EA040334B1 - ROTATING SYSTEM FOR MOVING A LAYER WITH MULTIPLE MONOLITHIC LAYERS TO REMOVE CO2 FROM THE ATMOSPHERE - Google Patents

Description

State of the art

The present invention relates to systems and methods for removing greenhouse gases from the atmosphere and, in particular, to systems and methods for removing carbon dioxide from a gas stream including ambient air.

As a further improvement on the system described in co-pending US Application No. 13/098370, filed April 29, 2011, a suitable system and method is provided that is now recognized to be usable in a wider range of applications than the range described in an earlier application, especially in the case of its additional modification. The description of said co-pending application is incorporated herein by reference in its entirety and as modified by the new description provided herein.

A lot of attention is currently focused on achieving three energy-related and somewhat conflicting goals:

1) providing affordable energy for economic development;

2) achieving energy security; And

3) prevention of destructive climate change caused by global warming.

However, there is no practical way to avoid the use of fossil fuels for the rest of this century if we are to have the energy needed for economic prosperity and prevent energy shortages that could lead to conflict.

It is no longer disputed by scientists that an increase in so-called greenhouse gases such as carbon dioxide (methane and water vapor are the other most important greenhouse gases) will increase the average temperature of the planet.

It is also clear that there is no solution that merely reduces the ongoing human contribution to carbon dioxide emissions and that can successfully address the risk of climate change. It is also necessary to remove additional CO ₂ from the atmosphere. With regard to air extraction and the ability to increase or decrease the amount of carbon dioxide in the atmosphere, they can in principle offset the damage from other greenhouse gases such as methane (simultaneously occurring in nature and produced by human activities), which can increase their concentrations and cause changes climate.

Up until the present inventor's recent inventions, it was generally accepted among experts in the art that, due to the low concentration of this compound in the atmosphere, it was not economically feasible to absorb carbon dioxide directly from the atmosphere in order to at least slow the rise in so-called greenhouse gases. gases in the atmosphere. Subsequently, earlier, concurrently pending applications by the same Applicant have shown practical and effective implementation of such CO2 reductions under specific conditions.

It has been shown that, at ambient conditions, CO2 can be efficiently removed from the air at ambient conditions using a suitable regenerated sorbent system and a low temperature (CO ₂ ) recovery or regeneration method, and that such a method can be extended to remove CO2 from an exhaust gas mixture, mixed with a significant amount of ambient air, with the ability not only to remove CO ₂ from the flue gas, but also to remove additional CO ₂ from the atmosphere to achieve an absolute reduction in CO ₂ in the atmosphere at lower cost and with higher efficiency.

The essence of the present invention

The present invention further provides new and useful systems and methods for removing carbon dioxide from a mass of carbon dioxide-laden air with higher efficiencies and lower overall costs, including lower capital cost (CAPEX) and lower operating cost (OPEX) .

In accordance with the present invention, a novel method and system has been developed that uses assemblies of multiple monoliths or layers that are combined with a single regeneration chamber in a ratio dependent on the ratio of adsorption rate to sorbent regeneration rate. In preferred embodiments of the invention, the monoliths are fixed on a closed tape guide device, preferably forming a closed curve; on the basis of which the monoliths rotate one by one along the guide device, while being exposed to a moving flow of ambient air or a mixture of gases with a large proportion of ambient air. At one point in the guide, rotation stops and one of the monoliths moves into a sealed treatment chamber to release CO2 from the sorbent to regenerate the sorbent. After regeneration of the sorbent, the monoliths continue to rotate along the guide until the next monolith takes a position corresponding to the entrance to the regeneration chamber, after which the rotation of all monoliths stops.

Each monolith is formed from a porous substrate containing on its surfaces amine-containing sites that adsorb carbon dioxide, preferably with a high relative content of primary amines. As the monoliths move along the guide, they adsorb CO2 from the moving gas streams until each of the monoliths reaches a hermetically sealed chamber. After the monolith is hermetically sealed in the chamber, the sorbent is processed to cause CO2 to be released from the sorbent, and the sorbent is regenerated. The released CO2 is removed from the chamber and captured. Then the regenerated sorbent monolith is removed from the sealed chamber and moves along the guide device along with another monolith, while again adsorbing CO ₂ until the next monolith turns into a position from which it moves into the regeneration chamber. At the CO ₂ release/regeneration site, the monolith may be moved to a chamber located above or below the guide at ground level, or the chamber may be positioned so that the monolith is moved to a chamber at the same ground level as the guide. forming a seal with the monolith. Several alternatives mentioned are further described below and shown graphically in the accompanying drawings.

In those instances where the recovery chamber is below or above ground level, the system would include a subsystem for raising or lowering the monolith. In systems where the recovery chamber is at ground level and flush with the guides, a more sophisticated sealing device will be required to seal along the sides and along the top and/or bottom surfaces.

CO2 adsorption and removal method.

The basic idea of this method is that CO2 is adsorbed from the atmosphere by passing air or a mixture of air and exhaust gas through the sorbent bed, preferably at or near ambient conditions. After the CO2 has been adsorbed by the sorbent, the CO2 must be collected and the sorbent regenerated. The last step is carried out by heating the sorbent with steam in a pressurized chamber to release CO2 and regenerate the sorbent. CO2 is collected from the chamber and then the sorbent is suitable for re-adsorption of CO2 from the atmosphere. Only one important limitation of the method is that the sorbent can be deactivated if it is exposed to air at too high a temperature. Therefore, the sorbent may be subjected to cooling before the monolith leaves the chamber and returns to the air stream.

Generally, the adsorption of CO ₂ from the ambient air takes longer than the release of CO ₂ during the regeneration step. With the current generation of sorbents, this difference would require an adsorption period in which, in the case of ambient air treatment, the duration of the adsorption stage is approximately ten times longer than the period required to release CO2 and regenerate the sorbent. Therefore, a system with ten monoliths and one regeneration unit was chosen as the operating basis for a particular rotating system. If the performance of the sorbent is to improve over time, this ratio of adsorption time to desorption time, and hence the number of monoliths needed in the system, should decrease. In particular, if a higher loading variant of the sorbent is used, an adsorption time of one hour could be appropriate, so one regeneration chamber would then be required to serve only five monoliths. In addition, the relative treatment times will vary depending on the concentration of CO ₂ in the gas mixture being treated, such that a higher CO ₂ content will correspond to a shorter adsorption time relative to the regeneration time, for example when mixing an effluent from combustion (flue gas), with ambient air using a gas mixing device.

The chemical and physical activity of the monoliths, both during the adsorption cycle and during the regeneration cycle in a hermetically sealed chamber, is essentially similar to the activity described in earlier co-pending applications No. 13/886207 and 13/925679. The descriptions of such co-pending applications are incorporated herein by reference in their entirety, as modified by the new description provided herein. In the system according to the present invention, each rotating system is provided with one hermetically sealed regeneration chamber for each group of rotating monoliths, the number of monoliths depending on the relative time periods to achieve the desired adsorption and the desired regeneration. In addition, it has been found that higher efficiencies and lower costs are achieved by arranging in space and temporally the two rotating systems in a suitable mutual relationship, ensuring that the regeneration chambers of the two rotating systems interact with the monoliths so that each chamber is preheated with using the heat remaining in the other chamber as a result of regeneration in the other chamber; it also allows the regenerated monolith to be efficiently cooled before it returns to its adsorption cycle on the rotating guide.

