Structure and method for enhanced carbon dioxide capture from ambient air

Abstract

The improved DAC unit and method includes an adsorption structure including an array of adsorption elements, the adsorption elements including a support layer and at least one sorbent layer on either side thereof, and at least one protective layer including a microporous material disposed around the support layer and the sorbent layer, the protective layer having a higher hydrophobicity than the sorbent material, the adsorption elements being parallel to each other and spaced apart to form parallel fluid paths for the flow-through of ambient air and / or desorption medium, and the method includes the following sequential, repeated steps: (a) adsorbing by flow-through; (b) isolating the sorbent; (c) injecting a flow of desorption medium through the parallel fluid paths to induce a temperature increase; (d) extracting desorbed carbon dioxide from the unit and separating it from the desorption medium; and (e) subjecting the sorbent material to ambient temperature conditions.

Description

[Technical Field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS This application claims the benefit of U.S. Provisional Application No. 63 / 397,977, filed August 15, 2022, and U.S. Provisional Application No. 63 / 532,584, filed August 14, 2023, the disclosures of which are incorporated by reference herein in their entireties for all purposes.

[0002] Field The present disclosure relates to a method for adsorption and desorption of sorbents used in cyclic adsorption-desorption for the direct capture of carbon dioxide (CO2) from ambient air or highly dilute sources, as well as the use of such a method and a device for such a method. The present disclosure further relates to an optimized configuration of an adsorbent structure having multiple parallel surfaces and its use for the efficient capture of carbon dioxide from ambient air. [Background technology]

[0003] background Gas separation by adsorption / desorption processes, more specifically the capture of carbon dioxide from the atmosphere, so-called direct air capture (DAC), is an area of ​​growing importance as a potential means aimed at mitigating greenhouse gas impacts. While conditioning the atmosphere and CO2 during adsorption is not an energetically feasible option at typical CO2 concentrations and adsorption conditions, the conditions under which contact with the sorbent material occurs can be influenced by the configuration of the adsorbent structure. Furthermore, the conditions leading to CO2 desorption from the sorbent are significantly more diverse and complex, and these are generally based on an extensive knowledge base from other industries in the gas separation field. Widely established CO2 capture from flue gases can generally rely only on a substantial change in CO2 partial pressure or system temperature to initiate CO2 release by the sorbent. However, DAC operating at low CO2 concentrations requires a combination of various means to shift the sorbent's CO2 absorption equilibrium to achieve economically attractive operating capabilities. Therefore, new methods specifically targeted at desorption in direct air capture processes have emerged and continue to emerge along with innovations in adsorbent structures.

[0004] Generally, flue gas CO2 separation processes aim for near-complete removal of CO2 from flue gas with recovery rates exceeding 80%. To this end, the configuration maximizes contact between the sorbent and the gas stream, with pressure drop and pumping being secondary concerns. Typical configurations include packed-bed columns or fluidized beds with typical lengths ranging from tens of centimeters to several meters, typically imposing pressure drops of several thousand pascals to several bar on the gas stream. More recently, structured adsorbents have also been used to capture CO2 from flue gas, such as the structures described in WO-A-2010096916 (Boulet et al.) and WO-A-2018085927 (Inventys Thermal Technologies Inc.), which specify parallel-passage contactors for flue gas CO2 capture. These adsorbent structures in flue gas capture configurations are designed for the high concentrations of CO2 present in flue gas and operate with the goal of capturing CO2 from flue gas at high recovery rates.

[0005] More specifically, WO-A-2018085927 discloses an adsorption gas separation apparatus and method. The adsorption structure includes a first adsorbent layer having at least a first adsorbent material, a second adsorbent layer including at least a second adsorbent material, and a barrier layer, the barrier layer being interposed between the first and second adsorbent layers. A parallel passage contactor is also disclosed, including a plurality of adsorption structures, each having a barrier layer, arranged to form a first fluid passage and a second fluid passage. An adsorption process is also provided for separating at least a first component from a multicomponent fluid stream using an adsorption structure.

[0006] US-A-2015139862 (L'Air Liquide Societe Anonyme pour l'Etude et l'Exploitation des Procedes Georges Claude) discloses a structured adsorbent sheet comprising a nano-adsorbent powder and a binder material, where the nano-adsorbent powder is combined with the binder material to form an adsorbent material, and a porous electric heating substrate, where the adsorbent material is applied to the porous electric heating substrate to form the structured adsorbent sheet. A structured adsorbent module is provided, comprising a plurality of stacked structured adsorbent sheets configured to form a plurality of fluid passages, the plurality of fluid passages having a cross-sectional shape in the direction of fluid flow. The structured adsorbent module can have a trapezoidal, rectangular, square, triangular, or sinusoidal cross-sectional shape. A structured adsorbent bed is provided, comprising a plurality of modules, stacked to provide a plurality of process fluid passages and process fluid inlets and process fluid outlets in fluid communication with a plurality of process fluids.

[0007] US-A-2012076711 (ETH ZURICH) discloses a structure comprising a sorbent having amine groups capable of reversible adsorption and desorption cycles for capturing CO2 from gas mixtures, said structure consisting of fiber filaments, the fiber material being carbon and / or polyacrylonitrile.

[0008] However, the low ambient concentration of CO in direct air capture means that much larger volumes of air must be passed through the adsorption structure at ambient conditions, thus precluding the use of a full-gas capture configuration due to the large pressure drop across it. Therefore, in direct air capture CO separation processes, a configuration of the sorbent material is desired that maximizes contact between the sorbent and the gas stream to maximize the mass transfer rate of the components being removed from the gas stream while minimizing the pressure drop across the air stream to minimize the energy required for the adsorption gas pump. These configurations are very different from those required for full-gas capture. Such configurations for DAC are disclosed, for example, in WO-A-2014170184 (Climeworks AG).

[0009] Recently, various capture methods using specially designed adsorbent structures for direct air capture have been disclosed. One common method is based on a cyclic adsorption / desorption process on chemically functionalized solid sorbent materials. For example, US-A-2011041688 (Eisenberger) discloses carbon dioxide capture / regeneration structures and techniques using fluidized beds of coated granular materials. Various wall flow structures for low pressure drop flow across granular adsorbent beds are disclosed in WO-A-2018083109 (Climeworks AG) and WO-A-2018210617 (Climeworks AG). Other solutions opt for structured adsorbents, such as monoliths as used in US-A-2014004016 (Eisenberger et al.), or liquid solutions dispersed throughout the contacting device, such as in WO-A-2009155539 (1446881 Alberta Ltd.) and WO-A-2010022339 (1446881 Alberta Ltd.). Packed-bed granular contactors generally aim to distribute the flow, reducing velocity and increasing the residence time of the adsorbed air stream within the bed, to counter the typically long diffusion paths and associated slow kinetics of these structures, as in WO-A-2018083109 and WO-A-2018210617. In contrast, structured adsorbents such as WO-A-2010027929 (Alstom Technology Ltd.), WO-A-2010151271 (Sri International), and sorbents supported on a support matrix such as WO-A-2009067625 (Global Research Technologies, LLC) have shorter diffusion paths and can reduce residence times by an order of magnitude, resulting in higher rates of direct throughflow.

[0010] Structured sorbents made from multilayer sheets of adsorbent material have been investigated for many applications. An early example is shown in U.S. Pat. No. 4,234,326 (United Kingdom Secretary of State for Defence), in which a parallel-flow filter structure is constructed from alternating layers of charcoal cloth and air-permeable spaces. Further development of layered structured adsorbents for hydrogen purification using rapid PSA is described in numerous patents. U.S. Pat. Nos. 5,082,473 (Keefer), 6,451,095 (QuestAir Technologies, Inc.), and 6,692,626 (QuestAir Technologies, Inc.) describe equilibrium-controlled pressure swing adsorption (PSA) processes that can be enhanced by configuring the adsorbent as a layered adsorbent laminate sheet parallel-passage contactor structure. Here, the adsorbent material is formed into adsorbent sheets, with or without suitable reinforcement incorporated into such sheets. The specific advantages of these structures in terms of kinetic selectivity are described in detail, for example, in U.S. Patent No. 7,645,324 (Xebec Adsorbation Inc.) for the incorporation of microporous sorbents into adsorbent sheets. An example of an air recovery device including pairs of individual sheets forming lamellae designed to remove CO2 from a flow is provided in WO-A-200914292 (Korea Research Institute of Chemical Technology et al.).

[0011] Newer methods specifically aimed at desorption in direct air capture processes have provided energy to the sorbent by various other means, such as WO-A-2016005226 (Climeworks AG) and WO-A-2014170184 (Climeworks AG). The desorption method combines a temperature swing achieved through the use of a heat exchanger with a vacuum swing and a steam purge gas flow. However, conductive heating is easily controlled, avoids near-saturation instabilities (i.e., wet steam), and does not load the sorbent material with large amounts of liquid water. Conductive heat transfer through a typical granular bed of highly porous sorbent material is generally very low. Furthermore, because the heat exchanger displaces the sorbent material, power output per unit volume is significantly reduced. With structured sorbents, such as monoliths, integrating a heat exchanger is not straightforward and presents its own challenges. Prolonged heating and drying of sorbents in this manner has been shown to substantially degrade the sorbent material, reducing its CO2 absorption capacity and shortening the overall operating life of the sorbent. Combined with high costs, such solutions are not necessarily economically feasible for widespread application of DAC. The use of steam for sorbent regeneration is not new, dating back several decades, as demonstrated in GB-A-1296889 (Aaron et al.) or DE-A-3030967 (Daimler Benz AG). However, in an attempt to overcome the aforementioned problems for direct air capture purposes, pure vapor desorption processes have recently gained attention in this field.US-A-2014096684 (Kawasaki Jukogyo Kabushiki Kaisha), US-A-2018214822 (Eisenberger), WO-A-2016038339 (Johnson Matthey Public Limited Company), US-A-2011088550 (Accucaps Industries Limited), WO-A-2014063046 (ADA-ES, Inc.), US-A-2011179948 (Choi et al.), US-A-2015209718 (Eisenberger et al.), EP-A-2874727 (Antecy BV), US-A-2007149398 (Jones et al.), US-A-2014130670 See (Eisenberger et al.), US-B-7288136 (US Department of Energy), WO-A-2016037668 (Giaura BV), US-A-2018272266 (Shell Oil Company), or US-B-8500854 (US Department of Energy). These are generally reference steam processes from other industries where both saturated and superheated steam are used for sorbent regeneration. Steam desorption methods allow for rapid and uniform heating of the sorbent, but have the inherent drawback of depositing substantial amounts of water on the sorbent material. These significant amounts of additional water can hinder the continued successful circulation of the material for CO2 capture. The addition of water can reduce the transport rate within the porous sorbent material or flush out the active phase, rendering the sorbent material inactive for further CO2 capture. Therefore, the key to effective operation is a combination of process and sorbent material that allows for cyclic operation of the direct air capture plant.

[0012] Devices for such processes have also been disclosed. Apart from introducing steam from an external source into the reaction chamber, previously published devices for such desorption techniques have, for example, disclosed a steam-generating reservoir within the sorbent chamber (US-A-2014096684, WO-A-2016005226) or described the recycling of steam within a limited number of reaction chambers (US-A-2013312606 (Eisenberger)).

[0013] Aspects relevant to the cyclic operation include the adsorption conditions, the pre-regeneration preparation, the regeneration temperature and pressure level, as well as the conditions of the steam used and the post-regeneration steps. Some process-oriented disclosures mention reducing the pressure in the reaction chamber or alternatively purging with air (EP-A-2874727, WO-A-2016037668, US-A-2011296872 (Eisenberger)), but most are silent on this point. The conditions of the steam used, if any, are saturated steam (US-A-2013312606, US-B-7288136).

[0014] Sorbent temperature during regeneration is particularly important because many common CO2 sorption systems exhibit a rapid decline in cyclic CO2 capture capacity due to degradation, primarily due to oxidation from exposure to sufficiently high temperatures and exposure to oxygen at sufficiently high temperatures. On the other hand, for most sorbents, higher temperatures result in faster desorption rates and greater amounts of CO2 desorbed.

[0015] US-A-2018214822 proposes a method for directly removing carbon dioxide from ambient air using a sorbent under ambient conditions to obtain relatively pure CO2. To capture the relatively pure CO2 and regenerate the sorbent for repeated use, CO2 is removed from the sorbent at a temperature of about 130°C or less using process heat, preferably in the form of steam. Efficiency can be enhanced by mixing a small amount of effluent gas, preferably pretreated and containing a high concentration of carbon dioxide, with the ambient air before contacting the sorbent. The captured carbon dioxide can be stored for further use or permanently sequestered. This method provides purified carbon dioxide for further use in agricultural and chemical processes or for permanent sequestration. This document discloses only flow velocity values ​​at the inlet opening of the complete sorbent structure, and does not disclose information regarding flow velocity within the channels of the sorbent structure. Summary of the Invention

[0016] Abstract The use of steam as a regeneration medium is widespread because steam is an effective way to transfer heat and can be found as a by-product of other industrial processes or scavenged from geothermal sources. However, the use of liquid water can have adverse effects, such as slowing the transport rate of the porous sorbent material or potentially washing away the active phase, rendering the sorbent material inactive for further CO2 capture, as disclosed in International Publication No. WO 2021 / 239747 filed by Climeworks AG (hereinafter, the "'747 Climeworks Publication"). Furthermore, liquid water can block the pores of mesoporous structures, a condition commonly known as "water lock." Water lock can slow the kinetic rate of the sorbent and make continued operation economically unfeasible. Furthermore, moist air contains water vapor, which condenses into liquid water when cooled below the flow dew point. Depending on the process and environmental conditions, structured sorbents can also be exposed to liquid water. Although it is generally accepted that liquid water can have a detrimental effect on sorbent life and process speed, the prior art is silent on any materials or techniques to mitigate this problem.

[0017] In the present disclosure, materials, combinations of materials, and methods are provided that allow water vapor (and heat) to selectively access the sorbent. Advantageously, water vapor is evaporated to facilitate cooling while simultaneously mitigating the deleterious effects of liquid water by minimizing and / or preventing its intrusion into the sorbent layer or sorbent bed of the device, which facilitates adsorption and desorption. As disclosed herein, in some instances, such benefits may be achieved through the use of thin, durable microporous membranes that exhibit a high degree of hydrophobicity. These materials may be configured as covers, additional layers, or internal channels, as further disclosed herein.

[0018] The disclosure of the '747 Climeworks publication relates to a method and device for adsorption and desorption of a sorbent used in cyclic adsorption desorption for the direct capture of carbon dioxide (CO2) from ambient air, and the use of such a method and device. Two defining aspects of the method are the essentially exclusive or completely exclusive use of steam to provide heating energy during the desorption process, and the use of a parallel-passage contactor, the configuration and sorbent of which are preferably optimized for direct air capture, as exemplified in WO-A-2010096916 and WO-A-2018085927. To enable efficient and economical cyclic operation, it is preferable to meet a number of additional requirements, which are described in detail.

[0019] In comparison, according to some examples of the present disclosure, the adsorption and desorption device also includes at least one protective layer comprising a microporous material (which may be formed from any suitable highly hydrophobic material) disposed around the support layer and sorbent layer of the adsorption and desorption device. The protective layer is hydrophobic and has a higher hydrophobicity than the sorbent material. In some examples, the at least one support layer includes multiple lumens extending therethrough, and a desorption medium stream (which may in some examples be one or more of a high-temperature liquid, steam, saturated steam, superheated liquid, or any substance that transfers heat) is injected by flow-through through the lumens to initiate CO2 desorption. In some examples, the desorption medium stream may be saturated or superheated prior to injection. In some examples, the desorption medium stream is injected through the lumens in a direction substantially perpendicular or substantially perpendicular to the direction in which ambient air flows through the parallel fluid passages. In some examples, the lumens are interconnected to one another. In some examples, the device also includes a spacer element, which includes a sorbent material configured to facilitate adsorption and desorption through the spacer element. The spacer element increases the ratio of the sorbent mass (adsorbent mass) of the adsorbent element to the total mass of the adsorbent element. In some examples, a protective layer can be disposed around the spacer element to provide protection for the spacer element from ambient or external elements.

[0020] Advantages of the aforementioned features of the present disclosure are provided herein. For example, a hydrophobic protective layer comprising a microporous material and a spacer element comprising a sorbent material advantageously improve the adsorption and desorption process. Specifically, the hydrophobic protective layer controls liquid water access through the sorbent material, for example, by minimizing and / or preventing liquid water intrusion. The lumen allows the flow of desorption media through the support layer of the sorbent layer in addition to flowing around or through the outer surfaces of these sorbent layers. In this regard, the lumen increases the proximity of the desorption media to the adsorbent elements (e.g., the sorptive material of the sorbent layer), promoting a more aggressive adsorption / desorption process. The spacer element provides additional volume or mass of the sorbent material, increasing the ratio of the sorbent mass of the adsorbent element to the total mass of the adsorbent element and advantageously improving the adsorption and desorption characteristics of the overall device. The spacer element can further advantageously increase the density of the sorbent article without changing the occupied volume of the adsorbent structure.

