Rotary continuous multi-capture system and apparatus for improved direct air capture (DAC +) of carbon dioxide

Abstract

A system and method for removing carbon dioxide from a carbon dioxide-rich gas mixture, the system including a set of carbon dioxide removal structures moving along a closed curvilinear track. A desorption box or a regeneration box is arranged at a position along the track, and each trapping structure enters the desorption box or the regeneration box for regeneration. A majority of the CO2 removal structure is supplied with ambient air, or a mixture of ambient air and a small portion of the flue gas, and CO2-depleted air is discharged. At least one selected such removal structure in each group is supplied with a flue gas comprising at least 4% CO2 by volume at a location immediately before it enters the trapping structure. A method of removing carbon dioxide from the atmosphere is provided that utilizes a system that operates in the same manner as the aforementioned system.

Description

[0001] This invention is a divisional application of "Application No. 202080093240.4, filed on November 21, 2020, entitled 'Rotating Continuous Multiple Capture System and Apparatus for Improving Direct Air Capture of Carbon Dioxide (DAC+)'". Background Technology

[0002] This invention generally relates to systems and methods for removing greenhouse gases from the atmosphere, and more particularly to novel and improved systems and methods for sequentially capturing carbon dioxide first from an airflow comprising ambient air, and subsequently capturing carbon dioxide from at least one airflow containing flue gas. The invention contemplates systems in which said sequence may include different carbon dioxide removal orders. The invention further envisions the second sequential step comprising more than one airflow containing flue gas.

[0003] This invention provides improvements to the systems described in U.S. Patent Application Nos. 13 / 098,370 (now US 8,500,855) and US 9,925,488, filed April 29, 2011. The proposed systems and processes can be considered to be used for a wider range of applications than those disclosed in the earlier applications, especially with further modifications. The disclosure of that co-pending application is incorporated herein by reference as if it were a complete repetition and modified by the new disclosure presented herein.

[0004] Much attention is currently focused on trying to achieve three energy-related goals that may be somewhat conflicting in some respects: 1) providing affordable energy for economic development; 2) achieving energy security; and 3) avoiding unique climate change caused by global warming. This assumes that if we are to have the energy needed for economic prosperity and if we are to avoid energy shortages that could lead to conflict, then there is no viable way to completely avoid fossil fuels for the remainder of this century.

[0005] Respected scientists have little disagreement that an increase in the amount of so-called greenhouse gases, such as carbon dioxide (methane and water vapor are other major greenhouse gases), will increase the Earth’s average temperature.

[0006] It is equally clear that the risks of climate change can only be eliminated by reducing humanity's continued contribution to carbon dioxide emissions. Removing additional CO2 from the atmosphere, known as direct air capture or direct air extraction (DAC), will also be necessary. The ability to extract air and reduce the amount of carbon dioxide in the atmosphere can, in principle, offset emissions of other greenhouse gases, such as methane (which exists naturally and enters the atmosphere through human activities), which also contributes to climate change.

[0007] Especially over the past decade, experts in this field have generally accepted the belief that capturing carbon dioxide directly from the atmosphere is economically feasible, albeit at low concentrations, in order to at least mitigate the increase of so-called "greenhouse" gases in the atmosphere. It is now understood that, under ambient conditions, CO2 can be efficiently extracted from the air using suitable regenerable adsorbent systems and stripping or regeneration processes at slightly higher but relatively lower temperatures. This process can be extended and combined with the removal of CO2 from mixtures of effluent gas and substantial amounts of ambient air, thus removing not only CO2 from flue gas but also additional CO2 from the atmosphere. This would achieve a net reduction in atmospheric CO2 at a lower cost and with greater efficiency. Invention Overview

[0008] This invention provides further new and useful improvements to DAC systems and methods to remove large amounts of carbon dioxide from carbon dioxide-rich air with greater efficiency and lower total cost (including lower capital expenditure (“CAPEX”) and lower operating expenditure (“OPEX”)).

[0009] Brief Summary of the Invention

[0010] According to the present invention, a novel process and system have been developed that utilizes components of multiple individual CO2 trapping structures. Each supporting substrate trapping structure may include a substrate particle bed combined with a single regeneration chamber, the ratio of the substrate particle bed to the regeneration chamber depending on the ratio of the adsorption rate from ambient air or any gas mixture treated to remove CO2 to the regeneration rate of the adsorbent rich in trapped CO2. In a preferred embodiment, the CO2 trapping structure is supported on a substantially continuous closed-loop track, preferably forming a closed curve; the CO2 trapping structure moves continuously longitudinally along the track while being exposed to a moving flow of ambient air or a gas mixture comprising most of the ambient air. Alternatively, the trapping structure may move longitudinally back and forth along an open-ended track.

[0011] At one point along the track, longitudinal movement is stopped and one of the CO2 trapping structures is moved to a sealed chamber for processing to desorb CO2 from the adsorbent and regenerate the adsorbent. While the adsorbent is regenerating, the trapping structure rotates around the track until the next CO2 trapping structure is in place to enter the regeneration chamber, at which point the rotation of all CO2 trapping structures stops again. An improvement of the invention provides at least one trapping structure to receive flue gas in place of ambient air, and preferably, at least most of the other trapping structures will be supplied with ambient air. Most preferably, the trapping structure receives the flue gas input at the final station or stage before entering the regeneration chamber; this can be pure but pretreated flue gas, or a mixture of flue gas and ambient air, which we refer to as carbureted flue gas.

[0012] The input flue gas velocity and concentration will be independently controlled on the input side, although the output is drawn out by a fan and may use a separate manifold. Ideally, in some cases, this could be a modification of a pure DAC unit. Additional CO2 will be added and the adsorbent in the trap structure substrate will be preheated before entering the regeneration chamber. After desorption in the regeneration chamber, the cooling of the trap structure substrate and adsorbent can remain constant, although the use of the removed heat may differ because the array has already been preheated before regeneration begins. The advantages of this integrated approach compared to separate DAC and carburetor units are as follows: 1. Increase the total CO2 output of each DAC plant by 30% to 50% as projected, thereby reducing capital expenditure per ton.

[0013] 2. Reduce the capital cost of flue gas capture components by using a plant with the same capital as the DAC.

[0014] 3. The energy consumed to produce one ton of CO2 is reduced: A. Because the amine sites that bind to high concentrations of CO2 have lower heat of reaction (note that different adsorbents or mixtures of adsorbents, such as adsorbents containing secondary amines, may be the best choice for this embodiment, rather than just adsorbents containing primary amines). B. Because the same sensible heat will produce more CO2, and C. Because the heat from the flue will be used to preheat the array.

[0015] Three cases need to be considered: 1. A standalone case where the Cogen plant is large enough to provide heat and electricity for the system facilities; 2. It is connected to a larger Cogen facility, so there is more heat and CO2 available than is used for the DAC unit, and it generates excess electricity and heat; 3. The case of a carbon-negative power plant, where CO2 is captured from the power source and the scale of the DAC (Diverterless Catalytic Converter) provided is determined based on the need to remove CO2 from the flue gas. In this case, one would be able to select the amount of flue gas CO2 captured based on cost, since the facility is carbon-negative overall (e.g., removing more CO2 than the power plant emits).