According to the present invention, such interaction between the regeneration chambers is achieved by reducing the pressure in the first chamber of the system so that the steam and water remaining in the first chamber evaporate after the release of CO ₂ and the system is cooled to the dew point

- 2 040334 steam at a lower partial vapor pressure. In addition, as described below, the heat released in such a process is used to preheat the second layer of sorbent and thus provide approximately 50% specific heat recovery with a beneficial effect on energy and water use. This concept can be applied even if an oxygen-resistant sorbent is used. The susceptibility of the sorbent to deactivation by oxygen at higher temperatures should be considered during the development process and sorbent performance is expected to improve over time.

As discussed above, the sorbent bed is preferably cooled before being exposed to air to avoid deactivation of the sorbent by atmospheric oxygen. Such cooling is provided by reducing the pressure in the system and thus lowering the temperature of the condensation of the steam. This has been shown to effectively eliminate sorbent deactivation by lowering the temperature of the system. This creates a significant amount of energy removed from the layer, which is cooled during the stage of depressurization. The incoming bed, which has completed its CO2 adsorption step, is subjected to heating to release CO2 and regenerate the sorbent. Said heat can be provided solely by atmospheric pressure steam, however, this is associated with additional operating costs. To minimize such operating costs, the concept of a two-chamber design was developed. With this concept, the heat which is removed from the chamber subjected to cooling by lowering the pressure in the system and thereby lowering the condensation temperature of the vapor is used to partially preheat the second chamber containing the layer in which the adsorption of CO ₂ from the air has been completed and which is heated to start the CO2 removal and sorbent regeneration step. Thus, by using the heat obtained from cooling the first chamber to raise the temperature of the second chamber, the steam flow rate is reduced. The rest of the heat load for the second chamber is provided by the addition of steam, preferably atmospheric pressure. This process is repeated in each of the two chambers for the other rotating monoliths, increasing the thermal efficiency of the system.

These and other features of the present invention are described in the following detailed description and accompanying drawings or will become apparent from the following detailed description and accompanying drawings.

Brief description of figures and illustrations

In FIG. 1 is a schematic plan view of a pair of interlocking multi-monolith rotary systems for removing carbon dioxide from the atmosphere, in accordance with an exemplary embodiment of the present invention.

In FIG. 2 is a schematic vertical sectional view of the multi-monolith rotating system shown in FIG. 1 to remove carbon dioxide from the atmosphere according to an exemplary embodiment of the present invention.

In FIG. 3 is a schematic top view of an alternative pair of interlocking multi-monolith rotating systems for removing carbon dioxide from the atmosphere, in accordance with yet another illustrative embodiment of the present invention.

In FIG. 4 is a schematic vertical sectional view of the multi-monolith rotating system shown in FIG. 3 to remove carbon dioxide from the atmosphere according to this exemplary embodiment of the present invention.

In FIG. 5 and 5A-5H are schematic illustrations of a remote vertical embodiment of a pair of regeneration chambers for removing carbon dioxide from the carrier monolith shown in FIG. 14 using a vertical movement system or a lifting device to move the monolith between the level of the rotary guide from the highest (longest) air contact position (where the air is moved by a mechanical blower) and the vertical position of the regeneration chamber.

In FIG. 6 is a plan view (schematic elevational view) of regeneration chambers and monoliths on adjacent monolith systems, showing the layout of the piping system for each chamber and between the chambers.

In FIG. 7A and 7B are schematic vertical sectional views showing fans that are stationary and fans that rotate with each monolith, respectively.

In FIG. 8A is a schematic vertical side view of the double acting ducted exhaust fans and gas collectors of FIG. 7A, 7B.

In FIG. 8B is a schematic vertical front view of the double acting ducted exhaust fans and gas collectors of FIG. 7A, 7B.

In FIG. 9 is a schematic vertical sectional view along lines 9-9 of FIG. 8B, constructions of double-acting ducted exhaust fans and gas collectors.

In FIG. 10 shows the design of monolithic sealing systems, where the angles and dimensions are enlarged for the purpose of explanation.

- 3 040334

In FIG. 11 is a schematic plan view of an interconnected pair of multi-monolith rotating systems for removing carbon dioxide from the atmosphere, in accordance with yet another illustrative embodiment of the present invention.

In FIG. 12 is a schematic vertical sectional view along lines 11-11 of FIG. 11, an interconnected pair of rotating systems with multiple monoliths to remove carbon dioxide from the atmosphere.

Detailed description of the invention

The principal design of the system for carrying out such operations is shown in Fig. 1 and 2. A slight modification of the concept is shown in FIG. 3 and 4. The general basic design has been discussed above and a detailed discussion of the operation and ancillary equipment that will be required is given below.

In this embodiment of the invention, there are ten monoliths arranged in a decahedral arrangement, which are located on an annular guide device. There are two annular/decahedral nodes associated with each processing unit, and they interact with each other (see Fig. 1-4). The air passes through the monoliths with the help of exhaust fans located on the inner sides of the monoliths. At one point, the monoliths are positioned adjacent to a single sealed chamber, into which each monolith then enters, as shown by vertically withdrawing the layer from the processing guide (i.e., into a chamber where the monoliths are heated to a temperature of no more than 130°C, and more preferably not higher than 120°C, preferably with precisely heated steam to release CO ₂ from the sorbent and regenerate the sorbent). Alternatively, the chamber may be at ground level. With this embodiment of the invention, the adsorption time for CO2 adsorption by the monolith is ten times longer than the sorbent regeneration time.

It should be understood that while the use of porous monoliths is preferred, it is advantageous to use, instead of a monolith, fixed layers of porous particulate or porous granular material mounted on a support frame. In both cases, the porous support serves as a carrier for the amine-containing CO ₂ sorbent if the layer has the same specific surface area as the monolithic adsorbent carrier.

Requirements for engineering and technical equipment.

In FIG. 1-4, 11 and 12 show the basic concepts of the system operation. There are ten monoliths 21, 22 located in each node in a ten-sided layout, which are movably fixed on the annular guide devices 31, 33. There are two annular/decahedral nodes A, B associated with each processing unit, and they interact with each other. Air is passed through each of the monoliths 21, 22 by means of exhaust fans 23, 26 positioned radially within each of the ten-sided assemblies causing air to flow away from the inner peripheral surface of each monolith and upwards out of the system. At one point along the guide 31, 33, the monoliths 21, 22 are adjacent to the sealed regeneration chamber 25, 27, in which the monoliths 22, 22 are placed for regeneration processing after completing one rotation around the guide.

Thus, as shown in FIG. 1 and 2, the first layer 21 rotates to a position below the recovery chamber 25 and then moves vertically upward into the treatment chamber 25; or if chamber 27 is located below ground (FIG. 4), layer 22 then moves vertically downwards into chamber 127 for treatment; or if the treatment chamber is located at ground level, the assembly is rotated, thereby removing the layer 21, 22 from the chamber 27 so that the layer 21, 22 is in such a position that the movement of all monoliths along the guide device stops. After the layer 21 has been regenerated, it returns to the guide again and the layer transfer unit is rotated so that the next layer 21-2, 22-2 is in the said position. Layer 2 then moves into the processing chamber and then returns to the ring. This process is repeated many times. The two annular assemblies function together, although the monoliths of each decahedron, as explained below, enter and leave their chambers at slightly different times, providing heat transfer between, for example, chamber 25 and chamber 27 when regeneration in one of them is completed to provide preheating. another camera. This saves heat at the beginning of regeneration and reduces the cost of cooling the bed after regeneration.