[0021] Suitable and preferred sorbent bed materials for acting as sorbents suitable, adapted, or even optimized for direct air capture in the process disclosed in the '747 Climeworks publication have process circulation CO2 capacities in the range of 0.3 to 3 mmol / g and / or water absorptions of less than 70% of their own weight. These take the form of solid materials, either as a single or aggregate of continuous layers / coatings or of specific nature (typically polymeric materials), surface-modified to provide carbon dioxide adsorption and / or porous. The corresponding surface modification can be provided by impregnation, grafting, and / or bonding of corresponding functional groups, particularly primary and / or secondary amine functional groups. The sorbent material is an amine-functionalized solid sorbent or X2CO3 (where X is K, Na, Li, or a mixture thereof), preferably impregnated onto a porous granular support such as activated carbon. For example, the material can be a weakly basic ion-exchange resin and / or an amine-functionalized cellulose and / or an amine-functionalized silica and / or an amine-functionalized carbon and / or an amine-functionalized metal-organic framework and / or other amine-functionalized polymeric sorbent. Another sorbent material suitable for use with the '747 Climeworks publication can be an amine-functionalized cellulose, as described in WO 2012 / 168346 (Empa Eidgenossische Materialprufungs- Und Forschungsanstalt). Such sorbents can include different types of amino-functionalization and polymers, such as immobilized aminosilane-based sorbents as reported in US-B-8834822 (Georgia Tech Research Corporation et al.), or materials from WO-A-2011 / 049759 (Lanxess Sybron Chemicals, Inc.), which describes ion-exchange materials containing amino-alkylated bead polymers for removing carbon dioxide from industrial applications. Another possible sorbent is that of WO-A-2016 / 037668 for reversibly adsorbing CO2 from gas mixtures, where the sorbent consists of a polymeric adsorbent having primary amino functional groups.The materials may be of the type disclosed in EP 20 186 310.7 (Climeworks AG, incorporated by reference), or they may be of the type disclosed in EP 20 181 440.7 (Climeworks AG, incorporated by reference), i.e., a solid inorganic or organic non-polymeric or polymeric support material functionalized with amino functional groups capable of reversibly binding carbon dioxide on its surface, and having a specific BET surface area of ​​1 to 20 m. 2 The solid inorganic or organic non-polymeric or polymeric support material can be an organic or inorganic polymeric support, preferably an organic polymeric support, in particular a polystyrene-based material, preferably a styrene-divinylbenzene copolymer, preferably forming a sorbent material surface functionalized with a primary amine, preferably a methylamine, most preferably a benzylamine moiety, the solid polymeric support material preferably being obtained by an emulsion polymerization process, or can be a non-polymeric inorganic support preferably selected from the group consisting of silica (SiO), alumina (AlO), titania (TiO), magnesia (MgO), clay, and mixed forms thereof such as silica-alumina (SiO-AlO), or mixtures thereof.

[0022] The sorbent material of the '747 Climeworks publication in general, and / or the solid inorganic or organic, non-polymeric or polymeric support material in the above cases, can take the form of at least one of a monolith, a layer or sheet, a hollow or solid fiber, preferably a woven or non-woven structure, a hollow or solid particle, or an extrudate, preferably in the form of essentially spherical beads with a particle size (D50) in the range of 0.01 to 1.5 m, preferably in the range of 0.30 to 1.25 mm, or the solid inorganic or organic, non-polymeric or polymeric support material takes the form of solid particles embedded in a porous or non-porous matrix. Preferred sorbent layer materials at the end of step (a) exhibit a carbon dioxide loading in the range of 0.3 to 4 mmol / g, preferably in the range of 0.5 to 3.5 mmol / g, and / or have a circulation carbon dioxide capacity in the range of 0.1 to 3.5 mmol / g, preferably in the range of 0.3 to 3 mmol / g. Furthermore, the carbon dioxide absorption rate, preferably taken as an average over a period of 5 to 10 minutes, is in the range of 0.5 to 10 mmol / g / h, preferably in the range of 1 to 6 mmol / g / h.More preferably, the water absorption is less than 70% by weight, preferably less than 50% by weight.

[0023] Preferred support layers in the '747 Climeworks publication are based on metal, polymer, carbon, carbon molecular sieve and graphene material layers, or layers based on combinations of these materials.

[0024] The adsorbent structure used in the method proposed in the '747 Climeworks publication includes a number of adsorbent elements arranged in an array. Each adsorbent element is a composite of a porous support layer or sheet and at least one sorbent layer attached to the porous support so as to be accessible from both sides of the adsorbent element. The sorbent layer comprises or consists of at least one sorptive material that selectively adsorbs CO2 over other major non-condensable gases in air in the presence of moisture. In another embodiment, the adsorbent element includes a carrier or support layer on either side of which are attached a first sorbent layer and a second sorbent layer, each of which comprises at least one sorptive material that selectively adsorbs CO2 over other major non-condensable gases in air in the presence of moisture or water vapor. The design of the sheet or laminate is optimized to maximize the active adsorbent fraction (greater than 75% or greater than 60%), thereby reducing the overall contactor volume at a fixed CO2 capture capacity.

[0025] According to the present disclosure, there is also at least one protective layer comprising a microporous material disposed around the support layer and the sorbent layer, which protective layer can control the flow of a suitable desorption medium. In some examples, the protective layer also has a higher hydrophobicity than the sorbent material. Advantageously, the hydrophobic protective layer controls the access of liquid water through the sorbent material, for example, by minimizing and / or preventing the intrusion of liquid water. This is particularly beneficial when steam is used as the desorption medium.

[0026] In some examples according to the present disclosure, at least one support layer includes multiple lumens extending therethrough, and a desorption medium flow is injected through the lumens to initiate CO2 desorption. In some examples, the desorption medium flow is injected through the lumens in a direction substantially perpendicular or orthogonal to the direction in which ambient air flows through the parallel fluid passages. In some examples, the lumens are interconnected. Advantageously, the lumens allow the desorption medium flow through the support layer of the sorbent layer, providing efficient heat transfer to the sorbent while minimizing contact between the sorbent and liquid water. The lumens increase proximity to the adsorption element (e.g., the sorptive material of the sorbent layer), promoting a more aggressive adsorption / desorption process.

[0027] Additionally, the adsorption structure of the '747 Climeworks publication preferably includes spacer elements to maintain open parallel pathways throughout the structure while minimizing flow resistance through the contactor.

[0028] However, while the goal of optimizing a sheet or laminate design as disclosed in the '747 Climeworks publication is to "maximize the active sorbent fraction (greater than 75% or greater than 60%) to reduce the overall contactor volume at a constant CO capture capacity" of the sheet or laminate design, the use of inert materials for the spacer elements in the '747 Climeworks publication limits such optimization. In this regard, the present disclosure beneficially facilitates further optimization by using spacer elements made at least in part of a sorptive material configured to facilitate adsorption and desorption via the spacer elements. Advantageously, spacer elements according to the present disclosure increase the ratio of the sorbent mass of the adsorbent element to the total mass of the adsorbent element, further maximizing the active sorbent fraction possible according to the '747 Climeworks publication, thereby reducing the overall contactor volume at a constant CO capture capacity. Thus, the spacer elements disclosed herein that include a sorbent material provide additional volume or mass of sorbent material, advantageously increasing the ratio of sorbent mass of the sorbent element to the total mass of the sorbent element, thereby beneficially improving the sorption and desorption characteristics of the overall device, as described above. Additionally, in some instances, a protective layer comprising a microporous material can be disposed around the spacer element to protect the spacer element from surrounding or external elements.

[0029] The '747 Climeworks publication proposes a method for separating gaseous carbon dioxide from a gas mixture in the form of ambient air containing gaseous carbon dioxide and an additional gas different from the gaseous carbon dioxide by cyclic adsorption / desorption using a sorbent material that adsorbs the gaseous carbon dioxide. The method uses a unit including an adsorbent structure containing the sorbent material. The adsorbent structure can withstand temperatures of at least 60°C for desorption of at least the gaseous carbon dioxide, and the unit is openable to the flow-through of the gas mixture and to contact with the sorbent material for the adsorption step. According to the proposed method, the carbon dioxide recovery rate, defined as the percentage of carbon dioxide recovered from the gas mixture by the sorbent material in the adsorption step, is preferably in the range of 10 to 75%.

[0030] The adsorbent structure is also designed to withstand large variations in mechanically and chemically adsorbed water loading during periodic injection and exposure to a desorption medium such as steam. According to the '747 Climeworks publication, the adsorbent structure includes an array of individual adsorbent elements in the form of sheets or laminates, each of which includes at least one layer containing a selectively porous or permeable solid adsorbent for CO2 capture, the adsorbent elements in the array being arranged essentially parallel to one another and spaced essentially equally apart from one another to form essentially parallel fluid pathways for the flow-through of the gas mixture and / or vapor. Open spaces between the sheets are preferably maintained by inserting spacer elements attached to the adsorbent sheets.

[0031] According to the present disclosure, the spacer elements include a sorbent material configured to facilitate sorption and desorption through the spacer element. The spacer elements increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element. Advantageously, the spacer elements as disclosed herein provide additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element, thereby improving the sorption and desorption characteristics of the overall device. Furthermore, in some examples, a protective layer comprising a microporous material can be disposed around the spacer element to protect the spacer element from surrounding or external elements.

[0032] According to the '747 Climeworks publication, the adsorbent structure comprises an array of individual adsorbent elements, each of which comprises at least one, preferably porous, support layer and at least one attached or integrated (surface) sorbent layer. The adsorbent material preferably selectively adsorbs CO2 over other major non-condensable gases in air in the presence of moisture or water vapor.

[0033] Typically, in the adsorbent structures of the '747 Climeworks publication, individual but essentially identical adsorbent elements form a regularly ordered stack, with the adsorbent elements being essentially congruently positioned along the height of the stack and the distance between adjacent adsorbent elements being essentially the same throughout the stack.

[0034] The adsorbent structure of the '747 Climeworks publication takes the form of a carrier layer, preferably a porous carrier layer, flanked on both sides by at least one sorbent layer. The adsorbent structure may be based on a porous carrier layer, with one or both surface layer portions chemically modified or coated to provide CO2 adsorption properties. Additionally, the adsorbent structure may be formed with a porous carrier layer, which also has the property of acting as a sorbent.

[0035] The adsorbent elements of the '747 Climeworks publication in the array are arranged essentially parallel to one another and spaced apart from one another to form parallel fluid passageways through which gas mixtures and / or vapors pass.

[0036] Flow-through of a gas mixture in this context is generally understood as flowing along parallel fluid paths and parallel to the sorbent layer, allowing carbon dioxide to be adsorbed onto the sorbent layer. The flow rate of ambient air through the adsorbent structure, or flow-through rate, as defined herein is not the air flow rate at the inlet of the entire adsorbent structure, but the air flow rate in these parallel fluid paths in step (d), and the same applies to the flow rate of vapor through the adsorbent structure in step (d). Generally, flow-through includes at least three types of flow, as shown in FIG. 4B. The first type (e.g., flow-through 401) is flow-through that moves parallel to the surface of a structure, such as a sorbent layer or adsorbent element 5, and can include flow through a space between two structures, such as two sorbent layers (e.g., fluid path 7 between adsorbent elements 5) or opposing walls of a channel (e.g., opposing walls of lumen 102 shown in FIG. 4A). The second type (e.g., flow-through 402) is a flow-through that passes through a surface and through a material, such as a porous sorbent layer supported by the surface (e.g., through adsorbent element 5), allowing air to diffuse out the opposite surface of the structure. The first type of flow-through can change to the second type of flow-through after passing through the material, and vice versa. The third type (e.g., flow-through 403) is a flow-through that represents the overall movement of the mass of the gas mixture through the structure (e.g., adsorbent structure 6) over a given time period, and can include one or both of the first and / or second types of flow-through as described above.

[0037] Of course, in such adsorbent structures of the '747 Climeworks publication in the form of a stack, the outermost adsorbent element may have only a carrier or porous layer with at least one sorbent layer therein.

[0038] In the '747 Climeworks publication, process gas flows primarily in a direction coplanar with the sheets or laminates between the stack inlet and outlet. The solid structured sorbent typically has only two parallel faces that are open to direct the process gas stream into the structured sorbent bed and provide a means for mechanical assembly into a separation unit. Alternatively, two sets of two parallel faces may be open to flow, with one process gas, such as an adsorbed gas stream, flowing from one face to the opposite parallel face, and another process gas, such as a vapor stream, flowing from a third face to a fourth parallel face.

[0039] The method according to the '747 Climeworks publication includes at least the following steps (a) through (e) repeated in sequence and in this order:

[0040] (a) contacting said gas mixture in the form of ambient air with a sorbent material to adsorb at least said gaseous carbon dioxide onto said sorbent material by flow-through through said parallel fluid passages under ambient atmospheric pressure and temperature conditions in an adsorption step, thereby typically capturing 10% to 75% of the CO passing through the adsorption structure.

[0041] (b) isolating the sorbent containing the adsorbed carbon dioxide in the unit from ambient atmospheric flow-through while maintaining the temperature within the sorbent.

[0042] (c) injecting a flow of saturated or superheated steam by flow-through through the parallel fluid passage (4), thereby inducing an increase in the temperature of the sorbent to a temperature of 60-110°C and, optionally, an increase in the internal pressure of the reactor unit, and initiating desorption of CO2.

[0043] (d) extracting at least the desorbed gaseous carbon dioxide from said unit and separating the gaseous carbon dioxide from the steam by condensation within said unit or downstream of said unit, while contacting said sorbent material with steam by injecting and / or (partially) circulating saturated or superheated steam into said unit, thereby flashing and purging both steam and carbon dioxide from said unit, typically in a steam to carbon dioxide molar ratio of from 4:1 to 40:1, while adjusting the extraction and / or steam supply to essentially maintain the sorbent temperature at the end of the preceding step (c) and / or to essentially maintain the sorbent pressure at the end of the preceding step (c).

[0044] (e) subjecting said sorbent material to ambient atmospheric conditions.

[0045] The steam downstream of the unit of the '747 Climeworks publication is either condensed or recycled in step d), or only a portion of the steam downstream of the unit is recycled and the remainder is condensed. The control of the molar steam / CO2 ratio in step (d) can be adjusted without special effort by the corresponding inflow and pressure / temperature levels of the steam introduced into the unit and the operation of the pumps and valves of the unit, based on monitoring of this ratio by corresponding sensors in the unit and / or upstream or downstream of the unit. This ratio is also a function of the sorbent properties and the local steam flow. The given ranges refer to conditions under which desorption is considered feasible.

[0046] The throughflow of gas, specifically CO2, is adjusted to generate a partial pressure of steam to achieve the target temperature and / or pressure in step (c) according to the '747 Climeworks publication. During step (c), steam can be injected in the form of fresh steam introduced through the corresponding inlet, but steam can also be at least partially or completely recycled from the steam outlet, if necessary. Such recycling involves reheating the recycled steam. When such steam recycling is performed, at least at the end of the process, the recycled steam does not contain pure steam but also carries desorbed carbon dioxide. This adjustment is aimed at generating a partial pressure of steam to achieve the target temperature and / or pressure in step (c) in the proposed process variant. Since steam is at least partially recycled in step (c), a mixture of CO2 and steam is injected in step (c), and therefore a certain portion of gas defined by the composition of the inlet gas is preferably continuously extracted. Conversely, in a variant in which only fresh steam is supplied, CO2 preferably does not need to be extracted in step (c) until the conditions for proceeding with step (d) are met. Thus, in step (c) above, no or substantially no extraction of desorbed gaseous carbon dioxide from the unit is performed, and in situations where only fresh steam is used, the stream of saturated or superheated steam is simply injected, but when step (c) uses not only fresh steam but also recycled steam, or when only recycled steam is used, at least partial extraction of carbon dioxide during step (c) is possible, and preferably performed.

[0047] The conditions of the process of the '747 Climeworks publication are controlled in this step (c) so that the internal pressure of the reactor is increased by the injection of a saturated or superheated steam stream. The increase in pressure is due, for example, to the expansion of steam within the reactor, and typically, the pressure increase is controlled by adjusting the operation of the valves and pumps of the unit and / or the pressure and / or temperature level of the saturated or superheated steam stream injected into the unit, as known to those skilled in the art. In a typical process, the pressure increases from the level indicated in step (b) to a value in the range of 200 mbar to 1500 mbar in this step (d).

[0048] In step (a) of the first aspect, the flow velocity of the gas mixture through the adsorbent structure is in the range of 2-9 m / s or 2-8 m / s, and in at least step (d), the flow velocity of the vapor through the adsorbent structure is at least 0.2 m / s, preferably in the range of 0.3-1.0 m / s if the flow plane during adsorption is the same as the air flow plane, or preferably in the range of 1-6 m / s if the flow plane during adsorption is approximately perpendicular to the air flow. The flow velocity is defined as the average velocity of the corresponding medium in the slots (fluid passages) between the individual adsorbent elements of the adsorbent structure.

[0049] In the context of the '747 Climeworks publication, the expressions "ambient atmospheric pressure" and "ambient atmospheric temperature" refer to the pressure and temperature conditions to which a plant operating outdoors is exposed; i.e., ambient atmospheric pressure typically refers to a pressure in the range of 0.8 to 1.1 bar (abs), and ambient atmospheric temperature typically refers to a temperature in the range of -40 to 60°C, more commonly -30 to 45°C. The gas mixture used as the input to the process is ambient air, i.e., air at ambient atmospheric pressure and temperature, which typically has a CO2 concentration in the range of 0.03 to 0.06% by volume. However, air with lower or higher CO2 concentrations can also be used as the input to the process, e.g., concentrations of 0.1 to 0.5% by volume; generally speaking, the input CO2 concentration of the input gas mixture is preferably in the range of 0.01 to 0.5% by volume.

[0050] According to a preferred embodiment of the '747 Climeworks publication, in step (a), the flow rate of the gas mixture through the adsorbent structure is in the range of 1 to 6 m / sec.

[0051] According to yet another preferred embodiment of the '747 Climeworks publication, at least in step (d), the flow rate of the vapor through the adsorbent structure is in the range of 0.3 to 6 m / sec.

[0052] At least in step (d), when the flow of the gas mixture in step (a) and the flow of the vapor in step (d) are along essentially the same flow path, the flow rate of the vapor through the adsorbent structure can be in the range of 0.3 to 1.0 m / sec.

[0053] At least in step (d), when the flow of the gas mixture in step (a) and the flow of the vapor in step (d) are along different flow paths, and more preferably when the flow of the vapor in step (d) is essentially perpendicular to the flow of the gas mixture in step (a), the flow velocity of the vapor through the adsorbent structure can be in the range of 1 to 6 m / s.

[0054] Another second or additional characterization of the '747 Climeworks process is not by the flow rates of the vapor and gas mixtures, but by the specific flow rates of the corresponding streams.

