Supply system for carbon dioxide-containing gas, application method, and method for producing carbon dioxide

Abstract

Provided is a system for supplying carbon dioxide-containing gas to a carbon dioxide demand unit, the system comprising: a heat storage tank that houses an adsorbent that generates heat by adsorbing an adsorbate, and delivers introduced air to be treated as dry air the temperature of which is higher than that of the air to be treated; and a carbon dioxide recovery tank that houses a carbon dioxide adsorbent capable of adsorbing and desorbing carbon dioxide, desorbs the carbon dioxide by means of the introduced dry air, and delivers the resultant gas to the demand unit as a carbon dioxide-containing gas.

Description

Technical Field

[0001] The present invention relates to a carbon dioxide-containing gas supply system , give method of use and a method for producing carbon dioxide.

Background Art

[0002] Conventionally, in protected horticulture using greenhouses such as plastic greenhouses, for the purpose of promoting crop growth and increasing yield, carbon dioxide-containing gas generated by burning fuels such as kerosene and propane gas is supplied into the greenhouse to promote photosynthesis of crops.

[0003] For example, Patent Document 1 discloses a supply apparatus for supplying carbon dioxide-containing gas to a crop production facility. The supply apparatus described in Patent Document 1 includes a combustion furnace for burning fuel, removes sulfur oxides, dust, nitrogen oxides, carbon monoxide and ethylene contained in combustion exhaust gas, and supplies the combustion exhaust gas purified by removing these substances to the crop production facility.

[0004] Further, Patent Document 2 discloses a carbon dioxide supply apparatus for horticultural facilities that utilizes carbon dioxide in combustion exhaust gas. The carbon dioxide supply apparatus described in Patent Document 2 is provided with a carbon dioxide recovery and storage means using a carbon dioxide adsorbent (such as zeolite or activated carbon) capable of adsorbing and desorbing according to the carbon dioxide concentration difference, recovers and concentrates carbon dioxide from combustion gas, stores the concentrated carbon dioxide, and releases the stored carbon dioxide into the greenhouse when the carbon dioxide concentration in the greenhouse decreases.

[0005] Further, as a means for recovering carbon dioxide to be supplied into a greenhouse, in addition to the adsorbents such as zeolite and activated carbon disclosed in the above-mentioned Patent Document 2, an ion exchange resin for extracting, separating and recovering carbon dioxide from gas as disclosed in Patent Document 3 is known. Compared with the above adsorbents that recover carbon dioxide by physical adsorption, this ion exchange resin can recover a large amount of carbon dioxide by a chemical means called ion exchange adsorption, so that the efficiency related to carbon dioxide recovery can be improved. [Prior art documents] [Patent Documents]

[0006] [Patent Document 1] Japanese Patent Publication No. 2016-36334 [Patent Document 2] Japanese Patent No. 6178815 [Patent Document 3] Japanese Patent No. 5849327 [Overview of the project] [Problems that the invention aims to solve]

[0007] Incidentally, this ion exchange resin is less heat-resistant than the adsorbent mentioned above and is generally used for carbon dioxide recovery from ambient air. That is, if an ion exchange resin is to be used to recover carbon dioxide from high-temperature combustion exhaust gas, as shown in Patent Documents 1 and 2, a means of cooling the combustion exhaust gas, such as a cooling tower, is required before the ion exchange resin, which leads to a larger carbon dioxide recovery system and increased costs.

[0008] On the other hand, when carbon dioxide recovered by ion exchange resin is applied to a greenhouse, if the temperature of the desorption air used to desorb carbon dioxide from the ion exchange resin is low, the amount of carbon dioxide desorbed from the ion exchange resin decreases. Therefore, in order to increase the desorption efficiency of carbon dioxide recovered by ion exchange resin, a means of heating the desorption air is required in front of the ion exchange resin, and from this perspective, there are concerns that the recovery system will become larger and more expensive.

[0009] This disclosure is made in view of the above circumstances and aims to provide a carbon dioxide-containing gas supply system capable of appropriately recovering carbon dioxide from high-temperature exhaust gas. [Means for solving the problem]

[0010] To address the aforementioned problems, the technology of this disclosure is a carbon dioxide-containing gas supply system to a carbon dioxide demand unit, characterized by comprising: a heat storage tank that houses an adsorbent that generates heat by adsorbing an adsorbate and sends out the taken-in air to be treated as dry air at a higher temperature than the air to be treated; and a carbon dioxide recovery tank that houses a carbon dioxide adsorbent capable of adsorbing and desorbing carbon dioxide, desorbs the carbon dioxide using the taken-in dry air, and sends the carbon dioxide-containing gas to the demand unit.

[0011] According to the above configuration, the air to be treated, which is to be supplied to the recovery tank containing the carbon dioxide adsorbent, is preheated by a heat storage tank containing the adsorbent, which is positioned upstream of the recovery tank. This improves the desorption efficiency of carbon dioxide from the carbon dioxide adsorbent, enabling the appropriate supply of carbon dioxide-containing gas to the carbon dioxide demand area. Furthermore, because the desorption efficiency of carbon dioxide can be improved in this way, the amount of carbon dioxide adsorbent to be filled into the recovery tank can be reduced, and as a result, the cost of the system configuration can be reduced.

[0012] Furthermore, the above configuration combines a heat storage tank that generates dry air from the air to be treated using physical adsorption, with a recovery tank that desorbs carbon dioxide using chemical reactions and physical adsorption. As a result, when applying carbon dioxide-containing gas to the demand area, it is not necessary to input energy such as electricity to generate the dry air used for carbon dioxide desorption (heating the air in the heat storage tank). Therefore, the energy consumption when generating carbon dioxide-containing gas for the demand area can be significantly reduced.

[0013] The demand unit may be a greenhouse in a protected horticulture facility. In this case, it is desirable to further provide a return air path for taking in the return air from the greenhouse as the air to be treated into the heat storage tank. In this case, the carbon dioxide-containing gas sent from the recovery tank into the greenhouse will be at least less humid than the return air flowing through the return air path. According to the above configuration, humid air from the greenhouse can be used as the air to be treated, and a low-humidity carbon dioxide-containing gas can be generated for supply to the greenhouse. This allows for dehumidification of the greenhouse, preventing diseases such as mold on the crops being grown.

[0014] The carbon dioxide-containing gas supply system may further include a carbon dioxide generation unit that generates carbon dioxide for recovery in the recovery tank by adsorbing it onto the carbon dioxide adsorbent. In this case, when recovering the carbon dioxide into the recovery tank, the heat storage tank takes in combustion gas from the carbon dioxide generation unit, desorbs the adsorbate from the adsorbent using the taken-in combustion gas, and sends it out as recovery air that is colder and more humid than the combustion gas. In the recovery tank, the carbon dioxide contained in the recovery air is adsorbed onto the carbon dioxide adsorbent, and the recovery air from which the carbon dioxide has been removed is discharged to the outside of the demand unit. According to the above configuration, carbon dioxide can be recovered by using the combustion gas from the carbon dioxide generation unit to collect carbon dioxide in the carbon dioxide adsorbent in the recovery tank. In this case, by selecting a factory or similar facility as the carbon dioxide generation unit, for example, the amount of carbon dioxide emitted into the atmosphere can be reduced, thereby reducing the environmental burden.

[0015] A transport unit may be further provided between the generating unit and the demanding unit to transport at least one of the heat storage tank and the recovery tank. According to the above configuration, even if the carbon dioxide generation unit and the carbon dioxide consumption unit are located in distant locations, carbon dioxide can be appropriately supplied to the consumption unit.

[0016] The carbon dioxide-containing gas supply system may further include a dehumidification unit for dehumidifying the recovery air that is sent from the heat storage tank and before being supplied to the recovery tank. According to the above configuration, the efficiency of carbon dioxide recovery (adsorption) in the recovery tank can be improved by dehumidifying the recovery air supplied to the recovery tank.

[0017] In one example, the carbon dioxide adsorbent may be an ion exchange resin. In this case, the ion exchange resin has an amine functional group in one example. In this case, carbon dioxide in the air to be treated can be properly adsorbed and recovered.

[0018] The carbon dioxide adsorbent may be selected from at least any one of ion exchange resins, moisture-resistant zeolites, activated carbon, porous coordination polymers (PCP), and metal-organic frameworks (MOF). Even in such a case, carbon dioxide in the air to be treated can be properly adsorbed and recovered.

[0019] In one example, the adsorbent can be selected from at least any one of zeolite or HUSKLEY (registered trademark). In this case, when applying carbon dioxide to the demand section, the air to be treated can be appropriately heated to a desired temperature, and the desorption efficiency of carbon dioxide from the ion exchange resin can be improved.

[0020] A technique according to another aspect of the present disclosure is a carbon dioxide-containing gas supply device, characterized by comprising: a heat storage tank configured to be capable of repeating a heat storage operation and a heat release operation by adsorption and desorption of an adsorbate with respect to an accommodated adsorbent; and a recovery tank configured to be capable of repeating recovery and supply of the carbon dioxide by adsorption and desorption of carbon dioxide with respect to an accommodated carbon dioxide adsorbent.

[0021] A technique according to still another aspect is a method for applying a carbon dioxide-containing gas to a carbon dioxide demand unit, the method comprising: a carbon dioxide recovery step including a combustion gas generation step of generating combustion gas by burning fuel, an adsorbate desorption step of desorbing an adsorbate from an adsorbent using the combustion gas to generate recovery air that is lower in temperature and higher in humidity than the combustion gas, and a carbon dioxide adsorption step of causing a carbon dioxide adsorbent to adsorb carbon dioxide contained in the recovery air; and a carbon dioxide supply step including an adsorbate adsorption step of causing the adsorbent to adsorb an adsorbate in target processing air supplied from the demand unit to generate dry air having a higher temperature than the target processing air, and a carbon dioxide desorption step of desorbing the carbon dioxide from the carbon dioxide adsorbent using the dry air and supplying the desorbed carbon dioxide as the carbon dioxide-containing gas to the demand unit.