Three locations for regeneration chambers 25, 27 are shown. FIG. 1 and 2 regeneration chambers 25, 27 are located above the rotating units for transferring layers (at the level of the conditional soil), and the monoliths rise vertically into the regeneration chambers. The only overhead structure is the structure needed for the chambers located above the rotating monoliths on the cantilever structure.

In FIG. 3 and 4, chambers 125, 127 are located below ground level and below the rotating units for transferring layers. The chambers may be located in a separate recess with appropriate access for preventive inspection and process piping. Layers are moved vertically down into the chambers.

In FIG. 11 and 12, regeneration chambers 321, 327 are located at ground level, along with rotating units for layer transfer. The chambers can be located with appropriate access for preventive inspection and process piping also at ground level. Suitable sealing surfaces in contact with each other can be located on the chamber and on each layer in order for the layer to rotate into position in the chamber, and the chamber 322, 327 is sealed.

In all cases, auxiliary equipment (such as pumps, control systems, etc.) can preferably be located at ground level within the closed loop of the guiding device, on which the rotary units 29, 39 for transferring the layers are fixed. In some situations, in particular, the regeneration chambers can be located at different levels without departing from the concept of the present invention.

Such designs, compared with the installation previously described in the prior art, can: minimize metal structures;

locate all critical equipment at ground level, with the exception of recovery chambers, which function only as containment tanks;

ensure that there is no obstruction to the air flow to the monoliths if the chambers are located at different levels relative to the guiding device;

require only one device to move the monoliths vertically, or the absence of such a device for introduction into one chamber of each group, for example, of 10 monoliths;

minimize or eliminate the time required to move layers in and out of the chamber, especially if the chambers are at ground level;

ensure that all pipelines are in fixed positions; and to provide two regeneration chambers adjacent to each other with a minimum gap between them to provide heat exchange, desirable for increased efficiency.

Mechanical operations with the necessary mechanisms and performance that will be required include:

rotating two sets of layer transfer units along an annular guiding device on the support device;

precise positioning of elements for precise localization of the position where the monoliths should stop with the ability to ensure the free movement of the monoliths into the regeneration chamber and out of the regeneration chamber;

removing the layer from the layer transfer assembly on the guide, introducing the layer into the recovery chamber, removing the layer from the recovery chamber, and reintroducing the layer to its position on the guide assembly. All said movements take place in the vertical direction or, alternatively, within the framework of a horizontal rotational movement along the guiding device. The monoliths and regeneration chambers are designed so that, in the case of vertically moving monoliths, an airtight seal is present between the top or bottom of each monolith and the chamber support device. Examples of some of the principal designs of such seals are shown in Figs. 10.

In all cases, with reference to FIG. 1-6, the layer 21-1 (ring A) is rotated to the (entry) position and then moved up or down to the treatment chamber 25. The pressure in chamber 25 (containing layer 21-1, ring A) is reduced, for example, using a vacuum pump 230, to less than 0.2 bar (absolute pressure). Chamber 25 is heated at atmospheric pressure with steam supplied through conduit 235, CO ₂ is removed from bed 21-1 and removed from chamber 25 through CO ₂ and condensate outlet conduit 237, which is separated in condenser 240 (FIG. 5A). Layer 22-1 (ring B) is then placed in chamber 27 (ring B) while chamber 25 is being treated as described above (FIG. 5B). The steam supply to the chamber 25 is stopped and the CO ₂ and condensate discharge pipe is closed. Chamber 25 and chamber 27 are connected by opening valve 126 in connecting conduit 125 (FIG. 5C).

Chamber 27 is depressurized using a vacuum pump 330 associated with chamber 27. This reduces the system pressure in both chambers and draws the vapor and inert gases remaining in chamber 25 through chamber 27 and then to the vacuum pump. This cools chamber 25 (and thus layer 21-1, ring A) to a lower temperature (i.e. to the condensing temperature at partial vapor pressure in the chamber), and reduces the possibility of deactivation of the sorbent by oxygen when layer 21- 1 returns to the air stream again. This method also preheats chamber 27 (and thus layer 22-1, ring B) from ambient temperature to the condensing temperature at the partial pressure of vapor in chamber 250. This reuses energy, and the amount of atmospheric pressure steam required for heating of the second chamber 27 (and layer 22-1, ring B) is reduced (FIG. 5D). As the vacuum pump 330 depressurizes chambers 25 and 27, the temperature in the first chamber 25 decreases (about 100° C. to some intermediate temperature) and the temperature rises in the second chamber 27 (from ambient temperature to the same intermediate temperature). CO2 and inert gases are removed from the system using the 330 vacuum pump.

The valve between the first chamber 25 and the second chamber 27 is closed and the chambers are isolated from each other.

- 5 040334 friends. The bed 21-1 (Ring A) is now cooled below the temperature at which oxygen deactivation of the sorbent is a concern when the bed is returned to the air stream again. The second chamber 27 and bed 22-1 (ring B) are preheated and therefore the amount of steam required to heat the chamber and bed is reduced (FIG. 5E). Then the layer 21-1 (ring A) is lifted back into the layer transfer assembly. Ring A with the layer transfer assembly is rotated one layer and then layer 21-2 (ring A) is introduced into chamber 25 where it is ready for preheating. Chamber 27 is heated with atmospheric pressure steam and the evolved CO ₂ is collected (FIG. 5F).

When the second chamber 27 (comprising layer 22-1, ring B) is fully regenerated, the steam supply to chamber 27 is stopped and the CO ₂ and condensate pipeline is shut off by valves 241, 242. Valves 126 between the first chamber 25 and the second chamber 27 are opened and chambers 25, 27 are depressurized using a vacuum pump system 230 for chamber 25. The temperature of the second chamber 27 (and thus bed 22-1, ring B) is reduced (see 5 above). The temperature of the first chamber 25 (containing layer 21-2, ring A) rises (see 5 above) (FIG. 5G). The vacuum pump 230 reduces the pressure in the chambers 25, 27. The temperature of the chamber 25 decreases (from about 100°C to some intermediate temperature). The temperature of chamber 27 rises (from ambient temperature to the same intermediate temperature). CO ₂ and inert gases are removed from the system using a vacuum pump 230. Layer 22-1 (ring B) again rises into the annular device assembly, and the assembly rotates one layer. Layer 22-2 (ring B) is then introduced into chamber 27. Chamber 25 (containing layer 21-2, ring A) is heated with atmospheric pressure steam to release CO ₂ and regenerate the sorbent (FIG. 5H). The chamber 27 is then preheated as described above. The process is repeated for all layers as the decahedrons are rotated many times.

Design parameters.

The current basis for design systems is as follows:

mass of a single monolith to be moved: 1500-10000 pounds (including support device);

approximate layer size:

width - 5-6 m, height - 9-10 m, depth - 0.15-1 m.

It should be noted that the layer sizes can be adjusted depending on the specific conditions at the geographic location of each pair of systems and the desired or achievable processing parameters.

