Carbon monoxide separation technology

Abstract

The invention provides a method for separating carbon monoxide (11) from a gaseous mixture (10) using a sorbent (40) having a specific surface area (As) of ≥10 m2 per gram, wherein the sorbent (40) comprises 0.001 - 25 mg / m2 of a first element (41) comprising an alkali metal or alkaline earth metal, and combinations thereof, and wherein the method comprises: (A) a sorption stage (58) comprising exposing the sorbent (40) to the gaseous mixture (10) at a sorption temperature Ts selected from the range of 250 - 700 °C to provide a loaded sorbent (48); and (B) a desorption stage (59) comprising exposing the loaded sorbent (48) to a desorption gas (20) at a desorption temperature Td selected from the range of 250 - 700 °C to provide a regenerated sorbent (49) and a gaseous product (30), wherein the desorption gas (20) comprises H2 (21) or water vapor (22).

Description

[0001] Carbon monoxide separation technology

[0002] FIELD OF THE INVENTION

[0003] The invention relates to a method for separating carbon monoxide from a gaseous mixture. The invention further relates to a system for separating carbon monoxide from a gaseous mixture.

[0004] BACKGROUND OF THE INVENTION

[0005] Methods for the separation of carbon monoxide from a gaseous mixture are known in the art. US4917711 A, for instance, describes a process for separating CO, unsaturated hydrocarbons, or mixtures thereof, from a mixed gas containing CO, unsaturated hydrocarbons, or mixtures thereof, together with a component selected from the groups consisting of H2, N2, Ar, He, CH4, C2H6, C3H8, CO2and mixtures thereof, which process comprises passing a stream of said gas through a mass of an adsorbent at a temperature in the range from 0 °C to 100 °C. and a pressure from 1 to 100 atmosphere, and releasing the adsorbed CO and / or unsaturated hydrocarbons by heating the adsorbent and / or lowering the pressure.

[0006] US2015008366A1 describes compositions and methods of preparing compositions for sorbents and other surfaces that can adsorb and desorb carbon dioxide. It is described that a sorbent or surface can include a metal compound such as an alkali or alkaline earth compound and a support. The sorbents can be prepared by several methods, including an incipient wetness technique and have a CO2 adsorption and desorption profile.

[0007] W02008150041 Al describes an adsorbent for separating carbon monoxide from a gas m ixture including hydrogen gas and a method of preparing the same. The adsorbent for selectively separating monoxide includes a solid material, which is a solid support impregnated and dispersed with a cuprous salt by bringing the solid support into contact with a cuprous salt solution stabilized by dissolving a cuprous salt or a cuprous salt mixture in a solvent.

[0008] US2024115987A1 describes a dual function material that captures carbon dioxide from ambient air, i.e., direct air capture, and converts the CO2 to a product such as methane. The material includes a high surface area carrier such as Al2O3upon which catalysts and alkaline adsorbents are positioned proximate each other. In the presence of reactive gas such as hydrogen, the catalysts reduce the adjacent adsorbents to generate additional active sites and enhance the amount of CO2 captured by the material. Once the material becomes saturated with CO2, hydrogen is reintroduced to reduce the catalyst, such as ruthenium, at which time the adsorbed CO2 can migrate from the adsorbent to the catalyst for catalytic conversion to methane. The materials can be employed in isothermal, cyclic reactor systems where target species are bound and then desorbed to reactivate the material, e.g., bind more target species for desorption and / or conversion to additional product.

[0009] US4917711A describes adsorbents for use in the separation of carbon monoxide and / or unsaturated hydrocarbons from mixed gases. An adsorbent for separating carbon monoxide or unsaturated hydrocarbon from mixed gases is made by heating a solid mixture comprising a copper compound and a support having a high surface area in a suitable atmosphere.

[0010] SUMMARY OF THE INVENTION

[0011] Carbon monoxide (CO) covers a fundamental role as chemical building block for the synthesis of important commodities. The mixture of CO and H2 (generally referred to as ‘syngas’) serves as basis for producing commercially significant compounds such as methanol, hydrocarbons and acetic acid. Furthermore, as the majority of CO used in the chemical industiy is derived from fossil fuels, its demand signi ficantly contributes to the disruption of the carbon cycle.