[0022] A technique according to yet still another aspect is a method for producing carbon dioxide, the method comprising: a carbon dioxide recovery step including an adsorbate desorption step of desorbing an adsorbate from an adsorbent using high-temperature low-humidity air to generate recovery air that is lower in temperature and higher in humidity than the high-temperature low-humidity air, and a carbon dioxide adsorption step of causing a carbon dioxide adsorbent to adsorb carbon dioxide contained in the recovery air; and a carbon dioxide supply step including an adsorbate adsorption step of causing the adsorbent to adsorb an adsorbate from low-temperature high-humidity air to generate dry air having a higher temperature than the low-temperature high-humidity air, and a carbon dioxide desorption step of desorbing the carbon dioxide from the carbon dioxide adsorbent using the dry air to generate a carbon dioxide-containing gas containing the carbon dioxide. [Effects of the Invention]

[0023] According to the technique of the present disclosure, it is possible to provide a carbon dioxide-containing gas supply system capable of appropriately recovering carbon dioxide from high-temperature exhaust gas. [Brief Description of the Drawings]

[0024] [Figure 1] This is an explanatory diagram schematically showing an outline of the system of the supply system according to the embodiment. [Figure 2]This is a system diagram showing the carbon dioxide capture operation of the supply system. [Figure 3] This is a system diagram showing the operation of the carbon dioxide supply system. [Figure 4] This graph shows the change in the temperature of the adsorbent over time. [Figure 5] This is an explanatory diagram showing an example configuration of a supply system according to another embodiment. [Figure 6] This is an explanatory diagram showing an example configuration of a supply system according to the second embodiment. [Figure 7] This is an explanatory diagram showing an example configuration of a supply system according to the third embodiment. [Figure 8] This is an explanatory diagram showing an example configuration of a supply system according to the fourth embodiment. [Figure 9] This is a flowchart showing the main steps of operation of the supply system according to the fourth embodiment. [Figure 10] This is a flowchart showing the main steps of operation of the supply system according to the fourth embodiment. [Modes for carrying out the invention]

[0025] Embodiments of the present invention will be described below. Figure 1 schematically shows the system of a carbon dioxide-containing gas supply system 1 (hereinafter simply referred to as "supply system 1") according to an embodiment. In one embodiment, supply system 1 comprises a greenhouse 10, a carbon dioxide generation unit 20 (hereinafter simply referred to as "generation unit 20"), a heat storage tank 30, and a carbon dioxide recovery tank 40 (hereinafter simply referred to as "recovery tank 40"). In the following description, the heat storage tank 30 and the recovery tank 40 may be collectively referred to as the "carbon dioxide supply device".

[0026] The greenhouse 10, which is the recipient of the carbon dioxide supply, is a crop production facility such as a plant factory or plastic greenhouse, where crops and other plants are grown (protected horticulture) inside. In one embodiment, an exhaust duct 11 is connected to the greenhouse 10. The exhaust duct 11 discharges the air inside the greenhouse 10 to the outside as exhaust EA, thereby reducing the humidity (relative humidity) inside the greenhouse 10, which may have increased due to, for example, evapotranspiration from crops, evaporation of water from the soil surface, or artificial humidification.

[0027] The generation unit 20 generates carbon dioxide for supply to the greenhouse 10. The configuration of the generation unit 20 is not particularly limited, but may be, for example, a boiler that burns supplied fuel (e.g., liquid fuel such as heavy oil or kerosene, or gaseous fuel such as natural gas) and emits high-temperature carbon dioxide-containing gas as combustion gas, or a factory that emits high-temperature carbon dioxide-containing gas as exhaust gas. In other words, the carbon dioxide-containing gas supplied from the generation unit 20 may be generated for supply to the greenhouse 10, or it may be generated secondarily in the generation unit 20.

[0028] The generation unit 20 is connected to the inlet side (upstream side) of the heat storage tank 30, which will be described later, via the first duct 21. Furthermore, a return air duct 22 is connected to the first duct 21 for taking in return air RA from the greenhouse 10 into the heat storage tank 30. One end of the return air duct 22 is connected to the first duct 21, and the other end is connected to the exhaust duct 11 mentioned above for discharging exhaust EA from the greenhouse 10. At least a portion of the exhaust EA from the greenhouse 10 flows through the return air duct 22 as return air RA, and this return air RA is configured to be taken into the heat storage tank 30 via the first duct 21. In other words, the first duct 21 is configured to take in either carbon dioxide-containing gas from the generation unit 20 or return air RA from the greenhouse 10 taken in via the return air duct 22 as the air to be treated, to the heat storage tank 30 described later.

[0029] The first duct 21 and the return air duct 22 are each provided with corresponding dampers D1 and D2. In the supply system 1, the opening and closing of these dampers D1 and D2 is controlled, which allows switching of the treated air (carbon dioxide-containing gas from the generation unit 20 or return air RA from the greenhouse 10) taken into the heat storage tank 30. As an example, motor dampers that are easy to control may be used as dampers D1 and D2.

[0030] Furthermore, the return air duct 22 and the exhaust duct 11 are each provided with corresponding dampers D3 and D4. In the supply system 1, the opening and closing of these dampers D3 and D4 is controlled to control the discharge of air from the greenhouse 10 (exhaust EA) or the circulation of air to the heat storage tank 30 (return air RA). For example, motor dampers that are easy to control may be used for these dampers D3 and D4.

[0031] Furthermore, the first duct 21 may be provided with an air supply unit 23 for taking in the air to be treated (carbon dioxide-containing gas from the generation unit 20, or return air RA from the greenhouse 10) into the heat storage tank 30, as shown in Figure 1.

[0032] The heat storage tank 30 has a filled section 31 partitioned by a breathable partition plate and filled with an adsorbent M, and spaces 32 and 33 are provided on the upstream and downstream sides of the filled section 31.

[0033] In one embodiment, the adsorbent M to be filled in the filling section 31 can be, for example, a granulated adsorbent. This adsorbent M can be a known adsorbent that generates heat by adsorbing an adsorbate (e.g., water, water vapor), and a granular body of an adsorbent having desired properties such as airflow resistance and heat / mass transfer can be used as an adsorbent with heat storage function. In such cases, a composite made of amorphous aluminum silicate and low-crystallinity clay, such as Huskclay® or a low-temperature regenerative adsorbent of polymer sorbent, or a conventional adsorbent (silica gel, zeolite, etc.) can be applied as the adsorbent M. The amount of adsorbent M to be filled into the heat storage tank 30 (filling section 31) is determined to be an amount that can appropriately achieve carbon dioxide adsorption and desorption in the recovery tank 40 described later. In one example, it is desirable that the amount of adsorbent M to be filled into the heat storage tank 30 (filling section 31) be at least one-third of the amount of ion exchange resin 41 to be filled into the recovery tank 40 described later.

[0034] A first duct 21 is connected to the space 32 on the inlet side of the heat storage tank 30 for taking in the air to be treated (carbon dioxide-containing gas from the generation unit 20, or return air RA from the greenhouse 10). The recovery tank 40, described later, is connected to the space 33, which is the outlet side (downstream side) of the heat storage tank 30, via the second duct 34.

[0035] In the heat storage tank 30, the air to be treated is taken in from the upstream space 32, passed through the filling section 31 to the space 33, and then sent to the recovery tank 40 via the second duct 34. At this time, the air to be treated is brought into contact with the adsorbent M filled in the filling section 31, thereby promoting the adsorption and desorption reaction of adsorbate to the adsorbent M, and thereby controlling the temperature and humidity of the taken-in air to be treated. Hereinafter, the operation of taking in high-humidity air to be treated and adsorbing the adsorbate in the air to be treated onto the adsorbent M is referred to as the "heat dissipation operation" of the heat storage tank 30. Also, the operation of taking in high-temperature air to be treated and desorbing adsorbate from the adsorbent M to the air to be treated is referred to as the "heat storage operation" of the heat storage tank 30. The detailed methods for the heat dissipation and heat storage operations of the heat storage tank 30 will be described later.

[0036] The recovery tank 40 contains an ion exchange resin 41, which acts as a carbon dioxide adsorbent, for separating and recovering carbon dioxide from the carbon dioxide-containing gas taken in by ion exchange. The type of ion exchange resin 41 is not particularly limited as long as it can separate and recover carbon dioxide from the carbon dioxide-containing gas, but for example, an ion exchange resin having an amine functional group, such as a weakly basic anion exchange resin, can be selected. Furthermore, the amount of ion exchange resin 41 to be filled into the recovery tank 40 is determined to be an amount that can cover the required amount of carbon dioxide-containing gas in the greenhouse 10, which is the target of the carbon dioxide-containing gas supply, that is, an amount that can adsorb more carbon dioxide than the required amount in the greenhouse 10.

[0037] Furthermore, the carbon dioxide adsorbent packed into the recovery tank 40 is not limited to ion exchange resin. For example, at least one of the following can be used in place of or in addition to the ion exchange resin: zeolite with moisture resistance (that does not easily adsorb moisture), activated carbon, and porous coordination polymer (PCP) / metal-organic framework (MOF). In the following explanation, we will use the case where the carbon dioxide adsorbent is an ion exchange resin 41 as an example.

[0038] The heat storage tank 30 is connected to the inlet side (upstream side) of the recovery tank 40 via the second duct 34 described above. The outlet side (downstream side) of the recovery tank 40 is connected to the greenhouse 10 via the third duct 42.

[0039] The recovery tank 40 then takes in the air to be treated, which is sent from the heat storage tank 30 from the upstream side. After passing the taken-in air through the ion exchange resin 41, it is sent towards the greenhouse 10 via the third duct 42. At this time, the air to be treated comes into contact with the ion exchange resin 41, which promotes the adsorption and desorption reaction of carbon dioxide to the ion exchange resin 41. The detailed operation of the recovery tank 40 will be described later.