In the case of a system including 10 monoliths in each of the ten-sided rings, the overall dimensions of the preferred annular/decahedral structure may be approximately 15-17 m, preferably approximately 16.5 m. , using electric motor and drive pulley; or it is possible to provide support devices at a specific location along the guide device and use one large motor to drive the guide device and all structures in a closed loop. In any case, the regeneration chamber is placed in one place, and all structures can stop their movement when one of the support devices is placed in such a way as to move into the regeneration chamber. The cost-effectiveness of using a single drive motor or motor, or multiple drive motors or motors, will depend on many factors such as their location and whether or not the drive unit is equipped with an electric motor or engine running on any fuel. The nature of the drive units themselves is not a feature of the present invention, and such units are well known to the person skilled in the art. Examples of suitable engines include internal combustion engines or external combustion engines or compressed gas engines, such as Stirling engine heat cycle engines, or steam engines, or hydraulic or pneumatic engines.

When the recovery chamber is located above the level of the guide, the top will be approximately 20 m above the level of the guide, and when the recovery chamber is located below the level of the guide, the top of the chamber will automatically be below the level of the guide. The chamber at ground level will be only at least higher than the tops of the monoliths, with the ability to keep the entire monolith in the chamber during regeneration.

If the recovery chamber is not at ground level, the lifting system for moving the monolith into and out of the recovery chamber should be capable of moving in and out of the chamber over a period of time ranging from 30 to 120 seconds, and preferably from 30 to 45 seconds. . A shorter time period corresponds to greater flexibility in the processing parameters that are appropriate for the process. It is recognized that there are certain systemic mechanical limitations on the movement of massive monoliths. One of the advantages of the method, when the regeneration chamber is at ground level, is that there is no need for a vertical

- 6 040334 movement, since the monolith simply rotates into the chamber as part of its rotational movement and hermetically closes in it; this eliminates vertical movement, loss of time and additional capital costs for lifting devices. In each case, the two ends of the bed are solid and form seals with the ends of the regeneration chamber.

Details of operation and design.

This section is divided into the following subsections.

Section i is a description of the general design of the system and the application of the carburetor type system for energy recovery.

Section ii is a description of the method, including a simplified flow diagram (PFD) and a description of the most important items of equipment.

Section iii is the principle mechanical design.

Section iv - factors that must be investigated in more detail in order to provide the final design with optimal performance.

Discussion.

i. CO2 adsorption and removal method.

In the method according to the present invention, CO2 is adsorbed from the atmosphere by passing air or mixtures of air and exhaust gases through the sorbent bed; suitable sorbents preferably include amines, and preferably polyamines, at least with a high relative content of amino groups on the sorbent, which are primary amines. After CO ₂ has been adsorbed by the sorbent, it is separated from the sorbent and collected as the sorbent undergoes regeneration. This stage is carried out by heating the sorbent with steam in a sealed chamber or in a regeneration chamber. This releases CO2 and regenerates the sorbent. CO2 is collected and the sorbent is then suitable for re-adsorption of CO2 from the atmosphere. The limiting parameter of the method is that the sorbent can be deactivated if exposed to air at too high a temperature. Therefore, usually the sorbent is subjected to cooling before returning it to the air stream for contacting. According to the present invention, this is achieved by depressurizing the system so as to evaporate the steam and water remaining in the regeneration chamber after the release of CO ₂ , thereby cooling the system to the condensing temperature of the steam at its new, lower partial pressure. In addition, as described below, the heat released by this method is used to preheat the CO ₂ rich sorbent bed, with the ability to recycle about 50% specific heat and have a beneficial effect on energy and water use. This concept is applicable even if an oxygen-resistant sorbent is used to further increase the useful life of the sorbent and monolithic support.

Typically, the adsorption of CO2 from the air by the sorbent takes a longer period of time than the period of time required for the release of CO2 during the regeneration step. With regard to the current generation of sorbents, this difference will require an adsorption period in which the duration of the adsorption stage is approximately ten times longer than the time required for the release of CO ₂ and regeneration of the sorbent. Therefore, a system with ten monoliths and one regeneration unit was chosen as the current basis. If a sorbent is used in the system that will have an adsorption period in which the duration of the adsorption stage is only approximately five times the period required for the release of CO ₂ and regeneration of the sorbent, the number of monoliths required in the system for each regeneration chamber can be reduced, for example, so that one regeneration chamber serves 5 monoliths. It also depends on the concentration of CO2 in the gas mixture being treated and the desorption time of any particulate sorbent.

As discussed above, the regenerated sorbent bed is preferably cooled prior to being exposed to air to avoid possible deactivation by atmospheric oxygen. According to the present invention, such cooling is achieved by lowering the system pressure in the regeneration chamber after completion of the regeneration stage, thereby reducing the dew point of the steam. According to the present invention, this is done so that a significant amount of energy released during the regeneration of the monolith during the stage of pressure reduction is transferred to the second layer containing the sorbent with a large amount of CO ₂ before the stage of its desorption, while providing some energy to heat the second layer to release CO ₂ and regenerate the sorbent. This heat transfer from one recovery chamber to another reduces the operating cost of providing exceptionally fresh steam to heat the bed of monoliths. The rest of the heat load for the second chamber is provided by the addition of atmospheric pressure steam, although the cost savings are smaller. This process is repeated in each of the two chambers for successive monoliths, and improves the overall thermal efficiency of the system. Such a concept is shown in Fig. 1-6, 11 and 12.

In a preferred embodiment of the invention, as shown in the drawings, there are ten monoliths arranged in a decahedral arrangement on an annular guiding device. There are two ring/decahedral knots associated with each

- 7 040334 processing unit, and they interact with each other (see Fig. 1 and Fig. 5A-5H). Air is passed through the monoliths by means of exhaust fans, preferably positioned radially against the inner surfaces of the monoliths. At one point, the monoliths are adjacent to a chamber into which the monoliths enter, as shown, by withdrawing the bed from the guide in the vertical direction for processing (i.e., into a chamber where they are heated with steam to release CO2 from the sorbent and regenerate the sorbent). Alternatively, the chamber may be at ground level so that the monolith simply moves along the guide into the regeneration chamber (1) or moves into a chamber at ground level outside of the guide. The latter method reduces the energy required to move the layer, while allowing the two regeneration chambers to be placed side by side, closer to each other.

The main stages in the operation of the systems shown in Fig. 1-4 and 11-12, as defined above, may be as follows.

1) Layer 21-1 (ring A) after one complete cycle of rotation is rotated to the indicated position and then moved, for example vertically, into the processing chamber 25 (FIGS. 1-4 and 5).

2) Chamber 25 (comprising layer 21-1 (ring A)) is heated with steam at atmospheric pressure and the recovered CO ₂ is removed, FIG. 5A-H.

3) Layer 22-1 (ring B) is placed in chamber 27 while chamber 25 is being treated to regenerate the sorbent.

4) The steam supply to chamber 25 is stopped and the CO ₂ and condensate outlet line is closed. Chamber 25 and chamber 27 are connected by opening valves in the connecting pipeline 125.