[0016] It will be observed that the same design holds true for all three of the above cases; the only change is the size of the carbon negative power plant – in case 1 above, it is determined by the energy demand of the DAC; in case 2 above, it is determined by the energy demand of the specific application (compression, etc.); and in case 3 above, it is determined by the size of the carbon negative power plant.

[0017] Alternatively, a world determined to reduce emissions could penalize pure flue gas facilities that emit 10% of their emissions from chimneys and credit the resulting carbon negatives. In this context, this implementation method could become a preferred approach from both climate change and economic perspectives. In this embodiment of the method, pure flue gas will be used at least in the last CO2 capture station immediately preceding regeneration.

[0018] Another preferred embodiment provides feedstocks that include pre-treated or partially captured flue gas, such as exhaust gas from a final or last-capture structure, or exhaust gas from a conventional CO2 removal system, for example, used long-term in industries with high CO2 exhaust emissions, such as fuel-fired power plants, cement plants, steel mills, etc. Such systems involving flue gas pretreatment are particularly important when treating exhaust gas from any combustion process of solids such as coal or liquids such as oil, which may contain particulate or non-particulate compounds toxic to the adsorbent.

[0019] In one such system, the plant that generates steam for heating the regeneration chamber provides the effluent that must be processed according to the present invention. Such systems include, for example, stand-alone plants primarily designed to provide steam for regenerating the adsorbent. A second option is to use the plant primarily for the co-production of another product, such as a power plant, cement plant, or steel mill, and, for example, an oil refinery. A preferred example is a cogeneration plant that produces fuel for the CO2 generated from the plant of the present invention. Another preferred example is a cogeneration plant that uses CO2 to produce fuel for sale or use elsewhere.

[0020] When the adjacent plant is a power plant, the products of such a plant include co-generated or surplus steam and electricity, at least partially including the steam or electricity required to operate the DAC plant. Combustion effluent or flue gas from such a power plant is at least partially purified before being fed into the final stage of CO2 capture and immediately before entering the regeneration chamber. Furthermore, as mentioned above, at the position immediately preceding or the eighth position of the capture structure, the partially CO2-reduced effluent can be used alone or mixed with ambient air; it is understood that in the case of 10 capture structures and only one regeneration chamber, the regeneration chamber is the 10th stage, the immediate preceding capture structure stage before the capture structure enters the regeneration chamber is the 9th stage, and the preceding stage is the 8th stage. Examples of suitable structures for this system are shown in the accompanying figures and descriptive text below.

[0021] Another preferred embodiment specifies that the CO2-rich feed includes flue gas that has been partially treated to capture CO2, such as exhaust gas from a final or last-capture structure or from a conventional CO2 removal system. This is typically used in industries with high CO2 emissions, such as fuel-fired power plants, cement plants, steel mills, etc. Such systems involving effluent pretreatment are particularly important when treating exhaust gas from any combustion process originating from solids such as coal or liquids such as oil, and typically include fine particulate matter, solid or liquid particles, and gases toxic to the adsorbent.

[0022] Another preferred embodiment is that the plant uses the CO2 generated from the DAC+ plant of the present invention to produce fuel for sale or use in other locations.

[0023] Each trapping structure is formed of a porous substrate with carbon dioxide adsorption sites on its surface, preferably amine groups, and most preferably amine groups with a high proportion of primary amines. As the trapping structures move along the track, they absorb CO2 from the moving gas stream until each trapping structure reaches the sealed regeneration chamber. According to this improvement, the method is further improved by introducing flue gas instead of ambient air into each CO2 trapping structure a few minutes before it reaches the regeneration chamber, during its partial movement around the loop.

[0024] However, as described above, the method of the present invention is a low-temperature (preferably ambient temperature to 100°C), semi-continuous method with unidirectional mass transfer at each stage of the method. Another novel aspect of the method is that the reaction for capturing CO2 from the gas mixture preferably occurs with a renewable material (in a preferred embodiment, on an amino polymer), such as a renewable material of an amino polymer adsorbent impregnated in a substrate.

[0025] In a preferred embodiment, the adsorbent-supported trapping structure comprises a monolithic substrate that is supported sequentially. 1. A frame that supports a substrate, which moves along a closed loop or an open path during CO2 capture. In a preferred embodiment, the substrate comprises a porous monolith having an adsorbent impregnated within the pores of the monolith; 2. In a preferred embodiment of the invention, the substrate may be formed of a ceramic material, such as cordierite, mullite, silica, alumina, titanium dioxide, or mesocellular foam (MCF) on mesoporous-γ-alumina, or on mesoporous-γ-alumina coated throughout the pores of MCF or other such materials, or a metal oxide (e.g., porous oxides of silica, alumina, titanium dioxide, or other metals, single or mixed, with sufficient structural strength and heat resistance to maintain its integral shape under conditions encountered during the CO2 capture phase or adsorbent regeneration, as described below). Since the thermal conditions are not harsh, other porous materials may be used, such as porous glass fibers, rigid polymeric plastics, or other structurally robust porous materials that can be formed into the desired shape by extrusion, corrugation, crimping, 3D printing, molding, or other known or to-be-developed processes.

[0026] 3. Impregnating adsorbent a. The most commonly used adsorbent is an amino polymer: i. Polyethyleneimine (PEI) has become the preferred adsorbent for most workers in this field because of its... 1. High activity at low CO2 concentrations, high amine density, and large-scale commercial availability; 2. However, PEI is limited by known oxidative degradation at high temperatures.

[0027] ii. Other amino polymers can be used as adsorbents, including primary, secondary, and tertiary amines of different grades, as well as different main-chain chemical compositions, molecular weights, degrees of branching, and additives. Among other known polyamines that can be used as CO2 adsorbents are polypropylene amine, polyglycolamine, polypropylene amines poly(vinylamine), and poly(allylamine) and their derivatives.

[0028] iii. Non-amino polymer adsorbents should be considered as useful adsorbents: 1. Metal-organic frameworks, covalent organic frameworks, POMs and other such materials are useful.

[0029] 2. Non-polymerized amine adsorbents (“Ph-XX-YY”), oligomers.

[0030] 3. Improvements to the system can be achieved by combining non-adsorbent additives with adsorbents to enhance stability (scavengers), activity (copolymers), accessibility (PEG), and many other substances known in the art or to be developed in the future.

[0031] The present invention is also intended to utilize contactors made of active adsorbents (e.g., by 3D printing). analyze

[0032] Typically, a DAC removal system (“System”) captures an additional portion of FGCO2 from the flue gas (preferably pretreated) in the final stage of CO2 capture; this results in the capture of additional CO2 (“FGCO2”) before the individual substrate enters the regeneration chamber. This increases the efficiency of the final stage, thereby increasing the amount of CO2 captured by the System during each cycle. First, compared to pure DAC (without added flue gas), CAPEX per tonne will be reduced by 1 / (1+FGCO2). This is due to the increased CO2 concentration in the flue gas compared to ambient air, which is several orders of magnitude higher. The effect of increasing the concentration varies depending on the adsorbent. The capital expenditure cost of additional equipment can also be avoided when treating a mixture of air and a small amount of flue gas in each stage.

