water changing into water vapor and absorbing heat from the latent heat of vaporization.

[0100] By simultaneously supplying steam and reducing the pressure inside the packed bed 3 using the pump 51, the partial pressure of carbon dioxide inside the packed bed 3 is lowered, allowing for effective recovery of carbon dioxide. By adjusting the pressure during depressurization, the pressure of the supplied steam can be adjusted to around the saturated water vapor pressure inside the packed bed 3.

[0101] In one embodiment, when the cooling capacity of the first cooling unit 40 and the second cooling unit 50 is sufficiently high, the temperature of the exhaust gas introduced from the exhaust pipe E into the second cooling unit 50 can be cooled to a temperature lower than the dew point temperature of the exhaust gas. Under these conditions, steam can be generated using the water stored in the second cooling unit 50, and carbon dioxide can be recovered from inside the packed bed 3. In other words, the second cooling unit 50 can be used instead of the steam supply unit 4, and an external steam supply mechanism such as the steam supply pipe connection J1 becomes unnecessary, thus simplifying the system. In this case, electricity or heat may be supplied from an external source for steam generation in the second cooling unit 50, or waste heat or electricity from the mobile unit may be utilized.

[0102] As shown in Figure 3, the steam supply unit 4 includes a steam generator 41 with a built-in heater and a pump 42. More specifically, a valve V5 is connected to one end (upstream side) of the steam generator 41 via piping P41, and a valve V2 is connected to the other end (downstream side) via piping P42. In addition, a supply water introduction pipe P43 is connected to one end (upstream side) of the pump 42, and the steam generator 41 is connected to the other end (downstream side) via piping P44.

[0103] The steam generator 41, valve V2, and pump 42 are electrically connected to the processing unit 8 and are controlled based on control signals transmitted from the processing unit 8.

[0104] With this configuration of the steam supply unit 4, the pump 42 is driven, supplying water to the steam generator 41, and steam at a predetermined temperature is generated in the steam generator 41. The generated steam is then supplied to the packed bed 3 via piping P42, valve V2, and steam supply piping P1. Here, the predetermined temperature is determined according to the operating temperature and operating pressure of the packed bed 3 in the recovery system 1. The predetermined temperature is preferably about 0°C to 50°C higher than the operating temperature of the packed bed 3 in the recovery system 1, and more preferably about 1°C to 20°C higher. As a result, when the operating pressure of the packed bed 3 is maintained at approximately the saturation vapor pressure of the operating temperature of the packed bed 3, an appropriate amount of steam can be supplied to the packed bed 3 due to the pressure difference.

[0105] When steam is supplied to the packed bed 3 by the steam supply unit 4, the carbon dioxide in the packed bed 3 is diluted by the steam, lowering its partial pressure. This allows for desorption at a lower vacuum level, reducing the amount of pressure reduction required by the pump described later. This reduces the cost of the pressure reduction, which in turn reduces the overall cost of the recovery system 1 and the cost of carbon dioxide recovery.

[0106] As described above, the steam supply unit 4 has a steam generator 41 that heats the supply water to generate steam. Therefore, a heat source for supplying heat used to heat the supply water is connected to the steam generator 41 via piping. In other words, in this embodiment, the piping functions as a heat or cold supply device. By supplying heat from the heat source to the steam generator 41 via the piping, it is possible to heat the supply water to a predetermined temperature range. In this way, the steam generator 41 functions as a heat exchanger.

[0107] In the above description, we have explained the case in which piping connected to the steam generator 41 is used as a heat or cold supply device, but it is also possible to configure the heat or cold supply device by other methods. For example, the steam generator 41 itself, the steam generator 41 and the surrounding piping P41 and P42, or the entire steam supply unit 4 can be housed in a container that can be filled with heat. Heat from a heat source is then supplied to the container via the connected piping. In other words, the container and piping function as a heat or cold supply device. This makes it possible to maintain or assist in maintaining the temperature of the steam heated by the steam generator 41.

[0108] The heat source for supplying heat or cold to the heat or cold supply unit can be either external to the recovery system 1 or internal to the recovery system 1. For example, when it is necessary to heat or maintain the temperature of a gas (maintaining a high temperature relative to the ambient temperature), at least one of the following can be used as a heat source: heat from power generation equipment, heat from factory equipment or electrical equipment, heat from phase transitions or compression of gas or liquid (water or liquefied natural gas as an example of a liquid), sensible heat of gas or liquid, naturally occurring heat, heat due to the Peltier effect, and combinations thereof. Specifically, in power generation equipment and factory equipment, various reactions such as combustion, methanation, nuclear fission, and nuclear fusion occur in at least a part of them, generating heat. In electrical equipment, heat is generated by driving various devices such as motors, compressors, and coolers installed in at least a part of it. In addition, liquefied natural gas, city gas, propane gas, air, and water undergo phase transitions and compression during their use, generating heat during these phase transitions and compressions. It is also possible to utilize this sensible heat. Furthermore, there is naturally occurring heat such as geothermal energy, hot springs, and sunlight. In this embodiment, these heat sources or heat transfer fluids heated by these heat sources are supplied through a heat or cold supply device. Of the heat sources exemplified above, it is preferable from the viewpoint of the energy cycle to use a power generation facility, factory facility, or electrical facility on which the recovery system 1 is installed as the heat source.

[0109] Furthermore, as a heat source or cooling source for supplying heat or cold to the heat or cold supply unit, one example is that which originates from within the recovery system 1 can be used. The recovery system 1 includes a carbon dioxide recovery unit 5 that concentrates carbon dioxide. In particular, the pump 51 of the carbon dioxide recovery unit 5 compresses the gas in the packed bed 3, so the gas becomes hot downstream of the pump 51 and heat is generated. Therefore, when it is necessary to heat or maintain the temperature of the supply gas or supply water (maintain a high temperature relative to the ambient temperature), the gas obtained downstream of the pump 51 can be used as a heat source.