5) Chamber 27 is depressurized using a vacuum pump 330 associated with chamber 27. This reduces the system pressure in both chambers and draws the steam and inert gases remaining in regeneration chamber 25 into another chamber 27 and then to vacuum pump 330. Chamber regeneration 25 (and at the same time layer 21-1 (ring A)) is cooled to a lower temperature (i.e. to the condensation temperature at partial vapor pressure in the chamber), while reducing the possibility of deactivation of the sorbent under the influence of oxygen when it is returned again into the air stream. In this way, chamber 27 is also heated (and thus layer 22-1 (ring B)) from its temperature after adsorption to the condensation temperature at the partial pressure of vapor in chamber 27. This reuses energy from the recovery chamber 25, and the amount of atmospheric vapor the pressure required to heat chamber 27 (and thereby layer 22-1 (ring B)) is reduced.

6) The valve 125 between the two chambers 25, 27 is closed and the chambers are isolated from each other. The bed 21-1 (Ring A) is now cooled below a temperature at which oxygen deactivation of the sorbent can occur when the bed is returned to the air stream again. The second chamber 27 and layer 22-1 (ring B) are preheated, and the amount of steam required to heat the chamber and layer is reduced.

7) Layer 21-1 (Ring A) is then moved vertically again onto the ten-sided guide assembly. Chamber 27 is heated with atmospheric pressure steam and CO ₂ is collected. Ring A with the layer transfer assembly is rotated one layer and then layer 21-2 (ring A) is introduced into the regeneration chamber 25 where it is ready for preheating (FIG. 5H).

8) When chamber 27 (containing layer 22-1 (ring B)) is fully regenerated, steam supply to chamber 27 is stopped and CO ₂ and condensate line 337 is shut off with valves. The valves between chamber 25 and regeneration chamber 27, where the regeneration has been completed, open and the pressure in chambers 27, 25 is reduced using vacuum pump 230 for chamber 25. The temperature of chamber 27 (and at the same time layer 22-1 (ring B)) decreases ( see point 5 above). The temperature of chamber 25 (containing layer 21-2 (ring A)) rises (see paragraph 5 above).

9) Layer 22-1 (ring B) is again moved to the layer transfer node and the node is rotated one layer. Layer 22-2 (ring B) is then introduced into chamber 27. Chamber 25 (containing layer 21-2 (ring A)) is heated with atmospheric pressure steam to release CO ₂ and regenerate the sorbent.

It is understood that reference to a layer includes both a monolithic substrate and a layer of particles in a jacket held in a volume of the same size.

This process is repeated many times and the two ring guide assemblies function together, despite the fact that the monoliths of each decahedron move in and out of their chambers at slightly different times in order for the heat from the cooling of the previous regeneration chamber to preheat the subsequent (second) chamber. when the next monolith takes its place in the chamber.

In FIG. 1 and 2, the chambers are located above the rotating layer transfer units (which are located at the level of the conditional soil), and the monoliths rise into the chamber. One lifting device is the device required for the chambers, which are located above the rotating monoliths on the cantilever structure.

In FIG. 3 and 4 chambers are located below the ground level and under the rotating transfer units

- 8 040334 layers. The chambers may be located in a separate recess with appropriate access for preventive inspection and process piping.

In FIG. 11 and 12, the chambers are located at ground level, preferably along a guiding device, so that there is no need for additional mechanisms for vertical movement. Alternatively, the regeneration chamber at ground level can be located outside the decahedrons, and move in the radial direction from the guide device.

In any case, auxiliary equipment (such as pumps, control systems, etc. see section 2) may be located at ground level in a radial direction inside the rotating layers transfer units.

ii. Technological equipment and controls.

In FIG. 6 shows the general design of the proposed system.

Each individual system has two decahedrons with monoliths. Therefore, a single system contains 20 (twenty) monoliths.

There are nine fan units for each decahedron (the fan kit is missing where the monoliths enter the chambers). It is currently preferred that there be two vertically arranged duct fans associated with each layer of the size described above, i. e. 10 m high and 5 m wide. Thus, for each individual system, 2x18=36 duct fans will be needed. However, the choice of the number and size of fans depends on many factors.

The nine fans on each decahedron are in a stationary state (i.e. they will not rotate with the layers). Preferably, each sealing system, such as resilient mechanical seal walls, is provided with a fan to minimize air bypass near the monoliths. It is clear that the monoliths do not move continuously, but rather, the monoliths stop as soon as one of the layers reaches the location of the chamber, and then start moving again as soon as such a layer leaves the regeneration chamber. Stationary fans are positioned so that when the layer enters the regeneration chamber, each layer is located opposite the fan unit and is hermetically connected to the fan unit. Alternatively, the fans may be attached to the rotating bed structure and attached to the layers. In this case, the number of fans can be increased up to 2x20=40 duct fans per individual system (see section 3).

In one double annular guide system there are two regeneration chambers 25, 27; each chamber serves one of the decahedrons.

The size of the monoliths is not standardized. Based on a preliminary estimate, each layer should be assumed to have the following dimensions: 5 m wide x 10 m high x 1 m deep. This initial size may vary based on economic analysis and other factors.

In FIG. 6 shows only the most important valves, and safe commercial operation requires additional valves, instrumentation, piping, and controls that are well known in the art.

During regeneration and release of CO ₂ from the layer, atmospheric pressure steam at a temperature of 100-120°C is supplied directly to the regeneration chamber 25, 27 containing the layer. The effect of steam supply is to heat the bed and chamber, and release CO2 and form condensation. The condensate is removed to the collection system. CO ₂ is removed from the chamber along with some steam and inert gases under the action of CO ₂ blowers 225, 227. The stream leaving the chamber passes through a heat exchanger (condenser) 240, where the stream is cooled and additionally condensate is obtained, which enters the condensate collection system 291 . Ultimately, the CO ₂ product is passed through conduit 229 to the storage and compression system, or the CO ₂ product can be applied without compression directly to another process, such as seaweed farming. Compression of CO ₂ is not included in the scope of the description of the present method. Preferably, the air is at least partially removed from the regeneration chamber 25, 27 after the bed chamber is hermetically sealed and before the start of the vapor flow, especially when the CO2 is then compressed.

Preferably, the pressure in the hermetically sealed regeneration chamber is reduced to no more than 0.2 bar (absolute pressure) before steam is introduced and CO2 is released. Preferably, non-condensables are removed from the air as much as possible to reduce compression costs.

It is desirable to reduce the amount of water in the CO ₂ stream leaving the condenser, since the presence of water in a higher amount will increase the compression costs associated with storing the CO ₂ product; if condensate is not removed in the inlet stream, more condensate will have to be removed at the compressor intercoolers. The amount of steam remaining in the storage effluent will depend on the lowest suitable refrigerant temperature and the size of the condenser installed. The determination of such parameters in any particular case is based on an economic assessment of the relative costs of compression (capital and operating), coolant temperature (eg, whether ambient air, chilled water, or refrigerant will be used), and heat exchanger capital costs.

When properly designed, the condenser must also be able to separate liquid and vapor flows. However, a drum separator or similar type may be required to separate the liquid and vapor streams before the vapor stream passes to the CO ₂ blower 225, 227.

The CO ₂ blower 225, 227 may be a liquid ring pump. If this type of unit is selected, it will be able to handle liquid condensate in the inlet stream and the condensate will be removed from the liquid ring system and sent to the condensate storage. If a liquid ring pump type is not used, additional steps may be required to ensure that the blower's incoming vapor stream does not contain a significant amount of liquid. Therefore, the choice of the type of unit used as a CO ₂ blower may influence the design of equipment located upstream.