[0055] The calculated flow rate conditions can be summarized as follows: JPEG2025529036000002.jpg116154

[0056] Thus, in step (a), the specific flow rate of the gas mixture passing through the adsorption structure as a function of the mass of the sorbent is between 20 and 10,000 m 3 / h / kg, preferably 30 to 9,000 or 100 to 7,000 m 3 / h / kg range, these values ​​should generally be understood as the average value of the specific flow rate of the gas mixture over the time range of step (a).

[0057] In step (a), the specific flow rate of the gas mixture passing through the adsorbent structure is between 4,000 and 500,000 m as a function of the volume of the sorbent. 3 / h / m 3 range, preferably 5,000 to 450,000 or 10,000 to 300,000 m 3 / h / m 3 can be adapted to the range

[0058] At least in step (d), the specific flow rate of the vapors through the adsorption structure can be adapted as a function of the mass of sorbent to a range of 1 to 500 kg / h / kg, preferably 2 to 300 or 50 to 250 kg / h / kg, and these values ​​should generally be understood as the average value of the specific flow rate of the vapor mixture over the time range of the respective step.

[0059] At least in step (d), the specific flow rate of the vapor through the adsorbent structure is between 200 and 15,000 kg / h / m as a function of the volume of the sorbent. 3 range, preferably 300 to 14,000 or 500 to 10,000 kg / h / m 3 can be adapted to be in the range

[0060] In particular, in the DAC recovery process of the '747 Climeworks publication, the carbon dioxide recovery rate, defined as the percentage of carbon dioxide recovered from the gas mixture by the sorbent material in the adsorption step, can be in the range of 10 to 75%, preferably in the range of 30 to 60%. Alternatively or additionally, the amount of carbon dioxide recovered on the sorbent per gram of sorbent can be at least 0.1 or in the range of 0.1 to 1.8 mmol / g for an adsorption time of at least 5 minutes or at least 10 minutes. Alternatively, characterized, the normalized amount of carbon dioxide recovered on the sorbent per gram of sorbent per hour can be in the range of 0.5 to 10 mmol / g / h, preferably in the range of 1 to 6 mmol / g / h.

[0061] The carrier layer of the '747 Climeworks publication can optionally comprise at least one of a metal, a polymer, carbon, a carbon molecular sieve, and a graphene material. The first sorbent layer comprises a first sorbent material and the second sorbent layer comprises a second sorbent material, and the first sorbent material and the second sorbent material can have different material or chemical compositions and / or physical properties.

[0062] In a preferred embodiment of the '747 Climeworks publication, the adsorbent structure comprises an array of individual adsorbent elements, each element comprising at least one layer comprising a selectively porous / permeable solid adsorbent for CO2 capture, the adsorbent elements in the array being arranged essentially parallel to one another and spaced essentially equally apart from one another to form parallel fluid pathways for the flow-through of gas mixtures and / or vapors. Open spaces between the sheets can be maintained by inserting spacer elements attached to the adsorbent elements.

[0063] In the present disclosure, the spacer elements include a sorbent material configured to facilitate adsorption and desorption through the spacer element. The spacer elements increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element. Advantageously, the spacer elements as disclosed herein provide an additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element, thereby improving the adsorption and desorption characteristics of the overall device. Furthermore, in some examples, a protective layer comprising a microporous material can be disposed around the spacer element to protect the spacer element from surrounding or external elements.

[0064] This concept, in another embodiment of the '747 Climeworks publication, can include an adsorption element including a first sorbent layer and a second sorbent layer, the first sorbent layer and the second sorbent layer being juxtaposed.

[0065] In a further preferred embodiment of the '747 Climeworks publication, the above-described adsorbent elements are arranged in a parallel passage contactor comprising a plurality of adsorbent elements as described above, the plurality of elements forming parallel fluid passages, each passage being bounded at least in part by the first sorbent layer of one adsorbent element and at least in part by the second sorbent layer of an adjacent adsorbent element.

[0066] Preferably, in the '747 Climeworks publication, the spacing between the adsorbent elements (height of the fluid passage between the adsorbent elements) is in the range of 0.2 to 5 mm, more preferably in the range of 0.4 to 3 mm.

[0067] In the present disclosure, spacing between adsorbent elements is maintained using spacer elements comprising a sorbent material configured to facilitate adsorption and desorption through the spacer elements. The spacer elements increase the ratio of the sorbent mass of the adsorbent element to the total mass of the adsorbent element. Advantageously, the spacer elements as disclosed herein provide additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the adsorbent element to the total mass of the adsorbent element, thereby improving the adsorption and desorption characteristics of the overall device. Furthermore, in some instances, a protective layer comprising a microporous material can be disposed around the spacer elements to protect the spacer elements from surrounding or external elements.

[0068] More preferably, in the '747 Climeworks publication, each adsorber element has a planar shape with a thickness (perpendicular to the plane) in the range of 0.1 to 1 mm, preferably 0.2 to 0.5 mm.

[0069] In the present disclosure, the 0.2-0.5 mm flat surface is surrounded by at least one protective layer comprising a hydrophobic microporous material, which may include, for example, a lumen formed through the adsorbent element flat surface such that the lumen is parallel to the surface of the adsorbent element flat surface. Advantageously, the hydrophobic protective layer controls liquid water access through the adsorbent material of the adsorbent element flat surface, for example, by minimizing and / or preventing liquid water intrusion. This is particularly beneficial when using steam or high-temperature liquids (or other types of heat transfer fluids in liquid form) as the desorption medium. In this regard, the lumen increases the proximity of the desorption medium (and heat) to the adsorbent element flat surface, promoting a more aggressive adsorption / desorption process.

[0070] The above-described embodiment of the adsorbent structure of the '747 Climeworks publication is incorporated into a gas separation process for removing at least one first component from a multi-component gas stream, and more specifically into an adsorption / desorption process for removing and recovering CO2 in high purity from ambient air, and possibly also removing and recovering a second component, gaseous water. The proposed method includes at least the following steps, repeated in sequence and in this order, performed using the adsorbent structure in a reactor unit:

[0071] (a) Adsorption: contacting the multicomponent gas mixture with multiple sorbent layers at the boundaries of a parallel fluid structure formed by a plurality of adsorbent elements and forcing the multicomponent fluid from the inlet side of the adsorption structure to the outlet side of the adsorption structure, thereby allowing at least the first component, preferably gaseous carbon dioxide, and possibly a second component, possibly gaseous water, to be adsorbed onto the sorptive material of the sorbent layers at the boundaries of the parallel passages under ambient atmospheric pressure and temperature conditions in the adsorption process.

[0072] This step in the '747 Climeworks publication is a flow-through adsorption step, typically carried out in a unit having two doors at opposite ends of the unit, both open during this process step, whereby a fan or ventilation device directs the flow of the multicomponent gas stream through parallel flow paths, and the pressure drop across the adsorption structure is typically 200 Pa to 1200 Pa, more preferably 200 Pa to 750 Pa or 200 Pa to 600 Pa, for a duration of 5 minutes to 40 minutes, preferably 10 minutes to 20 minutes, with an average fluid velocity in the parallel fluid flow paths of 2 m / s to 9 m / s, more preferably 4 m / s to 6 or 7 m / s. In embodiments, this step is referred to as Step (1).

[0073] (b) Isolation: Isolating the adsorbent structure containing the adsorbed components, preferably carbon dioxide, in the unit from the flow-through while maintaining the sorbent temperature, and then optionally evacuating the unit to a pressure in the range of 20-200 mbar (abs) or 700-1000 mbar (abs). When performed with a unit as described in the previous paragraph, this means that in a first substep (referred to in the embodiments as step (2)), the two doors are first closed, and then a vacuum is applied in a second (optional) substep within this step (b) (referred to in the embodiments as step (3)). In the embodiment shown in FIG. 11, no vacuum was applied, so no evacuation was applied and the adsorbent structure can be maintained essentially at ambient atmospheric pressure in step (a) or within ±100 mbar thereof.

[0074] (c) Heating: Inject a saturated or superheated steam stream, thereby inducing an increase in the internal pressure of the reactor unit (only before vacuum is applied in step (b)), in either case raising the temperature of the adsorbent structure, typically from ambient air temperature to a temperature of 60-110°C, and initiating CO2 desorption. The injected steam stream should be sufficient to bring the adsorbent structure to the desired temperature within 0.5-15 minutes, preferably 0.5-10 minutes. In embodiments, this step is referred to as step (5).

[0075] What is important about this step (c) of the '747 Climeworks publication is that the heating of the adsorbent structure occurs solely through contact with this saturated or superheated vapor stream, without the introduction of additional heat, for example, through internal or external heat exchange elements. Thus, when the vapor contacts the adsorbent structure, it is simultaneously heated and the desorption process begins. During this step (c), vapor can be injected in the form of fresh vapor introduced through a corresponding inlet; however, if necessary, vapor can also be recycled through a vapor outlet, with such recycling entailing reheating of the recycled vapor. When such vapor recycling is performed, the recycled vapor, at least at the end of the process, is not pure vapor but also carries desorbed carbon dioxide.

[0076] (d) Extraction: Extracting at least the desorbed gaseous carbon dioxide from the unit and separating the gaseous carbon dioxide from the vapor by condensing within the unit or downstream of the unit. The injected vapor stream should be sufficient to extract an economically viable amount of CO2 within 0.5 to 15 minutes, preferably 0.5 to 10 minutes. In an embodiment, this step is referred to as step (6).

[0077] During this step (d), preferably still saturated or superheated steam is injected into the unit or circulated through the unit as described above, thereby flushing and purging both steam and CO2 from the unit.

[0078] Step (d) is typically carried out at a steam to carbon dioxide molar ratio of between 4:1 and 40:1 (preferably calculated as a cumulative value over the entire process, thus taking the total steam and CO2 during the process), and is so controlled by adjusting the extraction and / or steam supply, essentially maintaining the temperature at the sorbent at the end of the preceding step (c).

[0079] Typically, in this step (d), the temperature in the unit is maintained at a level within ±20°C, preferably within ±10°C or ±5°C, of ​​the temperature of the sorbent at the end of the preceding step (c).

[0080] Alternatively or additionally, the process in step (d) can be controlled so that the pressure in the unit at the end of the preceding step (c) is essentially maintained, meaning that the pressure in the unit is maintained at a level within ±0.2 bar, preferably within ±0.1 bar, of the pressure in the unit at the end of the preceding step (c). (e) Bringing the adsorbent structure to ambient atmospheric pressure and temperature conditions, preferably by opening the door of the adsorbent structure in a first sub-step (referred to in an embodiment as step (8)) and flushing with the gas mixture in the form of ambient air in a second sub-step (referred to in an embodiment as step (9)).

[0081] According to a preferred embodiment of the '747 Climeworks publication, after step (d) and before step (e), the following steps are performed:

[0082] (d1) Stopping the steam injection and, if used, the steam circulation, and evacuating the unit to a pressure value of 20 to 500 mbar (abs), preferably in the range of 50 to 250 mbar (abs) within the unit, thereby evaporating water from the sorbent and drying and cooling the sorbent. In an embodiment, this step is referred to as step (7).

[0083] This step (d1) is preferred because it unexpectedly combines two effects in a single step: the sorbent must be cooled back to ambient conditions after steam treatment, but more importantly, it must also be dried. This step combines these two features in one treatment step, making the process faster and more economical. Adequate drying has been shown to be important for the successful operation of such processes, which rely on fast reaction rates resulting from short diffusion lengths.

[0084] After step (b) and before step (c), the following step can be carried out: (b1) flushing the unit with non-condensable gas by means of a non-condensable vapor stream while essentially maintaining the pressure of step (b), preferably while maintaining the pressure of step (b) within a range of ±50 mbar, preferably within a range of ±20 mbar, and / or while maintaining the temperature below 75°C or below 70°C or below 60°C, preferably below 50°C.

[0085] In a further embodiment of step b1 of the '747 Climeworks publication, the temperature of the adsorbent structure is increased from the conditions of step (a) to a range of 80 to 110°C, preferably 95 to 105°C.

[0086] In embodiments, this step in '747 Climeworks is referred to as step (4).

[0087] In step (b1), while maintaining the pressure of step (b1), the unit is flushed with saturated steam or steam superheated by up to 20°C at a rate of 0.3 to 13.3 kg / h or 1 kg / h to 10 kg / h of steam per liter volume of adsorption structure, preferably to purge the remaining ambient air from the reactor. The purpose of removing this portion of the ambient air is to improve the purity of the recovered CO2.

[0088] In step (c), steam can be injected in the form of steam introduced from the corresponding inlet of the unit, or steam can be recycled from the outlet of the unit to the inlet, preferably with reheating of recycled steam or by recycling steam from a different reactor.

[0089] In step (c), more preferably, the sorbent may be heated to a temperature in the range of 80 to 110°C or 80 to 100°C, preferably to a temperature in the range of 85 to 98°C.

[0090] According to yet another preferred embodiment of the '747 Climeworks publication, in step (c) the pressure in the unit is in the range of 700 to 950 mbar (abs), preferably in the range of 750 to 900 mbar (abs).

[0091] According to yet another preferred embodiment of the '747 Climeworks publication, in step (c), the pressure of the unit varies from the pressure of step (b) by less than + / - 100 mbar, more preferably by less than + / - 50 mbar. Particularly efficient release and removal of carbon dioxide is surprisingly possible when vapor passes through the adsorbent structure and the sorbent layer contained therein at particularly high velocities (typically while keeping the volumetric flow rate the same as in conventional processes). This high-velocity vapor purge can be carried out very efficiently in that the vapor of steps (c) and / or (d) takes a different path from the air flow in the parallel passages during adsorption in step (a), increasing the local vapor velocity within the parallel passages of the adsorbent structure during desorption. Preferably, and very efficiently, the overall flow paths during adsorption in step (a) and during vapor injection in steps (c) and / or (d) can be selected to be essentially orthogonal. Along these lines, according to another preferred embodiment, in step (c) and / or step (d), the flow velocity of the vapor within the adsorption structure is 0.1 m / s or more in the adsorption flow direction, preferably in the range of 0.3 to 1 m / s, and more preferably in the range of 1 to 6 m / s in the flow direction perpendicular to the adsorption flow direction.

[0092] As noted above in the '747 Climeworks publication, the flow-through of the gas mixture herein should generally be understood as flowing along parallel fluid paths and parallel to the sorbent layer, allowing carbon dioxide to be adsorbed onto said sorbent layer. Typically, the sorbent structure provides a stack of flow-through slots, the boundaries of which are provided by the layer of sorbent material. During adsorption in step (a), the ambient air stream flows through these slots in a first direction. During steps (c) and / or (d), the flow direction can be the same as during step (a), but is preferably provided as a counterflow through the flow-through slots, or as a flow in a direction perpendicular to the flow-through direction during adsorption in step (a). In step (a), in the situation where the flow-through slots between the sorbent layers are laterally bounded by side walls and the inlet and outlet sides of the flow-through slots are open during adsorption in step (a), this can be achieved by providing openings for the vapor inlet and outlet, respectively, on the opposite side walls while closing the inlet and outlet sides that are open during adsorption in step (a). Thus, different paths for adsorption and vapor injection can actually be achieved by providing a unit with a housing structure. The housing structure has a short flow-through length along a first direction, which is the adsorption flow-through direction, and a long flow-through length along a second, preferably perpendicular, direction, which is the vapor desorption flow-through direction. This is particularly to ensure maximum contact with the sorbent as the vapor passes through the unit. To this end, the unit can have large openings at both ends in the adsorption flow-through direction, which are open during adsorption and closed during desorption, and smaller openings in the opposing peripheral side walls of the unit that are closed during adsorption and open during desorption to allow the desorption vapor to pass in a direction perpendicular to the adsorption direction.

[0093] As noted above in the '747 Climeworks publication, the unit is preferably capable of maintaining a vacuum pressure of 400 mbar (abs) or less, step (b) preferably comprises isolating the sorbent containing adsorbed carbon dioxide in the unit from the flow-through while maintaining a temperature within the sorbent, and then evacuating the unit to a pressure in the range of 20 to 400 mbar (abs), and step (e) comprises subjecting the sorbent material to ambient atmospheric pressure and temperature conditions, preferably following step (d) and prior to step (e):

[0094] According to yet another preferred embodiment of the '747 Climeworks publication, step (d1) comprises stopping the steam injection and, if used, steam circulation, and evacuating the unit to a pressure value within the unit in the range of 20 to 500 mbar (abs), preferably 50 to 250 mbar (abs), thereby evaporating water from the sorbent and drying and cooling the sorbent.

[0095] Step (c) can be carried out simply by contacting the gas mixture with a sorbent material under ambient atmospheric pressure and temperature conditions, allowing water within the unit to evaporate and be removed, bringing the sorbent material to ambient atmospheric temperature conditions.

[0096] Preferably, in the '747 Climeworks publication, the gas mixture of step (a) flows through the parallel fluid passages essentially along a first direction, and the vapor in at least one or both of steps (c) and (d) flows essentially along the same first direction or essentially along a direction opposite to the first direction.

[0097] Alternatively, in the '747 Climeworks publication, the gas mixture in step (a) flows through the parallel fluid passages essentially along a first direction, and the vapor in at least one or both of steps (c) and (d) flows through the parallel fluid passages essentially along a direction perpendicular to the first direction.

[0098] Furthermore, the '747 Climeworks publication relates to a device for carrying out a method for separating gaseous carbon dioxide from a gas mixture in the form of ambient air comprising gaseous carbon dioxide and a further gas different from said gaseous carbon dioxide by cyclic adsorption / desorption using a sorbent material that adsorbs gaseous carbon dioxide, as detailed above.

[0099] The device of the '747 Climeworks publication comprises a steam source, at least one unit comprising an adsorbent structure with the adsorbent material, wherein the adsorbent structure is heatable to a temperature of at least 60°C for desorption of at least the gaseous carbon dioxide, the unit is openable to the flow-through of a gas mixture and to contact the gas mixture with the adsorbent material for the adsorption step, wherein the adsorbent structure is as described above, i.e., preferably comprises an array of individual adsorbent elements, each of which comprises a porous support layer and is attached to or integral with at least one sorbent layer comprising or consisting of at least one adsorbent material, or a central carrier layer and at least one sorbent layer comprising or consisting of at least one sorptive material on either side thereof, wherein the adsorbent elements in the array are arranged essentially parallel to one another and spaced apart from one another to form parallel fluid paths for the flow-through of the gas mixture and / or vapor, and at least one device, preferably a condenser, for separating carbon dioxide from water.