[0033] If the Cogen plant burns every year (MMbtu) Natural gas, then the energy M produced for heat and electricity is given by M=COGENEx. The amount of first-order energy given and discharged from the flue is MF = (1 - COGENE)x The energy figure excludes the reaction energy of CO2 (if captured) and water (if condensed). COGENE is the energy efficiency of the Cogen unit. The annual flue gas CO2 emissions (FTCO2) are FTCO2 = 0.056. tons / year.

[0034] If CO2 is captured from flue gas with the same efficiency as ECF (Extractable Carbon Free), then the amount of CO2 captured from the flue gas annually is: FGCO2 = ECF x FTCO2.

[0035] The ratio of FCCO2 to the total air CO2 captured by DACCO2 annually remains the same for each cycle. This means that for a DAC unit, tonnes of DACCO2 are captured annually, of which: DACCO2= (l / FGCO2) x ECF x FTCO2 The total amount of CO2 captured (TCCCO2) will be determined by the following formula: TCCO2= (l / FGCO2 +- l) x ECF x FTCO2.

[0036] The amount of CO2 emitted is (1ECF) FTCO2. The carbon burden of the entire plant is (1 / FGCO2+1) x (ECF-1)FTCO2.

[0037] For ECF=0.9 (the case where air is mixed with a small amount of flue gas (“carburetor”), this will change from 1.7 FTCO2 (FGCO2 = .S) to -0.8 FTCO2 (FGCO2 = 1). This means that the less FGCO2 flowing into the system, the higher the plant’s carbon load, but the higher the plant’s carbon load, the less the reduction in capital expenditure. This is the expected result: the higher the proportion of flue gas captured, the greater the reduction in capital expenditure, but the lower the overall carbon load of the plant.

[0038] For a Cogen unit designed to provide heat and electricity solely for the DAC unit, its CO2 is removed via a CO2 removal system, and the total energy (heat plus electricity) is, for example, 6 MMbtu per ton, resulting in a plant carbon negative of (1 - 0.9 x 6 x 0.056) or approximately 0.7. This clearly matches the case where FGCO2 equals 1. However, in the pure DAC scenario, no additional electricity is generated, resulting in higher CAPEX costs and greater energy consumption per ton captured. Therefore, this integrated implementation is preferred, for example, with lower CAPEX, less energy used for capture, and a higher carbon negative.

[0039] The next step is to assess how much energy needs to be reduced, thereby generating an additional amount of electricity. If the energy required to produce one ton of DAC is MDAC, and the energy required to capture one ton of flue gas is MFG (for MFG, we will assume that the flue gas composition has no additional sensible heat components and that the heat of reaction for releasing CO2 is reduced), then the total energy required to capture one ton of CO2 is determined by the following formula: MT CO2= ((1 / FGCO2) x MDAC + MFG) / ((1 / FGCO2} +l} =(MDAC+FGCO2x MFG} / (l+FGCO2}.

[0040] Compared to the following DAC cases, this has already saved energy per ton: MDAC - MTCO2= (MDAC-J\;1FG} FGCO2 / (l+ FGCO2} = (SHA+ ΔHR} x (FGCO2 / (l+FGCO2}} Where SHA is the total sensible heat, and ΔHR is the reduction in the heat of reaction of the flue gas components. Electricity consumption per ton will also decrease.

[0041] If the array can be preheated separately, thus using heat from the flue gas to provide ½ of the SHA, then an additional 0.5 SHA will be reduced. Note that this heat comes from the flue gas flow and therefore does not reduce power generation, as it is typically not used and is therefore true waste heat.

[0042] If additional SHA is recovered after regeneration, the potential ¾ of the sensible heat can, in principle, be collected by exchanging heat, as is done in dual regeneration box systems, such as those described in U.S. Patent 9,925,488. It is possible to do this directly using flue gas heat, but the increased temperature may reduce the additional CO2 captured (again, a trade-off between capacity and kinetics). In some applications, lower grades of heat may be used, including preheating water to the Cogen unit, but in a highly preferred embodiment, the best outcome is likely faster regeneration, since preheating occurs during the final stage of adsorption.

[0043] In this regard, it is worth noting that there is another degree of freedom in the flue gas design phase. This involves selecting the flue gas velocity and concentration to keep the product constant and match it to the rate of emitted CO2. Generally, high concentration and low velocity are desirable because low velocity makes the overall DAC appear to have a higher CPSI. If the overall CPSI is 100 and the decay index is 0.7 at 5 rpm / sec, then the decay index will be 3.5 at 1 m / sec. More generally, another feature of this implementation is that the efficiency of capture from the flue gas stream can be reduced, but the overall result will still be carbon negative. The optimal efficiency parameters for each system should be determined empirically based on the velocity and concentration of the flue gas components being treated.

[0044] Therefore, the remaining question becomes whether there is sufficient available heat in the flue gas flow passing through the contactor to provide the heat required to preheat the substrate prior to regeneration. The heat required to preheat the array can be provided by the heat generated by the condensate, the heat of reaction of CO2 captured from the flue gas flow, and the sensible heat of the flue gas flow, as follows: a. THF = Total heat in flue gas = SHF + Heat of condensation of water vapor in flue gas (HFCW) + Heat of reaction of CO2 per ton of CO2 collected during the last stage before regeneration (HFRC).

[0045] To very roughly estimate whether there is enough heat available, let's assume SHA is 2 MM BTU per ton of CO2 and the total heat required is 6 MM BTU, which is about 30% of the energy released when burning one ton of CO2.

[0046] a. CO2 capture will not increase much, as it is at most only half of the total CO2 collected, and the heat of reaction is low.

[0047] b.SHF = Sensible heat per ton of CO2 collected from flue gas = (1-COGENE) If the COGENE is within the 70% range, then 30% will rise into the flue; assuming 1 / 4 of the heat is available (through cooling from 200°C to 50°C). This is likely about half of the required heat.

[0048] However, the latent heat of available water vapor in the flue gas entering the final stage of the CO2 capture phase will be sufficient to preheat it before the CO2 capture unit enters the regeneration chamber. Therefore, in another preferred embodiment, the hot flue gas can be cooled by evaporating water, resulting in an incident flue gas flow temperature ΔT (e.g., 70°C) higher than the final temperature (e.g., 60°C), but with a high water vapor content sufficient to contain more latent heat than required to raise the substrate (“SA”) temperature to 60°C. It is noteworthy that in this case, the preheating time is 90 seconds. Assuming a velocity of 1 m / sec, the flue gas typically contains at least about 10% water, which equates to introducing pure steam at a velocity of 300 cm / sec over 30 seconds, clearly far exceeding the requirement. However, the excess water generated in this manner would become a valuable byproduct in water-scarce desert regions such as the southwestern United States or desert areas in Africa or Asia. If the SA enters the regeneration chamber at 60°C, the pressure can be reduced to 0.2 bar without significantly cooling the regeneration chamber; in fact, further cooling can be achieved by further reducing the pressure, but using steam to remove any trapped flue gas.