When the regeneration stage is completed, all valves are closed and both chambers are isolated. In order to carry out post-cooling of the chamber and bed that has just completed the release of CO ₂ and the sorbent regeneration step, and preheating the other chamber and bed that are at ambient temperature, the following steps are used.

The isolation valve 126 between the chambers is opened.

The vacuum pump 230, 330 associated with the layer is turned on at ambient conditions.

The action of the vacuum pump is to draw steam (at first, for example, at atmospheric pressure and approximately 100° C.) from the chamber in which CO ₂ production and bed regeneration have been completed (hot chamber) into the chamber at ambient temperature. The lower pressure will assist in cooling the hot regeneration chamber and the regenerated bed to a temperature substantially lower than the initial temperature after regeneration, i. e. approximately equal to 100°C, due to the reduction of the partial pressure of the steam, which reduces the dew point of the steam. As steam is drawn from the hot chamber and bed, this steam will begin to heat the second chamber and bed (at first at ambient temperature) due to steam condensation on the walls of the chamber and within the channels of the sorbent bed. As the operation of the vacuum pump continues, the pressure in both chambers decreases and reaches the final pressure (approximately 0.2 bar (absolute pressure) in this example). At this stage, both chambers and their monoliths will be at approximately the same temperature (approximately 60°C in this example). This will cool the hot bed to a temperature whereby when the hot bed is returned to the air stream to further adsorb CO2, the sorbent will not be deactivated to any significant extent due to the presence of oxygen in the air. Simultaneously, the bed, initially at ambient temperature, will be provided with a significant amount of heat necessary to increase its temperature to approximately 100° C. to release CO ₂ and regenerate the sorbent. The final pressure to which the combined chambers will be brought is determined by the temperature limitations associated with the deactivation of the sorbent in the presence of oxygen.

After the specified pressure level is reached in both chambers 25, 27, the operation of the vacuum pump 230, 330 is stopped, the isolation valve 126 between the chambers is closed, and the regenerated bed returns to atmospheric pressure.

The cooled layer returns to the annular guide assembly, where the assembly is rotated until the next layer is in position corresponding to the entrance to the chamber, and then the rotation stops.

The second chamber and bed in the second chamber 25, 27, which had been preheated to about 60° C., are meanwhile provided with atmospheric pressure steam and heated to 100° C. to remove CO2 and regenerate the sorbent. CO2, steam and inert gases are removed by a vacuum CO2 blower 225, 227 associated with this chamber (see text above and FIG. 6).

Then the process is repeated many times with alternating regeneration chambers 25, 27.

It is possible that only one CO2 blower and one _CO2 vacuum pump can be used for each pair of regeneration chambers; separate blower and pump for each chamber; or you can use a centralized system, ie. a single vacuum pump 230, 330 for CO ₂ and a single CO 2 blower 225, 227 to service the multiple pairs of the system.

In FIG. 1 and 2 show the principle mechanical design, in which each system has two decahedrons, and in which the layers rise into chambers or descend from chambers located above the annular guide system and fixed to the cantilever metal structure. In FIG. 3 and 4 show a similar concept, except that the chambers are located below ground level in a separate recess, and the monoliths are lowered into the chambers. It is also advantageous to have the chamber at ground level and simply rotate each layer until it seals against the chamber, due to the fact that the ring rotates and then stops when the layer is sealed in the recovery chamber.

In FIG. 7A shows the principal design of an auxiliary fan equipment system in the form of ducted exhaust fans. Vertical walls 38 adjacent to each end of the layers are located radially inward from the fans (only one such wall is shown in FIG. 7A) along the surface seal 136 where the walls are in contact with the end of the layers, plus top and bottom surfaces 36 , 37, shown in section and extending between the vertical walls, will prevent air from being bypassed near the layers 21, 22 by the fans 26 remaining in a fixed position. Preferably, each of the walls 38 and the top 36 and bottom 37 surfaces are provided with an elastomeric buffer 136 which cannot contact the front side of the layer 22 but which can be pressed against the ends of the layer when the layer 21 is fully rotated into the air trapping position.

In FIG. 7B shows a basic design where fans 326 rotate with their associated monoliths 21. Such a design may require fan supports to be part of an annular rotating system that can increase the power required to rotate the monoliths, in particular at initial starting torque. required to start the rotation. Such a choice would make it possible to avoid air bypass near the bed, since the seals may be permanent and do not have to move.

In FIG. 8A, 8B and 9 show a schematic layout of fans 326 and gas collectors 425, which can even be used to distribute air through monoliths using two fans per layer when the layers are 10 m high.

The mechanical operations that will be necessary to position the system to ensure that the monoliths move in and out of the chambers with the required accuracy include.

Rotation of two sets of layer transfer units along an annular guide on a support device.

Precise placement of the position where the monoliths must stop to allow free movement of the monoliths into and out of the recovery chambers, and enter and exit sealing contacts with air distribution walls and seals if the fans are stationary.

Removing the layer from the layer transfer assembly, introducing the layer into the recovery chamber, removing the layer from the chamber, and reinstalling the layer on the annular guide assembly, with the layer moving vertically. When the recovery chamber is at ground level, it may not be necessary to remove the layer.

The monoliths are designed such that there is an airtight seal between the monoliths and the interior of the chamber and between the bed and the fan support when they are in positions where air passes through the bed. In FIG. 10 shows the principal design of a side-by-side cone seal system that will seal the bed at predetermined positions in either the upper recovery chamber (FIG. 10A) or the lower recovery chamber (FIG. 10B). In FIG. 10C is a vertical sectional view.

Two seal systems, each corresponding to channel 150 in the regeneration chamber, are mounted end to end (side by side) on each support frame. One channel is located in the chamber, and the other channel is located on the annular guide assembly where the layer for removing CO ₂ from the air stream is located.

Each of the channels 150 in which the seals will pass is also tapered. When the applied seal is inserted at the top, it is narrower at the top compared to the channel, which is wide at the bottom compared to the seal. This results in the ability of the seal to be inserted into the channel, over which it will slide and seal the channel. The channel through which the seal slides is also tapered to match the taper of the seal. As the layer rises, the gap between the channel and the seal decreases. Such an operation gradually centers the layer at a predetermined location, and at the same time the gap between the seal and the channel is also gradually reduced. When the bed is fully raised, the seal and the channel are the same width from top to bottom, the seal seals against the channel to create a seal, and the layer is positioned precisely.

When the seal is inserted at the bottom, another type of seal is used which tapers at the bottom and which allows the seal to be inserted into a tapered channel (which is wider than the seal and has the same taper as the seal in the lower position) over which it will slide and seal the channel. With respect to the upward sealing operation, the gap between the seal and the cone will decrease as the layer is moved into position and centered in the chamber, creating the desired seal. In addition, there is also a seal centered between the bottom of the bed and the bottom of the recovery chamber above the guide, and between the top of the bed and the top of the recovery chamber when the chamber is below the guide, as in FIG. 3 and 4. When the recovery chamber is at ground level, as in FIG. 11-12, the ends or sides of the layer are used for compaction.

When designing a lifting system for vertical movement of the layer, either up or

- 11 040334 down, the approximate time required for the vertical movement of the layer between the guide device and the chamber, in the case of monoliths with a mass of approximately 10,000 pounds and with dimensions of 5x10x1 m, is from 30 to 120 seconds. The shorter such a period of time, the greater the flexibility of the processing parameters, which meets the requirements of process improvement. For these reasons, a regeneration chamber at ground level has some advantages.