[0040] The third duct 42 is connected to an exhaust duct 43 for exhausting the treated air sent from the recovery tank 40 to the outside without supplying it to the greenhouse 10. The exhaust duct 43 primarily functions in the carbon dioxide recovery process described later.

[0041] The third duct 42 and the exhaust duct 43 are each provided with corresponding dampers D5 and D6. In the supply system 1, the opening and closing of these dampers D5 and D6 can be controlled to switch between drawing the air to be treated from the recovery tank 40 into the greenhouse 10 or exhausting it to the outside via the exhaust duct 43. For example, motor dampers that are easy to control may be used for these dampers D5 and D6.

[0042] In the example shown in Figure 1, the exhaust duct 43 is connected to the third duct 42, but instead, the exhaust duct 43 may be connected to the recovery tank 40 independently of the third duct 42.

[0043] The supply system 1 configured as described above may also be provided with a control unit 2. The control unit 2 controls the operation of supplying carbon dioxide-containing gas to the greenhouse 10 by the supply system 1, more specifically, the operation of the various elements constituting the supply system 1 (greenhouse 10, generation unit 20, heat storage tank 30, recovery tank 40, and various dampers). The control unit 2 may be configured integrally with the supply system 1, or the supply system 1 may be configured to be controllable remotely.

[0044] The supply system 1 according to the embodiment is configured as described above. Next, an example of the operation of the supply system 1 described above will be explained. In the supply system 1 according to this embodiment, a carbon dioxide-containing gas is generated in the generation unit 20, and the carbon dioxide in the carbon dioxide-containing gas is recovered by adsorption onto the ion exchange resin 41 in a "carbon dioxide recovery operation," and the adsorbed carbon dioxide is desorbed from the ion exchange resin 41 and supplied to the greenhouse 10 in a "carbon dioxide supply operation," which is performed alternately and repeatedly. The details of these carbon dioxide recovery operation and carbon dioxide supply operation will be described below.

[0045] <Carbon dioxide capture operation of supply system 1> First, we will explain the carbon dioxide capture operation (carbon dioxide capture process) of supply system 1. Figure 2 is a schematic diagram showing an example of the operation of supply system 1 during carbon dioxide capture operation. In Figure 2, among the various dampers provided by supply system 1, dampers in the open state are shown in white, and dampers in the closed state are shown in black. Also, among the various ducts through which various types of air pass, ducts through which air is passing are shown with thick lines, and ducts through which air is not passing are shown with thin lines.

[0046] In the carbon dioxide recovery operation of supply system 1, first, the generation unit 20 generates a combustion gas containing carbon dioxide (carbon dioxide-containing gas) to be recovered into the recovery tank 40 (combustion gas generation step). Subsequently, damper D1 is opened and damper D2 is closed, thereby allowing the high-temperature, low-humidity carbon dioxide-containing gas ("CO2" in the figure), which is the air to be treated, generated in the generation unit 20, to be taken into the heat storage tank 30 via the first duct 21. In one example, the temperature and humidity of the carbon dioxide-containing gas taken into the heat storage tank 30 are 110°C or higher, 10%RH, and 75m³. 3 It is / h. At this time, prior to intake into the heat storage tank 30, the carbon dioxide-containing gas supplied from the generation unit 20 may be pre-treated to remove harmful gases and dust using a pre-treatment device that includes at least one of the following: a denitrification mechanism, a wet scrubber, a desulfurization mechanism, a bag filter, etc. This pre-treatment device may be located upstream of the heat storage tank 30, for example, on the first duct 21, or it may be included in the generation unit 20.

[0047] In the heat storage tank 30, heat storage operation is performed by taking in high-temperature, low-humidity carbon dioxide-containing gas. Specifically, the carbon dioxide-containing gas taken into the heat storage tank 30 is sent from the space 32 of the heat storage tank 30 to the filling section 31, and passes through the adsorbent M that is filled in the filling section 31. At this time, the moisture (adsorbate) adsorbed on the adsorbent M is desorbed by the high-temperature, low-humidity carbon dioxide-containing gas, and the carbon dioxide-containing gas is cooled by the latent heat of vaporization (cold) generated during this desorption of moisture (adsorbate desorption step). As a result, recovery air CA (hereinafter simply referred to as "recovery air CA") with a lower temperature and higher humidity than the taken-in carbon dioxide-containing gas is generated. In one example, the temperature and humidity of the recovery air CA are 20°C, 70%RH, and 75m 3 It is / h. The generated recovered air CA is sent downstream (to the recovery tank 40) via the second duct 34.

[0048] Next, in the recovery tank 40, carbon dioxide recovery (adsorption) is performed by taking in recovery air CA from the heat storage tank 30. Specifically, the recovery air CA taken into the recovery tank 40 passes through the ion exchange resin 41 housed in the recovery tank 40. At this time, for example, if an ion exchange resin 41 having an amine functional group is used as described above, the amine functional group acts as an adsorption filter for carbon dioxide, thereby allowing carbon dioxide in the recovery air CA to be adsorbed onto the ion exchange resin 41 and recovered (carbon dioxide adsorption step).

[0049] Subsequently, the recovered air CA, from which carbon dioxide has been removed in the recovery tank 40, is sent to the third duct 42. At this time, damper D6 is opened and damper D5 is closed, thereby discharging the recovered air CA from the recovery tank 40 as exhaust EA to the outside of the greenhouse 10 via the exhaust duct 43. The exhaust duct 43 may be connected to the exhaust system of the generation unit 20, for example, if the generation unit 20 is a factory, or it may be configured to discharge exhaust EA into the atmosphere. At this time, the exhaust EA from the exhaust duct 43 is clean exhaust from which heat and carbon dioxide have been removed in both the heat storage tank 30 and the recovery tank 40, thus appropriately reducing the environmental burden caused by the emission of exhaust EA.

[0050] The carbon dioxide capture operation of supply system 1 is controlled as described above.

[0051] As mentioned above, ion exchange resins are generally sensitive to heat, and their performance tends to deteriorate significantly at high temperatures. For example, the heat resistance of ion exchange resins is approximately 100°C in an oxygen-free environment and approximately 50°C to 60°C in an oxygen-containing environment. Therefore, if high-temperature carbon dioxide-containing gas from a production source (such as a boiler or factory) is supplied directly to the ion exchange resin, there is a risk that carbon dioxide may not be recovered properly.

[0052] In this regard, in the carbon dioxide recovery operation of the supply system 1 according to this embodiment, prior to supplying to the recovery tank 40, the adsorbent M contained in the heat storage tank 30 is used to cool the high-temperature carbon dioxide-containing gas generated in the generation unit 20 to a desired temperature, such as room temperature, in which adsorption of carbon dioxide onto the ion exchange resin 41 can be achieved. This suppresses the performance degradation of the ion exchange resin 41 due to high temperature, and allows for appropriate adsorption and recovery of carbon dioxide onto the ion exchange resin 41.

[0053] Furthermore, according to the supply system 1 of this embodiment, the high-temperature carbon dioxide-containing gas generated in the generation unit 20 can be cooled using only the desorption reaction of adsorbate from the adsorbent M. In other words, when cooling the carbon dioxide-containing gas, electricity is not required, unlike conventional cooling mechanisms (e.g., cooling towers, radiators, dehumidifiers, etc.), enabling carbon dioxide recovery at a lower cost and with greater energy savings.

[0054] <Carbon dioxide supply operation of supply system 1> Next, we will explain the carbon dioxide supply operation (carbon dioxide supply process) of supply system 1. Figure 3 is a schematic diagram showing an example of the operation of supply system 1 during carbon dioxide supply operation. As with Figure 2, among the various dampers provided by supply system 1, dampers in the open state are shown in white, and dampers in the closed state are shown in black. In addition, among the various ducts through which various types of air pass, ducts through which air is passing are shown with thick lines, and ducts through which air is not passing are shown with thin lines.

[0055] When supplying carbon dioxide using supply system 1, dampers D2 and D3 are first opened, and dampers D1 and D4 are closed. This allows the low-temperature, high-humidity return air RA, which is exhaust EA from inside the greenhouse 10, to be taken into the thermal storage tank 30 as the air to be treated via the return air duct 22 and the first duct 21. In one example, the temperature and humidity of the return air RA taken into the thermal storage tank 30 are 20°C, 70%RH, and 75m³. 3 It is / h. At this time, the damper D4 does not necessarily have to be completely closed; the opening of the damper D4 can be adjusted so that a portion of the exhaust EA is taken into the heat storage tank 30 as return air RA.

[0056] In the heat storage tank 30, heat dissipation is performed by taking in low-temperature, high-humidity return air RA. Specifically, the return air RA taken into the heat storage tank 30 is sent from the space 32 of the heat storage tank 30 to the filling section 31 and passes through the adsorbent M that is filled in the filling section 31. At this time, moisture (adsorbate) in the return air RA is adsorbed by the adsorbent M, and as a result the adsorbent M generates heat, and dry air DA (in one example, 60°C, 5%RH, 75m³) which is hotter and less humid than the return air RA is released. 3 (Adsorbate adsorption step) is generated ( / h). The generated dry air DA is sent from space 33 to the downstream side (recovery tank 40) via the second duct 34.

[0057] Here, the amount of heat released by the adsorbent M in the heat storage tank 30, in other words, the temperature of the dry air DA sent from the heat storage tank 30, is determined by the amount of adsorbent M packed into the packing section 31. For this reason, the amount of adsorbent M packed into the packing section 31 is determined so that it reaches a desired temperature (for example, 60°C) at which desorption of carbon dioxide from the ion exchange resin 41 can be achieved. In this case, it is desirable that the amount of adsorbent M packed into the packing section 31 in one embodiment be at least 1 / 3 of the amount of ion exchange resin 41 packed into the recovery tank 40, as described above.

