Rotating continuous mulch for improved direct air capture of carbon dioxide (DAC+)

Abstract

A new and useful system and method for removing carbon dioxide from a carbon dioxide-containing gas mixture with greater efficiency and at lower overall cost is provided. The system includes a group of carbon dioxide removal structures that travel along a closed curved track. At one location along the track is a desorption or regeneration box through which each capture structure passes to be regenerated. The majority of the CO2 removal structures are supplied with ambient air, or a mixture of ambient air and a small portion of flue gas, and vented CO2-purified air. At least one selected such removal structure in each group is supplied with flue gas containing at least 4% CO2 by volume at a location immediately prior to its entry into the capture structure. A method for removing carbon dioxide from the atmosphere is provided utilizing a system that operates similarly to the aforementioned system.

Description

[Background technology]

[0001] Capture Systems and Devices The present invention relates generally to systems and methods for removing greenhouse gases from the atmosphere, and more particularly to , first capturing carbon dioxide from a gas stream containing ambient air, then flue gas New and improved system for capturing carbon dioxide from at least one stream of gas containing The present invention relates to a system and method, wherein the sequence may include different sequences of carbon dioxide removal. The present invention contemplates a system for purifying a second gas mixture comprising two or more streams of gas, including flue gas. The following sequential steps are further contemplated:

[0002] The present invention relates to a method for producing a semiconductor device, a semiconductor manufacturing method, and a semiconductor device according to the present invention. (now U.S. Patent Application No. 8,500,855) and U.S. Patent Application No. 9,925,48 8, especially when further modified: It is recognized that the present invention may be utilized for a broader range of uses than those disclosed in the previous application. Systems and processes are presented that may be used in the present invention. as if repeated in its entirety, modified by any new disclosures contained therein. No. 6,029,499, filed Dec. 1, 2004, which is incorporated herein by

[0003] Currently, attention is focused on achieving three seemingly contradictory energy goals: 1) Providing affordable energy for economic development; 2) Energy 3) Avoid specific climate change due to global warming. To ensure we have the energy we need to prosper and avoid the energy shortages that could lead to conflict, Therefore, it is not feasible to completely avoid the use of fossil fuels for the rest of this century. Assume there isn't.

[0004] Carbon dioxide and other so-called greenhouse gases (methane and water vapor are also major greenhouse gases) It is widely accepted among respected scientists that an increase in the amount of carbon dioxide (CO2) will increase the average temperature of the Earth. There is almost no disagreement.

[0005] Furthermore, the risks of climate change can only be eliminated by reducing the amount of carbon dioxide humans emit. It is also clear that direct air capture or direct air extraction (DAC) is not possible. It is also necessary to remove additional CO2 from the atmosphere, which can be absorbed by the atmosphere. Its ability to reduce the amount of carbon dioxide in the atmosphere can help reduce the amount of methane and other gases that can cause climate change. Compensating for other greenhouse gas emissions (emitted into the atmosphere by both natural and human activities) can be compensated.

[0006] Particularly in the last decade, experts in this field have been increasingly concerned with the reduction of so-called "greenhouse" gases in the atmosphere. To at least slow the increase in CO2, even though the concentration is low, The idea that direct carbon dioxide capture is economically feasible is gaining popularity. Currently, there are suitable regenerable adsorbent systems and relatively low-temperature stripping or CO2 can be efficiently extracted from the atmosphere under ambient conditions using either a renewable or regenerative process, and Such processes can be expanded to remove CO2 from flue gas mixtures mixed with large amounts of ambient air. It can be combined with other technologies to remove CO2 from the flue gas as well as to It is understood that CO2 can be removed in a low-cost and highly efficient manner. This will result in a net reduction in CO2 in the atmosphere. Summary of the Invention

[0007] The present invention relates to a DAC system for removing carbon dioxide from carbon dioxide-laden air. and methods with higher efficiency and lower capital expenditures (“CAPEX”) and More new and effective solutions at lower overall costs, including lower operating expenses (“OPEX”). This provides a useful improvement.

[0008] SUMMARY OF THE INVENTION In accordance with the present invention, a novel process and method utilizes the assembly of multiple separate CO2 capture structures. A substrate capture assembly and system are developed, each of which may comprise a bed of substrate particles. The substrate capture structure supports the adsorbent with a high regeneration rate relative to the rate at which the adsorbent containing the captured CO2 is regenerated. , from ambient air, or from any gas mixture that is treated to remove CO2 are combined with a single regeneration box in a ratio that depends on the ratio of the adsorption rates of the In one embodiment, the CO2 capture structure is supported on a substantially continuous closed loop track, preferably Preferably, the CO2 capture structure forms a closed curve, on which the CO2 capture structure is regulated by the flow of air around it or the surrounding area. Continuously longitudinally along the track while exposed to a gas mixture containing most of the ambient air. Alternatively, the capture structure may be moved longitudinally back and forth along an open track. It can be moved.

[0009] At one point along the track, the longitudinal movement stops and one of the CO2 capture structures is treated. The CO2 is then stripped from the adsorbent and re-adsorbed. Once the adsorbent is regenerated, the next CO2 capture structure is positioned to enter the regeneration box. The capture structures rotate around the track until the CO2 capture structures rotate around the track. In a refinement of the invention, smoke is introduced into at least one of the capture structures instead of the surrounding air. Preferably, the other capture structures are provided with ambient air, at least in large part, to contain the gas. Most preferably, the last station before the regeneration box, i.e., the stage , pure but pretreated flue gas, or a mixture of flue gas and ambient air (here, charcoal The goal is to receive a flue gas input that is a mixed gas (called oxidized flue gas).

[0010] The velocity and concentration of the input flue gas is controlled independently at the input, but the output is controlled by a separate manifold. Ideally, in some circumstances, this would be It can be a pure DAC unit modification. Before entering the playback box, additional CO2 The adsorbent is preheated in the capture structure substrate by adding the The cooling of the material and adsorbent remains unchanged, but the array is already preheated before regeneration begins. The removed heat can be used differently. The DAC and carburetor units are separated. Compared to the traditional approach, this integrated approach offers the following advantages: 1.1 30% to 50% (expected) increase in total CO2 production per DAC plant thereby reducing capital expenditures per metric ton. 2. Use capital plants similar to DAC to reduce capital costs of flue gas capture components. do. 3. Less energy is used per metric ton of CO2 produced, which means: A. The amine moiety that binds high-concentration CO2 has a low reaction heat (note that in this embodiment In this case, not only adsorbents containing primary amines but also other adsorbents such as those containing secondary amines are used. (An agent, or a mixture, may be optimal.) B. Because more CO2 is produced for the same amount of sensible heat. C. Because the heat from the flue is used to preheat the array.

[0011] There are three cases to consider. 1. The combined heat and power unit is sized to provide heat and power for the system. When used alone. 2. Connected to a larger combined heat and power plant, resulting in available heat and flue gas CO 2 is more than is used in a DAC unit and would generate excess electricity and heat. 3. Based on the need for flue gas CO2 removal, CO2 is captured from the power source and In the case of a negative carbon power plant, which determines the size of the AC (in this case, the entire facility is negative carbon) Therefore, the amount of flue gas CO2 captured can be selected based on cost (e.g. , removing more CO2 than the power plant emits).

[0012] It can be seen that the same design holds for the above three cases. is only the size of the combined heat and power plant. In the above 2, the energy required for a particular application (e.g., compression) is used, and in the above 3, the micro The size of the carbon-neutral power plant is determined by its size.