[0110] The carbon dioxide recovery unit 5 comprises a pump 51, a heat exchanger 52, a gas-liquid separator 53, valves V51, V52, and V53, and a storage tank 54. More specifically, valve V3 is connected to one end (upstream side) of the pump 51 via piping P51, and the heat exchanger 52 is connected to the other end (downstream side) via piping P52. A gas-liquid separator 53 is connected to the downstream side of the heat exchanger 52 via piping P53. Furthermore, valve V51 is connected to the downstream side of the gas-liquid separator 53 via piping P54. Finally, piping P55 for discharging wastewater to the outside is connected to the gas-liquid separator 53. The carbon dioxide recovery unit 5 is configured to recover carbon dioxide separated in the packed bed 3.

[0111] As shown in Figure 3, a degassing pipe P56 for degassing gases other than carbon dioxide (stagnation gas) is connected to the downstream side of valve V51. Pipe P57 is connected to the branching point T51 of pipe P54, and one end of valve V52 is connected to the downstream side of pipe P57. Furthermore, a storage tank 54 is connected to the other end (downstream side) of valve V52 via pipe P58. The storage tank 54 is also connected to valve V5 via pipe P59.

[0112] A branch pipe P50 is provided between valve V52 and storage tank 54, branching off from branch point T52 of pipe P58. Valve V53 is installed in branch pipe P50. If the carbon dioxide concentration in the gas recovered from packed bed 3 is above a certain level, the recovered gas can be collected via valves V52 and V53. On the other hand, if the carbon dioxide concentration in the gas recovered from packed bed 3 is below a certain level, the gas can be discharged outside the device as stagnant gas via valve V51. To determine the carbon dioxide concentration, an analytical device for acquiring the carbon dioxide concentration may be provided between packed bed 3 and branch point T51 (downstream of packed bed 3 and upstream of branch point T51).

[0113] With the carbon dioxide recovery unit 5 configured as described above, the pump 51 drives a portion of the recovery system 1 (for example, the packed bed 3) to a reduced pressure. The introduced gas (carbon dioxide and water vapor) brought towards the carbon dioxide recovery unit 5 by this reduced pressure is heated or cooled by the heat exchanger 52 according to the temperature of these gases, and after being temperature-adjusted to a predetermined temperature range, it is supplied to the gas-liquid separator 53. For example, when the introduced gas is cooled by the heat exchanger 52, the water vapor contained in the introduced gas is condensed and separated as water. Here, the predetermined temperature range is determined according to the operating temperature of the packed bed 3 in the recovery system 1. For example, the predetermined temperature range is -78°C to 60°C. More preferably, it is -10°C to 20°C.

[0114] In the gas-liquid separator 53, moisture is removed from the introduced gas, and the removed moisture is discharged as wastewater through piping P55. More specifically, when water vapor is condensed and separated as water by the heat exchanger 52, this water is separated from the gas as condensed water in the gas-liquid separator 53, and this condensed water is discharged as wastewater. A suction pump capable of draining water may be provided in piping P55. As a result, the amount of moisture in the introduced gas passing through the gas-liquid separator 53 is adjusted, increasing the proportion of carbon dioxide, and it is supplied to the storage tank 54 via piping P54, branching point T51, piping P57, and valve V52. The carbon dioxide stored in the storage tank 54 is then sent to the steam supply unit 4 via piping P59, valve V5, and piping P41 at a predetermined timing, which will be described later. In other words, the carbon dioxide recovery unit 5, the steam supply unit 4, the packed bed 3, and the piping and valves connecting them constitute a carbon dioxide circulation path for circulating carbon dioxide.

[0115] The pump 51, valve V3, heat exchanger 52, valve V52, and valve V51 are electrically connected to the processing unit 8 and controlled based on control signals transmitted from the processing unit 8.

[0116] With the configuration and function of the carbon dioxide recovery unit 5 described above, it is possible not only to adjust the temperature of the stored carbon dioxide but also to remove unwanted moisture and store high-concentration carbon dioxide in the storage tank 54. If temperature adjustment is not required, the heat exchanger 52 does not need to be provided. Also, the arrangement of the pump 51 and the heat exchanger 52 may be reversed, and the temperature-adjusted introductory gas may be drawn in by the pump 51. In this case, the gas can be cooled and water vapor removed by the heat exchanger 52, and then the recovered gas can be compressed by the pump 51, reducing the capacity and power required of the pump 51. In this case, it is desirable that the piping P55 be equipped with a suction pump capable of draining water from the reduced pressure environment. The suction pump may be, for example, a peristaltic pump. Furthermore, the number of pumps 51 and heat exchangers 52 is not limited to one, but may be multiple depending on the amount of introductory gas drawn in and the temperature adjustment, and the number can be adjusted as appropriate. By dehumidifying, cooling, or further compressing the gas in multiple stages, the cost of pumps and compression power for carbon dioxide concentration can be reduced. Furthermore, the storage tank 54 is not mandatory and may be directly connected to a carbon dioxide reduction device (not shown). It is also possible to store the carbon dioxide as liquefied carbon dioxide or dry ice by pressurizing and cooling as needed.

[0117] As described above, the carbon dioxide recovery unit 5 heats or cools the introduced gas to a predetermined temperature range using the heat exchanger 52. Therefore, a heat source or cooling source for heating or cooling is connected to the heat exchanger 52 via piping. In other words, in this embodiment, the piping functions as a heat or cooling supply. By supplying heat or cold from the heat source or cooling source to the heat exchanger 52 via the piping, it is possible to heat or cool the introduced gas to a predetermined temperature range.