[0058] Next, in the recovery tank 40, a carbon dioxide supply (desorption) operation is performed by taking in dry air DA from the heat storage tank 30. Specifically, the dry air DA taken into the recovery tank 40 passes through the ion exchange resin 41 contained in the recovery tank 40. At this time, the carbon dioxide adsorbed on the ion exchange resin 41 is desorbed by the high-temperature dry air DA, and a carbon dioxide-containing gas (CO2 in the figure) is generated in which carbon dioxide is attached to the taken-in dry air DA (carbon dioxide desorption step). In one example, the temperature and humidity of the carbon dioxide-containing gas are 50°C, 15%RH, and 75m³. 3 It is / h.

[0059] The carbon dioxide-containing gas generated in the recovery tank 40 is sent to the third duct 42. At this time, damper D5 is opened and damper D6 is closed, thereby supplying the carbon dioxide-containing gas to the greenhouse 10 via the third duct 42. At this time, the carbon dioxide-containing gas supplied to the greenhouse 10 is used for heat dissipation operation in the heat storage tank 30, and therefore has a lower humidity than the return air RA sent from the greenhouse 10 to the heat storage tank 30 via the return air duct 22. In other words, by using the humid air inside the greenhouse 10 as the air to be treated and sent to the heat storage tank 30, moisture is adsorbed by the adsorbent M, thus dehumidifying the inside of the greenhouse 10.

[0060] The carbon dioxide supply operation of supply system 1 is controlled as described above.

[0061] Furthermore, in order to properly grow crops and other organisms (protected horticulture) inside greenhouse 10, it is desirable that the carbon dioxide concentration inside greenhouse 10 be controlled to a constant level at a predetermined set concentration.

[0062] From this perspective, the amount of carbon dioxide desorbed in the recovery tank 40, that is, the amount of carbon dioxide supplied to the greenhouse 10, may be controlled by the operation of the air supply unit 23. Specifically, the desorption of carbon dioxide in the recovery tank 40 may be controlled by controlling the airflow rate, ON / OFF control, and opening degree of the return air RA supplied by the air supply unit 23 toward the heat storage tank 30 during carbon dioxide supply operation.

[0063] Alternatively, instead of, or in addition to, controlling the air supply unit 23 as described above, the temperature of the dry air DA sent from the heat storage tank 30 to the downstream recovery tank 40 may be controlled. That is, in order to stabilize the desorption of carbon dioxide in the ion exchange resin 41 and to control the concentration of carbon dioxide-containing gas supplied to the greenhouse 10 to a constant level, the temperature of the dry air DA sent from the heat storage tank 30 to the downstream recovery tank 40 may be controlled to a constant level.

[0064] In this case, it is desirable that the timing of supplying dry air DA from the heat storage tank 30 to the recovery tank 40 be controlled after the temperature of the adsorbent M in the heat storage tank 30 has stabilized (reached equilibrium). Specifically, during heat dissipation operation, the temperature of the adsorbent M rises sharply after the reaction starts (after adsorption of moisture from the return air RA begins) (time t1 in Figure 4), then stabilizes (time t2 in Figure 4), and then gradually decreases (time t3 in Figure 4). The temperature of the adsorbent M at the time of temperature stabilization (time t2) (maximum temperature) and the duration (reaction time) vary depending on the amount and type of adsorbent M used. Therefore, in the heat storage tank 30 according to this embodiment, it is desirable to start supplying dry air DA to the recovery tank 40 at time t2 when the temperature of the adsorbent M has stabilized (at the equilibrium temperature of the adsorbent M), and to stop supplying dry air DA before time t3 when the temperature drops. In this case, the supply / stopping of dry air DA from the heat storage tank 30 to the recovery tank 40 may be controlled by opening and closing a damper (e.g., an easily controllable motor damper) not shown, which is provided on the second duct 34.

[0065] Furthermore, when controlling the amount of carbon dioxide desorbed in the recovery tank 40 by controlling the air supply unit 23 as described above, the temperature of the dry air DA sent from the heat storage tank 30 to the downstream recovery tank 40 does not necessarily need to be controlled to a constant level.

[0066] Generally, ion exchange resins readily desorb carbon dioxide at high temperatures due to their adsorption properties. For example, the desorption capacity of an ion exchange resin is approximately 50 mg / g (CO2 / adsorbent) at room temperature (e.g., 25°C) and approximately 100 mg / g (CO2 / adsorbent) at high temperature (e.g., 60°C). Therefore, the air taken into the recovery tank 40 during carbon dioxide supply operation must be preheated.

[0067] In this regard, in the carbon dioxide supply operation of the supply system 1 according to this embodiment, prior to supplying to the recovery tank 40, the return air RA from the greenhouse 10 is heated to a desired temperature, for example, 40°C to 100°C, using the adsorbent M contained in the heat storage tank 30, so that carbon dioxide can be desorbed from the ion exchange resin 41. This effectively desorbs carbon dioxide from the ion exchange resin 41, and carbon dioxide-containing gas can be appropriately supplied to the greenhouse 10.

[0068] Furthermore, according to the supply system 1 of this embodiment, by using high-temperature dry air DA from the heat storage tank 30 to desorb carbon dioxide from the ion exchange resin 41, the amount of carbon dioxide desorbed can be approximately doubled compared to the case where ambient temperature air is used, as described above. In other words, by combining the ion exchange resin 41 in the recovery tank 40 and the adsorbent M in the heat storage tank 30 in the supply system 1, the amount of ion exchange resin 41 to be filled into the recovery tank 40 can be significantly reduced. Furthermore, by using this inexpensive adsorbent M, the amount of expensive ion exchange resin 41 used can be reduced, thereby significantly lowering the cost of the supply system 1 compared to a conventional system that uses only ion exchange resin 41.

[0069] Furthermore, according to the supply system 1 of this embodiment, the heating of the return air RA from the greenhouse 10 can be performed using only the adsorption reaction of the adsorbate to the adsorbent M. More specifically, the return air RA can be heated using only the heat stored in the heat storage tank 30 during the carbon dioxide recovery operation of the supply system 1. For this reason, when supplying carbon dioxide-containing gas to the greenhouse 10, there is no need to provide an independent mechanism (e.g., a heater) for heating the return air RA as in the conventional method, and in other words, electricity is not required for the generation of dry air DA used for carbon dioxide desorption (heating of the return air RA by the heat storage tank). As a result, carbon dioxide can be applied to the greenhouse 10 at a lower cost and with less energy.

[0070] Thus, the supply system 1 according to the technology of this disclosure can be described as a method of separating and recovering carbon dioxide from a carbon dioxide-containing gas containing impurities generated in the generation unit 20 using an ion exchange resin 41, thereby purifying a carbon dioxide-containing gas to a purity at least higher than that of the original carbon dioxide-containing gas. In other words, the method of applying carbon dioxide using the supply system 1 according to the technology of this disclosure can be said to have aspects of a method for producing carbon dioxide for supply to a greenhouse 10.

[0071] <Effects and Effects of Supply System 1 According to the Embodiment> As described above, according to the supply system 1 of the technology disclosed herein, a heat storage tank 30 for controlling the temperature of the air supplied to the recovery tank 40 is arranged upstream of the recovery tank 40 which contains an ion exchange resin 41 for recovering / supplying carbon dioxide. This allows the temperature of the carbon dioxide-containing gas supplied to the recovery tank 40 to be lowered during the carbon dioxide recovery operation in the supply system 1, enabling proper adsorption of carbon dioxide onto the ion exchange resin 41. On the other hand, in the carbon dioxide supply operation of the supply system 1, the temperature of the return air RA supplied to the recovery tank 40 can be increased, thereby increasing the amount of carbon dioxide desorbed from the ion exchange resin 41 (improving desorption efficiency).

[0072] Furthermore, according to the supply system 1 of the technology disclosed herein, as described above, the amount of carbon dioxide desorbed from the ion exchange resin 41 can be increased (desorption efficiency can be improved), thereby reducing the amount of ion exchange resin 41 to be filled into the recovery tank 40, and thus reducing costs.

[0073] Furthermore, according to the supply system 1 of the technology disclosed herein, both the cooling of the carbon dioxide-containing gas supplied to the recovery tank 40 and the heating of the return gas RA can be performed using only the heat storage tank 30 located upstream of the recovery tank 40, as described above. Therefore, compared to conventional methods that involve independently connecting external heat sources such as cooling towers for cooling carbon dioxide-containing gases or heaters for heating return gas (RA), costs can be significantly reduced, and the system footprint can be drastically decreased.

[0074] In the above embodiment, the explanation was given using the example of a case where the carbon dioxide supply device (heat storage tank 30 and recovery tank 40) is installed between the generation unit 20, which is the source of carbon dioxide, and the greenhouse 10, which is the demand site for carbon dioxide. In other words, the operation of recovering carbon dioxide from the generation unit 20 by the recovery tank 40 and the operation of supplying carbon dioxide to the greenhouse 10 were performed at the same location. However, in this embodiment, the heat storage tank 30 and the recovery tank 40 that constitute the carbon dioxide supply device store heat and carbon dioxide, respectively, using physical adsorption and chemical adsorption, making it possible to store this heat and carbon dioxide for a long period of time.

[0075] From this perspective, the carbon dioxide supply device according to this embodiment can appropriately supply carbon dioxide to the greenhouse 10 using the recovery tank 40, even when the generation unit 20 and the greenhouse 10 are located in remote locations. Specifically, the carbon dioxide supply system 1 according to this embodiment may further include a transport unit 50 for transporting the carbon dioxide supply device (heat storage tank 30 and recovery tank 40) between the generation unit 20 and the greenhouse 10, as shown in Figure 5. The type of transport unit 50 is not particularly limited as long as it can carry and transport the carbon dioxide supply device, and includes, for example, a container for housing the carbon dioxide supply device, a trailer or ship for transporting the container, or an aircraft.

[0076] In the example shown in Figure 5, the supply system 1 performs a carbon dioxide capture operation at the generation unit 20, which is the carbon dioxide emission site, to store the carbon dioxide in the recovery tank 40. Then, the transport unit 50 transports the carbon dioxide supply device to the carbon dioxide demand site, and after that, a carbon dioxide supply operation is performed to supply carbon dioxide-containing gas from the recovery tank 40 to the greenhouse 10.