[0013] Also, in a world trying to reduce emissions, net combustion plants are responsible for 10% of the emissions coming out of their smokestacks. It could be argued that the government imposes a penalty of 100% and gives credits for the negative carbon generated. In this case, this embodiment is preferable from both the viewpoint of climate change and economic efficiency. In the process of this embodiment, the pure flue gas is at least Used at the final CO2 capture station.

[0014] Another preferred embodiment is to use previously pretreated, i.e., partially trapped, flue gas. For example, this flue gas may be supplied from the final or final capture structure. Exhaust, i.e., from fuel-burning power plants, cement manufacturing plants, steel plants, etc. Conventional CO2 removal systems, the type long used in industries with large CO2-containing exhaust gases, The flue gas pretreatment system is used to treat solid fuels such as coal. Non-toxic particulates or sorbents emitted from the combustion of bodies or liquids such as petroleum. This is particularly important when dealing with exhaust gases where particulate compounds may be present.

[0015] In such a system, the plant that generates steam to heat the regenerative chamber is According to this improved invention, a waste product to be treated is provided. Such a system comprises: For example, a separate plant whose primary purpose is to provide steam for regenerating the adsorbent. The second alternative is to build other facilities such as electric power plants, cement factories, steel mills, and oil refineries. A preferred example is the use of the plant for the cogeneration of products. It is a combined heat and power plant that produces fuel from CO2 generated from the plant. A particularly favourable example would be a cogeneration plant converting fuel intended for sale or use elsewhere into CO2 The goal is to produce from

[0016] If the adjacent plant is a power plant, the output of the power plant is co-generated and This includes excess steam and electricity, at least some of which is required to operate the DAC plant. The combustion waste from such power plants, i.e. flue gas, The waste is at least partially purified and then converted to CO immediately prior to being input into the regeneration chamber. Furthermore, as mentioned above, the partially CO2-reduced waste The waste material is released either alone or mixed with the surrounding air just before the capture structure, i.e., at the eighth position. Of course, there is a single regeneration chamber with 10 capture structures. In this case, the regeneration chamber is the 10th stage, and the capture structure is just before entering the regeneration chamber. The capture structure stage will be understood to be the ninth stage, and the previous stage will be understood to be the eighth stage. Examples of suitable structures for the system are shown in the figures and description below.

[0017] Another preferred embodiment is a flue gas that has been partially pre-treated to capture CO2. For example, the exhaust gas is transferred from the final or final capture structure to a CO2-containing supply. exhaust, or the conventional C that has traditionally been used in industries with large amounts of CO2-containing exhaust O2 removal systems (fuel-burning power plants, cement manufacturing plants, steel plants, etc.) Systems with pretreatment of such wastes can be used to treat solids such as coal, or oil. Fine particles, solid or liquid particles, toxic to adsorbents, emitted from the combustion process of liquids such as This is particularly important when dealing with exhaust containing certain gases.

[0018] A further preferred embodiment is a plant produced from a DAC+ plant of the present invention. This is the situation where CO2 is used to produce fuel for sale or use elsewhere.

[0019] Each capture structure has carbon dioxide adsorption sites, preferably amine groups, on its surface, and most preferably Preferably, the capture structure is formed from a porous substrate having amine groups with a high proportion of primary amines. As the structures move along the track, each capture structure reaches a sealed playback box. According to this improvement, the CO2 capture structure adsorbs CO2 from the moving gas stream until While traveling through the loop a few minutes before reaching the box, the flue gas is blown in instead of the ambient air. Treatment can be further improved by passing the gas through individual CO2 capture structures.

[0020] However, as explained above, the present process invention is suitable for use at low temperatures (preferably ambient to 1 00°C) with unidirectional mass transport during each phase of the process. A further novel aspect of the present invention is that the reaction of capturing CO from a gas mixture is carried out by reacting the carbon monoxide (CO2) from the carbon dioxide (CO2) on an amino polymer. In one preferred embodiment, the method is carried out using renewable materials, e.g., aminopoly Preferably, the polymer adsorbent is impregnated within the substrate.

[0021] The adsorbent-carrying capture structure, in a preferred embodiment, comprises a monolith supported in turn by: Includes thick substrate. 1. The substrate is placed along a closed loop or open line along which the substrate moves during the CO2 capture process. In one preferred embodiment, the substrate is impregnated into the pores of the monolith. a porous monolith having an adsorbent attached thereto; 2. In one preferred embodiment of the present invention, the substrate is, for example, cordierite, murai silica, alumina, titania, silica mesocellular foam (MCF), and mesoporous Coating throughout the pores of lath-γ-alumina, as well as MCF or other such materials Ceramic materials from mesoporous γ-alumina, metal oxides (e.g., single or formed from silica, alumina, titania, or porous oxides of other metals mixed conditions that are met during the CO2 capture stage or during the regeneration of the sorbent as described below. Sufficient structural strength and heat resistance to be able to maintain its monolithic shape under When the thermal conditions are not severe, porous glass fiber, hard polymer plastic or by extrusion, corrugation, crimping, 3D printing, or molding, or other known or developed methods. Other various materials, such as structurally robust porous materials, can be formed into desired shapes by the procedure described above. Porous materials may be used. 3. Impregnated adsorbent a. The most commonly used adsorbents are amino polymers. i. Polyethyleneimine (PEI) is used by most people working in the field for the following reasons: is the adsorbent of choice. 1. High activity at low CO2 concentrations, high amine density, and large-scale commercial availability. 2. However, it is limited by its known oxidative decomposition at high temperatures. ii. Other amino polymers contain varying degrees of primary, secondary, and tertiary amines, if and as adsorbents with a variety of backbone chemistries, molecular weights, branching degrees, and additives. Other known polyamines useful as CO2 adsorbents are polypropyleneamines, Polyglycolamines, polypropyleneamines (vinylamines), and poly(allylamine)s amine), and their derivatives. iii. Non-amino polymer adsorbents should be considered as useful adsorbents. 1. Metal-organic frameworks, covalent organic frameworks, POMs, and others Such materials are useful. 2. Non-polymeric amine sorbents ("Ph-XX-YY"), oligomers. 3. Improvements to the system include high stability (scavenger), activity (copolymer), and adhesion. (PEG), and many others known in the art or to be developed in the future. This can be achieved by the use of a non-adsorbing additive in combination with an adsorbent for the purpose of

[0022] It is understood that contactors constructed from activated adsorbents (e.g., 3D printing) may also be used. More planned.

[0023] analysis Generally, a DAC removal system ("System") consists of a regeneration chamber where each substrate enters the regeneration chamber. before feeding (preferably pre-treated) flue gas into the final stage of CO2 capture. By doing so, the excess FGCO2 from the flue gas per DAC cycle is captured. This captures additional CO2 ("FG CO2"). This increases efficiency on the first floor and increases the amount of CO2 captured during each cycle of the system. The capital investment per metric ton is calculated based on the ratio of pure DAC (without added flue gas) to This is because the amount of FGCO2 in the flue gas compared to the ambient air is reduced by 1 / (1+FGCO2). The effect of the increased concentration of CO2 in the gas varies depending on the type of adsorbent. Also, when processing air containing a small portion of flue gas at each stage, additional equipment is required. The cost of equipment can also be avoided.