[0100] In addition to at least one sorbent layer including at least one sorptive material, the present disclosure also provides at least one protective layer including a microporous material disposed around the porous support layer and the sorbent layer. The protective layer can have a higher hydrophobicity than the sorptive material. Advantageously, the hydrophobic protective layer controls liquid water access through the sorptive material, for example, by minimizing and / or preventing liquid water intrusion. This is particularly beneficial when steam is used as the desorption medium.

[0101] More specifically, the '747 Climeworks publication relates to devices for adsorption and desorption of sorbents used in cyclic adsorption-desorption for the direct capture of carbon dioxide (CO2) from ambient air, independent of the above-mentioned methods, as well as uses of such methods and devices for such methods.

[0102] While much of the experience with DAC processes comes from flue gas capture, a fundamental difference is the source of CO2, which essentially determines the vast differences in the solutions for both tasks. The low CO2 concentration in ambient air compared to flue gas means that large volumes of air must be moved to capture significant amounts of CO2. Therefore, to ensure that the energy required to move said air is not prohibitively high, adsorption structures with low pressure drops are required. At the same time, as in the case of flue gas capture, it is not necessary to guarantee near-complete capture of CO2 by the system with a recovery rate of 80% or more. With air capture, recovery rates well below 70% are feasible, as long as the pressure drop is low, providing another incentive to prioritize structures with fast loading.

[0103] The pressure drop across such an adsorbent structure can be estimated by the following formula:

number

[0104] Based on calculations, as further detailed below, functional relationships can be established, allowing for the dimensioning of an adsorbent structure comprising an array of individual adsorbent elements in the form of a sheet or laminate, each comprising at least one layer comprising a selectively porous or permeable solid sorbent for CO2 capture, the adsorbent elements in the array being arranged essentially parallel to one another and spaced essentially equally apart from one another to form essentially parallel fluid pathways for the flow-through of gas mixtures and / or vapors.

[0105] Correspondingly, the '747 Climeworks publication proposes a device for separating gaseous carbon dioxide from a gas mixture in the form of ambient air, comprising gaseous carbon dioxide and a further gas different from said gaseous carbon dioxide, by cyclic adsorption / desorption using a sorbent material that adsorbs gaseous carbon dioxide. Preferably, this device can be used in the above process.

[0106] The device comprises a vapor source, at least one unit comprising an adsorption structure comprising said sorbent material, wherein said adsorption structure is suitable and adapted to withstand a temperature of at least 60°C for desorption of at least said gaseous carbon dioxide, said unit being openable to the flow-through of the gas mixture and to contact the gas mixture with the sorbent material for the adsorption step.

[0107] The adsorbent structure comprises an array of individual adsorbent elements in the form of layers, each adsorbent element comprising at least one sorbent layer, the adsorbent elements in the array being arranged essentially parallel to one another and spaced essentially equally apart from one another to form parallel fluid paths for ambient air and / or vapor flow-through, the individual adsorbent elements having an element length L along the direction of ambient air flow-through in adsorption step (a), and an element thickness b along a direction perpendicular to the flow-through direction. element The spacing between the adsorption elements is a spacing width b spacer and at least one device for separating carbon dioxide from water.

[0108] According to the first characteristic feature of the '747 Climeworks publication, the gap width b spacer (The height of the fluid passage between the adsorption elements) is in the range of 0.4 to 5 mm, and the element length L is in the range of 100 to 3000 mm.

[0109] According to the '747 Climeworks publication, the open space between the sheets is preferably maintained by the insertion of spacer elements attached to the suction sheets.

[0110] In the present disclosure, the spacer elements include a sorbent material configured to promote sorption and desorption through the spacer element. The spacer elements increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element. Advantageously, in addition to maintaining open space between sheets, the spacer elements disclosed herein provide additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element, thereby improving the sorption and desorption characteristics of the overall device. Furthermore, in some examples, a protective layer comprising a microporous material can be disposed around the spacer element to protect the spacer element from ambient or external elements.

[0111] Typically, in an adsorbent structure, individual but essentially identical adsorbent elements form a regularly ordered stack, with the adsorbent elements being essentially congruently arranged along the height of the stack and the distance between adjacent adsorbent elements being essentially the same throughout the stack.

[0112] According to the '747 Climeworks publication, the adsorption structure includes an array of individual adsorption elements. Each adsorption element is a composite of a porous support layer or sheet and at least one sorbent layer attached to the porous support so as to be accessible from both sides of the adsorption element. The sorbent layer comprises or consists of at least one sorptive material that selectively adsorbs CO2 over other major non-condensable gases in air in the presence of moisture. In another embodiment of the '747 Climeworks publication, the adsorption element includes a carrier or support layer and includes a first sorbent layer and a second sorbent layer attached to either side of the carrier, each sorbent layer consisting of at least one sorptive material that selectively adsorbs CO2 over other major non-condensable gases in air in the presence of moisture or water vapor. The design of the sheet or laminate is optimized to maximize the active adsorbent fraction (greater than 60%), thereby reducing the overall contactor volume at a given CO2 capture capacity.

[0113] In the present disclosure, at least one protective layer comprising a microporous material is disposed around the support layer and the sorbent layer, the protective layer having a higher hydrophobicity than the sorbent material. In some examples, the porous support layer and the sorbent layer can each be individually covered or surrounded by a protective layer. In some examples of the present disclosure, a protective layer can be disposed around the carrier or support layer and the first sorbent layer and the second sorbent layer. Advantageously, the hydrophobic protective layer controls the access of liquid water through the sorbent material of the sorbent layer, for example, by minimizing and / or preventing the intrusion of liquid water. This is particularly beneficial when steam is used as the desorption medium.

[0114] In the '747 Climeworks publication, the individual adsorbent elements are in the form of sheets or laminates, each comprising at least one layer containing a selectively porous or permeable solid adsorbent for CO2 capture, and the adsorbent elements in the array are arranged essentially parallel to one another and are essentially evenly spaced from one another to form essentially parallel fluid pathways for the flow-through of gas mixtures and / or vapors. Open spaces between the sheets are preferably maintained by inserting spacer elements attached to the adsorbent sheets.

[0115] In the present disclosure, the spacer elements include a sorbent material configured to facilitate sorption and desorption through the spacer element. The spacer elements increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element. Advantageously, in addition to preserving open space between sheets, the spacer elements disclosed herein provide additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element, thereby improving the sorption and desorption characteristics of the overall device. Furthermore, in some instances, a protective layer comprising a microporous material can be disposed around the spacer element to provide protection from elements around or outside the spacer element.

[0116] According to the '747 Climeworks publication, the adsorbent structure preferably comprises an array of individual adsorbent elements, each of which comprises at least one preferably porous support layer and at least one attached or integrated (surface) sorbent layer. The adsorbent material preferably selectively adsorbs CO2 over other major non-condensable gases in air in the presence of moisture or water vapor.

[0117] The adsorbent structure can take the form of a carrier layer, preferably a porous carrier layer, with at least one sorbent layer on either side. The adsorbent structure may be based on a porous carrier layer, with one or both surface layer portions chemically modified or coated to provide CO2 adsorption properties. Additionally, the adsorbent structure may be formed by a porous carrier layer that also has the property of acting as a sorbent.

[0118] The adsorbent elements in the array are arranged essentially parallel to one another and spaced apart to form parallel fluid paths for the flow-through of the gas mixture and / or vapor. Of course, in such an adsorbent structure in the form of a stack, the outermost adsorbent element may have only a carrier layer and at least one sorbent layer inside.

[0119] The gap width is preferably in the range of 0.4 to 5 mm, and more preferably in the range of 0.4 to 3 mm or 0.5 to 3 mm.

[0120] The element length (L) is preferably in the range of 100 to 3000 mm, more preferably in the range of 200 to 2000 mm.

[0121] In simplified terms, the above equation can be reformulated to express the length L as a function of other parameters, namely:

number

number

[0122] This is the global parameter K global can be further simplified using

[0123] Therefore, the element length (L in [mm]) is preferably equal to the spacing width (b in "mm"). spacer ) and element thickness (b in "mm" element is given as a function of the thickness of the adsorbent element measured in a direction perpendicular to the plane of the parallel fluid passages) by the following equation:

number

[0124] The above formula allows specifying a range of lengths according to technically feasible operating conditions with pressure drops technically achievable by fans or ventilation devices. This range of lengths is technically feasible for CO2 capture from ambient air. Preferably, K is used, especially in devices with axial fans to drive the airflow through the adsorption structure. global is in the range of 70 to 1000 mm, preferably 400 to 800 mm -1 The range is.

[0125] In a device with a radial fan for propelling airflow through an adsorption structure, K global is preferably 200 to 2000 mm -1 range, preferably 800 to 1500 mm -1In devices with more powerful fans (such as multi-stage axial or radial fans) to propel the airflow through the adsorption structure, the K global is typically 500 to 2500 mm -1 range, preferably 1000 to 2000 mm -1 The range is.

[0126] In the above formula, preferably b element is in the range of 0.1 to 1 mm, preferably in the range of 0.1 to 0.5 mm, and / or b spacer is in the range of 0.4 to 5 mm, preferably in the range of 0.5 to 3 mm.

[0127] Typically, the adsorbent element of the '747 Climeworks publication comprises a central, preferably porous, support layer composited on either side with at least one sorbent layer.

[0128] In the present disclosure, at least one protective layer comprising a microporous material is disposed around the support layer and the sorbent layer, the protective layer having a higher hydrophobicity than the sorbent layer. Advantageously, the hydrophobic protective layer controls liquid water access through the sorptive material on both sides of the support layer and the sorbent layer, for example, by minimizing and / or preventing liquid water intrusion. This is particularly beneficial when steam is used as the desorption medium.

[0129] The adsorbent structure of the '747 Climeworks publication preferably comprises an array of individual adsorbent elements, each of which is preferably a composite of a porous support layer and at least one porous and / or permeable sorbent layer having chemically bonded carbon dioxide capture moieties, preferably in the form of amine groups, said porous sorbent layer preferably in the form of a woven or non-woven fiber-based structure.

[0130] Preferably, the carrier support layer of the '747 Climeworks publication is based on at least one of metal, polymer, carbon, carbon molecular sieve, and graphene materials.

[0131] The adsorbent elements in the array of the '747 Climeworks publication are arranged essentially parallel to one another and spaced apart by spacer elements to form parallel fluid passageways for the flow-through of ambient air and / or vapor.

[0132] In the present disclosure, the spacer elements comprise a sorbent material configured to facilitate adsorption and desorption through the spacer elements. The spacer elements increase the ratio of the sorbent mass of the sorbent elements to the total mass of the sorbent elements. Advantageously, in addition to maintaining the parallel arrangement of the sorbent elements in the array, the spacer elements disclosed herein provide additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the sorbent elements to the total mass of the sorbent elements, thereby improving the adsorption and desorption characteristics of the overall device. Furthermore, in some examples, a protective layer comprising a microporous material can be disposed around the spacer elements to protect the spacer elements from surrounding or external elements.

[0133] Preferably, in the '747 Climeworks publication, the spacing between layers is in the range of 0.2 to 5 mm, more preferably in the range of 0.4 to 3 mm, and more preferably, each adsorptive element has a planar shape with a thickness in the range of 0.1 to 1 mm, preferably in the range of 0.2 to 0.5 mm.

[0134] The device for separating carbon dioxide from water can be a condenser.

[0135] The device for separating carbon dioxide from water, preferably the gas outlet side of the condenser, may be provided with at least one, preferably both, of a carbon dioxide concentration sensor and a gas flow sensor for controlling the desorption process. Preferably, the device is suitable and adapted so that, in adsorption step (a), the flow velocity of ambient air through the adsorption structure is in the range of 2 to 9 m / s as described above. In terms of structural features, this is achieved in that the spacing width (height of the fluid passage between the adsorption elements) and element length are within the ranges further specified above, and that means for propelling the ambient air are provided to enable that flow velocity within the adsorption structure.

[0136] The flow rate is defined as the average velocity of the corresponding medium in the slots (fluid passages) between the individual absorbent elements of the adsorbent structure. Alternatively or additionally, in the vapor flow-through step (d), the vapor flow rate through the adsorbent structure is suitable and adapted to be in the range of at least 0.2 m / s. Also, in terms of structural features, this is achieved by having spacing widths (heights of the fluid passages between the adsorbent elements) and element lengths within the ranges further defined above, and by providing propulsion means that enable that flow rate within the adsorbent structure.

[0137] More preferably, the device is suitable and adapted such that in the adsorption step (a) the flow velocity of ambient air through the adsorbent structure is in the range of 4 to 6 m / s, or in the vapor flow-through step (d) the flow velocity of vapor through the adsorbent structure is in the range of 0.3 to 6 m / s.

[0138] According to yet another preferred embodiment of the '747 Climeworks publication, the device includes means for directing vapor in the vapor flow-through step (d) along a flow direction that is different from the flow direction of the ambient atmosphere flow-through direction in the adsorption step (a), preferably along a flow direction that is perpendicular to the flow-through direction of the ambient atmosphere in the adsorption step (a).

[0139] Preferably, at least in the vapor flow-through step (d), the flow velocity of the vapor through the adsorbent structure is in the range of 1 to 6 m / s when the flow of ambient air in step (a) and the flow of vapor in step (d) are along different flow paths, and more preferably when the flow of vapor in step (d) is essentially perpendicular to the flow of ambient air in step (a).

[0140] Additionally, the '747 Climeworks publication relates to the use of a device as described above for direct air capture.

[0141] The adsorption structure used in this method comprises a plurality of adsorption elements arranged in an array, each containing at least one sorbent layer that selectively adsorbs CO2 over other major non-condensable gases in air in the presence of moisture or water vapor. The design of the sheet or laminate is optimized to maximize the active sorbent fraction (greater than 60% or 75%), thereby reducing the overall contactor volume for a given CO2 capture capacity.

[0142] Additionally, and preferably, in the '747 Climeworks publication, the structured sorbent includes spacer elements to maintain open parallel passageways throughout the structure while minimizing flow resistance through the contactor.

[0143] In the present disclosure, the spacer elements comprise a sorbent material configured to promote sorption and desorption through the spacer elements. The spacer elements increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element. Advantageously, in addition to maintaining open parallel pathways throughout the structure while minimizing flow resistance through the contactor, the spacer elements disclosed herein provide additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element, thereby improving the sorption and desorption characteristics of the overall device. Furthermore, in some examples, a protective layer comprising a microporous material can be disposed around the spacer elements to protect the spacer elements from surrounding or external elements.

[0144] The adsorbent structure is also designed to withstand large variations in mechanically and chemically adsorbed water loading during periodic injection and exposure to steam. According to the '747 Climeworks publication, the adsorbent structure includes an array of individual adsorbent elements in the form of sheets or laminates, each of which includes at least one layer containing a selectively porous or permeable solid adsorbent for CO2 capture, the adsorbent elements in the array being arranged essentially parallel to one another and essentially evenly spaced from one another to form essentially parallel fluid pathways for the flow-through of the gas mixture and / or vapor. Open spaces between the sheets are preferably maintained by inserting spacer elements attached to the adsorbent sheets.

[0145] In the present disclosure, the spacer elements include a sorbent material configured to promote sorption and desorption through the spacer element. The spacer elements increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element. Advantageously, in addition to preserving open space between sheets, the spacer elements disclosed herein provide additional volume or mass of sorbent material to increase the ratio of the sorbent mass of the sorbent element to the total mass of the sorbent element, thereby improving the sorption and desorption characteristics of the overall device. Furthermore, in some examples, a protective layer comprising a microporous material can be disposed around the spacer element to protect the spacer element from ambient or external elements.

[0146] According to the '747 Climeworks publication, the adsorbent structure includes an array of individual sorbent elements, each of which preferably includes a porous support layer and at least one sorbent layer on one or both sides, or a composite thereof. The adsorbent elements in the array are arranged essentially parallel to one another and spaced apart to form parallel fluid paths for the flow-through of gas mixtures and / or vapors. Of course, in such adsorbent structures in the form of stacks, the outermost adsorbent elements may have only a carrier layer, with at least one sorbent layer on the inner side. Process gas flows primarily in a direction coplanar with the sheet or laminate between the inlet and outlet of the stack. Solid structured sorbents typically have only two parallel faces open to direct the process gas stream into the structured sorbent bed and provide a means for mechanical assembly into separation units. Alternatively, two sets of two parallel faces are open to flow, with one process gas, such as the adsorbent gas stream, flowing from one face to the opposite parallel face, and another process gas, such as the vapor stream, flowing from a third face to a fourth parallel face.

[0147] As noted above, the unit is preferably capable of maintaining a vacuum pressure of 400 mbar (abs) or less, step (b) preferably comprises separating the sorbent containing adsorbed carbon dioxide in the unit from the flow-through while maintaining the temperature within the sorbent, and then evacuating the unit to a pressure in the range of 20 to 400 mbar (abs), and step (e) comprises subjecting the sorbent material to ambient atmospheric pressure and temperature conditions.

[0148] Preferably, the above method or device is used for direct air capture or capture of carbon dioxide from ambient air.

[0149] Further embodiments of the '747 Climeworks publication are set out in the dependent claims. [Brief explanation of the drawings]

[0150] BRIEF DESCRIPTION OF THE DRAWINGS Preferred embodiments of the present disclosure will be described below with reference to the drawings. However, the drawings are intended to illustrate the preferred embodiments of the present disclosure and are not intended to limit the present disclosure.

[0151] [Figure 1] FIG. 1 (Prior Art) shows a schematic diagram of the essential and optional steps of the proposed method for obtaining CO2 in an economically viable cyclic adsorption and desorption process as found in the '747 Climeworks publication.