[0077] By configuring the carbon dioxide supply device to be transportable by the transport unit 50, as described above, even if the generation unit 20, which is the carbon dioxide supply source, and the greenhouse 10, which is the carbon dioxide demand site, are located in distant locations, the carbon dioxide-containing gas can be appropriately applied to the greenhouse 10.

[0078] Furthermore, in the supply system 1 relating to the technology disclosed herein, as described above, the amount of ion exchange resin 41 to be filled into the recovery tank 40 can be reduced. Therefore, according to the supply system 1 relating to the disclosed technology, even when transporting the carbon dioxide supply device between the generation unit and the greenhouse 10 in this manner, the amount of transport (load) can be reduced, thereby achieving further cost reductions.

[0079] In the example shown in Figure 5, the illustration illustrates a case where the heat storage tank 30 and the recovery tank 40, which constitute the carbon dioxide supply device, are transported together. However, the heat storage tank 30 and the recovery tank 40 may be configured to be transported independently. Alternatively, at least one of the heat storage tank 30 and the recovery tank 40 may be transported by the transport unit 50. For example, in the above example, only the carbon dioxide supply device (heat storage tank 30 and recovery tank 40) was transported by the transport unit 50, but in addition, an air supply unit 23 for taking in the air to be treated into the supply device may also be configured to be transportable.

[0080] In the above embodiments, the recovery air CA from the heat storage tank 30 was directly supplied to the recovery tank 40 during the adsorption of carbon dioxide onto the ion exchange resin 41 (carbon dioxide recovery operation). However, the recovery air CA from the heat storage tank 30 may be dehumidified (dried) prior to being supplied to the recovery tank 40.

[0081] Figure 6 schematically shows the system of the supply system 100 according to the second embodiment. In one embodiment, the supply system 100 has, in addition to the configuration of the supply system 1 shown in Figure 1, a dehumidification unit 110 located between the heat storage tank 30 and the recovery tank 40, in other words, in the second duct 34.

[0082] The dehumidification unit 110 dehumidifies (dries) the recovered air CA supplied from the heat storage tank 30 to the recovery tank 40 before it is taken into the recovery tank 40. The configuration of the dehumidification unit 110 is not particularly limited as long as it can dehumidify (dry) the recovered air CA, and any one of the following can be adopted, for example, a dehumidifier, an indirect heat exchanger, or a dehumidification tank filled with a desiccant.

[0083] Furthermore, in the supply system 100, by dehumidifying (drying) the recovery air CA prior to supplying it to the recovery tank 40 (ion exchange resin 41), the efficiency of carbon dioxide recovery (adsorption) by the ion exchange resin 41 in the recovery tank 40 can be improved. Specifically, since the ion exchange resin 41 has a physical adsorption effect in addition to the ion exchange effect, by dehumidifying (drying) the recovery air CA in advance in this manner, the physical adsorption of moisture to the ion exchange resin 41 can be suppressed, thereby increasing the amount of carbon dioxide that can be physically adsorbed.

[0084] In the embodiments described above, the heat storage tank 30 and the recovery tank 40 were configured as separate units, but these two units may be configured as a single unit. Figure 7 schematically shows the system of the supply system 200 according to the third embodiment in which the heat storage tank 30 and the recovery tank 40 are configured as a single unit.

[0085] In the supply system 200, a heat storage chamber 230 corresponding to the heat storage tank 30, a duct chamber 234 corresponding to the second duct 34, and a recovery chamber 240 corresponding to the recovery tank 40 are formed inside a single cylindrical body 210, separated in this order.

[0086] The heat storage chamber 230 is connected to the first duct 21 on its upstream side and to the recovery chamber 240 via the duct chamber 234 on its downstream side. A damper D7 is provided in the duct chamber 234 and is configured to control the supply of air from the heat storage chamber 230 to the recovery chamber 240. The third duct 42 is connected to the downstream side of the recovery chamber 240.

[0087] Furthermore, as shown in Figure 7, the supply system 200 according to this embodiment has a bypass chamber 235 that connects the duct chamber 234 and the third duct 42. The duct chamber 234, the bypass chamber 235, and the third duct 42 are each provided with dampers D8, D9, and D10, respectively. By controlling the opening and closing of these dampers, the airflow from the heat storage chamber 230 can be controlled as desired.

[0088] Specifically, by opening dampers D7, D8, and D10 and closing damper D9, the air generated by the heat dissipation operation of the heat storage chamber 230 flows through the duct chamber 234 and the recovery chamber 240 in that order. As a result, heat is supplied to the recovery chamber 240 from the duct chamber 234, and carbon dioxide desorption in the recovery chamber 240 can be carried out efficiently. Furthermore, during heat recovery, by opening dampers D7 and D9 and closing dampers D8 and D10, air flows through the duct chamber 234 and bypass chamber 235 in that order, and no air is supplied to the recovery chamber 240. As a result, air flows only through the heat storage chamber 230, which suppresses deterioration of the recovery chamber 240 due to the heat influence from the duct chamber 234. Furthermore, by integrating the heat storage tank 30 and the recovery tank 40 in this manner, transportation by the aforementioned transport unit 50 becomes easier.

[0089] In the embodiments described above, the heat storage tank 30 and the recovery tank 40 were installed outside the greenhouse 10, which is the target of carbon dioxide supply. However, these heat storage tank 30 and recovery tank 40 may also be installed inside the greenhouse 10. Figure 8 schematically shows the layout of the supply system 300 according to the fourth embodiment, in which the heat storage tank 30 and the recovery tank 40 are installed inside the greenhouse 10.

[0090] The supply system 300 includes a heat storage tank 30, a recovery tank 40, and a carbon dioxide generation unit 310 inside the greenhouse 10. The carbon dioxide generation unit 310 is, for example, a boiler that generates carbon dioxide by burning fuel such as kerosene. An exhaust duct 311 is connected to the carbon dioxide generation unit 310 to exhaust the generated carbon dioxide (exhaust EA) to the outside of the greenhouse 10.

[0091] In the supply system 300, the heat storage tank 30 is connected to the exhaust duct 311 via a first duct 321 on its upstream side. A damper D31 is provided in the first duct 321, and the opening and closing of this damper D31 allows control of the intake of exhaust EA from the exhaust duct 311 to the heat storage tank 30. Furthermore, a return air duct 322 is connected to the downstream side of the damper D31 of the first duct 321. The return air duct 322 is equipped with a damper D32, and the opening and closing of this damper D32 allows control over the intake of return air RA from the return air duct 322 to the heat storage tank 30. Furthermore, drain piping and a drain pot (not shown) are connected to the heat storage tank 30.

[0092] In the supply system 300, the upstream side of the recovery tank 40 is connected to the heat storage tank 30 via a second duct 334. A damper D33 is provided in the second duct 334, and the supply of air from the heat storage tank 30 to the recovery tank 40 is controlled. Furthermore, the downstream side of the recovery tank 40 is configured to supply carbon dioxide to the target crop F via a third duct 342. Furthermore, drainage piping (not shown) is connected to the recovery tank 40 and the second duct 334.

[0093] Furthermore, as shown in Figure 8, the supply system 300 according to this embodiment has a bypass duct 335 that connects the second duct 334 and the third duct 342. The second duct 334, the bypass duct 335, and the third duct 342 are each provided with dampers D34, D35, and D36, respectively. By controlling the opening and closing of these dampers, it is possible to control whether the air from the heat storage tank 30 is supplied to the recovery tank 40 or supplied to the third duct 342 without going through the recovery tank 40.

[0094] The third duct 342 is connected to an exhaust duct 312, which discharges the air flowing through the third duct 342 to the outside of the greenhouse 10 as exhaust EA without supplying it to the crops F. The third duct 342 and the exhaust duct 312 are equipped with dampers D37 and D38, respectively. By controlling the opening and closing of these dampers, it is possible to control whether the air flowing through the third duct 342 is supplied to the crops F or discharged to the outside of the greenhouse 10.

[0095] Furthermore, as shown in Figure 8, the third duct 342 may be provided with a flow meter 342a for measuring the flow rate of air passing through the third duct 342, and an air supply unit 342b for sending the air passing through the third duct 342 downstream.

[0096] Furthermore, the supply system 300 is provided with a control unit 350. The control unit 350 has, for example, a PLC that comprehensively controls the operation of the supply system 300. The control unit 350 also has an operation panel for instructing the operation of the PLC, a computer equipped with a processor such as a CPU and memory, and a data logger for recording the operation of the supply system 300. The computer described above may, in one example, have a program storage unit (not shown) and a memory unit. The computer may also be controlled remotely. The program may have been recorded on a non-temporary storage medium readable by the memory unit or computer described above, and may have been installed from the storage medium to the control unit 350. The control unit 350 then controls the opening and closing of various dampers (D31 to D38) and the operation of the air supply unit 342b based on the measurement results from measuring instruments (such as the flow meter 342a mentioned above, and thermometers, hygrometers, pressure gauges, or carbon dioxide concentration meters, not shown) installed at various points within the supply system 300.

[0097] The supply system 300 according to the fourth embodiment is configured as described above. Next, an example of the operation of the supply system 300 configured as described above will be explained.

[0098] <Carbon dioxide supply operation of supply system 300> First, the operation of the carbon dioxide supply system 300 will be explained with reference to the flow chart in Figure 9.

[0099] When the supply system 300 is in operation, the operator instructs the operation of the supply system 300 using the control panel (not shown) of the control unit 350 described above (step St1 in Figure 9). When the supply system 300 is started, first, it is determined whether the start time of the supply system 300 is the time when carbon dioxide supply operation should be performed (application time) or the time when carbon dioxide capture operation, described later, should be performed (capture time) (Step St2 in Figure 9). This determination is made, for example, based on the season and time when the operation was instructed.