[0024] If a combined heat and power plant burns M* (MMbtu) of natural gas per year, it will generate heat and electricity. The amount of energy M produced by the flue is given by M=COGENE×M*. The amount of primary energy released is MF = (1-COGENE) × M*, and the amount of that energy is includes the reaction energy when CO2 is captured and the energy of water when condensed. COGENE is the energy efficiency of the combined heat and power generation unit. Flue gas CO2 emissions , FT CO2 per year is FTCO2 = 0.056M * metric tons / year.

[0025] If the CO2 is captured from the flue gas at the efficiency of the capture ECF, The amount of CO2 captured by these plants is as follows: FGCO2=ECF×FTCO2 The ratio of FCCO2 to captured total air CO2 per year, DACCO2, is This is the same as the ratio per DAC unit per year for the following cases: This means capturing 2 metric tonnes of DACCO. DACCO2=(l / FGCO2)×ECF×FTCO2 Total captured CO2 (TCCCO2) is determined from: TCCO2=(l / FGCO2+-l)×ECF×FTCO 2. The amount of CO2 emitted is (l-ECF)FTCO2. For the entire plant, it is (1 / FGCO The amount of negative carbon is equal to (2+1)×(ECF-1)FTCO2.

[0026] For ECF=0.9 (mixed with a small proportion of flue gas ("carburetor") For air, this is 1.7 FTCO2 (FGCO2 = .S) to -0.8 FTCO2 (FGCO2=1). This means that the amount of FGCO2 entering the system is small. The greater the negative carbon of the plant, the greater the negative carbon of the plant. The larger the ratio, the smaller the reduction in Capex. This is because the proportion of flue gas captured The larger the ratio, the smaller the capital investment, but the larger the negative carbon, the smaller the overall plant. The result is expected to be:

[0027] A combined heat and power unit sized solely to provide heat and electricity for the DAC unit and the CO2 is discharged through a CO2 removal system, and the total energy If the energy (heat and electricity) is, for example, 6 MMbtu per metric ton, the plant The carbon content is (1 ~ 0.9 × 6 × 0.056) minus carbon or about 0.7. This clearly agrees well with the case where FGCO2 is equal to 1. However, in the pure DAC case, No excess power is generated, resulting in higher CAPEX costs per metric ton. This means, for example, that CAPEX is lower and This integrated implementation will be less energy-intensive and more carbon-neutral. The form becomes more favorable.

[0028] The next thing to evaluate is how much less energy is required and therefore which The question is how much extra electricity can be produced per metric ton of DAC produced. Energy required is MDAC per metric ton of flue gas to capture When the required energy is MFG (relative to MFG, the excess sensible heat component in the flue gas component) (assuming there is less heat of reaction to liberate CO2 rather than less heat of reaction) per metric ton The total energy required to capture CO2 is calculated as follows: MT CO2=((1 / FGCO2)×MDAC+MFG) / ((1 / FGCO2}+l }=(MDAC+FGCO2×MFG} / (l+FGCO2} This already saves energy per metric ton compared to DAC. It is being done. MDAC-MTCO2=(MDAC-J\;1FG}FGCO2 / (l+FGCO2}= (SHA+ΔHR}×(FGCO2 / (l+FGCO2}} where SHA is the total sensible heat and ΔHR is the decrease in the heat of reaction of the flue gas components. The amount of electricity used per torton will also decrease.

[0029] Additionally, the array is preheated using flue gas heat to provide half the SHA. If this can be achieved, there is a further reduction of 0.5SHA. Note that this heat is generated from the flue gas stream. Since it is generated and therefore not normally used, it does not reduce the amount of electricity generated and is completely waste heat. be.

[0030] If the SHA is recovered after regeneration, it can be used for example as described in US Patent 9,925,488. As in the two-box system, heat exchange reduces sensible heat by 3 / 4. In principle, it is possible to recover 4. Although it is possible to do this directly using the heat of the flue gas, , increasing temperatures may reduce the excess CO2 captured (again depending on capacity and power (There is a trade-off between the energy efficiency and the energy efficiency.) In some applications, preheating water to the combined heat and power unit is Although low heat including 0.1% by weight may be used, in a highly preferred embodiment, preheating is performed in the final stages of adsorption. As this is done, the best result may be faster playback.

[0031] At this point, it should be noted that there is another degree of freedom in the design of the flue gas stage: The flue gas flow rate and concentration are selected to control the rate at which the product is discharged from the flue gas CO2. Generally, a slower speed will keep the DAC monolith in the same position as a higher CPSI. High density and low velocity are desired to give the appearance of a monolith with 100 CPSI and If the decay exponent is 0.7 at 5 rn / s, then at 1 m / s the decay exponent is 3.5. Another more general feature of the embodiment may be to mitigate capture efficiency from the flue gas stream. However, the overall result is still negative carbon. The efficiency parameters are determined empirically from the velocities and concentrations of the flue gas components being treated. must be determined.

[0032] Therefore, the remaining question is: how to provide the heat necessary to preheat the substrate before regeneration? Whether there is sufficient usable heat in the flue gas stream passing through the contactor. The heat required to preheat the boiler is generated by the condensate and captured from the flue gas stream. The heat of reaction of the CO2 introduced and the sensible heat of the flue gas stream can be provided as follows: a. THF = total heat in flue gas = SHF + condensation of water vapor (HFCW) in the flue gas stream CO2( per metric ton of CO2 captured at the last station before heat + regeneration HFRC) reaction heat

[0033] A very rough estimate of whether there is enough heat is to calculate the SHA as 1 meter of CO2. Assuming 2MM BTU per ton, the overall heat required is 1 meter of CO2. 6MM BTU is about 30% of the energy released when burned per Torton. Assume that: a.CO2 capture accounts for only up to half of the total CO2 captured, due to the low heat of reaction , not much will be added. b. SHF = sensible heat in flue gas per metric ton of CO2 captured = (1-C COGENE)M*. If it is in the 70% range of COGENE, 30% goes up the flue. Here, 1 / 4 of that heat is available (by cooling from 200°C to 50°C). This may be about half what is needed.

[0034] However, the available water vapor in the flue gas input to the final CO2 capture stage The latent heat from the CO2 capture unit is sufficient to preheat it before it enters the regeneration box. Therefore, in another preferred embodiment, the hot flue gas is Evaporate the water to a final temperature, say 60°C, with a delta T higher (say 70°C). However, the water vapor content of the flue gas is high, and The material ("SA") contained more water vapor than the amount of latent heat required to raise its temperature to 60°C. Note that in this case, preheating is done for 90 seconds. The speed is assumed to be 1 m per second, and the flue Gases generally contain at least about 10% water, which is the pure water content of a gas at 300 cm per second for 30 seconds. This corresponds to a cool steam input. This is obviously excessive. However, The excess water produced can be used in places like the southwestern United States or the desert regions of Africa or Asia. This would be a valuable by-product in places such as desert regions where water is expensive. When entering the raw box, the pressure is reduced to 0.2 bar without significant cooling of the regenerator box. In fact, further reduction in pressure can result in even greater cooling. Although the flue gas can be cooled, water vapor can be used to flush out the trapped flue gas.

[0035] Once sealed in the regeneration box, the adsorbent is treated, e.g., by heating with steam. The CO2 is removed from the adsorbent and the adsorbent is regenerated. The capture structure with the regenerated adsorbent is then sealed and The trapping structure moves from the captured box until it is in position to move into the next regenerating box. and travels along the track with other capture structures to absorb more CO2. In the stripping / reclaiming position, the capture structure is mounted on a bore located above or below the grade of the track. The capture structure can be moved into the box or placed at the same grade level as the truck. A box may be positioned to move into the trapping structure and form a seal with it. Some alternatives are further defined below and illustrated in the accompanying drawings.