[0118] Alternatively, instead of the storage tank 54 of the carbon dioxide recovery unit 5, piping may be provided to directly supply the concentrated and recovered carbon dioxide to another device (such as a carbon dioxide reduction device).

[0119] The stagnant gas recovery unit 7 includes a buffer tank 71 and a valve V71. More specifically, one end (upstream side) of the valve V71 is connected to a pipe P71, and the pipe P71 is connected to a pipe P51 at a connection point (branching point) T3. The other end (downstream side) of the valve V71 is connected to the buffer tank 71 via a pipe P72.

[0120] When valves V71 and V3 are opened, stagnant gas accumulated in the packed bed 3 flows into the stagnant gas recovery unit 7. Here, stagnant gas is a gas containing carbon dioxide and unwanted gases, with a low carbon dioxide concentration. The stagnant gas can then be temporarily stored, and is finally discharged to the outside via the carbon dioxide recovery unit 5 and the deaeration pipe P56. This buffer tank 71 allows for rapid depressurization during carbon dioxide recovery, and furthermore, by minimizing the amount of carbon dioxide mixed with the stagnant gas, the carbon dioxide concentration during recovery can be increased. Note that the connection position of the deaeration pipe P56 is not limited to the above-mentioned position, and may be connected to any of the pipes P72, P71, P51, P52, P53, P1, or P42, and the stagnant gas may be discharged to the outside depending on the connection configuration. In addition, a separate pump may be installed from the pump 51 to discharge the stagnant gas.

[0121] Figure 4 is a block diagram showing an example of the configuration of a processing apparatus 8 according to one embodiment of the present disclosure. The processing apparatus 8 does not need to include all of the components shown in Figure 4; it is possible to omit some components or to add other components.

[0122] The processing unit 8 typically includes wireless communication-enabled terminal devices such as PLCs, industrial PCs, sequencers, laptop PCs, or desktop PCs, but is not limited to these devices alone. For example, any device capable of executing the program according to this disclosure can be suitably applied as a terminal device, such as a smartphone, feature phone, personal digital assistant, PDA, portable game console, or home game console.

[0123] The processing unit 8 includes an output interface 81, a processor 82, a memory 83 including RAM, ROM, or non-volatile memory (or possibly an HDD), a communication interface 84 including a communication processing circuit and an antenna, and an input interface 85 including a touch sensor and hard keys. Each of these components is electrically connected to the others via control lines and data lines.

[0124] The output interface 81 functions as an output unit that outputs images captured by a camera (not shown) and various displays output by executing the program according to this disclosure to devices such as displays and printers, in accordance with instructions from the processor 82. Such displays are composed of, for example, liquid crystal displays, organic EL displays, or electronic paper.

[0125] The processor 82 is composed of a CPU (for example, a microcomputer) and functions as a control unit that controls other connected components based on various programs stored in the memory 83. Specifically, the processor 82 reads and executes programs for running the application according to this disclosure and programs for running the OS from the memory 83. In this disclosure, the processor 82 controls the operation of each pump and each valve (details of the control are explained in Figures 5 to 7). The processor 82 may be composed of a single CPU, or it may be composed of a combination of multiple CPUs and GPUs.

[0126] Memory 83 consists of ROM, RAM, non-volatile memory, HDD, etc., and functions as a storage unit. ROM stores instruction commands for executing the application and OS according to this disclosure as programs. RAM is used to write and read data while the program stored in ROM is being processed by the processor 82. Non-volatile memory is memory in which data is written and read by the execution of the program, and the data written therein is preserved even after the execution of the program has finished. In this disclosure, memory 83 particularly stores programs for controlling the operation of each pump and each valve (details of the control are explained in Figures 5 to 7).

[0127] The communication interface 84 functions as a communication unit that transmits and receives information to and from each valve and each pump via the communication processing circuit and antenna. The communication processing circuit performs processing to transmit control information (control commands) to each valve or each pump in accordance with the progress of processing of programs and various information used in the recovery system 1.

[0128] The communication processing circuit processes data based on broadband wireless communication methods such as LTE, but it can also process data based on narrowband wireless communication methods such as wireless LAN (as represented by IEEE 802.11) or Bluetooth®, or contactless wireless communication methods. In addition to wireless communication, wired communication can also be used.

[0129] The input interface 85 consists of a touch panel, hard keys, etc., and functions as an input unit that accepts instruction inputs related to the execution of the program related to this disclosure, as well as operation inputs for registering various information. The touch panel is arranged to cover the output interface 81 and transmits position coordinate information corresponding to image data output from the output interface 81 to the display to the processor 82. Known touch panel methods such as resistive touch, capacitive coupling, and ultrasonic surface acoustic wave touch can be used. In this disclosure, the touch panel detects swipe and tap operations on each icon, etc., displayed on the output interface 81 by an indicator. In this disclosure, an input interface 85 provided in the processing unit 8 is used, but it is also possible to use an input interface 85 that is wirelessly or wired connected to a main unit equipped with a processor 82, etc., such as a mouse.

[0130] Figures 5, 6, and 7 illustrate the flow of carbon dioxide recovery in a recovery system 1 according to one embodiment of the present disclosure. Specifically, Figure 5 shows a rinsing process to increase the carbon dioxide concentration in the packed bed 3. Figure 6 shows a process to release the carbon dioxide adsorbed in the packed bed 3 and store it in the storage tank 54. Figure 7 shows a process to release the stagnant gas recovered by the stagnant gas recovery unit 7.

[0131] First, when the packed bed 3 is installed in its mounting position, the automatic opening and closing valves of the connecting parts attached to both ends of the housing 31 open. When the packed bed 3 is installed in its mounting position, it is sufficient that the concave joints attached to both ends of the housing 31 are connected to the convex joints attached to the ends of the steam supply pipe P1 and the convex joints attached to the ends of the recovery pipe P2.