[0049] Once sealed within the regeneration chamber, the adsorbent is treated, for example by heating with steam, to desorb CO2 from the adsorbent, thereby regenerating it. The desorbed CO2 is removed from the chamber and captured. The capture structure with the regenerated adsorbent is then removed from the sealed chamber and moves along a track with other capture structures to adsorb more CO2 until the next capture structure moves to its designated position within the regeneration chamber. At the desorption / regeneration position, the capture structure can be moved to a chamber located above or below the track grade, or the chamber can be positioned such that the capture structure moves to a chamber at the same grade level as the track, forming a seal with the capture structure. These alternatives are further defined below and illustrated in the accompanying drawings.

[0050] When the regeneration tank is below or above the horizontal plane, the system must include a subsystem for raising or lowering the trapping structure. In systems where the regeneration tank and track are on the same horizontal plane, a satisfactory sealing device is required to provide a seal along the sides and along the top and / or bottom surfaces.

[0051] CO2 adsorption and removal methods

[0052] The basic premise of this method is to adsorb CO2 from the atmosphere by passing air or a mixture of air and exhaust gas through an adsorbent bed, preferably under ambient or near-ambient conditions. Once CO2 has been adsorbed by the adsorbent, it must be collected and the adsorbent regenerated. Subsequent steps can be performed by heating the adsorbent with steam in a sealed container to release CO2 and regenerate the adsorbent. CO2 is collected from the container, and when it leaves the regeneration chamber, the adsorbent can then be used to re-adsorb CO2 from the atmosphere.

[0053] It is well known that most available adsorbents are prone to degradation and thus deactivation if exposed to air above a certain temperature. Therefore, the adsorbent on the substrate must typically be cooled before the trapping structure leaves the regeneration chamber and returns to the airflow.

[0054] In another preferred embodiment of the method of the invention, the flue gas, preferably in a purified form after the removal of any particulate solid or liquid substances and any gaseous substances toxic to the adsorbent, flows immediately through the trapping structure before entering the regeneration chamber. This flue gas treatment stage is preferably carried out in a closed chamber so that the pretreated flue gas does not escape into the environment before passing through the main surface of the porous substrate in the trapping structure.

[0055] Typically, due to the high CO2 concentration in flue gas, the time required to adsorb CO2 from ambient air is longer than the time required to adsorb it from flue gas. For current-generation adsorbents, this difference will require an adsorption period that, when treating ambient air, is approximately ten times longer than the time required for CO2 release and adsorbent regeneration. Therefore, based on the use of polyethyleneimine adsorbents, a system with ten trapping structures and a single regeneration unit has been adopted as the current basis for a single rotating system. If the performance of the adsorbent improves over time, the ratio of adsorption time to desorption time, and therefore the number of trapping structures required in the system, may decrease.

[0056] In particular, if a higher adsorbent loading is used, an adsorption time of one hour would be feasible, thus requiring a regeneration chamber to serve only five trap structures. Furthermore, the relative treatment time will vary with the CO2 concentration in the treated gas mixture; therefore, the higher the CO2 content, the shorter the adsorption time relative to the regeneration time. For example, by mixing combustion effluent ("flue gas") with ambient air via a gas mixer or "carburetor," the CO2 concentration of the mixture is significantly higher than that of air, but significantly lower than that of pure flue gas.

[0057] To ensure more complete removal of CO2 from the flue gas, the effluent from the ninth or final stage is returned to the second chamber immediately before regeneration, preferably to the preceding stage, i.e., the eighth stage of the adsorption cycle of the trapping structure.

[0058] The method of the present invention, in all the above embodiments, maintains a low-temperature (i.e., ambient temperature -- 100°C or lower) batch method, with unidirectional mass transfer at each stage of the method.

[0059] The chemical and physical activity within the trapping structure, as well as the mechanics of the trapping structure and the regeneration chamber, are substantially consistent with those described in U.S. Patents 10,413,866 and 10,512,880, during at least the first seven stages of the adsorption cycle and during the regeneration cycle in the sealed chamber. The disclosures of these patents are incorporated herein by reference as if completely repeated, and modified by the new disclosures presented herein. In the system according to the invention, each rotating system provides a sealable regeneration chamber for each set of rotating trapping structures, the number of trapping structures depending on the relative time required to achieve the desired adsorption and regeneration. Furthermore, it has been found that, in certain preferred embodiments, greater efficiency and lower cost are achieved by spatially associating and temporally operating the two rotating systems in an appropriate relationship to allow the regeneration chambers for the two rotating trapping structure systems to interact, such that the second is preheated by the residual heat in the first to enter its regeneration chamber by offsetting the time of each entry into the regeneration chamber, as a result of the regeneration process in the first chamber; this also effectively cools the regenerated trapping structure before returning it to the adsorption cycle on the rotating track.

[0060] According to the invention, this interaction between the regeneration chambers is achieved by reducing the pressure of the first chamber system, causing the residual steam and water in the first chamber to evaporate after CO2 release, and the system to cool to the saturation temperature of the steam at its reduced partial pressure. Furthermore, as described below, the heat released in this process is used to preheat the second adsorbent trapping structure, thus providing approximately 50% sensible heat recovery, which has a beneficial effect on energy and water usage. This concept can be used even with the use of antioxidant adsorbents. Using adsorbents that are less sensitive to oxygen at higher temperatures will result in performance improvements over time. It should be understood that the adsorbent and substrate will be at higher temperatures due to the higher concentration of CO2 adsorbed onto the adsorbent in at least the last stage just before the regeneration chamber, and possibly in one or more preceding stages, due to the exothermic nature of the adsorption reaction. This avoids the need to reduce the pressure in the regeneration chamber to the required low vacuum level when treating ambient air alone or mixed with a small amount of flue gas.

[0061] As discussed in the aforementioned earlier patents, the adsorbent trapping structure is preferably cooled before exposure to air to avoid deactivation by oxygen in the air. As described in co-pending U.S. Application 14 / 063,850, in polyamines, adsorbents with greater resistance to thermal degradation, such as poly(allylamine) and poly(ethyleneamine) and their derivatives, can be used. Cooling can be achieved, if necessary, by reducing the system pressure within the regeneration chamber, thereby lowering the steam saturation temperature. This has proven effective in eliminating the adsorbent deactivation problem because it lowers the system temperature. Therefore, a significant amount of energy is removed from the cooled first trapping structure during the depressurization step. Each time the CO2-rich substrate completes its CO2 adsorption stage and enters the second regeneration chamber, it must be heated to release CO2 and regenerate the adsorbent. This heat could be provided solely by atmospheric pressure steam supplied to the regeneration chamber, but this incurs additional operating costs. To minimize operating costs, a two-bed design concept has been developed. In this concept, as described in U.S. Patent No. 10,512,880, the heat removed from the first regeneration chamber by reducing the system pressure (and thus the steam saturation temperature) in the first regeneration chamber is used to at least partially preheat the CO2-rich substrate to be regenerated in the second regeneration chamber. Therefore, steam usage is reduced by increasing the temperature of the second chamber using the heat from the cooling of the first chamber. The residual heat duty of the first chamber is achieved by adding steam, preferably at atmospheric pressure. Other rotating trap structures repeat this process as they enter and exit both regeneration chambers, which significantly improves the thermal efficiency of the system.