[0152] [Figure 2] FIG. 2 (Prior Art) shows a schematic diagram of a single adsorbent (sorbent) element comprising a porous support and at least one sorbent layer as found in the '747 Climeworks publication.

[0153] [Figure 2A] FIG. 2A shows a cross-sectional view of a sorbent element as cut along line AA in FIG. 2 according to some embodiments of the present disclosure.

[0154] [Figure 2B] FIG. 2B shows a cross-sectional view of a sorbent element having a lumen extending therethrough in both an uncompressed and compressed configuration, according to some embodiments of the present disclosure. [Figure 2C] FIG. 2C shows a cross-sectional view of a sorbent element having a lumen extending therethrough in both an uncompressed and compressed configuration, according to some embodiments of the present disclosure.

[0155] [Figure 2D] FIG. 2D shows a cross-sectional view of a sorbent element having a lumen extending therethrough in both an uncompressed and compressed configuration, according to some embodiments of the present disclosure. [Figure 2E] FIG. 2E shows a cross-sectional view of a sorbent element having a lumen extending therethrough in both an uncompressed and compressed configuration, according to some embodiments of the present disclosure.

[0156] [Figure 2F] FIG. 2F is an image of interconnected lumens that can be implemented in a sorbent element according to some embodiments of the present disclosure.

[0157] [Figure 3] FIG. 3 (Prior Art) shows a schematic diagram of a single adsorbent (sorbent) element comprising a carrier layer and at least one sorbent layer on each side, as found in the '747 Climeworks publication.

[0158] [Figure 3A] FIG. 3A shows a cross-sectional view of a sorbent element taken along line AA of FIG. 3 according to some embodiments of the present disclosure.

[0159] [Figure 3B] FIG. 3B shows a cross-sectional view of a sorbent element having a lumen extending therethrough in both an uncompressed and compressed configuration according to some embodiments of the present disclosure. [Figure 3C] FIG. 3C shows a cross-sectional view of a sorbent element having a lumen extending therethrough in both an uncompressed and compressed configuration according to some embodiments of the present disclosure.

[0160] [Figure 3D] FIG. 3D shows a cross-sectional view of a sorbent element with a protective layer according to some embodiments of the present disclosure. [Figure 3E] FIG. 3E shows a cross-sectional view of a sorbent element with a protective layer according to some embodiments of the present disclosure.

[0161] [Figure 4] FIG. 4 (Prior Art) shows an exemplary schematic diagram of an adsorbent structure including multiple parallel adsorbent elements, thus forming multiple parallel fluid passageways, as found in the '747 Climeworks publication.

[0162] [Figure 4A]FIG. 4A shows a schematic diagram of an adsorption structure showing a first direction of air flow and a second direction of desorption media according to some embodiments of the present disclosure.

[0163] [Figure 4B] FIG. 4B shows a schematic diagram of an adsorbent structure illustrating different types of flow-through of gas mixtures within and / or through the structure as disclosed herein.

[0164] [Figure 5] FIG. 5 (Prior Art) shows a schematic diagram of a reactor unit with the inlets and outlets required for the proposed process as found in the '747 Climeworks publication.

[0165] [Figure 6] FIG. 6 (Prior Art) shows a schematic diagram of an adsorption structure with vertically oriented adsorption elements and subsequent parallel fluid passages, showing an axial, approximately horizontal flow direction of the multicomponent stream during adsorption and a horizontal counter-flow arrangement of the vapor during purging, as found in the '747 Climeworks publication.

[0166] [Figure 7] FIG. 7 (Prior Art) shows a schematic diagram of an adsorption structure with vertically oriented adsorption elements and subsequent parallel fluid passages, showing the axial, approximately horizontal flow direction of the multicomponent stream during adsorption and the vertical cross-flow arrangement of the vapor during purging, as found in the '747 Climeworks publication.

[0167] [Figure 8] FIG. 8 (Prior Art) shows a schematic diagram of an adsorption structure in which the adsorption elements and subsequent parallel fluid passages are arranged horizontally, showing the axial, approximately horizontal flow direction of the multi-component flow during adsorption and the horizontal counter-flow arrangement of the vapor during purging, as found in the '747 Climeworks publication.

[0168] [Figure 9]FIG. 9 (Prior Art) shows a schematic diagram of an adsorption structure with horizontally oriented adsorption elements and subsequent parallel fluid passages, showing the axial, approximately horizontal flow direction of the multicomponent stream during adsorption (a) and the horizontal cross-flow arrangement of the vapor during purging (d) as found in the '747 Climeworks publication.

[0169] [Figure 10] FIG. 10 (Prior Art) shows laboratory test results of an adsorbent structure (1″×½″×40 mm) at different adsorption conditions, delivering 1.2 to 1.6 mmol / g, as found in the '747 Climeworks publication.

[0170] [Figure 11] FIG. 11 (Prior Art) shows the average breakthrough curve (top curve) and average CO loading (bottom curve) for experimental runs of Example 1 using an adsorbent structure (360 mm x 360 mm x 100 mm) with vertical parallel channels and a process including a pumping step to below 200 mbar (abs) as found in the '747 Climeworks publication.

[0171] [Figure 12] FIG. 12 (Prior Art) shows the relative breakthrough curves (top curve) and CO loading (bottom curve) for experimental runs of Example 2 using a vertically parallel channel adsorption structure (360 mm x 360 mm x 100 mm) and a process without a venting step, as found in the '747 Climeworks publication.

[0172] [Figure 13] FIG. 13 (Prior Art) shows a summary of experimental results using an insufficiently long adsorbent structure according to embodiment 1, as found in the '747 Climeworks publication.

[0173] [Figure 14]FIG. 14 (Prior Art) shows a schematic plant layout that can be used to implement the proposed method, as found in the '747 Climeworks publication.

[0174] [Figure 15] FIG. 15 (Prior Art) shows the measured and calculated pressure drop for various spacer heights and surface velocities as found in the '747 Climeworks publication.

[0175] [Figure 16] FIG. 16 (Prior Art) shows the maximum length of the laminate for different spacer heights (mm) as a function of velocity in free air for a pressure drop of 300 Pa as found in the '747 Climeworks publication.

[0176] [Figure 17] Figure 17 (Prior Art) shows the mass per square meter inlet area of ​​the laminate sheet for different spacer heights (mm) as a function of velocity in free air (inlet velocity before the parallel passage) for a pressure drop of 300 Pa as found in the '747 Climeworks publication.

[0177] [Figure 18] Figure 18 (Prior Art) shows the time to 1 mmol / g uptake for different spacer heights (mm) as a function of velocity in free air at a pressure drop of 300 Pa and a recovery of 60% as found in the '747 Climeworks publication.

[0178] [Figure 19] FIG. 19 (Prior Art) shows comparative production rates for different spacer heights (mm) as a function of velocity in free air for a pressure drop of 300 Pa as found in the '747 Climeworks publication.

[0179] [Figure 20]FIG. 20 (Prior Art) shows the ratio of characteristic times for advection and diffusion for different spacer heights as a function of velocity in free air for a pressure drop of 300 Pa as found in the '747 Climeworks publication.

[0180] [Figure 21] FIG. 21 (Prior Art) shows the maximum laminate length for different spacer heights and DAC windows as a function of velocity in free air for a 300 Pa pressure drop as found in the '747 Climeworks publication.

[0181] [Figure 22] FIG. 22 (Prior Art) shows the recovery rate and recovery capacity as a function of adsorption time for a particular set of parameters as found in the '747 Climeworks publication. DETAILED DESCRIPTION OF THE INVENTION

[0182] Detailed Description The embodiments of the present disclosure presented below describe the proposed method in terms of a variable set of process steps that can be performed in various sequences, with the adsorbent structure exposed in a dedicated reaction unit. The process flow of the preferred embodiment method in the '747 Climeworks publication includes the following steps: 1. The sorbent layer is exposed to a sufficient amount of ambient air to adsorb CO2 onto the adsorption structure, resulting in CO2 recovery. The recovery rate is 10% to 75% (adsorption step (a), essential). 2. Isolating the adsorption structure in the reactor from the external ambient atmosphere (isolation step (b), required). 3. Establish a pressure in the reactor unit, typically between 50 and 400 mbar (abs), by venting (venting step in (b) - optional). 4. While maintaining the pressure of step 3 or ensuring that the temperature of the adsorption structure does not exceed 75°C, flush the non-condensable gases from the reactor unit with an initial flow of non-condensable steam (steam flush step (b1), optional). 5. Inject a saturated or superheated steam stream, typically at a temperature of at least 45°C, if venting was performed in step 3, to induce an increase in the internal pressure of the reactor unit and, preferably, an increase in the temperature of the adsorption structure to a temperature of 60-110°C depending on the saturation temperature of the current reactor pressure, thereby facilitating the desorption and release of CO2 (heating step (c) with steam, mandatory). 6. While steam is still being injected, the outlet of the reactor unit is opened and both steam and CO2 are flushed and purged from the adsorption structure and reactor unit, typically to a steam to CO2 molar ratio of 4:1 to 40:1, while the outflow rate is preferably adjusted to maintain some of the pressure achieved at the end of the previous step (steam purging step (d), required). 7. After stopping the steam injection, the unit pressure in the reactor unit is reduced to 50-250 mbar (abs) by evacuation, the water evaporates from the adsorption structure, and the sorbent material is then dried and cooled (vacuum cooling / drying step (d1), optional). 8. Remove the isolation of the reactor from the ambient atmosphere and repressurize the reactor unit if necessary (removal of isolation and repressurization step (e), required). 9. Dry the adsorbent structure with hot air at 40°C to 100°C (air drying step (e1), optional). Continue cycling from step 1.

[0183] A schematic of this process is shown in Figure 1 of the '747 Climeworks publication.

[0184] One embodiment of the configuration of an individual adsorbent element is shown in Figure 2 of the '747 Climeworks publication. Figure 2A, disclosed herein, is a cross-sectional view of Figure 2 taken along line AA. Each adsorbent element 5a comprises at least one sorbent layer 1a on a porous support layer 3a, which comprises at least one sorptive material including a selective porous solid adsorbent for CO2 capture, thus forming a sheet or laminate. Spacing and alignment of multiple elements is achieved by inserting spacer elements 4 on one or both planar sides of the elements.

[0185] In FIG. 2A of the present disclosure, the adsorber element 5a further includes a protective layer 100 surrounding the sorbent layer 1a and the support layer 3a. The protective layer 100 is made of any suitable microporous material, including, but not limited to, expanded polyethylene (ePE) or expanded polytetrafluoroethylene (ePTFE). The spacer elements 4 can be disposed on the surface of the protective layer 100 and are made of any suitable microporous material, including, but not limited to, polyethylene (PE) and polytetrafluoroethylene (PTFE). The protective layer 100 is configured to surround the edges of the sorbent layer 1a and the support layer 3a of the adsorber element 5a. Additionally, the example of FIG. 2A illustrates that the protective layer 100 is also disposed around the spacer elements 4 to protect them from ambient or external elements (e.g., to protect them from water intrusion into the spacer elements 4).

[0186] 2B and 2C, the support layer 3a defines a plurality of lumens 102 extending therethrough in a direction substantially parallel to the sorbent layer 1a disposed on one or both sides of the support layer 3a. As shown in FIG. 2C, in some instances, the support layer 3a is made from a flexible material that can be partially compressed when a force is applied, in which case the lumens 102 are compressed in height as shown, thereby reducing the element thickness b element 2B. In some examples, the spacer element 4 has a height b element In some instances, the spacer elements 4 may be made of a non-flexible or rigid material to maintain the uncompressed height b even when partially compressed. spacer The lumen 102 can be made from a partially flexible material, such that at least a portion of the desorption medium, which can be a vapor, is retained. That portion can be at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, or any suitable value or range therebetween. The lumen 102 facilitates the passage of the desorption medium, which can be a vapor, through the adsorbent element 5a.

[0187] The spacer element 4 can incorporate a sorbent material such as a CO2 adsorbent material, including, but not limited to, an ion exchange resin (e.g., a strong base anion exchange resin, e.g., Dowex™, Marathon™, resins available from The Dow Chemical Company), zeolite, activated carbon, alumina, metal organic frameworks, polyethyleneimine (PEI), or other suitable CO2 adsorbent materials, such as desiccants, carbon molecular sieves, carbon adsorbents, graphite, activated alumina, molecular sieves, aluminophosphates, silicoaluminophosphates, zeolite adsorbents, ion exchanged zeolites, hydrophilic zeolites, hydrophobic zeolites, modified zeolites, etc. lite, natural zeolites, faujasite, clinoptilolite, mordenite, metal exchanged silicoaluminophosphates, monopolar resins, bipolar resins, aromatic crosslinked polystyrene matrices, brominated aromatic matrices, methacrylate copolymers, graphite adsorbents, carbon fibers, carbon nanotubes, nanomaterials, metal salt adsorbents, perchlorates, oxalates, alkaline earth metal particles, ETS, CTS, metal oxides, chemisorbents, amines, organometallic reactants, hydrotalcite, silicalite, zeolitic imidazolate frameworks and metal organic framework (MOF) adsorbent compounds and combinations thereof.

[0188] In some instances, the use of a sorbent material in the spacer elements 4 may result in an air gap / parallel fluid passage or distance defining the distance between two adjacent adsorbent elements. spacer By implementing spacer elements 4 with adsorbent properties, the ratio of sorbent mass to total mass is increased while maintaining the adsorbent structure 6. Thus, spacer elements 4, when made from a sorbent polymer material, can have multiple functions in that (1) the spacer elements 4 maintain a parallel pathway through the adsorbent structure 6 as seen in FIG. 4, (2) the spacer elements 4 increase the adsorbent mass to total mass ratio, and (3) the spacer elements 4 increase the density of the sorbent article without changing the occupied volume of the adsorbent structure 6.

[0189] 2D and 2E, lumen 102 is defined by a plurality of support layer components 3a disposed near sorbent layer 1a and surrounded by protective layer 100. Support layer components 3a can each be fabricated in the shape of a tube extending substantially parallel to sorbent layer 1a. In some examples, as shown in the figures, support layer components 3a can be formed from a substantially rigid material such that the size of lumen 102 remains unchanged even when the thickness of surrounding sorbent layer 1a is compressed, as indicated by the decrease in minimum thickness "T" of sorbent layer 1a measured between support layer components 3a and protective layer 100 from FIG. 2D to FIG. 2E.

[0190] In Figure 2F, the lumens 102 are defined by a single support layer component 3a with interconnected channels 200. That is, each lumen 102 is interconnected with at least one, and in some cases all, other lumens 102 via one or more interconnected channels 200 incorporated into the support layer component 3a, but is not visible from the outside when the support layer component 3a is sandwiched between the sorbent layers 1a, e.g., from the perspective of Figures 2D and 2E. Thus, depending on the configuration of the support layer component 3a, the lumens 102 are either independent of each other (i.e., not connected to other lumens 102) or interconnected via channels 200.

[0191] Another embodiment of the configuration of an individual adsorbent element is shown in Figure 3 of the '747 Climeworks publication. Each individual adsorbent element 5b comprises a layered structure including a central carrier layer 3b flanked by adjacent first and second sorbent layers 1b and 2b, respectively. Each individual adsorbent element has a thickness b element and a length L along the adsorption flow direction. More specifically, in the embodiment used herein, each adsorption element 5b comprises a sheet or laminate including at least one layer containing a selective porous solid adsorbent for CO2 capture and, optionally, a central porous support layer. Spacing and alignment of multiple elements is achieved by inserting spacer elements 4 on one or both planar sides of the elements.

[0192] In FIG. 3A of the present disclosure, adsorbent element 5b further includes multiple protective layers 100 (i.e., 100A, 100B, and 100C as shown) in a multilayer "sandwich" configuration, each protective layer surrounding one of the previously mentioned layers (i.e., first sorbent layer 1b, central carrier layer 3b, and second sorbent layer 2b, respectively, as shown). Protective layers 100 are then adhered or attached to one another, such that first sorbent layer 1b, central carrier layer 3b, and second sorbent layer 2b are no longer directly attached to one another, but instead are attached via protective layers 100A, 100B, and 100C. FIGS. 3B and 3C show central carrier layer 3b including multiple lumens 102, as described above. It should be understood that a single protective layer 100 of Figures 2A-2E may be implemented to surround the first sorbent layer 1b, central carrier layer 3b, and second sorbent layer 2b of Figure 3A, and similarly, multiple protective layers 100 of Figure 3A may be implemented to surround the sorbent layer 1a and support layer 3a of Figures 2A-2E.

[0193] In the above example, sorbent layers 1a, 1b, and 2b can comprise hydrophobic porous materials. For example, sorbent layers 1a, 1b, and 2b and protective layer 100 (which may be 100A, 100B, or 100C, as shown in FIGS. 3A-3C) can comprise multiple layers or components of hydrophobic material 300. Each layer or component of hydrophobic material 300 may be referred to as a "composite region." For example, FIG. 3D shows first composite region 300a, second composite region 300b, and third composite region 300c, with second and third regions 300b and 300c sandwiching first region 300a. Regions 300a, 300b, and 300c can have different degrees of hydrophobicity. Hydrophobicity can be altered by various methods, such as the application of coatings or surface treatments, which may include, but are not limited to, plasma etching and the application of microtopographic features. The first composite region 300a can have a first hydrophobicity, the second region 300b can have a second hydrophobicity, and the third region 300c can have a third hydrophobicity. The first hydrophobicity can be lower than each of the second and third hydrophobicities. The second hydrophobicity can be lower, higher, or equal to the third hydrophobicity. The higher hydrophobicity of the second and third regions 300b and 300c can reduce liquid water penetration through the respective regions and form a barrier between the surrounding liquid water and the components of the first composite region 300a. This reduces liquid water-induced degradation of the sorptive material in the first composite region 300a, improving the life and durability of the sorbent layer and, therefore, the life and durability of the adsorbent structure 6. The increased hydrophobicity of second region 300b and increased hydrophobicity of third region 300c compared to the first hydrophobicity of first composite region 300a may be due, for example, to the absence of sorbent material in second region 300b and third region 300c.