[0100] If it is determined that the instruction time for operation is not the application time, the system will proceed to control the carbon dioxide capture operation described later (step St10 in Figure 9). On the other hand, if the instruction time for operation is determined to be the application time, first, the carbon dioxide concentration inside greenhouse 10 is measured using a carbon dioxide concentration meter (not shown) (Step St3 in Figure 9).

[0101] If, in step St3, the carbon dioxide concentration inside greenhouse 10 is above a threshold, for example, 800 ppm or more, the heat dissipation mode of the carbon dioxide supply operation in supply system 300 (hereinafter simply referred to as "heat dissipation mode") is started. Specifically, the control unit 350 opens the dampers D32, D33, D36, and D38, and then (for example, 10 seconds after the damper control) the operation of the air supply unit 342b is started. As a result, dry air DA at a desired temperature (e.g., 60°C) is generated in the heat storage tank 30 from the return air RA (e.g., 20°C) inside the greenhouse 10, and is supplied back into the greenhouse 10 without passing through the recovery tank 40. As a result, the air inside greenhouse 10 is ventilated from return air RA to dry air DA, and the internal temperature of greenhouse 10 can be increased without changing the carbon dioxide concentration inside greenhouse 10, depending on the operation of the supply system 300. Although the carbon dioxide concentration inside greenhouse 10 does not change with the operation of the supply system 300, the carbon dioxide concentration inside greenhouse 10 decreases over time as the crop F being grown performs photosynthesis.

[0102] After the heat dissipation mode has been performed for a predetermined time, the carbon dioxide concentration inside the greenhouse 10 is measured again using a carbon dioxide concentration measuring device (not shown) (Step St4 in Figure 9).

[0103] In step St4, if the carbon dioxide concentration inside greenhouse 10 is above a threshold, for example, 800 ppm or more, the determination is made again as to whether the time of measurement corresponds to the time of carbon dioxide application or recovery (step St5 in Figure 9).

[0104] If it is determined in step St5 that it is time for application, the heat dissipation mode is continued (maintaining the open / closed state of the various dampers). After the heat dissipation mode has been running for a predetermined time, the carbon dioxide concentration inside the greenhouse 10 is measured again using a carbon dioxide concentration meter (not shown) (step St4 in Figure 9). On the other hand, if it is determined in step St5 that it is not time for application, the heat dissipation mode is terminated. Specifically, the control unit 350 stops the operation of the air supply unit 342b, and then (for example, 10 seconds after the control of the air supply unit 342b), the dampers D32, D33, D36, and D38 are closed, and the control of the carbon dioxide recovery operation described later is initiated (step St10 in Figure 9).

[0105] In step St4, if the carbon dioxide concentration inside the greenhouse 10 is below a threshold, for example, below 800 ppm, the heat dissipation mode is terminated and the carbon dioxide application / heat dissipation mode (hereinafter simply referred to as "application mode") of the carbon dioxide supply operation in the supply system 300 is started. Specifically, the control unit 350 opens dampers D34 and D35, and then (for example, 10 seconds after the opening of dampers D34 and D35) closes damper D36. This application mode is also started if the carbon dioxide concentration inside the greenhouse 10 is below a threshold, for example, less than 800 ppm, in step St3. In this case, after the carbon dioxide concentration inside the greenhouse 10 is measured in step St3, the control unit 350 opens the dampers D32, D33, D34, D35, and D38, and then (for example, 10 seconds after the damper control) the operation of the air supply unit 342b is started to initiate the application mode.

[0106] As described above, when it is determined in step St3 or step St4 that the carbon dioxide concentration inside the greenhouse 10 is below the threshold, and the opening and closing of various valves and the operation of the air supply unit 342b are controlled, the application mode is started. In application mode, dry air DA at a desired temperature (e.g., 60°C) is generated in the heat storage tank 30 from the return air RA (e.g., 20°C) inside the greenhouse 10, and then carbon dioxide-containing gas is generated from the dry air DA in the recovery tank 40. The generated carbon dioxide-containing gas is then supplied to the inside of the greenhouse 10. As a result, the air inside greenhouse 10 is ventilated from the return air RA to a carbon dioxide-containing gas, thereby increasing the internal temperature of greenhouse 10 while simultaneously increasing the carbon dioxide concentration inside greenhouse 10.

[0107] Once the application mode has been executed for a predetermined time, the carbon dioxide concentration inside the greenhouse 10 is measured again using a carbon dioxide concentration meter (not shown) (step St6 in Figure 9).

[0108] In step St6, if the carbon dioxide concentration inside greenhouse 10 is below a threshold, for example, less than 1000 ppm, the determination is made again as to whether the time of measurement corresponds to the time of carbon dioxide application or recovery (step St7 in Figure 9).

[0109] If it is determined in step St7 that it is time for application, the application mode is continued (maintaining the open / closed state of the various dampers). After the application mode has been running for the predetermined time, the carbon dioxide concentration inside the greenhouse 10 is measured again using a carbon dioxide concentration meter (not shown) (step St6 in Figure 9). On the other hand, if it is determined in step St7 that it is not time for application, the application mode is terminated. Specifically, the control unit 350 stops the operation of the air supply unit 342b, and then (for example, 10 seconds after the control of the air supply unit 342b), the dampers D32, D33, D34, D35, and D38 are closed, and the control of the carbon dioxide recovery operation described later is initiated (step St10 in Figure 9).

[0110] In step St6, if the carbon dioxide concentration inside greenhouse 10 is above a threshold, for example, 1000 ppm or more, the determination is made again as to whether the time of measurement corresponds to the time of carbon dioxide application or recovery (step St8 in Figure 9).

[0111] In step St8, if it is determined that it is time for application, the application mode is terminated and the heat dissipation mode described above is started. Specifically, the control unit 350 opens damper D36, and then (for example, 10 seconds after opening damper D36) dampers D34 and D35 are closed. After the heat dissipation mode has been executed for a predetermined time, the carbon dioxide concentration inside the greenhouse 10 is measured again using a carbon dioxide concentration meter (not shown) (step St4 in Figure 9). On the other hand, if it is determined in step St8 that it is not time for application, the application mode is terminated. Specifically, the control unit 350 stops the operation of the air supply unit 342b, and then (for example, 10 seconds after the control of the air supply unit 342b), the dampers D32, D33, D34, D35, and D38 are closed, and the control of the carbon dioxide recovery operation described later is initiated (step St10 in Figure 9).

[0112] The carbon dioxide supply operation of the supply system 300 according to this embodiment is performed as described above. Specifically, in the carbon dioxide supply operation of the supply system 300, when the operating time of the supply system 300 is the application time in the greenhouse 10, the above-described heat dissipation mode and application mode are repeatedly executed alternately according to the carbon dioxide concentration in the greenhouse 10. More specifically, in this embodiment, the application mode is executed until the carbon dioxide concentration inside the greenhouse 10 reaches a first threshold, for example, 1000 ppm, and after the carbon dioxide concentration inside the greenhouse 10 reaches the first threshold, the heat dissipation mode is executed until the carbon dioxide concentration inside the greenhouse 10 falls below a second threshold, for example, 800 ppm. In other words, the heat dissipation mode and the application mode are repeatedly executed alternately so that the carbon dioxide concentration inside the greenhouse 10 is between the first threshold and the second threshold.

[0113] <Carbon dioxide capture operation of supply system 300> Next, the carbon dioxide capture operation of the supply system 300 will be explained with reference to the flow diagram 10 in Figure 10. Note that, during the carbon dioxide capture operation of the supply system 300, fuel is supplied to the carbon dioxide generation unit 310 in advance, and carbon dioxide-containing gas is generated as exhaust EA via the exhaust duct 311.

[0114] When the supply system 300 is in operation, as shown in Figure 9, the operator instructs the operation of the supply system 300 using the control panel (not shown) of the control unit 350 (step St1 in Figures 9 and 10). When the supply system 300 is started, it is first determined whether the start time of the supply system 300 is the time of carbon dioxide application or the time of carbon dioxide recovery (Step St2 in Figure 10).

[0115] If it is determined that the instruction time for operation is not the recovery time, the system will switch to the control of the carbon dioxide supply operation described above (step Sp10 in Figure 10). On the other hand, once it is determined that it is time for recovery, first, the temperature of the exhaust gas EA (carbon dioxide-containing gas) flowing through the exhaust duct 311 is measured using a thermometer (not shown) (step Sp1 in Figure 10).

[0116] If the exhaust gas EA temperature is below a threshold, for example, below 250°C, in step Sp1, the start of carbon dioxide supply operation in the supply system 300 is stopped, and a determination is made again as to whether it is application time or recovery time (step St2). If it is application time, the control of the carbon dioxide supply operation described above is initiated (step Sp10 in Figure 10). On the other hand, if the exhaust gas EA temperature is above a threshold, for example, 250°C or higher, the carbon dioxide concentration of the air flowing downstream of the recovery tank 40 is then measured using a carbon dioxide concentration meter (not shown) (step Sp2 in Figure 10).

[0117] If the carbon dioxide concentration downstream of the recovery tank 40 in step Sp2 is above a threshold, for example, 7% or more, the drying mode of the carbon dioxide recovery operation in the supply system 300 (hereinafter simply referred to as "drying mode") is started. Specifically, the control unit 350 opens the dampers D31, D33, D36, and D37, and then (for example, 10 seconds after the damper control) the operation of the air supply unit 342b is started. As a result, the high-temperature exhaust EA from the carbon dioxide generation unit 310 is passed through the heat storage tank 30, and the adsorbent M contained in the heat storage tank 30 is dried (heat storage operation of the heat storage tank 30). The exhaust EA used to dry the adsorbent M is then discharged to the outside of the greenhouse 10 without passing through the recovery tank 40. As a result, the heat storage tank 30 can be operated without ventilating the air inside the greenhouse 10, that is, without changing the carbon dioxide concentration inside the greenhouse 10.