[0062] The acronyms used above can be defined as follows: FG-CO2 = The ratio of flue gas CO2 to air CO2 captured per cycle. DA. CO2 = Amount of air CO2 captured per cycle FGCAPEX = Flue gas CAPEX in a pure carburetor implementation, which is the mixture of ambient air and flue gas fed into each capture structure. = Total natural gas burned in MMBTu units M = Available heat and electricity generated COGENE = Thermoelectric efficiency = M /

[0063] FGCCO2 = CO2 captured from flue gas annually DACCO2 = Annually captured atmospheric CO2 FTCO2 == Combustion Total flue gas CO2 produced during natural gas production MTCO2 = Total CO2 captured per year = Total CO2 captured from flue gas and air per year ECF = Flue Gas Capture Efficiency MDAC = Energy Captured per Ton of Air CO2 MFG = Energy captured per ton of CO2 from flue gas SHA = Sensible heat of the entire array Delta HR = Difference in heat of reaction between DAC CO2 and flue gas CO2 sites. THF = Total heat source of flue gas vapor - sensible heat + heat of CO2 reaction + heat of water condensation - (Note that the calorific value of natural gas is not consistent)

[0064] These and other features of the invention are described in the following detailed description and drawings, or are apparent from the following detailed description and drawings. Attached Figure Description

[0065] Figure 1 This is a schematic top view of a pair of cooperating rotating multi-capture structure systems for removing carbon dioxide from the atmosphere according to an exemplary embodiment of the present invention, showing the regeneration chamber for the level of each loop and the trap structure group, and two trap structures adjacent to the upstream of each regeneration chamber shown in a sealable housing provided with sealable conduits for delivering clean flue gas to the trap structures.

[0066] Figure 2 It is used from Figure 1 A schematic diagram of a pair of regeneration chambers for removing carbon dioxide in a capture structure, showing several inlet and outlet conduits connected to one of the regeneration chambers and a sealable connection conduit connecting the two regeneration chambers;

[0067] Figure 3 This is a schematic diagram of the regeneration chamber and flue gas capture structure on each adjacent loop, showing the arrangement of the piping system between each regeneration chamber and the regeneration chamber;

[0068] Figure 4 This is a frontal view of a fan, showing a fan that is relatively stationary and rotates with each of the trapping structures.

[0069] Figure 5 yes Figure 4 A schematic side front view of the design of the Dual Induced Axial Fan and the Plenum chamber;

[0070] Figure 6It is a schematic front view of a pair of rotating multi-capture structure systems that work together, showing the orbital horizontal regeneration chamber for removing carbon dioxide from the atmosphere, and the two capture structure shells immediately in front for processing the flue gas flow to capture CO2.

[0071] Figure 7 This is a conceptual diagram showing the general operation of the system between the final adsorption stage and the CO2 desorption and regeneration steps, illustrating a system in which ambient air is treated during the adsorption stage.

[0072] Figure 8 This is a conceptual diagram illustrating the general operation of one of the preferred embodiments of the system of the present invention. In the final adsorption-flue gas stage between the final adsorption stage and the CO2 desorption and regeneration steps, in this embodiment, the final adsorption stage, such as the ninth stage, receives pure flue gas or flue gas mixed with ambient air immediately upstream of the "desorption unit". The next preceding stage, such as the eighth stage, may receive exhaust gas from the ninth stage, which is a mixture of exhaust gas and ambient air, or only ambient air, depending on the composition of the exhaust gas from the ninth stage.

[0073] Figure 9 This is a conceptual diagram illustrating the general operation of another preferred embodiment of the system of the present invention, between the final adsorption-mixing air-flue gas stage and the CO2 desorption and regeneration steps. In this embodiment, the final adsorption stage, for example, the ninth stage, receives flue gas mixed with ambient air immediately upstream of the "desorption unit"; and

[0074] Figure 10 An example of a seal extending around all sides of each trapping unit in the housing of a desorption unit or flue gas adsorption unit is depicted when each housing is at the horizontal plane height and the trapping structure enters each housing as each trapping structure moves along the track. Implementation

[0075] A simplified description of the design of the system used to perform these operations is provided below. Figures 1 to 6 The operation and required auxiliary equipment are shown below, similar to those shown in commonly owned U.S. Patents 10,413,866 and 10,512,880.

[0076] In this embodiment, there are ten “capture structures,” preferably, but not necessarily, arranged in a decagonal pattern and positioned on substantially circular or arc-shaped tracks. Two substantially circular (or oval) / decagonal components are associated with each processing unit, and they interact as shown. In this preferred embodiment, air is passed through the capture structures by an induced draft fan located inside the capture structures. In one location, the capture structures are positioned adjacent to a single sealable chamber, into which each capture structure is inserted for processing as it moves along the tracks. In the sealable regeneration chamber, the capture structures are heated to no higher than 130°C, more preferably no higher than 120°C, and most preferably no higher than 100°C, preferably using process hot steam to release CO2 from the adsorbent and regenerate the adsorbent. Alternatively, the regeneration chamber may be above or below the waterline. In this embodiment, the adsorption time for CO2 by the capture structures is preferably ten times the adsorbent regeneration time.

[0077] It should be understood that although a porous monolithic substrate is preferred in the trapping structure, a fixed bed of porous particles or granular material within a frame supported on the trapping structure may be used, if feasible. In either case, when the granular trapping structure has the same pore volume as the monolithic trapping structure used to support the adsorbent, the porous substrate preferably supports the amine adsorbent for CO2.

[0078] The schematic diagram illustrates the basic operational concept of the system according to the invention. Ten "capture structures" 21, 22 are located in each decagonal assembly arrangement and are movably supported on circular tracks 31, 33. Two circular / decagonal assemblies A, B are associated with each processing unit and they interact with each other. Air or flue gas passes through each capture structure 21, 22 via induced draft fans 23, 26, which are located radially inside each decagonal assembly and guide the exhaust gas out of the inner circumferential surface of each capture structure and upward away from the system. At one location along tracks 31, 33, the capture structures 21, 22 are adjacent to sealable regeneration chambers 25, 27, into which the capture structures 21, 22 are inserted after completing one rotation around the track for regeneration processing.

[0079] Therefore, as Figure 1 and Figure 2 As shown, the first collection structure 21 is rotated into position within the regeneration chamber 25 for processing; for the regeneration chamber 25, which is horizontal. Once the collection structure is in place within the regeneration chamber 25, movement of all collection structures along the track is stopped. Alternatively, constant speed movement can be achieved by increasing the diameter of the track and the collection structure, and by having a suitable sealing system on the regeneration chamber and any flue gas adsorption housings (121, 221, 122, 222). Figure 1As shown, when the trapping structures 21 and 22 have been regenerated, the regenerated trapping structures are removed from the regeneration chambers 25 and 27 as all trapping structures move, so that the next trapping structure 21 or 22 can move in after the flue gas has been treated. This process is essentially repeated continuously. In the preferred embodiment shown in the figures, one or more trapping structures on each track will be removed from the flue gas adsorption housing (121, 221, 122, 222) because the adsorption time is preferably matched with the flue gas desorption time. Alternatively, the movement of the trapping structure can be stopped each time it enters the regeneration chamber and one or more flue gas adsorption housings (121, 221, 122, 222), and then restarted when desorption and flue gas adsorption are complete.