[0132] Next, the processor 82 of the processing unit 8 generates control signals to open and close the valves and transmits these control signals to each valve to open and close them. Specifically, the processor 82 generates and transmits control signals to open valves V2, V3, and V5. As a result, valves V2, V3, and V5 open. At this point, valves V51 and V71 are kept open. Valve V52 is kept closed. As a result, as shown in Figure 5, a gas flow path is formed to the storage tank 54, steam supply unit 4, packed bed 3, and back to the carbon dioxide recovery unit 5 of the carbon dioxide recovery unit 5. A gas flow path is also formed to the storage tank 54, steam supply unit 4, packed bed 3, and stagnant gas recovery unit 7 of the carbon dioxide recovery unit 5. Before valves V2, V3, and V5 are opened, the buffer tank of the stagnant gas recovery unit 7 is kept under vacuum.

[0133] In this state, the processor 82 of the processing unit 8 generates a control signal and transmits this control signal to the pump 42. As a result, the pump 42 is driven and the supply water is supplied to the steam generator 41 via piping P43, the pump 42, and piping P44. Heat is supplied to the steam generator 41 from the heat source through the heat transfer medium in the piping. Therefore, in this state, the supply water is heated and steam is generated. The pump 51 is also continuously driven. Alternatively, the steam generated in the steam generator 41 may be supplied to the heat exchanger 52 and used for heating or cooling in the heat exchanger 52.

[0134] As described above, the buffer tank 71 is in a vacuum state before valve V3 and the like are opened. Therefore, when valve V3 is opened, the stagnant gas remaining in the packed bed 3 is introduced into the buffer tank 71 via recovery piping P2, valve V3, piping P51, piping P71, valve V71, and piping P72. Also, it is assumed that a certain amount of carbon dioxide is stored in the storage tank 54 before valves V2, V3, and V5 are opened. Therefore, when valves V2, V3, and V5 are opened, the stagnant gas can be quickly removed from the packed bed 3, and the steam generated in the steam generator 41 and the carbon dioxide stored in the storage tank 54 are drawn into the packed bed 3. Specifically, the steam is introduced into the packed bed 3 via piping P42, valve V2, and steam supply piping P1, and the carbon dioxide is introduced into the packed bed 3 via piping P59, valve V5, piping P41, steam generator 41, piping P42, valve V2, and steam supply piping P1. In other words, steam and carbon dioxide are introduced into the packed bed 3 via the same gas pathway from a certain point. This allows the carbon dioxide to be humidified and supplied to the packed bed 3, preventing the absorbent material from drying out.

[0135] Subsequently, when the buffer tank 71 is filled with stagnant gas, the pump 51 drives the remaining stagnant gas in the packed bed 3 to be introduced into the heat exchanger 52 via the recovery pipe P2, valve V3, pipe P51, pump 51, and pipe P52. Here, the buffer tank 71 first transitions from a vacuum state to a state filled with stagnant gas, which mitigates the sudden pressure change of the pump 51. This suppresses the load on the pump 51 and prevents malfunction. Then, the processor 82 of the processing unit 8 generates a control signal to close the valve V71 and transmits the said control signal. As a result, the buffer tank 71 is disconnected, and the rate of removal of stagnant gas can be improved.

[0136] Furthermore, the processor 82 of the processing unit 8 continuously controls the temperature in the heat exchanger 52 to approximately 24°C. Specifically, the heat exchanger 52 is supplied with cold energy from a cold energy source through a refrigerant in the piping. Therefore, when the stagnant gas is introduced into the heat exchanger 52 of the carbon dioxide recovery unit 5, the stagnant gas is cooled to approximately 24°C in the heat exchanger 52 in order to make it possible to discharge the stagnant gas from the recovery system 1.

[0137] The stagnant gas cooled to 24°C in the heat exchanger 52 is introduced into the gas-liquid separator 53 via piping P53. Here, the stagnant gas contains a lot of moisture because, even in the state of the supply gas (containing carbon dioxide), the relative humidity was over 80%. Therefore, the cooled stagnant gas contains a lot of water vapor, and moisture is removed from the stagnant gas in the gas-liquid separator 53. The removed moisture is discharged as wastewater through piping P55. On the other hand, the stagnant gas, from which the moisture has been removed, is discharged to the outside of the recovery system 1 via piping P54, valve V51, and degassing piping P56.

[0138] Meanwhile, in the packed bed 3, stagnant gas is discharged, and the amount of vapor increases. In addition, the carbon dioxide introduced into the packed bed 3 is adsorbed onto the adsorbent material 33 by maintaining a relative humidity of 80% or higher, and the release of carbon dioxide due to a decrease in the partial pressure of carbon dioxide at this point is prevented. As a result, the amount of carbon dioxide adsorbed in the packed bed 3 is maintained, and the removal of impurities in the packed bed 3 (in other words, the rinsing process) is completed.

[0139] Alternatively, instead of reducing the pressure and drawing carbon dioxide into the packed bed 3 during the rinsing process (the rinsing treatment described above), it may be supplied to the packed bed 3 at approximately 1 atm after the sorbing process. In this case, a pump can be installed in piping P41 or P42 as needed. This allows for the expulsion of stagnant gas from the internal space 32 of the packed bed 3 before the pressure is reduced. In this case as well, the buffer tank 71 is useful because it can quickly reduce the pressure. However, in this case, since high-purity carbon dioxide is stored inside the buffer tank 71, the gas inside the buffer tank 71 can also be recovered. Whether to perform this rinsing process before or after the pressure is reduced can be arbitrarily decided in consideration of the characteristics of the sorbent 33 and the need for stable operation of the equipment.