[0036] In instances where the regeneration box is down or uphill, the system will raise or lower the capture structure. The playback box must have a subsystem for descending the track. In systems with seals along the sides and along the top and / or bottom A satisfactory sealing arrangement is required to provide it.

[0037] CO2 adsorption and removal process The main premise of this treatment is to purify air or a mixture of air and exhaust gas, preferably at room temperature or By passing it through an adsorbent bed in a similar state, CO2 can be absorbed from the atmosphere. Once the CO2 is adsorbed onto the adsorbent, it must be captured and the adsorbent regenerated. The latter step involves heating the absorbent with steam in a sealed containment box to release the CO2. This can be done by releasing CO2 and regenerating the adsorbent. The adsorbent is then re-adsorbed from the atmosphere as it leaves the regeneration box. It is available for

[0038] Most commercially available adsorbents are easily decomposed when exposed to air above a certain temperature. Therefore, in many cases, the adsorbent on the substrate is The capture structure must be cooled before it leaves the regeneration box and is returned to the air stream.

[0039] In another preferred embodiment of the process of the present invention, preferably any particulate solid or liquid The flue gas in purified form after removing any gaseous material toxic to the material and adsorbent is captured The structure is flowed through the capture structure just prior to entering the regeneration chamber. The treatment step is preferably carried out in a closed chamber, so that the The pretreated flue gas is prevented from escaping into the environment before passing through the major surface of the porous substrate. I can't.

[0040] In general, the time required for CO2 adsorption from ambient air is longer than that from flue gas. The CO2 concentration is much higher. With the current generation of sorbents, this difference is The time required for extraction and adsorbent regeneration is roughly 10 times shorter when treating ambient air. Therefore, based on the use of polyethyleneimine adsorbent, A system having two capture structures and a single playback unit is provided for each rotation system. If the performance of the adsorbent improves over time, The ratio between attachment time and desorption time, and therefore the number of capture structures required in the system, may be reduced. There is a possibility.

[0041] In particular, when higher loading adsorbent embodiments are used, adsorption times of 1 hour are performed. It is possible, therefore, to accommodate only five capture structures, one playback box is required. In addition, the relative treatment time depends on the concentration of CO2 in the treated gas mixture. The higher the CO2 content, the shorter the adsorption time relative to the regeneration time. The waste ("flue gas") is mixed with the surrounding air through a gas mixer, or "carburetor." By combining, the mixture has a significantly higher CO2 concentration than air, but the pure flue gas It has a significantly lower concentration than gas.

[0042] To ensure more complete removal of CO2 from the flue gas, the 9th stage immediately before regeneration The waste from the last stage is returned to the second chamber. It is returned to the previous stage, ie, the eighth stage of the capture structure's adsorption cycle.

[0043] In all of the above embodiments, the process of the present invention is carried out at low temperatures (i.e., ambient temperature, 100 °C or less) remains a batch process, with unidirectional mass transport at each stage of the process.

[0044] At least the first 7 stages of the adsorption cycle and the regeneration cycle in a sealed box Chemical and physical activity within the capture structure and between the capture structure and the re- The raw chamber mechanism is described in U.S. Patents 10,413,866 and 10,512,880. The disclosures of these patents are incorporated herein by reference. as if fully recited herein, as modified by any new disclosures made therein. In a system according to the invention, each rotating system includes a rotating capture structure. One sealed regeneration box is provided for each group of capture structures. The number of capture structures is determined by the desired adsorption and and the relative times to achieve the desired regeneration. The two rotating capture structures allow for the interaction of the playboxes. , two of the rotating systems are spatially related and temporally operated in the appropriate relationship. It has been found that greater efficiency and lower costs can be achieved by By offsetting the time you enter in the playback box, the playback will occur in the first box. As a result, the second one is preheated with the remaining heat from the first one and enters the regeneration box. The regenerated capture structure is efficiently cooled before returning to its adsorption cycle on the rotating track. It is also possible to do so.

[0045] This interaction between the regenerative boxes, in accordance with the present invention, reduces the pressure in the first box system to This is achieved by lowering the CO2 remaining in the first box after the release. The steam and water vaporize and the system cools to the saturation temperature of the steam at its reduced partial pressure. Additionally, as described below, the heat released in this process is absorbed by a second sorbent capture structure. It is used to preheat the structure, resulting in approximately 50% sensible heat recovery and energy savings. This concept has a beneficial effect on the use of ghee and water. Adsorbents with low oxygen sensitivity can be used at higher temperatures, resulting in improved performance. This will improve over time. At least in the final stage just before the playback box. In some cases, the direct flue gas injection in one or more previous stages is highly concentrated, resulting in adsorption. The concentration of CO2 adsorbed by the adsorbent increases, and due to the exothermic nature of the adsorption reaction, the adsorbent and substrate It will be appreciated that this will result in higher temperatures, which is why it is more cost-effective to treat only ambient air. When mixing with a small proportion of flue gas, the pressure in the regenerator chamber is increased to the required level. Accordingly, it is possible to avoid the need to draw down to a vacuum.

[0046] As discussed in the prior patent, the adsorbent trapping step avoids deactivation by atmospheric oxygen. The structure is preferably cooled before being exposed to air. As described in No. 0, among polyamines, poly(allylamine) and poly(biphenylamine) are Adsorbents with greater resistance to thermal decomposition, such as methylamine, and their derivatives If necessary, the system pressure can be reduced in the regeneration box to allow steam Cooling can be achieved by lowering the gas saturation temperature. Lowering the temperature has been shown to be effective in eliminating the adsorbent deactivation problem. As a result, a significant amount of energy is released from the first capture structure as it cools during the depressurization step. The CO2-containing substrate that has completed the CO2 adsorption stage is input into the second regeneration box. Each time, the adsorbent needs to be heated to release the CO2 and regenerate it. This can be supplied solely by atmospheric steam fed to the regeneration box, but this In order to minimize this operating cost, the two-bed design concept This concept was developed using the method described in U.S. Patent No. 10,512,880. As shown in the figure, the system pressure (and therefore the steam saturation temperature) in the first regeneration box is lowered. The heat removed from the first regeneration box, which is cooled by lowering the It is used to at least partially preheat the CO2-containing substrate that is regenerated in the raw box. Therefore, steam usage is calculated by using heat from the cooling of the first box to raise the temperature of the second box. The remaining heat load of the second box is preferably reduced by increasing the This is achieved by adding steam under pressure. This process is carried out by passing the water through two regeneration boxes. Repeating this for other rotating capture structures will significantly improve the thermal efficiency of the system. .

[0047] Some of the acronyms above may be defined as follows: FG-CO2 = captured air per cycle where FG-CO2 is flue gas CO2 captured CO2 ratio DA. CO2 = Amount of air CO2 captured per cycle FGCAPEX = Flue gas operating expenses in a pure carburetor embodiment, i.e. That is, if a mixture of ambient air and flue gas is supplied to each capture structure, M*=MMBT Total natural gas burned in u M = usable heat and generated electricity COGENE = Combined Heat and Power Efficiency = M / M* FGCCO2 = Flue gas CO2 captured per year DACCO2 = Air CO2 captured per year FTCO2 = Total flue gas CO2 produced by burning J\11 * natural gas MTCO2 = Total CO2 captured per year = Smoke captured per year Total CO2 from road gas and air ECF = flue gas capture efficiency MDAC = Energy per metric ton of captured air CO2 MFG = energy per metric ton of captured flue gas CO2 SHA = Sensible Heat of Monolith Array Delta HR = difference in heat of reaction between the DAC CO2 site and the flue gas CO2 site THF = Total heat source in flue gas steam - sensible heat + CO2 reaction heat + water condensation heat - (heat value of natural gas) (Note that is not constant.)