[0194] In some examples, the sorbent layer also includes edge seal regions formed by applying an additional layer of sealing material 302 to a sorbent layer, such as sorbent layer 1b, as shown in FIG. 3D. The sealing material 302 may be the same or different from the material of the second region 300b and the third region 300c. For example, the sealing material 302 may be ePTFE, ePE, a silicone elastomer, or other suitable non-porous and / or hydrophobic material that protects the first composite region 300a. In other embodiments, the edge seal regions 302 may be formed by stretching the second region 300b and the third region 300c and then bonding (e.g., pinching, gluing) the regions 300b, 300c together. The addition of this edge sealing step benefits the composite by protecting the sorbent retained in the adsorbent structure 6 and strengthening the leading edge of the sorbent layer (the area most likely to be damaged by airborne debris and high-velocity impacts). In some examples, the sealing material 302 and regions 300b, 300c may be formed from a continuous material, such as a tube or sheet, with ends connected to form a closed loop to form a seamless protective layer 304 over region 300a, as shown in FIG. 3E.

[0195] In the present disclosure, either the protective layer and / or the sealing material may be formed using copolymers of PTFE or tetrafluoroethylene (TFE) with other monomers. Such monomers may include ethylene, chlorotrifluoroethylene, or fluorinated propylenes such as hexafluoropropylene. These monomers may be used in very small amounts, with homopolymers being preferred because they exhibit optimal crystalline / amorphous structure for the processes and products of the present disclosure. Therefore, the amount of comonomer is generally less than 0.2%, and PTFE may be preferred. It should be understood that a wide variety of materials can be incorporated as fillers, including carbon black, various types of pigments, and inorganic materials such as mica, silica, titanium dioxide, glass, and potassium titanate. Additionally, dielectric fluids or fluid-containing materials, such as polysiloxane materials, as disclosed in U.S. Patent No. 3,278,673, assigned to W.L. Gore and Associates Inc., may be used.

[0196] Figure 4 of '747 Climeworks shows how individual adsorbent elements 5 are combined to form an adsorbent structure 6 by arranging them in an array of parallel layers, with fluid passages 7 between the parallel layers for the passage of air during the adsorption step and vapor during the desorption step, each passage corresponding to one adsorbent element 1. N sorbent layer and the next adsorption element 2 N+1 The width of these channels is b spacer is.

[0197] In the individual adsorber elements 5 shown in FIG. 4A of the present disclosure, two adjacent adsorber elements 1 N and 2 N+1Each of the fluid passages 7 includes a plurality of lumens 102, as described above, through which, during the desorption phase, a desorption medium, which can be a heat transfer fluid in the form of a gas, vapor, or liquid, can pass in a direction different from the direction in which airflow is facilitated through the fluid passage 7, as shown. The heat transfer fluid can be any suitable glycol-based heat transfer fluid, such as water, saline, ethylene glycol, a mixture of water and another suitable substance, or any other suitable type of fluid for facilitating heat transfer. As airflow is directed from one end of the fluid passage 7 to the other, the desorption medium can be directed, for example, substantially perpendicular or orthogonal to the direction of airflow. In some instances, vapor can pass through the fluid passage 7, and the desorption medium (which can be a heat transfer fluid in the form of a liquid) can pass through the lumens 102. In some instances, vapor may not be present in the fluid passage 7, and only the desorption medium passes through the lumens 102. In some instances, air and / or vapor can pass through the fluid passage 7 along the direction of airflow, as shown.

[0198] A diagram of the reactor unit and the necessary flows, as well as the inlets and outlets, is shown schematically in Figure 5 of the '747 Climeworks publication. In this case, the ambient air flow during adsorption is along a direction perpendicular to the direction of vapor flow during desorption. To enable this flow scheme using the layered structure of the adsorbent structure, the individual adsorbent elements in a reactor according to this scheme must be parallel to the plane of the paper.

[0199] In embodiment 1, the adsorbent structure is arranged so that the adsorbent elements 5 and parallel passages 7 are vertically oriented, as shown in Figure 6 of the '747 Climeworks publication. In step 1, the sorbent bed is contacted with the adsorption stream a for 5 to 40 minutes along the main flow direction perpendicular to the maximum available peripheral surface of the adsorbent structure, thereby allowing a throughflow of air along the parallel passages at a velocity of 2 to 9 m / s.

[0200] After this adsorption step 1, the reactor unit containing the adsorption structure is closed in step 2. The pressure in the reactor unit is then reduced in evacuation step 3 to a pressure of between 50 mbar (abs) and 400 mbar (abs).

[0201] Subsequently, in heating step 5, the adsorbent structure is brought to a temperature of 60°C to 110°C by injection of steam until the necessary reactor pressure is achieved to reach the desired adsorbent structure temperature by condensation and adsorption of the steam on the adsorbent structure within 0.5 to 15 minutes.

[0202] In the subsequent purge step 6, steam flows through the parallel passages in the same plane as the adsorption flow in step 1, in the same flow direction or in the opposite direction (indicated by d), preferably at a speed of 0.3 to 1 m / s for 0.5 to 15 minutes, to purge the desorbed CO2 from the parallel passages at a ratio of 4 to 40 moles of steam per mole of CO2.

[0203] In the following step 7, steam injection is stopped and the reactor unit is evacuated to a pressure of 50-250 mbar (abs). In the final step 8, the reactor unit is opened to ambient conditions before the cycle is restarted from step 1.

[0204] Embodiment 2 is essentially embodiment 1, except that during steps 5 and 6, the vapor flow is introduced at a velocity preferably between 1 m / s and 6 m / s, and completely through the parallel passages in a plane perpendicular to the adsorption flow. The vertical arrangement of the adsorption elements and parallel passages involves essentially top-to-bottom or bottom-to-top vapor flow, as shown in FIG.

[0205] Embodiment 3 shown in FIG. 8 is essentially embodiment 1, but the adsorber structure is arranged so that the adsorber elements and parallel passages are horizontal, as shown in FIG.

[0206] Embodiment 4 is essentially embodiment 3, except that during steps 5 and 6, the vapor flow is introduced at a velocity preferably between 1 m / s and 6 m / s, completely through the parallel passages in a plane perpendicular to the adsorption flow. The vertical arrangement of the adsorption elements and parallel passages results in essentially left-to-right or right-to-left vapor flow, as shown in Figure 9 of the '747 Climeworks publication.

[0207] In the non-vented embodiment 5, the adsorbent structure is arranged with the adsorbent elements and parallel passages oriented vertically, as shown in Figure 6. In step 1, the sorbent bed is contacted with adsorption stream a for 5 to 40 minutes along a main flow direction perpendicular to the periphery of the largest available adsorbent structure, allowing air throughflow along the parallel passages at velocities of 2 to 9 m / s.

[0208] After this adsorption step 1, in step 2 the reactor unit containing the adsorption structure is closed.

[0209] Subsequently, in the steam purge step, the adsorbent structure is brought to a temperature of 60°C to 110°C by injecting steam under ambient pressure until the local vapor pressure within the adsorbent structure increases its temperature by condensation and adsorption of the steam on the adsorbent structure within 0.5 to 30 minutes or 0.5 to 15 minutes, while the reactor outlet is open to extract the gases initially present after step 2, followed by CO2 and steam. The steam flows in the same or opposite direction (denoted by d) through a parallel passage in the same plane as the adsorption flow in step 1, preferably at a velocity of 0.3 to 1 m / s, for 0.5 to 30 minutes or 0.5 to 15 minutes, purging the desorbed CO2 from the parallel passage at a ratio of 4 to 40 moles of steam per mole of CO2.

[0210] In the final step 8, the reactor unit is opened to ambient conditions before the cycle begins again from step 1.

[0211] Embodiment 5 of the '747 Climeworks publication can be similarly carried out using the flow conditions and adsorbent configurations of embodiments 2-4, again without evacuation.

[0212] Figure 10 of the '747 Climeworks publication shows loading curves obtained from a wide range of hot air purges at 95°C after adsorption on a laboratory-scale Breakthrough analyzer at the conditions shown in the figure, and is believed to represent the maximum potential of such adsorption structures where the present sorbent material is embedded in the first and / or second sorbent layers, reaching loadings of 1.2 to 1.6 mmol / g.

[0213] Successful operation of embodiment 1 is shown in Figure 11 of the '747 Climeworks publication. At an adsorption throughflow velocity of approximately 4 m / s in the parallel passages, an average CO yield of 0.4 mmol / g was achieved within 10 minutes under fully dry ambient conditions, increasing to 0.8 mmol / g after 40 minutes. The exhaust pressure for steps 3 and 7 was 150 mbar (abs), and the pressure after the 2-minute heating step 5 and during the 3-minute purge step 6 was 850-950 mbar (abs). The vapor flow during these steps followed the same path as the initial adsorption flow, with an average velocity of 0.72 m / s in the parallel passages.

[0214] The successful operation of embodiment 5 is shown in Figure 12 of the '747 Climeworks publication. Three cycles according to embodiment 5 were run in succession, producing 0.8-0.9 mmol / g CO2.

[0215] A summary of the experimental results for Embodiment 1 is shown in Figure 13 of the '747 Climeworks publication, demonstrating successful cyclic operation over at least 10 cycles at several ambient conditions. The results are very promising, and significant improvements are expected by optimizing the adsorbent structure and sorbent materials for DAC purposes.

[0216] Figure 14 of the '747 Climeworks publication shows a general scheme of a plant layout suitable and adapted for carrying out the described method.

[0217] The plant contains T major units required for the desired plant capacity.

[0218] Each unit contains X subunits, where X:1 is the relationship between the total cycle time and the time required for desorption / regeneration. For example, Tower N has an adsorption structure containing six subunits, one of which desorbs and the rest adsorb.

[0219] Each subunit contains one or more reaction chambers that operate simultaneously to perform the same process step.

[0220] Each subunit may be mechanically sealed from the surrounding atmosphere by a valve, flap or door.

[0221] Each subunit can be as large as a 40-foot shipping container, primarily in terms of length (12.2 m) and height (2.6 m).

[0222] Each reaction chamber contains an adsorption structure, in this case a laminate stack as described above. The inlet to the adsorber is the largest open area provided by the subunit, so it is less than length x height (12.2 m x 2.6 m).

[0223] For example, considering six reaction chambers, a viable inlet section is six adsorption structure inlets with lengths of 1.6 m to 2 m and heights of 1.6 m to 2.4 m.

[0224] The total volume of the adsorption structure subunit behind this inlet is 1.5 m 3 (1.6m x 1.6m x 6 x 0.1m) ~ 60m 3 The area is (2m x 2.4m x 6 x just over 2m).

[0225] The mass of one subunit adsorption structure ranges from 75 kg to 3000 kg depending on the optimum configuration.

[0226] Each subunit will provide steam in the range of 6 to 20 tonnes per hour.

[0227] 100,000 m / h for each subunit 3 ~650,000m / h 3 can generate an adsorption air flow of

[0228] Example 1 from the '747 Climeworks publication: The results shown in Figures 11, 12, and 13 were obtained in the experimental setup in April and May 2020. The adsorber structure was operated as shown in Example 1 and Figure 6, measuring 360 mm x 360 mm x 100 mm, with the gas inlet and outlet each having a maximum surface area of ​​360 mm x 360 mm. The adsorber elements included at least one layer of functionalized silica for CO2 adsorption and were approximately 0.25 mm wide. Spacers were used, providing a spacing of approximately 0.5 mm between parallel adsorber elements. The entire adsorber structure therefore consisted of approximately 480 individual adsorber elements.

[0229] The operational embodiment, the results of which are shown in Figure 11, used adsorption step 1 with durations of 10 and 40 minutes and a flow rate of 4 m / s in the parallel channels. In steps 2 and 3, the reactor unit was isolated and evacuated to 150 mbar (abs). In heating step 5, steam injection increased the chamber pressure to 950 mbar (abs) in less than 2 minutes, followed by a 3-minute steam purge step 6 with a flow rate of 0.72 m / s in the channels and a pressure of 850 mbar (abs). In step 7, steam injection was stopped and the pressure in the reactor unit was reduced to 150 mbar (abs) before the unit was pressurized again to ambient pressure in step 8.

[0230] The operational embodiment, the results of which are shown in Figure 11, used an adsorption step 1 with a duration of 40 minutes and a flow velocity in the parallel channels of 4 m / s. In step 2, the reactor unit was isolated but not evacuated. No dedicated heating step was envisaged. Instead, an immediate steam purge step 6 was carried out for 6 minutes at ambient pressure with a flow velocity in the channels of 0.72 m / s, simultaneously heating and purging the adsorption structure. After steam injection was stopped and the unit was de-isolated, it resumed adsorption again.

[0231] As noted above, the pressure drop across such an adsorbent structure can be estimated by the following equation:

number

[0232] where ΔP is the pressure drop across the structure (Pa), L is the length (cm) of the parallel passage through which the gas flows, K is the experimentally determined roughness coefficient, typically in the range of 1 to 10; U inlet is the velocity at the inlet face of the adsorbent structure (not the velocity in the parallel passage) in m / s, b spacer is the height of the spacer (mm) that determines the width of the parallel passages).

[0233] FIG. 15 shows such pressure drops calculated for various spacer heights and surface velocities.

[0234] An exemplary configuration for Flue Gas collection requires a system 2 m long with 0.35 mm spacing, with a surface velocity of 5 m / s. Such a configuration would result in a pressure drop of well over 3 bar. Such a pressure drop is achievable in Flue Gas systems operating at high pressures, but not in DAC applications.

[0235] DAC applications are generally limited by the feasible pressure drop of commercially available fans and ventilation systems. For axial fans, the maximum pressure drop is approximately 300 Pa before substantial volumetric flow rates are achieved, and for radial fans, it can increase to 600 Pa or 700 Pa, even up to 1200 Pa. Using this correlation, for a given adsorber type and spacer height, a map of maximum flow path, and therefore laminate length, can be determined as a function of inlet flow velocity, also called superficial velocity, or velocity in free air to achieve a target pressure drop across the adsorber. See Figure 16.

[0236] Knowing the length of this adsorptive structure, the thickness and density of the individual adsorptive sheets, and the height of the spacers, the mass of the adsorptive structure per inlet area can be determined (see also Figure 17).

number

[0237] Furthermore, knowing the flow rate and assuming the capture rate (the percentage of the total CO2 passing through the contactor that is captured, in this case 60%), we can estimate the time until a particular sorbent loading is achieved (see also Figure 18).

[0238] The ratio of the mass of the adsorbent structure and the achieved CO2 loading per unit area divided by the time required for adsorption is an indicator of the CO2 production rate and is a directly comparable parameter (see Figure 19).

[0239] This assumes that the incoming air recovery rate is constant, so it is the same for all spacer heights and increases linearly with velocity. This assumption can be verified or adjusted once the specific kinematic and geometric parameters of the sorbent and structure are known. To determine the optimal spacer height for such a system, another parameter is required. This can be achieved by analyzing the kinematics involved in the adsorption process. This involves the advection characteristic time, Tadv, which represents the time window related to flow, and the diffusion characteristic time, T, which represents the time window related to the diffusion of CO2 into the sorbent layer. diff This is done by comparing the

[0240]

number

number

number

[0241] The characteristic time of pore diffusion is the element thickness and the pore mass transfer coefficient k p is given as a function of

number

[0242] Using these correlations, an analysis of the ratio of advection characteristic time to diffusion characteristic time can be performed, as shown in FIG.

[0243] The important point here is that, again, larger spacing strategies, due to the length allocated to maintain a desired pressure drop, exhibit smaller advection-to-diffusion time ratios, requiring longer diffusion times compared to the smaller spacer heights associated with shorter beds. The efficiency of the recovery process during adsorption is largely determined and limited by diffusion into the sorbent.

[0244] Therefore, the above observations indicate that for DAC, larger spacer heights and longer beds yield better adsorption results than theoretically similar solutions with narrower spacing and shorter beds. Therefore, DAC applications (see Figure 21) operate optimally with larger spacer heights, within the technically feasible range of 0.4–3 mm, at technically feasible inlet velocities of 2–6 m / s, and bed lengths of 100–3000 mm. At this stage, another factor must be mentioned in addition to practical and technical implementation. The cost of such adsorption structures, which inevitably require more initial sorbent material for larger spacing structures and therefore increased investment costs, creates an adverse trade-off in most practical implementations.

[0245] Example 2 from the '747 Climeworks publication: In parallel-passage-based adsorption structures where maximum recovery capacity is desired, several factors must be considered, including allowable pressure drop, sorbent capacity, effective sorbent density, and recovery kinetics. For example, large volumes of air are required to fully pack a high-capacity sorbent, which correspondingly requires wide channels to comply with pressure drop limitations. Accordingly, such systems can have low sorbent densities, limiting potential recovery capacity.

[0246] In this example, related to Figure 22, the behavior of an adsorbent structure, in line with the disclosure of the '747 Climeworks publication, is numerically investigated for a direct air capture process using a specific sorbent and adsorbent structure. 2 , parallel passage spacing b spacer For a specific sorbent material with a diameter of 1.7 mm, a passage inlet air velocity of 7 m / s, and a length L of 1.2 m, the critical pressure drop is assumed to be 750 Pa. The capture process is numerically simulated using a linear driving force model and a CO2-air mass transfer formulation to determine the optimum capture capacity (tons CO2 captured / m2) by varying the adsorption period together with the associated desorption process period. 2 The optimal adsorption process duration in this case was found to be 840 seconds (14 minutes), corresponding to an average recovery rate of just under 2 mmol / g / h, which is well within the target range specified in the '747 Climeworks publication.