[0140] Furthermore, since the purpose of the rinsing process is to remove stagnant gas present in the voids within the internal space 32 of the packed bed 3, an amount of carbon dioxide and vapor sufficient to remove the stagnant gas can be flowed through it. For example, an amount of carbon dioxide and vapor equal to 0.1 to 10 times the column volume can be flowed through it. Generally, the more gas is flowed through it, the less stagnant gas remains in the internal space 32, but the greater the loss of carbon dioxide, so an appropriate amount should be determined based on the target recovery amount and recovery purity. Also, depending on the relationship between the carbon dioxide concentration of the supply gas and the carbon dioxide concentration of the gas used for rinsing, some of the carbon dioxide may be adsorbed onto the sorbent material 33, or some of the carbon dioxide adsorbed onto the sorbent material 33 may be released. If a low purity of recovered carbon dioxide is not a problem, or if a low recovery rate is not a problem, the rinsing process can be omitted.

[0141] Next, the processor 82 of the processing unit 8 generates control signals to open and close the valves and transmits these control signals to each valve to open and close them. Specifically, the processor 82 generates and transmits control signals to close valves V5 and V51. On the other hand, the processor 82 generates and transmits a control signal to open valve V52. Subsequently, valves V5 and V51 close and valve V52 opens. At this point, the open and closed states of the other valves are maintained. As a result, gas flow paths leading to the steam supply unit 4, the packed bed 3, and the carbon dioxide recovery unit 5 are formed, as shown in Figure 6.

[0142] In this state, pump 42 continues to operate, so supply water is supplied to the steam generator 41 via piping P43, pump 42, and piping P44, and steam is continuously generated in the steam generator 41. Also, since pump 51 continues to operate, the generated steam is continuously introduced into the packed bed 3. As a result, the partial pressure of carbon dioxide in the packed bed 3 decreases, and carbon dioxide is released from the sorbent 33. Here, when carbon dioxide is released, the temperature of the sorbent 33 decreases due to the heat of reaction. For this reason, it is possible that the carbon dioxide release performance of the sorbent 33 decreases. However, as the temperature decreases, the pressure of the steam becomes greater than or equal to the saturated water vapor pressure at the temperature of the sorbent 33 in at least a part of the packed bed 3 (i.e., near the sorbent 33), so a portion of the steam supplied from the steam supply unit 4 is adsorbed or condensed on the sorbent 33. As a result, the latent heat of vaporization when a portion of the steam condenses into water is supplied to the sorbent 33, and the aforementioned temperature decrease is suppressed. In other words, the reaction heat due to the release of carbon dioxide and the latent heat of vaporization due to the condensation of vapor cancel each other out, and the carbon dioxide release performance of the sorbent 33 is maintained.

[0143] The released carbon dioxide, along with the steam, is introduced into the heat exchanger 52 via the recovery piping P2, valve V3, piping P51, pump 51, and piping P52, due to the depressurization caused by the operation of pump 51. This completes the release process, which involves supplying steam to the sorbent material 33 to lower the partial pressure of carbon dioxide, and then sorbing or condensing the steam onto the sorbent material 33 to release carbon dioxide from the sorbent material 33.

[0144] In this process, the processor 82 of the processing unit 8 generates a control signal for temperature control within the heat exchanger 52 to adjust the cooling temperature of the carbon dioxide, and transmits the control signal to the heat exchanger 52. Cooling is supplied to the heat exchanger 52 from the cooling source through a refrigerant in the piping. Therefore, when carbon dioxide and steam are introduced into the heat exchanger 52 of the carbon dioxide recovery unit 5, they are cooled to a predetermined temperature by the heat exchanger 52 in order to remove steam from the carbon dioxide.

[0145] The carbon dioxide and steam cooled in the heat exchanger 52 are introduced into the gas-liquid separator 53 via piping P53. Here, some of the water is removed in the gas-liquid separator 53. As a result, the concentration of carbon dioxide in the gas passing through the gas-liquid separator 53 increases. The carbon dioxide that has passed through the gas-liquid separator 53 is then introduced into the storage tank 54 via piping P54, piping P57, valve V52, and piping P58. As a result, high-concentration carbon dioxide (concentrated carbon dioxide) is stored in the storage tank 54. This completes the recovery process, in which the carbon dioxide released from the sorbent 33 is recovered while removing the steam. In this recovery process, the pressure in the carbon dioxide recovery path is a predetermined value below the saturated water vapor pressure at the operating temperature upstream of the pump 51, and at or above the ambient pressure downstream of the pump 51.

[0146] Next, the processor 82 generates and transmits control signals to close valves V2, V3, and V5. As a result, valves V2, V3, and V5 are closed. At the same time as this control, the processor 82 generates and transmits control signals to open valves V51 and V71. Meanwhile, the processor 82 also generates and transmits a control signal to close valve V52. Subsequently, valves V51 and V71 open, and valve V52 closes. This forms a gas flow path leading to the stagnant gas recovery unit 7 and the carbon dioxide recovery unit 5. Then, the processor 82 of the processing unit 8 generates and transmits a control signal to drive the pump 51.

[0147] Here, the buffer tank 71 is filled with the stagnant gas that had accumulated in the packed bed 3 due to the previous carbon dioxide recovery process. As a result, a gas flow path is formed to the stagnant gas recovery section 7 and the carbon dioxide recovery section 5. When the pump 51 is driven, the stagnant gas filled in the buffer tank 71 is introduced to the heat exchanger 52 via piping P72, valve V71, piping P71, piping P51, pump 51, and piping P52, and is discharged to the outside of the recovery system 1 via degassing piping P56.