[0048] These and other features of the present invention are set forth in the following detailed description and accompanying drawings. or is evident from them. [Brief explanation of the drawings]

[0049] [Figure 1] FIG. 1 is a schematic top view of a pair of rotating multi-capture structure systems interacting to remove carbon dioxide from the atmosphere, according to an exemplary embodiment of the present invention, showing graded-level regenerative chambers for each loop and each group of capture structures, with the two capture structures shown within a hermetic housing immediately upstream of each of the regenerative chambers, and the hermetic housing including a hermetic conduit for supplying purified flue gas to the capture structures.

[0050] [Figure 2] FIG. 2 is a schematic diagram of a pair of regeneration chambers for removing carbon dioxide from the capture structure of FIG. 1, showing several inlet and outlet conduits connected to one of the chambers, as well as a hermetically sealed connecting conduit connecting the two chambers.

[0051] [Figure 3] FIG. 1 is a schematic diagram of the regenerative chambers and flue gas capture structures on each of the adjacent loops, showing the piping system configuration for each chamber and between the chambers.

[0052] [Figure 4] 10A-10C are schematic elevation views showing fans that are relatively stationary and rotate with each capture structure, respectively;

[0053] [Figure 5] FIG. 5 is a schematic side view of the dual-induction axial fan and plenum design of FIG.

[0054] [Figure 6] FIG. 1 is a schematic elevation view of one of an interacting pair of rotating multi-capture structure systems showing a truck-level regeneration chamber for removing carbon dioxide from the atmosphere and two immediately preceding capture structure housings for processing the flue gas stream for CO2 capture.

[0055] [Figure 7] FIG. 1 is a conceptual diagram showing the general operation of this system between the final adsorption stage and the CO2 desorption regeneration step, showing a system in which all of the adsorption stages treat ambient air.

[0056] [Figure 8] FIG. 1 is a conceptual diagram illustrating the general operation between the final adsorption flue gas stage and the CO2 desorption regeneration step in one of the preferred embodiments of the present invention of the system, in which the final adsorption stage immediately upstream of the "desorption unit", e.g., stage 9, receives flue gas either pure or mixed with ambient air, and the next preceding stage, e.g., stage 8, can receive exhaust from stage 9, a mixture of that exhaust and ambient air, or just ambient air, depending on the composition of the stage 9 exhaust.

[0057] [Figure 9] FIG. 1 is a conceptual diagram illustrating the general operation between the final adsorption mixed air flue gas stage and the CO2 desorption and regeneration steps in another preferred embodiment of the present invention of the system, in which the final adsorption stage, e.g., stage 9, immediately upstream of the "desorption unit," receives flue gas mixed with ambient air.

[0058] [Figure 10] FIG. 1 shows an example of a seal extending around all sides of each capture unit within the desorption unit or within one of the flue gas adsorption unit housings as each of the housings is at a graded level and each capture structure moves along the track to enter each housing. DETAILED DESCRIPTION OF THE INVENTION

[0059] A more detailed description of this embodiment of the invention A simplified depiction of the design of a system that performs these operations described above is shown in Figures 1-6. A detailed description of the operation and auxiliary equipment required is provided below and is shared with The same is shown in U.S. Pat. Nos. 10,413,866 and 10,512,880. It is similar to the above.

[0060] In this embodiment, there are ten "capture structures." The capture structures are arranged in a decagonal configuration. Preferably, the tracks are arranged on a substantially circular or arcuate track, but There are two substantially circular (or oval) / decagonal shapes associated with each processing unit. assemblies are present and they interact as shown. In this preferred embodiment Air is forced through the capture structure by an induced draft fan located inside the capture structure. At one location, the capture structure captures the material as it moves along the track for processing. Each capture structure is located adjacent to a single sealed chamber box into which it is inserted. In a typical regenerative chamber box, they are kept below 130°C, more preferably below 120°C, Optimally, it is heated to a temperature below 100°C, preferably with hot steam, to remove CO2 from the adsorbent. Alternatively, the regeneration chamber may be located above or below the gradient. In this embodiment, the time for CO2 adsorption by the capture structure can be determined by the adsorbent regeneration time. Preferably, the growth time is 10 times longer.

[0061] It is preferred to use a porous monolithic substrate in the capture structure, but if possible For example, porous particles supported in a frame on a capture structure, i.e., a static bed of granular material. It should be understood that a particle capture structure carrying an adsorbent may also be used. If the porous substrate has the same pore volume as the monolith capture structure for CO2, the mesh for CO2 It is preferable to support an ion adsorbent.

[0062] The schematic diagrams show the basic operating concepts of the system according to the present invention. 1 mounted in a decagonal assembly configuration and movably supported on circular tracks 31, 33. There are 0 "capture structures" 21, 22. Two circles associated with each processing unit There are two shaped / decagonal assemblies, A and B, which interact with each other. Air or flue The gas is blown through induced draft fans 23, 26 located radially inward of each of the decagonal assemblies. and passes through each of the capture structures 21, 22 and is removed from the system from the inner circumferential surface of each capture structure. Inducing a flow of exhaust gases away from the track 31, 33. The capture structures 21, 22 are adjacent to hermetic regeneration boxes 25, 27, and the capture structures 22, 22 completes one rotation around the track and then is inserted into it for playback processing. It will be entered.

[0063] Therefore, as shown in Figures 1 and 2, the first capture structure 21 is The object is rotated to a position within the playback box 25. This is because the playback box 25 is on a slope. When the capture structure is in position within the playback box 25, movement along the track Alternatively, the diameter of the track and the catch structure may be increased. By increasing the size of the regeneration box and optional flue gas adsorption housing (12 1, 221, 122, 222) by having a suitable sealing system on The capture structures 21 and 22 are regenerated and all of the capture structures move. When the regenerated capture structure is removed from the regeneration box 25, 27, as shown in FIG. , so that the next capture structure 21, 22 can be moved after processing the flue gas. The process is repeated substantially continuously. In the preferred embodiment shown in the drawings, One or more of the capture structures on the rack are flue gas adsorption housings (121, 221, 122, 2 22), the timing of which should preferably coincide with the timing of flue gas desorption. Alternatively, the capture structure may comprise a regeneration box and one or more flue gas adsorption housings (e.g., 121, 221, 122, 222), the movement of the capture structure can be stopped. Transfer is then resumed once desorption and flue gas adsorption are complete.

[0064] However, as explained above, the present process invention is suitable for use at low temperatures (preferably ambient to 1 00°C) with unidirectional mass transport during each phase of the process. In a further novel aspect of the present invention, the reaction of capturing CO from a gas mixture is carried out using an amino polymer In one preferred embodiment above) is generated from renewable materials, e.g., amino This preferably occurs with the polymeric adsorbent impregnated within the porous substrate.

[0065] In a preferred embodiment, the adsorbent-carrying capture structures are formed by a frame for forming each capture structure. The substrate includes a monolithic substrate that is in turn supported by a framework.