4.1. Characteristics of the sorbent and layer thickness.

It should be understood that the specific dimensions and other numerical parameters set forth above are based on the use of the currently commonly known polyethyleneamine (PEA) as the sorbent. As improved sorbents are marketed that are able to adsorb more rapidly and/or are less sensitive to oxygen at elevated temperatures, for example, overall dimensions and operating temperatures, as well as the number of layers per regeneration chamber and the speed of movement of layers through guiding device.

Currently, the pressure drop across the sorbent bed (which is typically a porous silica or alumina support with PEI on its surface) is preferably limited to 1 inch w.c. (H ₂ O) and the currently specified structure of the sorbent layer; and the surface air velocity used in the design (2.5 m/s in the free-flow channel) results in the described depth (in the direction of air flow) of the layer. This in turn affects the depth of the camera. The expected pressure drop, bed porosity, channel size, surface air velocity may change due to changes in the sorbent and/or substrate, which, in combination with the performance of the sorbent, may lead to a different preferred bed depth. One improved system is provided by using an alumina-coated silica substrate with a primary amine polymer such as poly(allyl)amine or one of its derivatives deposited on their surfaces.

4.2. Minimum design pressure in regeneration chambers.

The influence of the selected minimum design pressure will most significantly affect the cost of chambers used to heat monolithic sorbents. The minimum design pressure is chosen based on the ability to provide such a vapor condensation temperature (partial vapor pressure in the chamber at minimum design pressure) that the bed is cooled below the temperature at which significant deactivation of the sorbent occurs when it is exposed to oxygen in the air stream. The lower the pressure, the thicker the sorbent layers and the heavier the structures needed to strengthen the chamber. When using a virgin polyamine, such as poly(allyl)amine, which is currently commonly available, it is preferable that a chamber with a minimum design pressure of 0.2 bar (absolute pressure) be large, heavy and with expensive equipment even in in the case of a layer with dimensions of approximately 3x5x1 m. In an industrial scale plant, it would be desirable to have a larger layer. However, since the mass of the layer and the cost of the chamber increase with the increase in the layer size, the dependence of the power (not linear) on the chamber dimensions will increase. In addition, a higher minimum design pressure could allow more thermal energy to be recycled, since the cold chamber can be heated to a higher temperature, and this may require less atmospheric pressure steam. Thus, the possibility of using a higher minimum design pressure (ie, above 0.2 bar absolute pressure) could provide significant benefits if a sorbent is used that will not deactivate at a higher temperature.

4.3. Construction materials for the camera.

When the recovery chamber is constructed from carbon steel and stainless steel, this results in a structure that is heavy and expensive. Other construction materials include, for example, carbon fiber (or other man-made material) which could provide cost savings as well as weight savings.

4.4. Air distribution inside and outside the monoliths.

It is necessary that the air flow through the monoliths be as uniform as possible. In such a context, the use of ducted exhaust fans with suitably designed gas collectors to direct the air flow is useful, for example, with petrochemical-based air-cooling units.

The second factor related to air distribution involves the rate of air exit from the ring of monoliths in the decahedral system. Depending on the ratio of the height of the layer to its width, the air velocity in the air jet rising from the round hole formed from above relative to the monoliths can be high and must be taken into account in the design of the gas collectors.

4.5. The use of a single outlet gas collector with the possibility of recycling energy.

It is clear that if the size of the monoliths is reduced, it is possible to use one very large duct fan installed horizontally in a round hole from above.

- 12 040334 regarding monoliths. It would allow air to be drawn through the monoliths and then move all the air vertically out of the node. The gas collector could be above the fan to direct the air and prevent recirculation. In addition, the outlet gas collector can be designed to provide some degree of energy recovery with slight compression and then expansion, as is the case in conventional fan and gas collector cooling towers. If the amount of air moved becomes too large, then this option cannot be applied in practice.

4.6. The use of a central CO ₂ blower and a condensing unit (steam) and the number of condensers required before the CO ₂ blower.

In the current design, a condenser 240 is located upstream of the CO ₂ blower 225. It removes water and reduces the steam load on the blower. Alternatively, one central condensing unit (steam) can be used; which could handle all CO ₂ finished product streams from all single cells in multiple system vapors. This could reduce the complexity of the systems and reduce costs. However, the cost of this choice may be that each CO ₂ blower must be designed to handle the wet steam stream at a higher throughput. Each system should be evaluated to determine the most cost-effective choice.

4.7. The use of a central vacuum pump to remove CO ₂ .

During depressurization of the system and transfer of heat from the hot recovery chamber to the cold recovery chamber, a vacuum pump 230 is used to remove CO2. In the preferred design shown, a vacuum pump is connected to each regeneration chamber. Under certain circumstances, one CO2 removal vacuum pump can serve both chambers in a two-ring system. Alternatively, one large CO2 removal vacuum pump can be used to serve multiple systems. Reducing the number of vacuum pumps should reduce the capital costs associated with the system.

Preferably, the use of a liquid ring type pump seems to be advantageous since any condensate that forms will be in the liquid ring system and more easily removed.

4.8. Layer removal/sorbent replacement.

Monoliths with sorbent will be used during the whole process. This may include maintenance work on bed transfer systems (both rotational and vertical), sorbent replacement, preventive maintenance, etc. Such work may be carried out on the monoliths in working position, or they may require removal of the monoliths from the assembly. Removal of the monoliths is accomplished by installing a second lift system which can then lift the monoliths out of the guide for access. Alternatively, the monoliths may be designed to be removed using a crane. Other choices are possible.

In view of the foregoing description, it is believed that those skilled in the art will recognize various other ways of operating multilayer systems for removing carbon dioxide from a gas mixture in accordance with the principles of this application, including the use of many well known steps and components that are well known or will become well known and may be used in the practice of the present invention, not on their own, but as part of the invention. The scope of the present invention is to be determined only in accordance with the scope of the following claims.

Claims (20)