[0148] Furthermore, the processor 82 of the processing unit 8 generates a control signal for temperature control within the heat exchanger 52 to adjust the cooling temperature of the stagnant gas, and transmits the control signal to the heat exchanger 52. Cooling is also supplied to the heat exchanger 52 from a cooling source through a refrigerant in the piping. Therefore, when the stagnant gas is introduced into the heat exchanger 52 of the carbon dioxide recovery unit 5, the stagnant gas is cooled to approximately 24°C in the heat exchanger 52 in order to make it possible to discharge the stagnant gas from the recovery system 1. Here, the cooling temperature is not limited to 24°C, and it is assumed that there are cases where the temperature of the stagnant gas must be at room temperature as a condition for discharge of the stagnant gas.

[0149] The stagnant gas cooled to 24°C in the heat exchanger 52 is introduced to the gas-liquid separator 53 via piping P53. Here, the stagnant gas contains a lot of moisture because the relative humidity was over 80% even in the state of the supply gas (containing carbon dioxide). Therefore, the cooled stagnant gas contains a lot of water vapor, and moisture is removed from the stagnant gas in the gas-liquid separator 53. The removed moisture is discharged as wastewater through piping P55. On the other hand, the stagnant gas, with the moisture removed, is discharged to the outside of the recovery system 1 via piping P54, valve V51 and degassing piping P56. Here, the pressure in the path from the buffer tank 71 to the degassing piping P56 is around 0 atm, which is a very small value compared to the pressure at the exhaust gas discharge section.

[0150] As described above, the discharge of the stagnant gas creates a vacuum inside the buffer tank 71, making it possible to temporarily store the stagnant gas in the process described above.

[0151] By performing the above-described process, the storage tank 54 can be filled with a higher concentration of carbon dioxide. In other words, high-concentration carbon dioxide is recovered downstream from the valve V53.

[0152] Figure 8 shows an overview of the mobile body side system 101 according to another embodiment. The mobile body side system 101 includes, for example, an inlet passage 35, a first cooling section 40, a second cooling section 50, a packed bed 3, and an outlet passage 75. Note that the attachment / detachment section 60, the inlet passage valve 80, and the outlet passage valve 90 are not shown in Figure 8. Also, a description of a configuration similar to the one described using Figure 1 is omitted.

[0153] The inlet passage 35 is a passage that takes in gas discharged from the exhaust pipe E of the mobile unit. The inlet passage 35 is also a passage that guides the gas discharged from the mobile unit to the packed bed 3. The first cooling unit 40, the second cooling unit 50, and the packed bed 3 are the same as those described with reference to Figure 1.

[0154] The outlet passage 75 is connected at one end to the packed bed 3. The outlet passage 75 also guides the gas that has passed through the packed bed 3 into the atmosphere. Therefore, the mobile body side system 101 according to this embodiment differs from the embodiment described with reference to Figure 1 in that it does not have a bypass 20.

[0155] The outlet passage 75 releases gas in the direction opposite to the direction of movement of the moving body. In other words, the gas that has passed through the packed bed 3 is released into the atmosphere in the direction opposite to the direction in which the moving body moves forward. Unlike the illustration in Figure 8, the distance between the exhaust pipe E of the moving body and the inlet passage 35 may be, for example, several centimeters. In this case, when the moving body moves forward, negative pressure acts near the outlet of the outlet passage 75. As a result, the gas discharged from the exhaust pipe E of the moving body can be taken into the inlet of the inlet passage 35. Alternatively, wind pressure generated by the forward movement of the moving body acts at the inlet of the inlet passage 35. As a result, the inlet passage 35 can take in the gas discharged from the exhaust pipe E of the moving body and air from the atmosphere.

[0156] In the embodiments described above, gasoline or diesel fuel may be used as the fuel for the heat engine. Alternatively, a high-pressure gas such as propane gas may be used as the fuel for the heat engine. In this case, the recovery system 1 may include a gas supply section that guides the gas discharged from the mobile body to the packed bed 3 by utilizing the expansion work generated when the high-pressure gas expands. For example, the turbines T1, T2 and shaft S1, which will be described later, correspond to the gas supply section.

[0157] Figure 9 shows an example of a recovery system 1 equipped with a gas supply section. The mobile body and recovery system 1 comprises a fuel tank FT, a heat engine EN, piping P101, P102, P103, P104, P105, turbines T1 and T2, a shaft S1, a connector C, and an exhaust pipe E. The fuel tank FT is a tank for storing high-pressure gas used as fuel. Piping P101 is piping for supplying high-pressure gas from the fuel tank FT to the turbine T1. The turbine T1 converts the expansion work of the high-pressure gas supplied by piping P101 into rotational work. In other words, the turbine T1 rotates by receiving force from the high-pressure gas. As the turbine T1 rotates, the shaft S1 and turbine T2 also rotate.

[0158] The high-pressure gas that has passed through turbine T1 is sent to the heat engine EN through piping P102. The gas discharged from the heat engine EN is sent to turbine T2 through exhaust pipe E and piping P104. The exhaust pipe E and piping P104 are connected by connector C. Piping P103 may branch off from a portion of exhaust pipe E. In this case, piping P103 releases the gas discharged from the heat engine EN into the atmosphere. In other words, a portion of the gas discharged from the heat engine EN is sent to piping P104.

[0159] The turbine T2 rotates due to the rotational force transmitted through the shaft S1. As the turbine T2 rotates, negative pressure is created inside the piping P104, drawing gas discharged from the heat engine EN into piping P104, which is then sent to piping P105. The gas sent to piping P105 passes through filters, cooling sections, etc., before being sent to the packed bed 3. This ensures that the gas discharged from the heat engine EN is efficiently delivered to the packed bed 3.

[0160] In the embodiment described above, if the gas discharged from the heat engine EN is at high pressure, the recovery system 1 may include a gas supply section that utilizes the pressure of the high-pressure gas to guide the gas discharged from the heat engine EN to the packed bed 3. For example, the turbines T3, T4 and shaft S2, which will be described later, correspond to the gas supply section.