[0066] The two decagonal ring assemblies operate relative to each other, but the capture structure for each decagonal ring Bodies enter and exit their detachment / regeneration boxes at slightly different times, as explained below. This allows, for example, when playback in box 25 is completed, Heat is passed between box 25 and box 27 to heat the other box, e.g., a regeneration box. This allows preheating of the refrigerant 27. This saves heat at the start of regeneration and reduces the amount of heat required after regeneration. Reduces the cooling costs of the capture structure.

[0067] The location of the regeneration boxes 25, 27 is a rotating capture structure that does not allow continuous movement. Three positions are available: above or below the body, or at a slope level. See US Pat. Nos. 13,866 and 10,512,880.

[0068] The regeneration chambers 321, 327 are mounted on the slope of the rotating capture structure assembly. The box is also installed on a slope with adequate access for maintenance and process piping. Suitable mutual sealing surfaces are provided on the box and on each capture structure, which When the capture structure moves into position within the box, the moving regeneration box is raised. Up into the play box, or down into the play box below the slope. box 322, whether it is a straight run to a play box on a slope, 327 is sealed. The flue gas adsorption housing (121, 221, 122, 222) is The same is true for embodiments that may be below or above the distribution or gradient. along the track to feed the gas or partially scrubbed flue gas into the capture structure. There is also an optional closed chamber for the position just before the

[0069] In all cases, auxiliary equipment (pumps, control systems, etc.) must be installed on the rotating capture structure assembly. Preferably, the assembly 29 is installed on a slope within the circumference of the track that supports it or on the outside. .

[0070] The playback box and housing may be specifically configured without departing from the concept or scope of the present invention. It may be installed at different levels in certain situations.

[0071] An alternative design within the scope of the present invention is to provide a pair of regenerative chambers 25 in the track. This provides a system that allows the playback box 25 to move along the track. The track design requires reciprocating movement by capture structures along a straight track to prevent separation into enclosures. In comparison with existing disclosed devices in the prior art, This is as follows: Minimize structural steel. All major equipment is placed at grade level, except for the regeneration box, which acts only as a containment vessel. do. If the box is at a different level to the track, ensure that the air flow to the capture structure is blocked. Don't let them interfere. A larger version that rotates all of the capture structures and moves them into the playback box. Prevents movement of multi-unit systems. To allow for desirable heat exchange for increased efficiency, a minimum of two regenerator boxes are used. It is possible to place them adjacent to each other with a gap of .

[0072] Mechanical operations with required machinery and power include: Two sets of capture structure assemblies are rotated around a substantially circular track on a support structure. and accurately positioning the component until the capture structure is stopped. Reliable and free movement in and out of the regeneration box and any flue gas adsorption housing do. Remove only the capture structure or the substrate, insert the capture structure into the regeneration box, and Remove the body from the playback box and reinsert the capture structure into its position on the track assembly. All of these movements are vertical, or alternatively horizontal, rotational movements on the track. The capture structure and the regeneration box are designed for a vertically movable capture structure. and forming a substantially airtight seal between the top or bottom of each of the capture structures and the support structure of the box. Such regeneration boxes or flue gas adsorption housings are designed to have a seal. For a gradient of the ring, the seals can be on the sides as well as on the top and bottom. A sealed door that closes when the structure moves into the regeneration box or flue gas absorption housing Examples of several conceptual designs for such seals are available in previously published U.S. This is shown in Figure 10 of the Isenberger patent and this application.

[0073] In all cases, in one preferred embodiment, and with reference to FIGS. 1-9, capture structure 2 1-1 (Ring A) is rotated into position and then regenerated or detached for processing. It is moved to box 25. Desorption box (containing capture structure 21-1, ring A) The pressure in 25 is reduced to below 0.2 bar, for example, using a vacuum pump 230 Box 25 is heated with steam at atmospheric pressure via line 235. CO2 is generated from 21-1, and CO2 and condensate are separated on condenser 240. The wastewater is then removed from the wastewater box 25 via the outlet pipe 237 (Fig. SA). As shown in Figure 5B, while box 25 is being processed, capture structure 22-1 (ring B) is placed in box 27 (ring B). The steam supply to box 25 is stopped and CO Box 25 and box 27 are connecting pipes. The connection is made by opening valve 126 in 125 (Fig. SC).

[0074] The pressure in box 27 is reduced using a vacuum pump 330 associated with box 27. This reduces the system pressure in both boxes, causing the The remaining steam and inert elements are drawn through box 27 and then into a vacuum pump. This allows the box 25 (and therefore the capture structure 21-1, Cooling the gas (bag A) to a lower temperature (i.e., the saturation temperature at the partial pressure of the vapor in the box) This reduces the possibility of oxygen deactivation of the sorbent when the capture structure 21-1 is placed back into the air stream. This process also reduces the likelihood of the trapping structure 22-1 being trapped in box 27 (and therefore trapped in trapping structure 22-1). , ring B) is preheated from ambient temperature to saturation temperature by partial pressure of steam in box 250. Thus, energy is recovered and transported to the second box 27 (capture structure 22-1 ring B The amount of atmospheric pressure steam required to heat the boiler is reduced (Fig. SD). When the pressure in boxes 25 and 27 is reduced, the temperature in the first box 25 (approximately The temperature of the second box 27 drops (from 100°C to some intermediate temperature) and The CO2 and inert gas are pumped to a vacuum pump 330. Thus, it is removed from the system.

[0075] The valve between the first box 25 and the second box 27 is closed, and the boxes are The capture structure 21-1 ring A is placed back into the airflow. When the adsorbent is cooled, it is cooled to a temperature below the temperature at which oxygen deactivation of the adsorbent is a concern. The box 27 and the capture structure 22-1, ring B are preheated, so the box and The amount of steam required to heat the trapping structure is reduced (Fig. 5E). Structure 21-1 Ring A is moved into the capture structure assembly. Ring A capture structure assembly The assembly is rotated by one capture structure, and then capture structure 21-2 ring A is , and inserted into box 25, which is ready for preheating. Box 27 is heated by atmospheric steam. The separated CO2 is collected (Figure 5F).

[0076] Once the second box 27 (containing the capture structure 22-1 ring B) is fully regenerated, The steam supply to Box B is isolated, and the CO2 and condensate lines are connected to valves 241 and 242. The valve 126 between the first box 25 and the second box 27 is opened. The pressure in boxes 25 and 27 is released by the vacuum pump 230 system for box 25. The second box 27 (hence the capture structure 22-1, ring B) The temperature of the first (capture structure 21-2, housing ring A) decreases (see 5 above). The temperature of the box 25 increases (see point 5 above) (FIG. 5G). The pressure in boxes 25 and 27 is reduced. The temperature of box 25 (approximately 100°C) The temperature of box 27 drops (from ambient temperature to the same intermediate temperature). The CO2 and inert gases are removed from the system by the vacuum pump 230. The capture structure 22-1, ring B, is placed back into the ring assembly, and the assembly is assembled. The bed is then rotated. Then, the capture structure 22-2, ring B, is inserted into the box 27. The box 25 (containing the capture structure 21-2 ring A) is heated with atmospheric steam. The CO2 is released to regenerate the adsorbent (Fig. 5H). Next, preheating of box 27 is performed as described above. This process is repeated for all beds as the decagon is rotated multiple times. .