[0080] However, as described above, the method of the present invention is a low-temperature (preferably ambient temperature to 100°C), semi-continuous method with unidirectional mass transfer at each stage of the method. Another novel aspect of the method is that the reaction for capturing CO2 from the gas mixture preferably occurs together with a renewable material (in a preferred embodiment, on an amino polymer), such as an amino polymer adsorbent impregnated in a porous substrate.

[0081] In a preferred embodiment, the adsorbent-supported trapping structure comprises an integral substrate supported sequentially by a frame to form each trapping structure.

[0082] The two decagonal ring assemblies operate together, although the trapping structures of each decagonal ring move into and out of their desorption / regeneration chambers at slightly different times, as described below, to allow heat transfer, for example, between chambers 25 and 27, such as when regeneration in chamber 25 is complete to preheat the other chamber (e.g., regeneration chamber 27). This saves heat at the start of regeneration and reduces the cost of cooling the trapping structures after regeneration.

[0083] The three positions of the regeneration chambers 25 and 27 are available: above or below the rotating trapping structure where continuous movement is not permitted, or on the same horizontal plane. See U.S. Patents 10,413,866 and 10,512,880.

[0084] The regeneration chamber 327 is located on the same horizontal plane as the rotating collection structure assembly. These chambers are positioned with sufficient inlets to allow for maintenance and treatment of the piping on the same horizontal plane. Suitable mutually sealing surfaces are located on the chambers and each collection structure, such that chamber 327 is sealed when the collection structure moves into its position within the chamber, regardless of whether the movement is upward into an elevated regeneration chamber, downward into a regeneration chamber below the horizontal plane, or straight into a regeneration chamber on the same horizontal plane; the same applies to embodiments where the flue gas adsorption housings (121, 221, 122, 222) can be on the same horizontal plane or below or above the horizontal plane. Optional enclosed chambers are also available at the immediate preceding positions along the track for supplying flue gas or partially cleaned flue gas into the collection structure.

[0085] In all cases, auxiliary equipment (such as pumps, control systems, etc.) is preferably located at the same level plane inside or outside the circumference of the track supporting the rotating trapping structure assembly 39.

[0086] Without departing from the concept or scope of the invention, the recycling box and housing may be located at different heights, in certain circumstances.

[0087] An alternative design falling within the scope of this invention provides a system in which the regeneration box, chamber 25 pair can move along a track. This is best used where the track design allows for reciprocating movement along a straight track by means of a trapping structure, so that the regeneration box 25 does not become significantly separated. Compared to the previously disclosed apparatus in the prior art, this will: Reduce structural steel; Except for the regeneration tank, which is used solely as a containment vessel, all major equipment is placed at the same level. Ensure that the airflow to the trapping structure is undisturbed, with the box and track at different heights; Rotate all capture structures to move them into the regeneration box to avoid moving larger, multi-unit systems. Two regeneration chambers are allowed to be adjacent to each other with minimal clearance to allow for the necessary heat exchange to improve efficiency.

[0088] The required mechanical operations, which require the necessary machinery and power, include: Two sets of capture structure components rotate around a roughly circular track on the support structure, precisely positioning the elements at the stop position of the capture structure to ensure that the capture structure can freely move in and out of the regeneration box and any flue gas adsorption housing.

[0089] The trapping structure is removed, or only the substrate is removed, the trapping structure is inserted into the regeneration chamber, removed from the regeneration chamber, and reinserted into its position on the track assembly. All these movements occur in the vertical direction, or as part of a horizontal rotational movement on the track. The trapping structure and regeneration chamber are designed such that, for vertically movable trapping structures, there is a substantially airtight seal between the top or bottom of each trapping structure and the support structure of the chamber. For such regeneration chambers or flue gas adsorption housings at the same level, the seal may be on the side surfaces as well as the top and bottom surfaces, or there may be a sealing door that closes when the trapping structure moves into the regeneration chamber or flue gas adsorption housing. Examples of some conceptual designs of such seals are shown in previously granted U.S. patents by Eisenberger and in this application. Figure 10 middle.

[0090] In all cases of a preferred embodiment, refer to Figures 1 to 9 The trapping structure 21-1 (ring A) is rotated into place and then moved to the regeneration or desorption tank 25 for processing. The pressure in the desorption tank 25 (containing the trapping structure 21-1, ring A) is reduced to less than 0.2 bar using, for example, a vacuum pump 230. The tank 25 is heated by vapor at atmospheric pressure through line 235, CO2 is generated from the trapping structure 21-1 and removed from the tank 25 through outlet pipe 237, and then condensed in condenser 240 (…). Figure 3 The condensate and CO2 are separated on the surface. Then, the trapping structure 22-1 (ring B) is placed in box 27 (ring B) while simultaneously processing box 25, as above. Figure 3 Stop supplying steam to tank 25 and isolate the outlet pipes for CO2 and condensate. Tanks 25 and 27 are connected by opening connecting pipe 125. Figure 3 It is connected to valve 126 in )

[0091] The pressure in chamber 27 is reduced using a vacuum pump 330 associated with chamber 27. This reduces the system pressure in both chambers and draws the remaining vapor and inert elements from chamber 25 through chamber 27 and then into the vacuum pump. This cools chamber 25 (and thus trapping structure 21-1, ring A) to a lower temperature (i.e., the saturation temperature under the vapor partial pressure in the chamber) and reduces the likelihood of adsorbent oxygen deactivation when trapping structure 21-1 is returned to the airflow. The process also preheats chamber 27 (and thus trapping structure 22-1, ring B) from ambient temperature to the saturation temperature under the vapor partial pressure in chamber 25. Therefore, energy is recovered, and the atmospheric pressure vapor required to heat the second chamber 27 (and trapping structure 22-1, ring B) is reduced. Figure 3As vacuum pump 330 reduces the pressure in chambers 25 and 27, the temperature of the first chamber 25 decreases (from approximately 100°C to an intermediate temperature) and the temperature of the second chamber 27 increases (from ambient temperature to the same intermediate temperature). Vacuum pump 330 removes CO2 and inert gases from the system.

[0092] The valve between the first chamber 25 and the second chamber 27 is closed, isolating them from each other. The trapping structure 21-1 and ring A are now cooled below the temperature required for oxygen deactivation of the adsorbent when the trapping structure is returned to the airflow. The second chamber 27 and the trapping structure 22-1 and ring B have been preheated, thus reducing the amount of steam required to heat the chambers and trapping structures. The trapping structure 21-1 and ring A are then removed into the trapping structure assembly. The ring A trapping structure assembly is preheated by rotating one trapping structure, then inserting trapping structure 21-2 and ring A into chamber 25. Chamber 27 is heated with atmospheric pressure steam, and the separated CO2 is collected.