[0161] Figure 10 shows an example of a recovery system 1 equipped with a gas supply section. The mobile body and recovery system 1 include a heat engine EN, piping P106, P107, P108, P109, turbines T3, T4, shaft S2, connector C, and exhaust pipe E. The heat engine EN generates driving force using a predetermined fuel. The heat engine EN also generates high-pressure exhaust gas.

[0162] Piping P106 is used to deliver high-pressure exhaust gas from the heat engine EN to the turbine T3. The turbine T3 converts the pressure of the high-pressure gas delivered by piping P106 into rotational force. In other words, the turbine T3 rotates by receiving force from the high-pressure gas. As the turbine T3 rotates, the shaft S2 and the turbine T4 also rotate.

[0163] The high-pressure gas that has passed through turbine T3 is sent to turbine T4 through exhaust pipe E and piping P108. Exhaust pipe E and piping P108 are connected by connector C. Piping P107 may branch off from a portion of exhaust pipe E. In this case, piping P107 releases the gas discharged from the heat engine EN into the atmosphere. In other words, a portion of the gas discharged from the heat engine EN is sent to piping P108.

[0164] The turbine T4 rotates due to the rotational force transmitted through the shaft S2. As the turbine T4 rotates, negative pressure is created inside the piping P108, drawing gas discharged from the heat engine EN into piping P108, which is then sent to piping P109. The gas sent to piping P109 passes through filters, cooling sections, etc., before being sent to the packed bed 3. This ensures that the gas discharged from the heat engine EN is efficiently delivered to the packed bed 3.

[0165] In the embodiment described above, steam is supplied to the packed bed 3 by supplying steam from the steam supply pipe P1 to desorb carbon dioxide. In other words, in the embodiment described above, water vapor is used as the sweep gas. However, the sweep gas is not limited to water vapor. For example, the recovery system 1 may be equipped in the recovery stand with a sweep gas supply unit that supplies a first sweep gas different from steam to the packed bed 3, either in place of the steam supply unit 4 or in addition to the steam supply unit 4.

[0166] Figure 11 shows an example of a recovery system 1 equipped with a sweep gas supply unit. The configuration other than the sweep gas supply unit 9 is the same as the configuration shown in Figure 3. The sweep gas supply unit 9 comprises a sweep gas supplyer 91 and a pump 92. The sweep gas supplyer 91 is connected to pipes P41, P42, and P44. The pump 92 is connected to the introduction pipes P43 and P44.

[0167] Pump P92 takes in a first sweep gas from the inlet pipe P43 and sends it to pipe P44. The first sweep gas is, for example, air. That is, the inlet pipe P43 takes in air from the atmosphere. The inlet pipe P43 may be equipped with a filter to remove dust and other particles contained in the air.

[0168] The first sweep gas sent to piping P44 is taken in by the sweep gas supply unit 91. The sweep gas supply unit 91 sends the air it has taken in along with the carbon dioxide released from the storage tank 54 toward the packed bed 3. In this way, the sweep gas supply unit 9 can effectively deliver the first sweep gas to the packed bed 3.

[0169] In the embodiments described above, the recovered carbon dioxide may be used for photosynthesis. Photosynthesis is carried out by organisms such as vegetables, plants, algae, and photosynthetic fungi. The recovery system 1 can, for example, supply the carbon dioxide desorbed from the packed bed 3 to a greenhouse, thereby promoting photosynthesis carried out by vegetables and other organisms grown in the greenhouse. In other words, the recovery system 1 realizes at least a part of the method of utilizing carbon dioxide.

[0170] As described above, the recovery system 1 comprises a packed bed 3 attached to a mobile body and having an sorbent material for absorbing carbon dioxide, and a detachable part 60 provided on the mobile body that allows the packed bed 3 to be attached to and detached. In other words, according to the recovery system 1 of this disclosure, the mobile body does not need to be equipped with a recovery device for recovering carbon dioxide taken into the packed bed 3. Therefore, the recovery system 1 mounted on the mobile body can be made lighter. As a result, the energy efficiency when recovering carbon dioxide can be increased. In addition, the packed bed 3 is detachable from the mobile body. Therefore, according to the recovery system 1 of this disclosure, it is not necessary to stop the mobile body when recovering carbon dioxide from the packed bed 3. Therefore, the recovery system 1 can prevent a decrease in the operating rate of the mobile body.

[0171] Furthermore, in the recovery system 1, carbon dioxide is contained in the gas emitted from the mobile vehicle's heat engine EN. In other words, the recovery system 1 can reduce the amount of carbon dioxide emitted from the mobile vehicle while preventing a decrease in the mobile vehicle's operating rate.

[0172] Furthermore, the sorbent 33 can sorb carbon dioxide at least at atmospheric pressure. Therefore, the housing 31 that contains the sorbent 33 can be made of a lightweight material such as resin. As a result, the manufacturing cost of the recovery system 1 can be reduced.

[0173] Furthermore, the sorbent 33 can sorb carbon dioxide at or near room temperature. Therefore, the housing 31 that houses the sorbent 33 can be made of a material such as resin. If the sorbent 33 had the function of absorbing carbon dioxide at high temperatures, the housing 31 that houses the sorbent 33 would need to be made of a heat-resistant material such as metal. In contrast, the sorbent 33 according to this disclosure can sorb carbon dioxide at or near room temperature. Therefore, the housing 31 can be made of a lightweight and inexpensive material such as resin.

[0174] Furthermore, the recovery system 1 includes a stand-side system 200 that recovers carbon dioxide from the packed bed 3 removed from the mobile unit, and the stand-side system 200 has a sweep gas supply unit 9 that supplies a first sweep gas to the packed bed 3. Therefore, the recovery system 1 can desorb carbon dioxide using the first sweep gas, and can recover carbon dioxide while keeping energy costs down.