[0077] Both rings are equipped with a pair of flue gas adsorption housings just before the input to the regeneration box. , when dealing with the preferred embodiment shown in FIG. 8, a supply of preferably pre-treated flue gas For example, the ninth adsorption stage just before the regeneration box typically provides about 10-15% Pre-treated flue gas with CO2 or pre-treated flue gas with ambient air The exhaust from that stage contains, for example, 2-8% CO2. Preferably, when CO2 in the upper range is emitted, most preferably The exhaust gas is further adsorbed through the housing of the previous desorption stage, and the exhaust gas is released into the atmosphere. The amount of heat generated is reduced to a level suitable for the purpose.

[0078] Preferred Design Parameters The currently preferred basic principles for system design are as follows: Weight of each capture structure to be moved: 1,500 to 10,000 lbs. (including support structure) Approximate bed size: Width: 5-6 meters Height: 9-10 meters Depth: 0.15 to 1 meter

[0079] The size of the capture structure will depend on the specific conditions and desired geographic location of each pair of the system. , i.e., can be adjusted depending on the achievable processing parameters.

[0080] For a system with 10 capture structures in each of the decagonal rings, a preferred circular / The outer diameter of the decagonal structure is approximately 15 to 17 meters, preferably approximately 16.5 meters. The capture structure support structure is attached to the truck by, for example, an electric motor and drive wheels. Alternatively, the support structure may be driven at a specific position along the track. , and is used to drive the track and all structures around the closed loop It may be fixed to a single large motor. In either case, the regeneration box must be in one location. When the structure is placed and one of the support structures is installed to be moved into the regeneration box, All of the structures can stop their movement. A single drive motor or engine Alternatively, the economy of multiple drive motors or engines may be realized by reducing the space and drive to electric motors. This can be achieved by a variety of methods, such as by a gas turbine or by some fuel-driven engines. The nature of the drive unit itself is not a primary feature of the present invention, and many Examples of suitable engines are those using the Stirling engine cycle, for example. internal or external combustion engines or gas-powered engines, process steam engines, or includes hydraulic or pneumatic engines.

[0081] If the playback box is installed above the track level, the top should be approximately 2 meters above the track level. 0 meters above the track. If the playback box is installed below the track gradient, The top of the box is just below the gradient of the track. The box above the gradient will The capture structure is positioned at a minimum height above the top of the capture structure to fully contain the capture structure within the chamber. can be.

[0082] To move the capture structure in and out of the regeneration box if the regeneration box is not on grade. The lifting system is configured to lift the ball within a period of 30 to 20 seconds, preferably within a period of 30 to 45 seconds. The shorter the period, the more the processing parameters can be adjusted. Moving large capture structures requires certain inherent mechanical It is recognized that there are limitations. One advantage of having the regeneration box on a slope is that it The capture structure rotates into the box as part of the rotational motion. Simply seal it away, avoiding vertical travel, lost time and additional capital costs for elevators In both cases, the two edges of the capture structure are solid, and the edges of the regeneration box Form a seal with the seal. [Prior art documents] [Patent documents]

[0083] [Patent Document 1] U.S. Patent Application No. 13 / 098,370 (now U.S. Patent Application No. 8,500,855) [Patent Document 2] U.S. Patent Application No. 9,925,488

Claims

1. 1. A system for removing carbon dioxide from a carbon dioxide-containing gas mixture, comprising: a carbon dioxide removal structure, each removal structure in each group being supported on said structure by a porous Each porous substrate has an adsorbent supported within its pores, and the adsorbent is Removing carbon dioxide from a gas mixture by adsorbing or binding carbon dioxide. a group of carbon dioxide removal structures and an infinite loop for said group of said removal structures; an endless loop support, the endless loop support being exposed to a flow of a carbon dioxide-containing gas mixture; and an infinite number of groups of the removal structures arranged to allow movement of the removal structures of each group along a closed curve. A loop support and a removal structure can be sealingly installed along the endless loop support. A single-position sealed regeneration box with a removal structure in place therein. When sealed, the carbon dioxide adsorbed by the adsorbent is stripped from the adsorbent and captured. and a sealed regeneration box in which the adsorbent is regenerated, and the adsorbent is CO from the gas mixture ２ and exposing the mixture to a flow of a carbon dioxide-containing gas mixture to allow removal of Each of the removal structures supports the porous substrate and the regeneration box in a position such that the porous substrate is The number of removal structures relative to the number of gases (CO) removed from the gas mixture ２ (for removing Adsorption time (the amount of CO released from the adsorbent on the porous substrate) ２ (for peeling) regeneration time and The adsorption time is directly determined by the ratio of CO ２ is the time it takes for the adsorbent to adsorb from its base level to a desired level, and the regeneration time continues to increase the CO2 concentration until the desired level on the adsorbent is restored to the base level. ２ Peeled off the system exposes the first chamber at a location along the track. wherein the first chamber encloses each capture structure moving along the track. It is designed to accommodate The first chamber contains CO ２ Inlet designed to be connected to a source of contained flue gas a mouth and the CO ２ CO after at least a portion of the ２ Purification flue and an outlet for the gas.

2. 10. The system of claim 1, wherein the first chamber is located immediately adjacent to the regeneration box. Stem.

3. When the flue gas flows into the first chamber, the first chamber 10. The system of claim 1, wherein the system is designed to seal the capture structure within a single chamber. Hmm.

4. A seal is provided inside the first chamber and a seal is provided outside each of the capture structures. and a seal combination configured to separate the flue gas from the The capture structure within the first chamber is sealed to prevent leakage from within the first chamber. The system of claim 1 , wherein the system is designed to seal.

5. a second chamber at a location along the track upstream of the first chamber; 、 The second chamber moves along the track before entering the first chamber.

10. The system of claim 1, wherein the system is designed to hermetically house each capture structure. 。

6. to connect the outlet from the first chamber to the inlet to the second chamber. a capture structure in the second chamber configured to capture the first Any CO emitted from the chamber ２ Designed to be exposed to purified flue gases, claims Item 6. The system according to item 5.

7. Each carbon dioxide removal structure in the second group, each respective removal structure in each group The body comprises a porous solid substrate supported on the removal structure, each porous substrate having a pore therein. The adsorbent is supported on the carrier, and the adsorbent adsorbs or binds carbon dioxide. a second group of carbon dioxide removal structures capable of removing carbon dioxide from a gas mixture; and, a second endless loop support for the second group of removal structures, the second An infinite loop support controls the movement of each removal structure of the second group along a closed curve. a second endless loop support and one removal structure arranged to allow sealing A second hermetic regeneration may be arranged at a location along each of the endless loop supports. a box, wherein one removal structure is sealed in place therein to the adsorbent; The adsorbed carbon dioxide is stripped and captured from the adsorbent, and the adsorbent is regenerated. and a second hermetic recycling box, wherein the hermetic recycling box is a sealed conduit connecting the regeneration box to a source of treatment steam, each of said second group of removal structures connected to an exhaust pump for removing gas from said gas supply; At least one major surface of the substrate is exposed to a flow of a carbon dioxide-containing gas mixture; The opposite major surface of the substrate is directly exposed to the atmosphere, and the adsorbent is When exposed to a flow of the mixture, CO ２ The regeneration box can be removed. a porous substrate supported at a location along the closed loop support outside the regeneration box; the number of removal structures relative to the number of CO ２ adsorption (to remove time (from the adsorbent on the porous substrate to CO ２ Ratio of regeneration time (to peel off) and the adsorption time is determined directly by the amount of CO removed from the gas mixture onto the adsorbent. ２ of, the time it takes for the adsorbent to adsorb from its base level to a desired level, and the regeneration time is until the desired level on the adsorbent is returned to the base level. ２ Peel off The system of claim 1 , wherein the time is time.