[0093] When the second chamber 27 (containing trap structure 22-1, ring B) has been fully regenerated, the vapor supplied to chamber B is isolated, and the piping for CO2 and condensate is isolated using valves 241 and 242. Valve 126 between the first chamber 25 and the second chamber 27 is opened, and the pressure in chambers 25 and 27 is reduced using the vacuum pump 230 system for chamber 25. The temperature of the second chamber 27 (and therefore trap structure 22-1, ring B) decreases. The temperature of the first chamber 25 (containing trap structure 21-2, ring A) increases. The vacuum pump 230 reduces the pressure in chambers 25 and 27. The temperature of chamber 25 decreases (from approximately 100°C to some intermediate temperature). The temperature of chamber 27 increases (from ambient temperature to the same intermediate temperature). CO2 and inert gases are removed from the system by the vacuum pump 230. Trapping structure 22-1 and ring B are moved back into the ring assembly, and the assembly rotates by one bed. Then trap structure 22-2 and ring B are inserted into chamber 27. The chamber 25 (containing the trapping structure 21-2 ring A) is heated with atmospheric pressure steam to release CO2 and regenerate the adsorbent. Preheating of chamber 27 then occurs as described above. This process is repeated for all beds as the decagon rotates multiple times.

[0094] When processing such Figure 8In the preferred embodiment shown, the two rings include a pair of flue gas adsorption shells immediately preceding the regeneration chamber, providing feed for the preferably pretreated flue gas. For example, a ninth adsorption stage immediately preceding the regeneration chamber is supplied with pretreated flue gas typically having about 10-15% CO2, or a mixture of pretreated flue gas and ambient air. The exhaust gas from this stage may contain, for example, 2 to 8% CO2. Preferably, when the upper limit of CO2 is reached, the exhaust gas is most preferably passed to a shell immediately preceding the desorption stage for further adsorption to reduce the exhaust gas to a suitable level before being released into the atmosphere. Preferred design parameters

[0095] The preferred system design criteria are as follows: Weight of the individual trap structure to be moved: 1,500–10,000 pounds (including supporting structure) Approximate bed dimensions: Width -- 5-6 meters Height -- 9-10 meters Depth -- 0.15-1 meter

[0096] It should be noted that the size of the trap structure can be adjusted according to the specific conditions at the geographical location of each pair of systems and the desired or available processing parameters.

[0097] For a system comprising 10 trapping structures in each decagonal ring, the preferred external dimensions of the circular / decagonal structures would be approximately 15-17 meters, preferably approximately 16.5 meters. The trapping structures and support structures can be driven individually, for example by an electric motor and drive wheels along the track, or the support structures can be fixed to specific locations along the track, and a single large motor is used to drive the track and all the structures around the closed loop. In either case, the regeneration box is positioned, and all structures can stop moving when one of the support structures is positioned to move into the regeneration box. The economics of a single drive motor or engine or multiple drive motors or engines will depend on many factors, such as location and whether the drive is performed by an electric motor or by a fuel-powered engine. The nature of the drive unit itself is not a primary feature of the invention, and many drive units are well known to those skilled in the art. Examples of suitable engines include internal combustion engines or external combustion engines or pneumatically driven engines, such as those operating using a Stirling engine cycle, or process steam engines, or hydraulic or pneumatic engines.

[0098] When the regeneration box is above the track plane, its top will be approximately 20 meters above the track level. When the regeneration box is below the track level, its top will be just below the track level. The box above the level will be only slightly above the minimum height of the capture structure, so that the capture structure is completely contained within the box during regeneration.

[0099] When the regeneration chamber is not horizontal, the lifting system used to move the trapping structure into and out of the regeneration chamber should be able to complete the movement within 30 to 120 seconds, preferably between 30 and 45 seconds. The shorter the time period, the greater the flexibility of the process parameters available for the process. It is well known that certain inherent mechanical limitations exist when moving large-scale trapping structures. One advantage of having the regeneration chamber horizontal is that vertical movement is not required, as the trapping structure simply rotates into the regeneration chamber as part of its rotational movement and seals itself; thus avoiding vertical movement of the lifting system, time losses, and additional capital costs. In each case, both edges of the trapping structure are solid and form a seal with the edge of the regeneration chamber.

Claims

1. A method, characterized in that, The method includes: CO2 is captured from a first gas by an adsorbent, wherein the first gas has a first CO2 concentration; After capturing CO2 from the first gas, CO2 is captured from a second gas by the adsorbent, wherein the second gas has a higher CO2 concentration than the first CO2 concentration; and After capturing CO2 from the first and second gases, the adsorbent is regenerated.

2. The method according to claim 1, characterized in that, The first gas is ambient air, and the second gas includes flue gas.

3. The method according to claim 1, characterized in that, The first gas is ambient air, and the second gas includes exhaust gas from the CO2 removal system.

4. The method according to claim 1, characterized in that, The first gas is ambient air, and the second gas is a mixture of ambient air and flue gas.

5. The method according to claim 1, characterized in that, The time required to capture CO2 from the first gas is longer than the time required to capture CO2 from the second gas.

6. The method according to claim 1, characterized in that, The method further includes: capturing CO2 from the effluent of the second gas using the adsorbent after capturing CO2 from the first gas and before capturing CO2 from the second gas.

7. The method according to claim 1, characterized in that, Regenerating the adsorbent involves heating the adsorbent.

8. The method according to claim 1, characterized in that, Regenerating the adsorbent involves placing the adsorbent under a vacuum.

9. The method according to claim 1, characterized in that, The adsorbent is an amino polymer.

10. The method according to claim 1, characterized in that, The adsorbent is impregnated in a porous solid substrate.

11. A system, characterized in that, The system includes: Adsorbents are used to capture CO2 from gases. One or more first stations, comprising the adsorbent and configured to capture CO2 from a first gas having a first CO2 concentration; One or more second stations, comprising the adsorbent and configured to remove CO2 from a second gas having a second CO2 concentration higher than the first CO2 concentration; A desorption unit for regenerating the adsorbent; and A system configured to move the adsorbent from one or more first stations to one or more second stations and subsequently from one or more second stations to the desorption unit.

12. The system according to claim 11, characterized in that, The first gas is ambient air, and the second gas includes flue gas.

13. The system according to claim 11, characterized in that, The first gas is ambient air, and the second gas includes exhaust gas from the CO2 removal system.

14. The system according to claim 11, characterized in that, The first gas is ambient air, and the second gas is a mixture of ambient air and flue gas.

15. The system according to claim 11, characterized in that, The system also includes: At least one first fan is used to guide a first airflow of the first gas to the one or more first stations; and At least one second fan is used to guide a second airflow of the second gas to the one or more second stations.

16. The system according to claim 11, characterized in that, The system also includes: One or more third stations, comprising the adsorbent and configured to capture CO2 from the effluent of the second gas, wherein the one or more third stations are arranged prior to the one or more second stations.

17. The system according to claim 11, characterized in that, The desorption unit is configured to heat the adsorbent.

18. The system according to claim 11, characterized in that, The desorption unit is connected to the vacuum pump.

19. The system according to claim 11, characterized in that, The adsorbent is an amino polymer.

20. The system according to claim 11, characterized in that, The one or more first stations and the one or more second stations include a set of carbon dioxide removal structures, wherein each of the carbon dioxide removal structures in the set of carbon dioxide removal structures supports a porous solid substrate, and wherein the adsorbent is impregnated within the porous solid substrate.