CLAIM 1. A system for removing carbon dioxide from a mixture of gases containing carbon dioxide, wherein the gas mixture containing carbon dioxide is selected from the group consisting of ambient air and mixtures with a large part of the ambient air by volume and a less significant part of the flue gas by volume, system contains: two groups of individual carbon dioxide removal structures, each individual carbon dioxide removal structure in each group comprising a porous solid support supported by the removal structure, each porous support comprising a sorbent supported by its surfaces; while the sorbent is able to adsorb or bind carbon dioxide to remove carbon dioxide from a mixture of gases; a closed continuous belt support for each group of structures to remove carbon dioxide; and a pressurized regeneration chamber at one location along each of the closed belt supports, each closed continuous belt support and a group of individual carbon dioxide removal structures supported thereon are arranged so as to allow movement of the individual carbon dioxide removal structures of each group along the closed loop relative to the sealed regeneration chamber and ensure that the gas mixture containing carbon dioxide is exposed to the flow of a mixture of gases containing carbon dioxide on individual structures for removal - 13 040334 carbon dioxide and when moving near the sealed regeneration chamber, it moves to a sealed regeneration chamber in which the structure for removing carbon dioxide can be sealed; wherein the sealed regeneration chamber further comprises a sealed pipe connecting the regeneration chamber to a source of process steam, and a pipe connected to an exhaust pump to remove gases from the regeneration chamber; wherein each of the carbon dioxide scavenging structures maintains the porous substrates in position along a closed belt support outside of the regeneration chamber so that the substrate is exposed to a flow of a gas mixture containing carbon dioxide to remove CO2 from the gas mixture; the number of structures for removing carbon dioxide relative to the number of regeneration chambers is determined directly by the ratio of the adsorption time (for removing CO2 from a mixture of gases) to the regeneration time (for separating CO2 from a sorbent on a porous substrate); moreover, the adsorption time is the time required for the adsorption of CO2 from a mixture of gases on the sorbent from the base level to the desired level on the sorbent, and the regeneration time is the time of release of CO2 from the desired level back to the base level on the sorbent, so that the ratio between the number of sealed chambers regeneration and the number of structures to remove carbon dioxide can be easily determined. 2. The system of claim 1, wherein each of the two groups of carbon dioxide removal structures comprises one regeneration chamber and five to ten carbon dioxide removal structures. 3. The system of claim 1, wherein each of the regeneration chambers and the carbon dioxide removal structures further comprises cooperating fluid seals such that when the carbon dioxide removal structure is retained in the regeneration chamber, fluid-tight seals are formed. 4. The system of claim 1, further comprising a pressurized fluid connection between each regeneration chamber and a bleed pump for reducing atmospheric pressure within the pressurized regeneration chamber after the carbon dioxide removal structure is sealed in the regeneration chamber. 5. The system of claim 4, further comprising a sealed fluid connection between each of the regeneration chambers and a process hot steam source for each regeneration chamber; and a fluid-tight connection between each recovery chamber and the CO ₂ collection chamber. 6. The system of claim 1, wherein the regeneration chamber for each group of carbon dioxide removal structures is located at a different vertical level than the carbon dioxide removal structures, further comprising a lifting device for vertical movement of the carbon dioxide removal structure from the continuous belt in a sealed position in the regeneration chamber and from said position in the regeneration chamber and back to the continuous belt support. 7. The system of claim 2 further comprising fans for sucking in ambient air for admixing into the high concentration CO2 flue gas to create a flow of a mixture of gases containing carbon dioxide through each of the carbon dioxide removal structures to allow the sorbent to adsorb CO ₂ from a mixture of gases. 8. The system of claim 1, further comprising a sealed fluid conduit between the two regeneration chambers, wherein the rotational movement of each of the two groups of carbon dioxide removal structures is shifted such that the carbon dioxide removal structure enters one of the regeneration chambers. after the start of regeneration of the structure to remove carbon dioxide in another regeneration chamber. 9. The system of claim 7, wherein the fans are stationary and placed at positions radially inward of the continuous band support such that when one of the carbon dioxide removal structures in a group of carbon dioxide removal structures is in the regeneration chamber for that group , each of the other structures for removing carbon dioxide is in a sealed position with one of the fans to receive the flow of a mixture of gases containing carbon dioxide. 10. The system of claim 7, wherein the fans are positioned radially inside the guide in a closed curve and each of the fans is attached to one of the carbon dioxide removal structures so as to move in the closed curve with its carbon dioxide removal structure. . 11. A method of removing carbon dioxide from a gas mixture containing carbon dioxide, using the system according to claim 1, and the gas mixture containing carbon dioxide is selected from the group consisting of ambient air and mixtures with a large volume of ambient air and less a significant part of the flue gas by volume, the method comprises the steps of: moving each of the at least two groups of carbon dioxide removal structures along one of at least two closed continuous loops while being exposed to a gas mixture containing carbon dioxide, each carbon dioxide removal structure in each group comprising a porous solid support, supported by the structure, with each porous - 14 040334 the substrate contains a sorbent supported on its surfaces, and the sorbent is able to adsorb or bind carbon dioxide to remove carbon dioxide from the mixture of gases; sealing the carbon dioxide removal structures in a sealed regeneration chamber located at one location along each of the continuous loops such that when the carbon dioxide removal structure is sealed in the sealed regeneration chamber, carbon dioxide sorbed on the sorbent is released from the sorbent and captured, and the sorbent is regenerated; each of the carbon dioxide removal structures supporting the porous substrates on a closed continuous loop is positioned such that the sorbent is exposed to a flow of carbon dioxide containing gas mixtures at ambient temperature to ensure removal of CO2 from the gas mixture by the sorbent, and when the structure for removal of carbon dioxide is placed in the regeneration chamber, the sorbent is subjected to process heat treatment at a temperature of less than 130°C to release CO2 from the sorbent; the number of carbon dioxide removal structures relative to the number of regeneration chambers is determined directly by the ratio of the adsorption time (for removing CO2 from a gas mixture by adsorption on a porous support) to the regeneration time (for releasing CO2 from a sorbent on a porous support), the adsorption time being the time required to adsorb CO2 from the mixture of gases on the sorbent from the base level to the desired level on the sorbent, and the regeneration time is the time required to release CO ₂ from the desired level on the sorbent back to the base level on the sorbent. 12. The method of claim 11, wherein each of the two groups of carbon dioxide removal structures comprises five to ten carbon dioxide removal structures, and wherein two regeneration chambers are placed adjacent to each other. 13. The method of claim 12, further comprising reducing atmospheric pressure in the sealed regeneration chamber after the carbon dioxide removal structure is sealed in the regeneration chamber, but before heating the sorbent with process heat. 14. The method according to claim 13, and the sorbent is heated by process heat by passing process hot steam at a temperature of not more than 130°C into the regeneration chamber after reducing atmospheric pressure in the regeneration chamber to release CO ₂ ; and passing the recovered CO ₂ from the recovery chamber to the CO ₂ collection chamber. 15. The method of claim 11, wherein the regeneration chamber for each group of carbon dioxide removal structures is located at a different vertical level than the continuous belt structure, and further comprising vertically moving the carbon dioxide removal structure to a sealed position in and out of the regeneration chamber. sealed position in the regeneration chamber. 16. The method of claim 13, wherein the movement of each of the two groups of carbon dioxide removal structures is shifted such that the carbon dioxide removal structure enters the second of the regeneration chambers after regeneration of the carbon dioxide removal structure in the first regeneration chamber is started. 17. The method according to claim 16, further comprising reducing the atmospheric pressure in the second regeneration chamber to a predetermined pressure; opening the sealed connection between the two regeneration chambers after completion of said regeneration of the carbon dioxide removal structure in the first regeneration chamber so as to exhaust the steam remaining in the first regeneration chamber to preheat the second regeneration chamber and cool the carbon dioxide removal structure in the first regeneration chamber ; and returning the cooled carbon dioxide removal structure from the first regeneration chamber back to the continuous belt device, and resuming such a cycle as the carbon dioxide removal structures move through the continuous belt device and cycle back into the regeneration chamber. 18. The method of claim 17, wherein the steam entering each regeneration chamber is at a temperature of no more than about 120°C. 19. The method of claim 18, wherein the second regeneration chamber is preheated to a temperature of no more than about 60° C. and the first regeneration chamber is cooled to a temperature below the temperature at which the sorbent undergoes deactivation upon contact with oxygen. 20. The method of claim 14 wherein the sorbent is a polymer based on a primary amine. - 15 040334