[0118] On the other hand, if the carbon dioxide concentration downstream of the recovery tank 40 is below a threshold, for example, less than 7%, in step Sp2, the carbon dioxide recovery / drying mode (hereinafter simply referred to as "recovery mode") of the carbon dioxide recovery operation in the supply system 300 is started. Specifically, the control unit 350 opens the dampers D31, D33, D34, D35, and D37, and then (for example, 10 seconds after the damper control) starts the operation of the air supply unit 342b. As a result, in the heat storage tank 30, recovered air CA is generated from the exhaust EA (carbon dioxide-containing gas) and the heat storage operation of the heat storage tank 30 is performed. Furthermore, in the recovery tank 40, carbon dioxide is recovered (adsorbed) from the recovered air CA by the ion exchange resin 41. The recovered air CA from which carbon dioxide has been recovered by the ion exchange resin 41 is then discharged to the outside of the greenhouse 10. As a result, the heat storage operation of the heat storage tank 30 and the carbon dioxide recovery operation of the recovery tank 40 can be performed without ventilating the air inside the greenhouse 10, that is, without changing the carbon dioxide concentration inside the greenhouse 10. Furthermore, the carbon dioxide concentration downstream of the recovery tank 40 increases as carbon dioxide recovery in the recovery tank 40 progresses.

[0119] Once the recovery mode has been performed for a predetermined time, the carbon dioxide concentration of the air flowing through the upstream and downstream stages of the recovery tank 40 is measured using a carbon dioxide concentration measuring instrument (not shown) (step Sp3 in Figure 10).

[0120] In step Sp3, if the carbon dioxide concentration downstream of the recovery tank 40 is above a threshold, for example 9% or more, and the difference in carbon dioxide concentration between the upstream and downstream stages of the recovery tank 40 is below a threshold, for example 2% or less, a determination is made to terminate the recovery mode (step Sp5 in Figure 10, described later). On the other hand, if in step Sp3 the carbon dioxide concentration downstream of the recovery tank 40 is below a threshold, for example, less than 9%, and the difference in carbon dioxide concentrations upstream and downstream of the recovery tank 40 is also below a threshold, for example, less than 2%, the temperature of the exhaust gas EA flowing through the exhaust duct 311 is measured again, and a determination is made again as to whether the time of this measurement is the carbon dioxide recovery time or the application time (step Sp4 in Figure 10).

[0121] If, in step Sp4, the exhaust EA temperature is determined to be above a threshold, for example, 250°C or higher, and it is determined that it is time for recovery, the recovery mode is continued (maintaining the open / closed status of various dampers). After the recovery mode operation continues for a predetermined time, the carbon dioxide concentration is measured again using a carbon dioxide concentration meter (not shown) (step St3 in Figure 10). On the other hand, if step Sp4 determines that the exhaust EA temperature is below a threshold, for example, below 250°C, or that it is not time for recovery, a determination is made to terminate the recovery mode (step Sp5 in Figure 10, described later).

[0122] If the determination to end the recovery mode is made in step Sp3 or step Sp4 described above, the temperature of the exhaust EA flowing through the exhaust duct 311 is measured again, and a determination is made again as to whether the time of this measurement is the carbon dioxide recovery time or the application time (step Sp5 in Figure 10).

[0123] In step Sp5, if the exhaust EA temperature is below a threshold, for example, below 250°C, or if it is determined that it is not time for recovery, the recovery mode is terminated. Specifically, the control unit 350 stops the operation of the air supply unit 342b, and then (for example, 10 seconds after the control of the air supply unit 342b), the dampers D31, D33, D34, D35, and D37 are closed, and the control of the carbon dioxide supply operation described above is initiated (step Sp10 in Figure 10). On the other hand, if in step Sp5 the exhaust EA temperature is determined to be above a threshold, for example, 250°C or higher, and it is determined that it is time for recovery, the recovery mode is terminated and the control of the drying mode described above is initiated. Specifically, the control unit 350 opens damper D36, and then (for example, 10 seconds after damper D36 is opened) dampers D34 and D35 are closed.

[0124] After step Sp2 or step Sp6 described above, once the drying mode has been executed for a predetermined time, the temperature of the exhaust EA flowing through the exhaust duct 311 and the temperature of the air flowing downstream of the heat storage tank 30 are measured, and a determination is made again as to whether the time of this measurement is the carbon dioxide recovery time or the application time (step Sp6 in Figure 10).

[0125] If, in step Sp6, the exhaust EA temperature is above a first threshold, for example, 250°C or higher, the air temperature downstream of the heat storage tank 30 is below a second threshold, for example, 150°C or lower, and it is determined that it is the recovery time, the drying mode is continued (maintaining the open / closed state of the various dampers). After the drying mode operation continues for a predetermined time, the exhaust EA temperature is measured again, and it is determined whether the time at this measurement is the carbon dioxide recovery time or the application time (step Sp6 in Figure 10).

[0126] On the other hand, if in step Sp6 the temperature of the air flowing downstream of the heat storage tank 30 is below the second threshold, for example, below 150°C, or if it is determined that it is not time for recovery, the drying mode is terminated and the moisture release mode of the carbon dioxide recovery operation (hereinafter simply referred to as "moisture release mode") is started. Specifically, the control unit 350 opens the damper D32, and then (for example, 10 seconds after the opening of damper D32) closes damper D31. As a result, the return air RA (for example, 20°C) from the greenhouse 10 is taken into the heat storage tank 30, and any moisture remaining in the heat storage tank 30 after the drying mode is discharged to the outside of the greenhouse 10 as exhaust EA without passing through the recovery tank 40. Subsequently, if the moisture release mode continues for a predetermined time (for example, 30 to 60 seconds), the operation of the moisture release mode is terminated. Specifically, the control unit 350 stops the operation of the air supply unit 342b, and then (for example, 10 seconds after the control of the air supply unit 342b), the dampers D32, D33, D36, and D37 are closed. If the time at the end of this moisture release mode operation is the time for carbon dioxide application, the control transitions to the carbon dioxide supply operation described above (step Sp10 in Figure 10); if it is the recovery time, the operation is stopped and the system waits until the application time arrives.

[0127] Furthermore, if in step Sp6 the temperature of the air flowing downstream of the heat storage tank 30 is above the second threshold, for example, 150°C or higher, but the temperature of the exhaust EA is below the first threshold, less than 250°C, the drying mode is terminated, and the system proceeds to control the carbon dioxide supply operation described above without going through the moisture release mode described above (step Sp10 in Figure 10). Specifically, the control unit 350 stops the operation of the air supply unit 342b, and then (for example, 10 seconds after the control of the air supply unit 342b), the dampers D31, D33, D36, and D37 are closed.

[0128] The carbon dioxide recovery operation of the supply system 300 according to this embodiment is performed as described above. That is, in the carbon dioxide recovery operation of the supply system 300, when the operating time of the supply system 300 is the recovery time in the greenhouse 10, the recovery mode, drying mode, and moisture release mode described above are executed sequentially. At this time, the recovery mode and moisture release mode described above can be omitted as appropriate depending on the measured carbon dioxide concentration, the exhaust EA, and the temperature downstream of the heat storage tank 30. More specifically, in this embodiment, if the exhaust EA temperature is above a first threshold, for example 250°C, the recovery mode is performed until the carbon dioxide concentration downstream of the recovery tank 40 is 9% or higher, and the difference in carbon dioxide concentration between the recovery tank and the upstream tank is 2% or less. Subsequently, if the exhaust EA temperature is above the first threshold, for example 250°C, the drying mode is performed until the air temperature downstream of the heat storage tank 30 is above a second threshold, for example 150°C. Furthermore, after that, the moisture release mode is performed for a predetermined time, for example 30 to 60 seconds, to remove any remaining moisture in the heat storage tank 30.

[0129] In the supply system 300 according to this embodiment, the operating time of the supply system 300 is alternately repeated between the carbon dioxide supply operation and the carbon dioxide capture operation, depending on whether it is the time of carbon dioxide application or the time of capture.

[0130] The embodiments disclosed herein should be considered in all respects as illustrative and not restrictive. The embodiments described above may be omitted, replaced, or modified in various ways without departing from the scope and spirit of the appended claims. For example, the constituent elements of the embodiments described above can be combined in any way. Such any combination will naturally yield the functions and effects of each constituent element in the combination, as well as other functions and effects that will be apparent to those skilled in the art from the description herein.

[0131] Furthermore, the effects described herein are merely descriptive or illustrative and not limiting. In other words, the technology relating to this disclosure may produce other effects that will be apparent to those skilled in the art from the description herein, in addition to or instead of the effects described herein.