21. A system for removing CO2, characterized in that, The system includes: A set of carbon dioxide removal structures, wherein each carbon dioxide removal structure in the set of carbon dioxide removal structures includes one or more porous solid substrates, each of the one or more porous solid substrates having an adsorbent supported within its pores, the adsorbent being capable of capturing carbon dioxide. The first set of stations includes one or more of the carbon dioxide removal structures and is configured to remove CO2 from the first gas; At least one additional station includes one or more of the carbon dioxide removal structures and is configured to remove CO2 from a second gas, wherein the second gas has a second CO2 concentration that is higher than the CO2 concentration of the first gas; A sealable regeneration chamber for regenerating the adsorbent, wherein the at least one additional station is located after the first set of stations and before the regeneration chamber; and A system for moving the set of carbon dioxide removal structures between the first set of stations, the at least one additional station, and the regeneration box, wherein the system for moving the set of carbon dioxide removal structures includes an open track.

22. A method for removing CO2, characterized in that, The method includes: A set of carbon dioxide removal structures is moved from one station to another while being exposed to a first gas in the first set of stations. Subsequently, each carbon dioxide removal structure in the set is sequentially exposed to a second gas. Moving the set of carbon dioxide removal structures includes moving it on an open track. The second gas has a higher CO2 concentration than the first gas. Each carbon dioxide removal structure in the set comprises one or more porous solid substrates, each of which supports an adsorbent within its pores. The adsorbent is capable of capturing carbon dioxide. After exposure to the second gas, each carbon dioxide removal structure in the group is sequentially placed into the regeneration chamber in a sealable manner, wherein the carbon dioxide captured by the adsorbent is desorbed from the adsorbent, and the adsorbent is regenerated during the regeneration time in the regeneration chamber.

23. A method for removing CO2, characterized in that, The method includes: A carbon dioxide removal structure is exposed to a first gas including CO2 for a first exposure time, wherein the carbon dioxide removal structure comprises a porous solid substrate, wherein an adsorbent is supported within one or more pores of the porous solid substrate, wherein during the first exposure time, the carbon dioxide removal structure loads CO2 onto the adsorbent at a first CO2 loading amount. After exposing the carbon dioxide removal structure to the first gas, the carbon dioxide removal structure is exposed to a second gas including CO2 for a second exposure time, wherein during the second exposure time, the carbon dioxide removal structure is loaded with a second CO2 load on the adsorbent, wherein the first CO2 load is lower than the second CO2 load. Regenerate the carbon dioxide removal structure to remove at least a portion of the loaded CO2 adsorbed on the adsorbent; and CO2 is continuously removed from the first gas and the second gas using a set of carbon dioxide removal structures, wherein the continuous removal includes moving the set of carbon dioxide removal structures on an open track.

24. A system for removing CO2, characterized in that, The system includes: A set of carbon dioxide removal structures, wherein each carbon dioxide removal structure in the set of carbon dioxide removal structures includes one or more porous solid substrates, each of the one or more porous solid substrates having an adsorbent supported within its pores, the adsorbent being capable of capturing carbon dioxide. The first set of stations includes one or more of the carbon dioxide removal structures and is configured to remove CO2 from the first gas; At least one additional station includes one or more of the carbon dioxide removal structures and is configured to remove CO2 from a second gas, wherein the second gas has a second CO2 concentration that is higher than the CO2 concentration of the first gas; A sealable regeneration chamber for regenerating the adsorbent, wherein the at least one additional station is located after the first set of stations and before the regeneration chamber; and A system for moving the group of carbon dioxide removal structures between the first set of stations, the at least one additional station, and the regeneration box, wherein the system for moving the group of carbon dioxide removal structures includes a track, the track being a continuous closed loop track.

25. A method for removing CO2, characterized in that, The method includes: A set of carbon dioxide removal structures is moved from one station to another while being exposed to a first gas in the first set of stations. Subsequently, each carbon dioxide removal structure in the set is sequentially exposed to a second gas. Moving the set of carbon dioxide removal structures involves moving the set of structures along a continuous closed-loop track. The second gas has a higher CO2 concentration than the first gas. Each carbon dioxide removal structure in the set comprises one or more porous solid substrates, each of which supports an adsorbent within its pores. The adsorbent is capable of capturing carbon dioxide. After exposure to the second gas, each carbon dioxide removal structure in the group is sequentially placed into the regeneration chamber in a sealable manner, wherein the carbon dioxide captured by the adsorbent is desorbed from the adsorbent, and the adsorbent is regenerated during the regeneration time in the regeneration chamber.

26. A method for removing CO2, characterized in that, The method includes: A carbon dioxide removal structure is exposed to a first gas including CO2 for a first exposure time, wherein the carbon dioxide removal structure comprises a porous solid substrate, wherein an adsorbent is supported within one or more pores of the porous solid substrate, wherein during the first exposure time, the carbon dioxide removal structure loads CO2 onto the adsorbent at a first CO2 loading amount. After exposing the carbon dioxide removal structure to the first gas, the carbon dioxide removal structure is exposed to a second gas including CO2 for a second exposure time, wherein during the second exposure time, the carbon dioxide removal structure is loaded with a second CO2 load on the adsorbent, wherein the first CO2 load is lower than the second CO2 load. Regenerate the carbon dioxide removal structure to remove at least a portion of the loaded CO2 adsorbed on the adsorbent; and A set of carbon dioxide removal structures is used to continuously remove CO2 from the first gas and the second gas, wherein the continuous removal includes moving the set of carbon dioxide removal structures on a continuous closed loop track.

27. A system for removing carbon dioxide from a gas, characterized in that, The system includes: A set of carbon dioxide removal structures, wherein each carbon dioxide removal structure in the set of carbon dioxide removal structures includes one or more porous solid substrates, each of the one or more porous solid substrates having an adsorbent supported within its pores, the adsorbent being capable of capturing carbon dioxide. An endless loop support for the group of carbon dioxide removal structures, the endless loop support being arranged to allow each of the carbon dioxide removal structures in the group to move along a closed curve while being exposed to a first gas; and At least one sealable regeneration chamber is provided, supported along an endless loop, in which one or more carbon dioxide removal structures of the group are sealably placed, such that when the one or more carbon dioxide removal structures are sealed therein, at least a portion of the carbon dioxide captured by the adsorbent is removed from the adsorbent, and the adsorbent is regenerated, wherein the total number of carbon dioxide removal structures relative to the total number of regeneration chambers corresponds to the ratio of the time taken to capture CO2 from a baseline level to a desired level by the adsorbent to the time taken to remove the captured CO2 from the desired level of the adsorbent back to the baseline level.

28. A method for removing carbon dioxide from a gas, characterized in that, The method includes: A set of carbon dioxide removal structures is moved around a closed, unended loop while being exposed to a first gas. Each of the carbon dioxide removal structures in the set includes one or more porous solid substrates, each of the one or more porous solid substrates having an adsorbent supported within its pores, wherein the adsorbent is capable of capturing carbon dioxide from the gas mixture during the adsorption time. Each of the carbon dioxide removal structures in the group is hermetically placed in at least one regeneration chamber along the endless loop support, such that when the one or more carbon dioxide removal structures are sealed in the regeneration chamber, carbon dioxide captured by the adsorbent is removed from the adsorbent, and the adsorbent is regenerated during the regeneration time, wherein the total number of carbon dioxide removal structures relative to the total number of regeneration chambers corresponds to the ratio of the time for capturing CO2 from the base level to the desired level by the adsorbent to the time for removing the captured CO2 from the desired level of the adsorbent back to the base level.

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