[0175] Furthermore, the recovery system 1 includes a stand-side system 200 that recovers carbon dioxide from the packed bed 3 after it has been removed from the mobile unit, and the stand-side system 200 has a steam supply unit 4 that supplies steam to the packed bed 3. Therefore, the recovery system 1 can recover carbon dioxide from the packed bed 3 in a short time by utilizing heat.

[0176] Furthermore, the steam supply unit 4 controls the temperature inside the packed bed 3 when carbon dioxide is recovered from the packed bed 3. This allows the steam supply unit 4 to prevent excessive moisture from being adsorbed onto the adsorbent material 33. In addition, the recovery system 1 can rapidly flow a large amount of steam into the packed bed 3. As a result, the recovery system 1 can recover carbon dioxide at high speed.

[0177] Furthermore, the steam supply unit 4 controls the internal pressure of the packed bed 3 when carbon dioxide is recovered from the packed bed 3. This allows the steam supply unit 4 to prevent excessive moisture from being adsorbed onto the adsorbent material 33. In addition, the steam supply unit 4 can lower the partial pressure of carbon dioxide in the packed bed 3. Moreover, the steam supply unit 4 can rapidly flow a large amount of steam into the packed bed 3. As a result, the recovery system 1 can rapidly recover carbon dioxide from the packed bed 3.

[0178] Furthermore, the packing density of the sorbent 33 in the packed bed 3 is 10% to 95% by volume. This allows the recovery system 1 to reduce pressure loss when carbon dioxide is recovered from the packed bed 3. As a result, the recovery system 1 can recover carbon dioxide from the packed bed 3 at high speed.

[0179] Furthermore, in the recovery system 1, the packed bed 3 is composed of at least a housing 31, and automatic on / off valves are provided at both ends of the housing 31. The automatic on / off valves are opened when the housing 31 is attached to the attachment / detachment part 60, and closed when the housing 31 is removed from the attachment / detachment part 60. Therefore, the recovery system 1 can prevent carbon dioxide adsorbed on the adsorbent material 33 from leaking out of the housing 31 when the housing 31 is removed from the attachment / detachment part 60.

[0180] Furthermore, the recovery system 1 can use the carbon dioxide recovered by the carbon dioxide recovery unit 5 for photosynthesis. This allows for the effective utilization of the recovered carbon dioxide.

[0181] The processes and procedures described herein can be implemented not only by those expressly described herein, but also by software, hardware, or a combination thereof. Specifically, the processes and procedures described herein can be implemented by implementing the logic corresponding to the process on a medium such as an integrated circuit, volatile memory, non-volatile memory, magnetic disk, or optical storage. Furthermore, the processes and procedures described herein can be implemented as computer programs and executed by various computers, including terminal devices and server devices.

[0182] Even if it is stated that the processes and procedures described herein are performed by a single device, software, component, or module, such processes or procedures may be performed by multiple devices, multiple software programs, multiple components, and / or multiple modules. Similarly, even if it is stated that the various types of information described herein are stored in a single memory or storage unit, such information may be distributed and stored in multiple memories within a single device or in multiple memories distributed across multiple devices. Furthermore, the software and hardware elements described herein may be implemented by integrating them into fewer components or by decomposing them into more components.

[0183] 1 Recovery system 100 Mobile system 101 Mobile system 200 Stand system 3 Packed bed 31 Housing 32 Internal space 33 Adsorbent 4 Steam supply unit 5 Carbon dioxide recovery unit 7 Retained gas recovery unit 20 Bypass 21 Branch 22 Confluence 30 Inlet passage 40 First cooling unit 50 Second cooling unit 60 Detachable unit 70 Outlet passage 80 Inlet passage valve 90 Outlet passage valve 8 Processing unit

Claims

A packed bed attached to a mobile body, having an sorbent material that sorbs carbon dioxide, The movable body is provided with a detachable part that allows the filling layer to be attached and detached, A recovery system equipped with [the following features]. 　 The recovery system according to claim 1, wherein the carbon dioxide is contained in at least the gas emitted from the heat engine of the mobile body. 　 The recovery system according to claim 1, wherein the sorbent material is capable of sorbing carbon dioxide at least at atmospheric pressure. 　 The recovery system according to claim 1, wherein the sorbent is capable of sorbing carbon dioxide at least at room temperature. 　 The system includes a stand-side system for recovering carbon dioxide from the packed bed removed from the mobile body, The recovery system according to claim 1, wherein the stand-side system has a sweep gas supply unit that supplies a first sweep gas to the packed bed. 　 The system includes a stand-side system for recovering carbon dioxide from the packed bed removed from the mobile body, The recovery system according to claim 1, wherein the stand-side system has a steam supply unit that supplies steam to the packed bed. 　 The recovery system according to claim 6, wherein the steam supply unit controls the temperature inside the packed bed when carbon dioxide is recovered from the packed bed. 　 The recovery system according to claim 6, wherein the steam supply unit controls the pressure inside the packed bed when carbon dioxide is recovered from the packed bed. 　 The recovery system according to claim 1, wherein the packing density of the sorbent in the packed bed is 10% to 95% by volume. 　 The filling layer consists of at least a housing, The recovery system according to claim 1, wherein automatic opening and closing valves are provided at both ends of the housing. 　 The recovery system according to claim 10, wherein the automatic opening and closing valve is in an open state when the housing is attached to the detachable part, and in a closed state when the housing is removed from the detachable part. 　 The carbon dioxide contained in the gas emitted from the heat engine of the mobile body is adsorbed onto the adsorbent material of the packed bed attached to the mobile body, In a stand-side system installed at a collection stand, the carbon dioxide is recovered from the packed bed removed from the mobile body, A method that includes this. 　 The method according to claim 12, wherein the recovered carbon dioxide is used for photosynthesis.

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