8. 8. The system of claim 7, wherein the two groups of carbon dioxide removal structures are substantially identical to each other. Tem.

9. After each recycling box and removal structure is sealed within the recycling box, a sealed fluid connection between the exhaust pump and the drying box for reducing the atmospheric pressure; a sealing between each of the regeneration boxes and a source of process hot steam for each regeneration box; Fluid connections and each regeneration box and CO ２ a sealed fluid connection between the collection chamber and the Furthermore, The rotational movement of each of the two groups of carbon dioxide removal structures is After the regeneration of the carbon dioxide removal structure is started, the other carbon dioxide removal structure of the regeneration box 9. The system of claim 8, wherein the input structure is offset to input.

10. The system of claim 9 , wherein the adsorbent is a polymeric amine.

11. 1. A method for removing carbon dioxide from a carbon dioxide-containing gas mixture, comprising: A group of diacids is introduced into the closed infinite loop while being exposed to a flow of the gaseous mixture. and moving the carbon dioxide removal structures such that each removal structure in the group is positioned on the structure. a plurality of supported porous solid substrates, each of the porous substrates having an adsorbent supported within its pores; The adsorbent adsorbs or binds carbon dioxide to the gas mixture during the adsorption period. It can remove carbon dioxide from the object, and one removal structure can remove it. When the adsorbent is sealed in place, the carbon dioxide adsorbed in the adsorbent The infinite loop is then set up so that the adsorbent is regenerated during the regeneration period. A carbon dioxide removal structure is sealingly positioned within the regeneration box at one location along the loop support. and a removal structure supporting the porous substrate on the closed infinite loop. each of which is configured to separate the gas mixture except when the removal structure is disposed within the regeneration box. CO from materials ２ The adsorbent is adapted to adsorb carbon dioxide containing gas mixtures so as to enable the removal of the removal structure is located within the regeneration box so as to be continuously exposed to the Once placed in the adsorbent, the adsorbent is exposed to processing heat at a temperature of less than 130°C to remove HCl from the adsorbent. The CO ２ are peeled off, and the number of the removal structures relative to the number of the regeneration boxes is The adsorption time is directly determined by the ratio of the adsorption time to the regeneration time. the carbon dioxide-containing gas mixture on the adsorbent while the adsorbent is exposed to the flow of the carbon dioxide-containing gas mixture. et al. CO ２ is the time it takes for the adsorbent to adsorb from a base level to a desired level, The regeneration time is the time required to reach the desired level on the adsorbent while each structure is in the regeneration box. CO on the adsorbent until the level returns to the base level. ２ is the time to adsorb The method includes: discharging CO into a first chamber located along the track; ２ Flue gas content wherein the first chamber flows into each capture chamber moving along the track. The adsorbent in the porous substrate on the capture structure is adsorbing and removing carbon dioxide from the flue gas during the Before moving the capture structure from the first chamber along the rack, From the chamber to the CO ２ passing the purified flue gas.

12. 12. The method of claim 11, wherein the first chamber is located immediately adjacent to the regeneration box. method.

13. a second chamber located along the track upstream of the first chamber; Established, The second chamber moves along the track before entering the first chamber.

13. The method of claim 12, wherein each capture structure is hermetically enclosed.

14. connecting the outlet from the first chamber and the inlet to the second chamber; a conduit designed to connect the capture structure in the second chamber to the first chamber; Any CO emitted from the chamber ２ 10. The method of claim 1, further comprising exposing the system to purified flue gas.

3. The method according to claim 3.

15. A second group of removal structures and a second moving endless loop for supporting said second group are provided. each of which moves around said second closed infinite loop, and each The removal structures include a porous solid substrate supported on each of said removal structures, and each porous substrate The adsorbent is supported in the pores, and the adsorbent adsorbs or absorbs carbon dioxide. and During the adsorption period, each carbon dioxide removal structure is passed through the carbon dioxide-containing gas mixture. removing carbon dioxide from the gas mixture by exposing the gas mixture to a flow of CO from materials ２ The adsorbent is adapted to adsorb carbon dioxide containing gas mixtures so as to enable removal of carbon dioxide. supporting said porous substrate on each of said closed infinite loops in a position such that said porous substrate is exposed to a low each of the removal structures is configured to remove; providing a playback box adjacent to each loop in one location; At one location along each of the endless loop supports, and sealingly placing the respective ones of the above in a regeneration box. When one removal structure is sealed in place therein, the adsorbed material on the adsorbent Carbon dioxide is stripped from the adsorbent and captured, and the adsorbent is regenerated. During the regeneration time, the adsorbent is applied to each removal structure sealed in each regeneration box for 130 minutes. CO ２ and stripping the adsorbent from the adsorbent, The number of removal boxes provided in each loop is compared to the number of playback boxes provided adjacent to each loop. The number of structures is directly proportional to the ratio of the adsorption time to the regeneration time, and and the adsorption time is the time required to remove CO from the gas mixture on the adsorbent. ２ a base on the adsorbent the regeneration time is the time it takes for the adsorbent to adsorb from the desired level to the desired level, and The CO2 on the adsorbent is then cooled to the desired level until it returns to the base level. ２ It's time to peel off the Item 13. The method according to item 12.

16. After the removal structure is sealed in the regeneration box, the atmosphere in each sealed regeneration box is 16. The method of claim 15, further comprising reducing the pressure.

17. After the atmospheric pressure in the regeneration box is reduced, the treated hot steam is passed through the regeneration box. and filtering the CO ２ and removing the removed CO ２ from the playback box to C O ２ 17. The method of claim 16, further comprising passing the solution into a collection chamber.

18. one of the two groups of carbon dioxide removal structures has an adjacent first regeneration box; The other of the two groups of carbon dioxide removal structures has an adjacent second regeneration box, The method further comprises: after the regeneration of the carbon dioxide removal structure has begun in the first regeneration box, The carbon dioxide removal structure is connected to the second regeneration box. offsetting the rotational movements of each of the two groups of carbon dioxide removal structures; reducing the atmospheric pressure in the other regeneration box to a preset pressure; The two regeneration boxes are then regenerated after the designated regeneration of the removal structure in the first regeneration box is completed. The sealed connection between the first and second regeneration boxes is opened, and the remaining steam in the first regeneration box is drawn out. and preheating the second regeneration box by removing the removal structure in the first regeneration box. and removing the cooled removal structure from the first regeneration box to the infinite loop. and the removal structure moves around the endless loop and removes the regeneration box. and continuing this cycle by periodically re-entering the 9. The method according to claim 9.

19. The process heat is added to the regeneration box in the form of process heat steam, and each of the regeneration boxes When regeneration is completed in each box, the steam remains in that box and the atmospheric pressure in the other boxes to a preset pressure; and After the designated regeneration is completed, open the sealed connection between the two regeneration boxes. The remaining steam in the first regeneration box is extracted to prepare the second regeneration box. heating and cooling the removal structure in the first regeneration box; removing the removal structure from the first playback box back onto the infinite loop; The structure moves around the infinite loop and cyclically re-enters the playback box. and continuing the cycle.

20. The process hot steam enters each regeneration box at a temperature of about 120° C. or less, and the second regeneration The box is preheated to a temperature of about 60° C. or less, and the first regeneration box is 20. The method of claim 19, wherein the cooling is performed to a temperature below the activation temperature.

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