[0132] Furthermore, the following configuration examples also fall within the technical scope of this disclosure. (1) A system for supplying carbon dioxide-containing gas to a carbon dioxide demand center, A heat storage tank that houses an adsorbent that generates heat by adsorbing an adsorbent, and delivers the air to be treated as dry air at a higher temperature than the air to be treated, A carbon dioxide-containing gas supply system comprising: a carbon dioxide recovery tank that houses a carbon dioxide adsorbent capable of adsorbing and desorbing carbon dioxide, desorbs the carbon dioxide using the dry air taken in, and sends the carbon dioxide-containing gas to the demand section. (2) The demand unit is a greenhouse in protected horticulture, The carbon dioxide-containing gas supply system according to (1), further comprising a return air path for taking in the return air from the greenhouse as the air to be treated into the heat storage tank. (3) The carbon dioxide-containing gas supply system according to (2), characterized in that the carbon dioxide-containing gas sent from the recovery tank into the greenhouse is at least less humid than the return air flowing through the return air path. (4) The carbon dioxide generation unit further comprises a carbon dioxide generation unit that generates carbon dioxide for collection into the collection tank by adsorbing it onto the carbon dioxide adsorbent, When recovering carbon dioxide from the recovery tank, In the heat storage tank, combustion gas from the generation unit is taken in, the adsorbate is desorbed from the adsorbent using the taken-in combustion gas, and the recovered air, which is colder and more humid than the combustion gas, is sent out. A carbon dioxide-containing gas supply system according to any one of (1) to (3), characterized in that, in the recovery tank, the carbon dioxide contained in the recovery air is adsorbed onto the carbon dioxide adsorbent, and the recovery air from which the carbon dioxide has been removed is discharged to the outside of the demand unit. (5) The carbon dioxide-containing gas supply system according to (4), further comprising a transport unit for transporting at least one of the heat storage tank and the recovery tank between the generating unit and the demand unit. (6) The carbon dioxide-containing gas supply system according to (4) or (5), further comprising a dehumidifying unit for dehumidifying the recovery air that is sent out from the heat storage tank and before being supplied to the recovery tank. (7) A carbon dioxide-containing gas supply system according to any one of (1) to (6), characterized in that the carbon dioxide adsorbent is an ion exchange resin. (8) The carbon dioxide-containing gas supply system according to (7), characterized in that the ion exchange resin has an amine functional group. (9) A carbon dioxide-containing gas supply system according to any one of (1) to (6) above, characterized in that the carbon dioxide adsorbent is selected from at least one of an ion exchange resin, a moisture-resistant zeolite, activated carbon, a porous coordination polymer (PCP), and a metal-organic frame (MOF). (10) The carbon dioxide-containing gas supply system according to any one of (1) to (6), characterized in that the adsorbent is selected from at least one of zeolite or hask clay (registered trademark).

[0133] (11) A gas supply device containing carbon dioxide, A heat storage tank configured to repeatedly perform heat storage and heat release operations by adsorption and desorption of adsorbent material to the contained adsorbent, A carbon dioxide-containing gas supply device comprising a recovery tank configured to repeatedly recover and supply carbon dioxide by adsorption and desorption of carbon dioxide onto a contained carbon dioxide adsorbent.

[0134] (12) A method for applying a carbon dioxide-containing gas to a carbon dioxide demand area, A combustion gas generation step in which combustion gas is generated by burning fuel, The adsorbent desorption step involves desorbing the adsorbent from the adsorbent material using the combustion gas to generate recovery air that is colder and more humid than the combustion gas, A carbon dioxide recovery process including a carbon dioxide adsorption step of adsorbing carbon dioxide contained in the recovered air onto a carbon dioxide adsorbent, The adsorbate adsorption step involves adsorbing the adsorbate in the air to be treated supplied from the demand unit onto the adsorbent, thereby generating dry air at a higher temperature than the air to be treated. A method for applying a carbon dioxide-containing gas, comprising a carbon dioxide desorption step of desorbing carbon dioxide from the carbon dioxide adsorbent with the dry air and supplying the carbon dioxide-containing gas to the demand unit, and a carbon dioxide supply step.

[0135] (13) A method for producing carbon dioxide, An adsorbent desorption step involves desorbing the adsorbate from the adsorbent using high-temperature, low-humidity air to generate recovery air that is lower in temperature and higher in humidity than the said high-temperature, low-humidity air, A carbon dioxide recovery process including a carbon dioxide adsorption step of adsorbing carbon dioxide contained in the recovered air onto a carbon dioxide adsorbent, An adsorbent adsorption step involves adsorbing an adsorbate onto the adsorbent material from low-temperature, high-humidity air to generate dry air that is hotter than the low-temperature, high-humidity air. A method for producing carbon dioxide, comprising: a carbon dioxide desorption step, which includes a carbon dioxide supply step, which includes a carbon dioxide desorption step, which includes desorbing the carbon dioxide from the carbon dioxide adsorbent with the dry air to produce a carbon dioxide-containing gas containing the carbon dioxide; and a carbon dioxide production step. [Industrial applicability]

[0136] The present invention is useful as a carbon dioxide capture system at the emission site of carbon dioxide-containing gas, and / or as a carbon dioxide supply system at the demand site of carbon dioxide-containing gas. Examples of carbon dioxide-containing gas emission sites include power plants, ironworks, waste disposal sites, commercial buildings (office buildings, multi-purpose facilities, schools, government buildings, etc.), or factories that primarily emit combustion exhaust gases, but the facilities in which the supply system 1 (recovery system) related to the technology disclosed herein is introduced are not limited to these. Furthermore, while greenhouses 10 used for horticultural purposes are a prime example of the demand sites for the carbon dioxide-containing gas mentioned above, the facilities in which the supply system 1 relating to the technology of this disclosure is introduced are not limited to these.

[0137] More specifically, it could be applied to manufacturing plants for oxygen-containing compounds such as urethane and polycarbonate, as well as chemicals derived from biomass and olefins. Furthermore, potential applications include biomass fuels using photosynthetic microalgae, and biofuels derived from biomass. Furthermore, it could be applied to processes that involve absorbing carbon dioxide into the interior of concrete products and structures during their manufacturing. Furthermore, potential applications include "BECCS: Bioenergy with Carbon Capture and Storage," which combines biomass fuel with CCS (Carbon dixide Capture and Storage), and "blue carbon," where seaweed and seagrass absorb carbon dioxide to store it in the ocean. [Explanation of symbols]

[0138] 1. Supply System 2 Control Unit 10 Greenhouse 11 Exhaust duct 20 Generation part 21. Duct No. 1 22 Return air duct 23 Air supply unit 30 Heat storage tank 31 Filling section 32 Space (upstream side) 33 Space (downstream side) 34. Duct No. 2 40 Recovery tanks 41 Ion exchange resin 42 Third Duct 43 Exhaust duct 110 Dehumidification section D Damper DA dry air EA Exhaust M Adsorbent RA return air

Claims

1. A system for supplying carbon dioxide-containing gas to a carbon dioxide demand center, A heat storage tank that houses an adsorbent that generates heat by adsorbing an adsorbent, and delivers the air to be treated as dry air at a higher temperature than the air to be treated, A carbon dioxide recovery tank containing a carbon dioxide adsorbent capable of adsorbing and desorbing carbon dioxide, which desorbs the carbon dioxide using the dry air taken in and sends the carbon dioxide-containing gas to the demand section, The system includes a carbon dioxide generation unit that generates carbon dioxide for collection in the recovery tank by adsorbing it onto the carbon dioxide adsorbent, When recovering carbon dioxide from the recovery tank, In the heat storage tank, combustion gas from the generation unit is taken in, the adsorbate is desorbed from the adsorbent using the taken-in combustion gas, and the recovered air, which is colder and more humid than the combustion gas, is sent out. A carbon dioxide-containing gas supply system characterized in that, in the recovery tank, the carbon dioxide contained in the recovery air is adsorbed onto the carbon dioxide adsorbent, and the recovery air from which the carbon dioxide has been removed is discharged to the outside of the demand unit.

2. The aforementioned demand unit is a greenhouse in protected horticulture, The carbon dioxide-containing gas supply system according to claim 1, further comprising a return air path for introducing the return air from the greenhouse into the heat storage tank as the air to be treated.

3. The carbon dioxide-containing gas supply system according to claim 2, characterized in that the carbon dioxide-containing gas sent from the recovery tank into the greenhouse is at least less humid than the return air flowing through the return air path.

4. The carbon dioxide-containing gas supply system according to claim 1, further comprising a transport unit for transporting at least one of the heat storage tank and the recovery tank between the generating unit and the demand unit.

5. The carbon dioxide-containing gas supply system according to claim 1, further comprising a dehumidification unit for dehumidifying the recovery air that is discharged from the heat storage tank and supplied to the recovery tank.

6. A carbon dioxide-containing gas supply system according to any one of claims 1 to 5, characterized in that the carbon dioxide adsorbent is an ion exchange resin.

7. The carbon dioxide-containing gas supply system according to claim 6, characterized in that the ion exchange resin has an amine functional group.

8. A carbon dioxide-containing gas supply system according to any one of claims 1 to 5, characterized in that the carbon dioxide adsorbent is selected from at least one of an ion exchange resin, a moisture-resistant zeolite, activated carbon, a porous coordination polymer (PCP), and a metal-organic frame (MOF).

9. A carbon dioxide-containing gas supply system according to any one of claims 1 to 5, characterized in that the adsorbent is selected from at least one of zeolite or hask clay (registered trademark).

10. A method for applying carbon dioxide-containing gas to a carbon dioxide demand area, A combustion gas generation step in which combustion gas is generated by burning fuel, The adsorbent desorption step involves desorbing the adsorbent from the adsorbent material using the combustion gas to generate recovery air that is colder and more humid than the combustion gas, A carbon dioxide recovery process including a carbon dioxide adsorption step of adsorbing carbon dioxide contained in the recovered air onto a carbon dioxide adsorbent, The adsorbate adsorption step involves adsorbing the adsorbate in the air to be treated supplied from the demand unit onto the adsorbent, thereby generating dry air at a higher temperature than the air to be treated. A method for applying a carbon dioxide-containing gas, comprising a carbon dioxide desorption step of desorbing carbon dioxide from the carbon dioxide adsorbent with the dry air and supplying the carbon dioxide-containing gas to the demand unit, and a carbon dioxide supply step.

11. A method for producing carbon dioxide, An adsorbent desorption step involves desorbing the adsorbate from the adsorbent using high-temperature, low-humidity air to generate recovery air that is lower in temperature and higher in humidity than the said high-temperature, low-humidity air, A carbon dioxide recovery process including a carbon dioxide adsorption step of adsorbing carbon dioxide contained in the recovered air onto a carbon dioxide adsorbent, An adsorbent adsorption step involves adsorbing an adsorbate onto the adsorbent material from low-temperature, high-humidity air to generate dry air that is hotter than the low-temperature, high-humidity air. A method for producing carbon dioxide, comprising: a carbon dioxide desorption step, which includes a carbon dioxide supply step, which includes a carbon dioxide desorption step, which includes desorbing the carbon dioxide from the carbon dioxide adsorbent with the dry air to produce a carbon dioxide-containing gas containing the carbon dioxide; and a carbon dioxide production step.

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