[0247] Also disclosed herein are methods of removing gaseous carbon dioxide (CO2) from the atmosphere using any suitable means, method, process, or device for removing carbon dioxide (CO2) from the atmosphere disclosed herein. In some examples, the carbon dioxide removal service provider is a person, device, air treatment facility, carbon dioxide removal plant, software, internet site, electronic interface, organization, or corporate agency or entity (including a control center, headquarters, data management center, intermediate data collection or processing center, or support organization that provides information and / or control functions or services to the provider), or an electronic device or display associated with or accessible to the provider, that is capable of receiving and / or perceiving information regarding the diffusion of a first quantity of gaseous CO2 in the atmosphere at a first location. The information can be complete, partial, derived, or summarized, and can be received in the form of an electronic display, electronic alert, notification, or other electronic communication (e.g., email message, telephone call, or video call), and can include digital data representing the amount (e.g., in tons of CO) and / or rate (e.g., in tons of CO per minute, hour, day, etc.) of gaseous CO diffusing at the first location, as well as data associated with the first location, such as city and / or country name, GPS location, weather information, etc. In some examples, the information can be in the form of an electronic communication (e.g., a first electronic communication) received from and / or provided to a computing device and / or electronic display device that includes information regarding the diffusion of a first amount of gaseous CO 2 into the atmosphere at the first location.

[0248] The carbon dioxide removal service provider can initiate immediate or subsequent separation of a second amount of gaseous CO2 or a separation method at a second location, which can be different from the first location. The second location can be remote from the first location, for example, if the first location is in a densely populated commercial area and the second location is near a geothermal or other hazardous energy source that powers the separation process at the second location. The second amount can be at least a portion of the first amount, such as 0%-10%, 10%-20%, 20%-30%, 30%-40%, 40%-50%, 50%-60%, 60%-70%, 70%-80%, 80%-90%, 90%-100%, or any other suitable value, combination, or range therebetween. The second amount can be a portion of the first amount or the entire first amount, and the second amount can be associated with a partial delivery of carbon removal services that include multiple separation cycles. The separation can include the use of any suitable method or process disclosed herein or any suitable device disclosed herein. In some examples, the separation can be initiated by sending or transmitting instructions or confirmation to a location capable of performing such separation. In some examples, the separation can be performed by a carbon capture device capable of performing any method for separating gaseous CO from a gas mixture in the form of ambient air, as disclosed herein. In some examples, the distance from the first location to the second location can be between 100 km and 200 km, between 200 km and 500 km, between 500 km and 800 km, between 800 km and 1000 km, between 1000 km and 2000 km, between 2000 km and 3000 km, between 3000 km and 4000 km, between 4000 km and 5000 km, between 5000 km and 6000 km, between 6000 km and 7000 km, between 7000 km and 8000 km, between 8000 km and 9000 km, between 9000 km and 10,000 km, between 10,000 km and 15,000 km, between 15,000 km and 20,000 km, or any other suitable value or range therebetween.

[0249] The carbon dioxide removal service provider can initiate reporting of data regarding the second amount that will be, is being, or has been removed from the atmosphere. Initiation can be an initial step taken to initiate immediate or subsequent reporting of the data, which can be performed via any suitable electronic communication or data transmission means, which can be wired or wireless. In some examples, reporting can include preparing information to be included in such a report or a later report, and subsequently sending or transmitting instructions or confirmation to another entity or device capable of initiating or fully executing such reporting. The reported data can be associated with the carbon capture device as disclosed herein regarding the second amount. For example, the carbon capture device can generate or provide data related to the separation of the second amount of gaseous CO, which can be obtained directly or indirectly (e.g., via an intermediate entity or device) from the carbon capture device. In examples, at least a portion of the data generated by the carbon capture device is provided in an electronic communication. As another example, the data can be summarized or otherwise processed, and a display of the data provided in an electronic communication (e.g., a second electronic communication). In some examples, the second electronic communication can be transmitted to a computing device or a display device. In some examples, the second electronic communication may be sent to an additional computing or display device, which may be separate or different from the aforementioned computing or display device.

[0250] In some examples, a method for removing gaseous CO from the atmosphere can involve a carbon dioxide removal service provider (as described above) receiving and / or becoming aware of information regarding a first quantity of gaseous CO, which can include a dispersion of gaseous CO. The information can be complete, partial, derived, or summarized, and can be received in the form of an electronic display, electronic alert, notification, or other electronic communication (e.g., email message, telephone call, video call, etc.), and can include digital data representing the amount (e.g., tons of CO) and / or diffusion rate (e.g., tons of CO per minute, hour, day, etc.) of gaseous CO diffusing at the first location, as well as data associated with the first location, such as city and / or country name, GPS location, weather information, etc. Such an amount can represent the amount (e.g., tons of CO) and / or diffusion rate (e.g., tons of CO per minute, hour, day, etc.) of gaseous CO diffusing at a location. In some examples, the information can be received as an electronic communication from another entity or device that sends or transmits instructions regarding gaseous CO removal as disclosed herein. In some examples, the electronic communication (e.g., the first electronic communication) includes information regarding the diffusion of the first quantity of gaseous CO2 that can be received from and / or provided to the computing device and / or electronic display device.

[0251] The carbon dioxide removal service provider can separate or begin separating a second amount of gaseous CO from the atmosphere, where the second amount is at least a portion of the first amount, such as 0%-10%, 10%-20%, 20%-30%, 30%-40%, 40%-50%, 50%-60%, 60%-70%, 70%-80%, 80%-90%, 90%-100%, or any other suitable value, combination, or range therebetween. The second amount can be a portion of the first amount or the entire first amount, and the second amount can be associated with a partial delivery of a carbon removal service that includes multiple separation cycles. The separation can include use of any suitable method or process disclosed herein or any suitable device disclosed herein. In some examples, the separation can be performed by a carbon capture device capable of performing any method for separating gaseous CO from a gas mixture in the form of ambient air, as disclosed herein.

[0252] The carbon dioxide removal service provider can report data regarding the second amount that will be, is being, or has been removed from the atmosphere. The reporting of the data can be performed via any suitable electronic communication or data transmission means, which can be wired or wireless. In some examples, the reporting can be performed in response to receiving an instruction or confirmation transmitted from another entity or device capable of initiating or fully executing such reporting. The reported data can be associated with a carbon capture device disclosed herein regarding the second amount. For example, the carbon capture device can generate or provide data related to the separation of the second amount of gaseous CO, which data can be obtained directly or indirectly (e.g., via an intermediate entity or device) from the carbon capture device. In examples, at least a portion of the data generated by the carbon capture device is provided in an electronic communication. As another example, the data may be summarized or otherwise processed such that a display of the data is provided in an electronic communication (e.g., a second electronic communication). In some examples, the second electronic communication can be transmitted to a computing device or a display device. In some examples, the second electronic communication may be sent to an additional computing or display device that is separate or different from the aforementioned computing or display device.

[0253] In some examples, a method for removing gaseous CO from the atmosphere can involve a carbon dioxide removal service provider (as described above) that can transmit, transmit, or send information regarding the diffusion of a first amount of gaseous CO into the atmosphere at a first location. The information can be complete, partial, derived, or summarized, and can be received in the form of an electronic display, electronic alert, notification, or other electronic communication (e.g., email message, telephone call, or video call), and can include digital data representing the amount (e.g., in tons of CO) and / or diffusion rate (e.g., in tons of CO per minute, hour, day, etc.) of gaseous CO diffusing at the first location, as well as data associated with the first location, such as city and / or country name, GPS location, weather information, etc. The transmission can be a transmission and / or sending performed via any suitable means of electronic communication or data transmission, which can be wired or wireless, and may not be received by the intended recipient or any recipient. In some examples, the information may be in the form of an electronic communication (e.g., a first electronic communication) including information regarding the diffusion of a first quantity of gaseous CO2 into the atmosphere at a first location, which information is transmitted, transmitted, and / or sent to a computing device, but such transmission, transmission, and / or sending is not necessarily received by a recipient.

[0254] The carbon dioxide removal service provider can request immediate or subsequent separation or a method of separating a second amount of gaseous CO2 from the atmosphere at a second location. The second location can be located remotely from the first location, for example, if the first location is in a densely populated commercial or industrial area and the second location is near a geothermal or other hazardous energy source that powers the separation process at the second location. The second amount can be at least a portion of the first amount, such as 0%-10%, 10%-20%, 20%-30%, 30%-40%, 40%-50%, 50%-60%, 60%-70%, 70%-80%, 80%-90%, 90%-100%, or any suitable value, combination, or range therebetween. The second amount can be a portion of the first amount or the entire first amount, and the second amount can be associated with a partial delivery of carbon removal services that include multiple separation cycles. The separation can include the use of any suitable method or process disclosed herein or any suitable device disclosed herein. The request for or initiation of separation can be performed via any suitable means of electronic communication or data transmission, which can be wired or wireless. In some examples, the request can be made by sending, originating, or transmitting an initiation command indication to a location capable of initiating or fully performing such separation. In some examples, the separation can be performed by a carbon capture device capable of performing any method for separating gaseous CO from a gas mixture in the form of ambient air, as disclosed herein. In some examples, the distance from the first location to the second location can be between 100 km and 200 km, between 200 km and 500 km, between 500 km and 800 km, between 800 km and 1000 km, between 1000 km and 2000 km, between 2000 km and 3000 km, between 3000 km and 4000 km, between 4000 km and 5000 km, between 5000 km and 6000 km, between 6000 km and 7000 km, between 7000 km and 8000 km, between 8000 km and 9000 km, between 9000 km and 10,000 km, between 10,000 km and 15,000 km, between 15,000 km and 20,000 km, or any suitable value or range therebetween.

[0255] The carbon dioxide removal service provider can receive a report regarding the second amount that will be, has been, or has been removed from the atmosphere, an indication of such a report, and / or an indication of data availability. Receipt of the report can be accomplished without the need for human inspection or verification, simply by making the report accessible without subsequent review or verification, and / or can be performed via any suitable means of electronic communication or data transmission, which can be wired or wireless. In some examples, receipt of the report can be regarding the second amount, such as the amount of gaseous CO2 separated within a predetermined time period, e.g., within one day, one week, or one month. The reported data can be associated with the carbon capture device as disclosed herein regarding the second amount. For example, the carbon capture device can generate or provide data related to the separation of the second amount of gaseous CO2, and the data can be obtained directly or indirectly (e.g., via an intermediate entity or device) from the carbon capture device. In examples, at least a portion of the data generated by the carbon capture device is provided in an electronic communication. As another example, the data can be summarized or otherwise processed such that a representation of the data is provided in an electronic communication (e.g., a second electronic communication). In some examples, the second electronic communication is received from a computing device, in some examples, the second electronic communication is received in response to transmitting the first electronic communication, in some examples, the second electronic communication is received from a computing device or a display device in response to transmitting the first electronic communication to the computing device or a display device.

[0256] As used herein, "receiving" information should be understood as a "receiving" act that only one party (or entity, device, etc.) needs to perform, without another party being required to perform a "sending" act.

[0257] As used herein, "initiating" a separation (or separation method) should be understood as an "initiation" act, including the initial or completed act of preparing or sending instructions to another party or device with the intent to perform or start a separation process, or to associate an initiation step with a separation process that has already begun. For example, the act of "initiating" the separation of gaseous CO may result in a carbon capture device subsequently receiving, directly or indirectly (e.g., via an intermediate entity or device), instructions to begin separation, in response to which the carbon capture device operates. In another example, the act of "initiating" the separation of gaseous CO (or separation method) may include a carbon dioxide removal service provider associating carbon dioxide already removed from the atmosphere (or currently in an active removal process) with the initiation of a subsequent separation. It will be understood that the instructions received by the carbon capture device need not be provided as part of such an "initiation" operation. Furthermore, the act of "separation" of CO2 need not necessarily be part of the act of "initiating" such separation, for example, where the "initiation" of the separation is performed by a first party and the subsequent "separation" itself is performed by a second party different from the first party. Moreover, the act of "separation" need not be accomplished or fully completed by either the first or second party. It will also be understood that the act of initiation can be performed entirely in one jurisdiction or country, even if acts subsequent to or related to the confirmation or initiation of initiation are performed in another jurisdiction or country.

[0258] As used herein, "initiating" a report (e.g., of data) should be understood as an "initiating" act that includes the initial or complete act of preparing or sending instructions to another party to later prepare, initiate, or complete the report. Thus, the act of "reporting" data is not necessarily part of the act of "initiating" such a report, such as when, for example, the "initiating" of a report is performed by a first party (the "initiating party") and the "reporting" itself is performed by a second party (the "reporting party") that is different from the first party (the "initiating party"). Furthermore, the act of "reporting" need not be accomplished or fully completed by either the first or second party. It will be understood that an initiating act can be performed entirely in one jurisdiction or country, even if acts subsequent to or related to the authorization or initiation of the initiation are performed in another jurisdiction or country.

[0259] As used herein, "reporting" of data should be understood as an act of "reporting" that need only be performed by one party (the reporting party). Furthermore, the act of "reporting" does not require receipt (or confirmation of receipt) of such report by another party (the receiving party). Reporting can be the storage of data or the display of data in a location accessible to the intended recipient, and may be considered reporting even if the intended recipient does not access or confirm the data.

[0260] As used herein, "sending" information should be understood as an act of "sending" that need only be performed by one party (the sending party). Furthermore, the act of "sending" does not require a recipient (e.g., the receiving party) or receipt (e.g., confirmation of receipt) of the transmitted information.

[0261] As used herein, "requesting" separation (or initiating a separation method) should be understood as a "requesting" act that need only be performed by one party (the requesting party). Also, the "separation" act requested by the "requesting" act may be performed by another party (the separating party). Furthermore, the "requesting" act need only be intended or initiated, not achieved or fully completed (e.g., if separation does not result from the act of "requesting" such separation). In one example, the act of "requesting" separation of gaseous CO2 (or initiating a separation method) may include a carbon dioxide removal service provider associating carbon dioxide that has already been removed from the atmosphere (or is currently in an active removal process) with a subsequent separation request. It will be understood that a requesting act can be performed entirely in one jurisdiction or country, even if confirmation of the request or acts subsequent to or related to the request occur in another jurisdiction or country.

[0262] As used herein, "receiving" a report or a representation of a report should be understood as the act of "receiving" without the need for a sender (e.g., the sending party). Receiving is the storing of data or the display of data in a location accessible to the intended recipient, and can be considered receiving even if the intended recipient does not access or review the data.

[0263] As will be understood, the first amount, the second amount, and the portion of the first amount can be estimates or predictions. It will further be understood that the carbon dioxide gas released or diffused at the first location does not necessarily contain or be the same CO molecules as separated or collected at the second location, and the second amount can be an equivalent amount of released or diffused CO. The portion of the first amount of CO may be non-gaseous. The portion of the first amount or the second amount may refer to carbon dioxide that has been captured in a sorbent, stored, or converted to another form as disclosed herein. The portion of the first amount or the second amount may include gases other than carbon dioxide. For example, the second amount may be non-gaseous or combined with other materials.

[0264] As used herein, "carbon capture device" refers to one or more devices disclosed herein that can separate gaseous CO from the atmosphere at the location where the device is installed or located. A carbon capture device can refer to a single device or multiple devices, or a facility including one or more such devices or component devices operating in concert. A device can include, for example, a desorption media source and an adsorption structure disclosed herein. A device can be operable by a user or operator using an electronic device. A device can generate data related to its operation, which can be detected, for example, by one or more sensors and / or, in other examples, can include log data.

[0265] As used herein, an "electronic device" refers to a device capable of performing one or more electronic operations, such as a computer, a smartphone, or a smart tablet. An electronic device may include, for example, a display device and / or one or more processing units and one or more memory units. The processing unit may include a central processing unit (CPU), a microprocessor, a system-on-chip (SoC), or any other processor capable of performing such operations. The memory unit may be a non-transitory computer-readable storage medium that stores one or more programs or instructions that, when executed on the processing unit, cause the processing unit or electronic device to perform one or more methods disclosed herein. The memory unit may include one or more memory chips, such as volatile or non-volatile memory, static or dynamic random access memory, or any variation thereof, that store data and allow the processing unit to access storage locations. In some examples, an electronic device may be referred to as a computing device.

[0266] Technical advantages of removing gaseous CO from the atmosphere using the methods or processes disclosed herein include, but are not limited to, facilitating a network of entities and / or devices that can communicate with other entities and / or devices to remotely provide instructions, or facilitate the separation and removal of gaseous CO without being physically present at the location. Furthermore, the methods and processes disclosed herein provide a robust network of inter-agency communications, allowing each entity (which may be an agency associated with a physical location) to simultaneously direct or initiate gaseous CO separation and removal at multiple locations, as well as the ability to flexibly change locations where gaseous CO separation and removal is determined to cease. Location changes can be performed in real time or near real time to minimize the time lag between when instructions are provided and when separation of gaseous CO occurs at a designated location. In some examples, the methods or processes disclosed herein provide a flexible communications network that allows entities or devices performing gaseous CO separation and removal at designated locations to provide timely reports (e.g., operational summaries and / or bills for services rendered) related to the amount of gaseous CO removed during a given period. Such reports may be generated automatically or manually, at predetermined time intervals (e.g., daily, weekly, monthly, etc.), or in a more flexible manner as determined manually (e.g., whenever requested by a user or entity), or in response to the achievement or exceedance of predetermined thresholds, including, but not limited to, for example, the amount of gaseous CO2 separated and removed from the atmosphere (e.g., every 1 ton, 5 ton, 10 ton of gaseous CO2 removed from the atmosphere, etc.), or any other suitable terms as determined and agreed upon by the entities involved.

[0267] List of reference numbers 1-First sorbent layer 2- Second sorbent layer 3a-Porous support layer 3b - Carrier layer 4-Spacer Elements 5- Individual adsorption elements 6-Perfect adsorption structure 7 - a fluid passage, one side of which is connected to the first sorbent layer of one adsorption element (1 N ) and the second sorbent layer (2 N+1 ) is formed as a boundary. 100-protective layer 102-lumen 200-channel 300 - Hydrophobic material or composite area 302-Sealing materials 304-Seamless protective layer 401 - First type of flow-through 402 - Second type flow-through 403-Third Type Flow-Through A-Entrance area a-flow direction of multicomponent flow during adsorption b element -Element thickness of the adsorption element b spacer -Spacing width d - direction of vapor flow during desorption ΔP - pressure drop across the adsorbent structure K surface -Roughness coefficient K linear -Linear roughness coefficient k f -film mass transfer coefficient k p -pore mass transfer coefficient L - length of the adsorbent element along the flow-through direction during adsorption m - mass of adsorbed structure ρ element -Density of individual suction sheets T adv - characteristic time of advection T diff - characteristic time of diffusion T film - Characteristic time of film diffusion T pore - characteristic time of pore diffusion U inlet -Inlet plane velocity U interstitial - velocity between plates in the channel

Claims

1. 1. A method for separating gaseous carbon dioxide from ambient air containing gaseous carbon dioxide and also containing additional gases different from gaseous carbon dioxide by cyclic adsorption / desorption using a sorbent material that adsorbs gaseous carbon dioxide, comprising: using a unit including an adsorbent structure comprising said sorbent material, wherein said adsorbent structure can withstand temperatures of at least 60°C for desorption of at least gaseous carbon dioxide, said unit being openable to ambient air flow-through and openable for contact with said sorbent material for the adsorption step; The adsorbent structure includes an array of individual adsorbent elements, each of which includes at least one support layer, at least one sorbent layer including at least one sorptive material, and at least one protective layer including a microporous material disposed around the support layer and the sorbent layer, the sorbent material being capable of condensing CO2 more than other major non-condensable gases in air in the presence of moisture or water vapor. ２ and the protective layer has a higher hydrophobicity than the sorbent material; The adsorbent elements in the array are arranged essentially parallel to one another and spaced apart to form parallel fluid paths for the flow-through of at least one of ambient atmosphere and desorption medium, and the method comprises at least the following consecutive steps (a) through (e) repeated in this order: (a) in an adsorption step, contacting the ambient air with the sorbent material by flow-through through the parallel fluid passages under ambient atmospheric pressure and temperature conditions to adsorb at least the gaseous carbon dioxide onto the sorbent material; (b) isolating the sorbent containing adsorbed carbon dioxide in the unit from the flow-through while maintaining the temperature of the sorbent; (c) injecting a flow of desorption medium, thereby inducing an increase in the temperature of the sorbent to a temperature of 60-110°C, ２ Initiating desorption of (d) extracting at least the desorbed gaseous carbon dioxide from the unit and separating the gaseous carbon dioxide from the desorption medium by condensing it within the unit or downstream of the unit, while contacting the sorbent material with the desorption medium by injecting and / or partially circulating the desorption medium into the unit, thereby separating the desorption medium and the CO ２ from said unit at a molar ratio of said desorption medium to carbon dioxide of from 4:1 to 40:1, while adjusting the extraction and desorption medium feed, or both, to essentially maintain the sorbent temperature at the end of the preceding step (c), or essentially maintain the sorbent pressure at the end of the preceding step (c), or both; (e) subjecting the sorptive material to ambient atmospheric conditions; Including, In step (a), the flow velocity of ambient air through the adsorptive structure is in the range of 2 to 9 m / sec, inclusive; and at least in step (d), the flow rate of the desorption medium through the adsorbent structure is at least 0.2 m / sec; A method wherein in steps (c) and (d) said desorption medium is used essentially exclusively or completely exclusively for the supply of heating energy during the desorption process.

2. 2. The method of claim 1, wherein in step (a), the flow velocity of ambient air through the adsorption structure is in the range of 2 to 9 m / sec, or at least in step (d), the flow velocity of desorption medium through the adsorption structure is in the range of 0.3 to 6 m / sec.

3. In step (a), the specific flow rate of ambient air through the adsorbent structure is between 20 and 10,000 m, inclusive, as a function of the mass of the sorbent. ３ / h / kg, or In step (a), the specific flow rate of ambient air through the adsorbent structure is between 4,000 and 500,000 m as a function of the volume of the sorbent. ３ / h / m ３ or or wherein, at least in step (d), the specific flow rate of the desorption medium through the adsorbent structure is in the range of 1 to 500 kg / h / kg as a function of the mass of the sorbent; At least in step (d), the specific flow rate of the desorption medium through the adsorbent structure is between 200 and 15,000 kg / h / m as a function of the volume of the sorbent. ３ The method according to claim 1 or 2, wherein the range is:

4. the carbon dioxide recovery, defined as the percentage of carbon dioxide recovered from the ambient atmosphere by the sorbent material in the adsorption step, is in the range of 10 to 75%, inclusive; or The amount of carbon dioxide recovered by the sorbent per gram of sorbent is at least 0.1 over an adsorption time range of at least 5 minutes or at least 10 minutes; or 4. The method of any one of claims 1 to 3, wherein the normalized amount of carbon dioxide recovered by the sorbent per gram of sorbent per hour is in the range of 0.5 to 10 mmol / g / h, inclusive.

5. 5. The method of any one of claims 1 to 4, wherein the adsorbent structure comprises an array of individual adsorbent elements, each adsorbent element comprising a central carrier layer or porous support flanked on either side by at least one porous or permeable sorbent layer having carbon dioxide capture moieties chemically attached thereto.

6. the adsorbent elements in the array are arranged essentially parallel to one another and spaced apart from one another by spacer elements to form parallel fluid paths for flow-through of at least one of ambient atmosphere and desorption medium, the spacer elements comprising a sorptive material configured to facilitate adsorption and desorption through the spacer elements; or The spacing between the adsorption elements (b spacer ) is in the range of 0.2 to 5 mm, inclusive; or Each adsorption element has a thickness (b) in the range of 0.1 to 1 mm inclusive. element 6. The method according to claim 1, wherein the surface has a planar shape having a surface having a thickness of 100 nm or less.

7. 7. The method of any one of claims 1 to 6, wherein the unit is evacuable to a vacuum pressure of 400 mbar (abs) or less, step (b) comprises isolating the sorbent containing adsorbed carbon dioxide in the unit from the flow-through while maintaining the temperature of the sorbent, and then evacuating the unit to a pressure in the range of 20 to 400 mbar (abs), inclusive, and in step (c), injecting a stream of desorption medium also induces an increase in the internal pressure of the reactor unit, and step (e) comprises subjecting the sorbent material to ambient atmospheric pressure and temperature conditions.

8. 1. A device for carrying out a method for separating gaseous carbon dioxide from a gas mixture in the form of ambient air, which also contains gaseous carbon dioxide and a further gas different from gaseous carbon dioxide, by cyclic adsorption / desorption using a sorbent material which adsorbs gaseous carbon dioxide, comprising: The device comprises: a desorption medium source; at least one unit comprising an adsorbent structure having said sorbent material; at least one device for separating carbon dioxide from water; Including, the adsorbent structure is heatable to a temperature of at least 60°C for desorption of at least the gaseous carbon dioxide, the unit being openable to ambient air flow-through and openable for contact with the sorbent material for an adsorption step; The adsorbent structure includes an array of individual adsorbent elements, each of which includes at least one sorbent layer including at least one sorptive material and at least one protective layer including a microporous material disposed around the support layer and the sorbent layer, the sorbent material being capable of condensing CO2 more than other major non-condensable gases in air in the presence of moisture or water vapor. ２ wherein the protective layer has a higher hydrophobicity than the sorbent material, and the adsorbent elements in the array are arranged essentially parallel to one another and spaced apart from one another to form parallel fluid paths for flow-through of at least one of ambient atmosphere and a desorption medium.

9. Interval width (b spacer ) is in the range of 0.4 to 5 mm, inclusive; or The device of claim 8, wherein the element length (L) is in the range of 100 to 3000 mm, inclusive.

10. The element length (L) is the spacing width (b spacer ) and as a function of element thickness (b element ) is given by the following formula: [Equation 1] (In the above formula, K global is 70 to 2500 mm including the end value －１ 10. The device according to claim 8 or 9, wherein the

11. The adsorption element includes a central carrier layer and at least one sorbent layer on either side of the central carrier layer; or the adsorber structure comprises an array of individual adsorber elements, each of which comprises a central porous carrier layer or support flanked on one or both sides by at least one porous and / or permeable sorbent layer; or 11. The device of any one of claims 8 to 10, wherein the adsorbent structure comprises an array of individual adsorbent elements, each of which comprises a central carrier or support layer and at least one porous and / or permeable sorbent layer having carbon dioxide capture moieties chemically attached to either side thereof.

12. the adsorbent elements in the array are arranged essentially parallel to one another and spaced apart from one another by spacer elements to form parallel fluid paths for the flow-through of ambient air and / or desorption media, the spacer elements comprising a sorptive material configured to facilitate adsorption and desorption through the spacer elements; or A device according to any one of claims 8 to 11, wherein the spacing between the adsorption elements is in the range of 0.2 to 5 mm inclusive.

13. the flow velocity of ambient air through the adsorbent structure is in the range of 2 to 9 m / s, inclusive; or the flow rate of the desorption medium through the adsorption structure is in the range of at least 0.2 m / sec, inclusive; or the flow velocity of ambient air through the adsorbent structure or at the inlet to the adsorbent structure is in the range of 4 to 7 m / s, inclusive; or A device according to any one of claims 8 to 12, wherein the flow rate of the desorption medium through the adsorption structure is in the range of 0.3 to 6 m / sec, inclusive.

14. 14. The device of any one of claims 8 to 13, comprising means for directing the desorption medium in the desorption medium flow-through step (d) along a flow direction different from the flow direction of the ambient atmosphere flow-through direction in the adsorption step (a).

15. The method according to any one of claims 1 to 7, which is carried out for direct air recovery or for the recovery of carbon dioxide from ambient air.

16. or, when the flow of ambient air in step (a) and the flow of desorption medium in step (d) are along essentially the same flow path, the flow rate of the desorption medium through the adsorbent structure in at least step (d) is in the range of 0.3 to 1.0 m / sec; or 3. The method of claim 2, wherein, when the flow of ambient air in step (a) and the flow of desorption medium in step (d) are along different flow paths, or when the flow of desorption medium in step (d) is essentially perpendicular to the flow of ambient air in step (a), the flow velocity of the desorption medium through the adsorption structure is in the range of 1 to 6 m / sec, at least in step (d).

17. In step (a), the specific flow rate of ambient air through the adsorbent structure is between 100 and 7,000 m as a function of the mass of the sorbent. ３ / h / kg, or In step (a), the specific flow rate of ambient air through the adsorbent structure is between 10,000 and 300,000 m as a function of the volume of the sorbent. ３ / h / m ３ or or wherein, at least in step (d), the specific flow rate of the desorption medium through the adsorbent structure is in the range of 50 to 250 kg / h / kg as a function of the mass of the sorbent; At least in step (d), the specific flow rate of the desorption medium through the adsorbent structure is between 500 and 10,000 kg / h / m as a function of the volume of the sorbent. ３ The method according to any one of claims 1 to 7, wherein the range is

18. a carbon dioxide recovery rate, defined as the percentage of carbon dioxide recovered from the ambient atmosphere by the sorbent material in the adsorption step, in the range of 30 to 60%; or The amount of carbon dioxide recovered by the sorbent per gram of sorbent is in the range of 0.1 to 1.8 mmol / g over a sorption time range of at least 5 minutes or at least 10 minutes; or 18. The method of any one of claims 1 to 7 and 17, wherein the normalized amount of carbon dioxide recovered by the sorbent per gram of sorbent per hour is in the range of 1 to 6 mmol / g / h.

19. the adsorbent structure comprises an array of individual adsorbent elements, each adsorbent element comprising a central carrier layer or porous support flanked on either side by at least one porous and / or permeable sorbent layer having chemically attached carbon dioxide capture moieties in the form of amine groups, the porous sorbent layer being in the form of a woven or nonwoven fiber-based structure; 19. The method of any one of claims 1 to 7, 17 and 18, wherein the carrier layer or porous support layer can be based on at least one of metal, polymer, carbon, carbon molecular sieve and graphene materials.

20. The spacing between the adsorption elements (b spacer ) is in the range of 0.4 to 3 mm, or Each adsorption element has a thickness (b element 20. The method of any one of claims 1 to 7 and 17 to 19, wherein the thickness of the surface of the substrate is 0.2 to 0.5 mm.

21. the unit is capable of being evacuated to a vacuum pressure of 400 mbar (abs) or less, step (b) comprises isolating the sorbent with adsorbed carbon dioxide in the unit from the flow-through while maintaining the temperature within the sorbent, and then evacuating the unit to a pressure in the range of 20 to 400 mbar (abs), in step (c) injecting a stream of saturated or superheated desorption medium also induces an increase in the internal pressure of the reactor unit, step (e) comprises bringing the sorbent material to ambient atmospheric pressure and temperature conditions, and after step (d) and before step (e), the following steps are carried out: (d1) stopping the injection and, if used, the circulation of the desorption medium, and evacuating the unit to a pressure value between 20 and 500 mbar (abs) or bringing the pressure in the unit to a range of 50 to 250 mbar (abs) to evaporate water from the sorbent and dry and cool the sorbent, step (e) is carried out exclusively by contacting ambient air with the sorbent material under ambient atmospheric pressure and temperature conditions to evaporate and remove moisture within the unit and bring the sorbent material to ambient temperature conditions; or the ambient atmosphere in step (a) flows through the parallel fluid passages along essentially a first direction, and in at least one or both of steps (c) and (d), the desorption medium flows along essentially the same first direction or along a direction essentially opposite to the first direction; or 21. The method of any one of claims 1 to 7 and 17 to 20, wherein in step (a), the ambient atmosphere flows through the parallel fluid passages essentially along a first direction, and in at least one or both of steps (c) and (d), the desorption medium flows through the parallel fluid passages essentially along a direction perpendicular to the first direction.

22. 15. A device according to any one of claims 8 to 14 for carrying out a method for separating gaseous carbon dioxide from a gas mixture in the form of ambient air, which also contains gaseous carbon dioxide and a further gas different from gaseous carbon dioxide, by cyclic adsorption / desorption with a sorbent material which adsorbs gaseous carbon dioxide, comprising: The device comprises: a desorption medium source; at least one unit comprising an adsorbent structure having said sorbent material; Including, the adsorbent structure is heatable to a temperature of at least 60°C for desorption of at least the gaseous carbon dioxide, the unit is openable to ambient atmospheric flow-through and contact with a sorbent material for the adsorption step, and the unit is evacuable to a vacuum pressure of 400 mbar (abs) or less; The adsorbent structure includes an array of individual adsorbent elements in the form of layers, each adsorbent element including at least one support layer and at least one sorbent layer including or consisting of at least one sorptive material, the sorptive material being capable of condensing CO2 more than other major non-condensable gases in air in the presence of moisture or water vapor. ２ wherein the adsorption elements in the array are arranged essentially parallel to and spaced apart from one another and are spaced apart at essentially equal intervals from one another to form parallel fluid paths for the flow-through of ambient air and / or desorption medium.

23. The individual adsorbent elements have an element length (L) along the flow-through direction of the ambient atmosphere in the adsorption step (a), and the individual adsorbent elements have an element thickness (b) along a direction perpendicular to the flow-through direction. element ), and the spacing between the adsorption elements is a spacing width (b spacer ), and further, the spacing width (b spacer 23. The device of any one of claims 8 to 14 and 22, wherein the element length (L) is in the range of 0.4 to 5 mm and the element length (L) is in the range of 100 to 3000 mm.

24. 24. The device according to any one of claims 8 to 14, 22 and 23, wherein at least one device for separating carbon dioxide from water is a condenser.

25. 25. The device according to any one of claims 8 to 14 and 22 to 24, wherein the gas outlet side of the device for separating carbon dioxide from water is provided with at least one or both of a carbon dioxide concentration sensor and a gas flow sensor for controlling the desorption process.

26. Interval width (b spacer ) is in the range of 0.5 to 3 mm, or A device according to any one of claims 8 to 14 and 22 to 25, wherein the element length (L) is in the range of 200 to 2000 mm.

27. The element length (L) is the spacing width (b spacer ) and as a function of element thickness (b element ) is given by the following formula: [Equation 2] (In the above formula, K global is 200 to 1000 mm －１ or b element is in the range of 0.1 to 1 mm, or in the range of 0.1 to 0.5 mm, or b spacer The device of any one of claims 8 to 14 and 22 to 26, wherein is in the range of 0.4 to 5 mm, or 0.5 to 3 mm.

28. The adsorption element comprises a central carrier layer and at least one sorbent layer on either side thereof; or the adsorbent structure comprises an array of individual adsorbent elements, each adsorbent element comprising a central porous carrier layer or support and at least one porous and / or permeable sorbent layer on one or both sides thereof having chemically attached carbon dioxide capture moieties in the form of amine groups, the porous sorbent layer being in the form of a woven or nonwoven fiber-based structure; The carrier layer or porous support layer may be based on at least one of metal, polymer, carbon, carbon molecular sieve and graphene materials, or the adsorbent structure comprises an array of individual adsorbent elements, each of which comprises a central carrier or support layer flanked on either side by at least one porous and / or permeable sorbent layer having chemically attached carbon dioxide capture moieties in the form of amine groups, the porous sorbent layer being in the form of a woven or non-woven fiber-based structure; or 28. The device of any one of claims 8 to 14 and 22 to 27, wherein the support or carrier layer is based on at least one of metal, polymer, carbon, carbon molecular sieve and graphene materials and is porous.

29. 29. The device of any one of claims 8 to 14 and 22 to 28, wherein the spacing between the adsorption elements is in the range of 0.5 to 3 mm, and each adsorption element has a planar shape with a thickness in the range of 0.2 to 0.5 mm.

30. means for directing the desorption medium in the desorption medium flow-through step (d) along a flow direction different from the flow-through direction of the ambient atmosphere in the adsorption step (a), the flow direction being perpendicular to the flow-through direction of the ambient atmosphere in the adsorption step (a); 30. The device of any one of claims 8 to 14 and 22 to 29, wherein, at least in the desorption medium flow-through step (d), when the flow of the gas mixture in step (a) and the flow of the desorption medium in step (d) are along different flow paths, and further when the flow of the desorption medium in step (d) is essentially perpendicular to the flow of the gas mixture in step (a), the flow velocity of the desorption medium through the adsorption structure is in the range of 1 to 6 m / s.

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