[0012] Alternati ve, more sustainable, sources of CO exist, but some severe limitations impede their exploitation. Carbon monoxide is frequently encountered in exhaust streams from industrial operation, refineries, processing of hydrocarbons, internal combustion engines and biomass gasification processes. Often, in these waste streams, carbon monoxide is found in complex mixtures that include air and hydrocarbons. In view of en vironmental concerns waste stream purification may be in high demand.

[0013] Due to its toxicity and the difficulties in gas separation of CO from complex mixtures, carbon monoxide is preferentially burned to CO2 to recover heat energy at the price of increased greenhouse gas emissions. Nonetheless, there is an increasing interest in carbon capture and the reutilization of CO from waste streams, driven by the goal of reducing CO?, emissions and achieving a circular economy with a closed carbon loop.

[0014] Carbon monoxide is present in various exhaust streams including industrial manufacturing, refinery, fossil fuels combustion, internal combustion engines. Current technologies aiming at carbon capture from gas effluents allow, after effluent conditioning, the selecti ve separation of CO2 from the gas stream. However, the removal of CO represents a big challenge, because of the similarity in terms of physical properties between the CO and N2 molecules. Due to this fact, conventional separation technologies are not able to provide an effective and selective separation of CO from N2-containing mixtures. As a consequence, CO is rarely recovered from exhaust gas streams and in order to be emitted, the CO may need to be converted in a further catalytic process to avoid its emission.

[0015] Physisorpti on-based adsorption methods may be inherently limited by the presence of O2and H2O in CO-containing streams and have narrow operating windows in terms of pressure and temperature. Also, the regeneration of the sorbent is often conducted at different operative conditions (temperature, pressure) than the separation process, increasing the operational costs.

[0016] For example, a prior art physisorption-based separation process comprises adsorbing carbon monoxide on a copper (i.e. Cu(l)) compound dispersed on a support (i.e. boehmite, alumina, silica, activated carbon and zeolite). The adsorption of CO takes place in an adsorption tower maintained at a temperature of 0 °C to 100 °C. The discharge of the adsorbed carbon monoxide is performed by vacuum desorption using a vacuum pump. Such prior art processes are limited to a thin range of separation conditions (low temperature < 100 °C, high CO partial pressure, absence of O2 and H2O in the gaseous mixture), which would result in the requirement of extra gas stream conditioning processes.

[0017] Alternatively, prior art processes may use cryogenic separation. However, such processes may be undesirable due to a high energy requirement to maintain the low (cryogenic) temperatures.

[0018] Thus, it is desirable to develop a novel CO separation process which resolves the constraints of the state of the art solutions. Especially, a method may be desired that can effectively separate CO from waste streams containing complex mixtures (including N2, H2O and O2) and reutilize the separated CO as a chemical source.

[0019] Hence, it is an aspect of the invention to provide an alternative method, which preferably further at least partly obviates one or more of above -described drawbacks. The present invention may have as object to overcome or ameliorate at least one of the disadvantages of the prior art, or to provide a useful alternative.

[0020] In a first aspect, the invention may provide a method for separating carbon monoxide from a gaseous mixture using a sorbent. In embodiments, the sorbent may comprise a support material. Especially, the support material may have a specific surface area (As) of at least 10 m2per gram. Further, in embodiments, (a sorbent surface of) the sorbent may comprise 0.001 - 25 mg / nr of a first element. In embodiments, the first element may comprise an alkali metal or alkaline earth metal. Especially, the first element may be selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof. In further embodiments, the method may comprise a sorption cycle comprising a sorption stage and a desorption stage. In embodiments, the sorption stage may comprise exposing the sorbent to the gaseous mixture at a sorption temperature Tsto provide a loaded sorbent. Especially, Tsmay be selected from the range of 250 - 700 °C. Furthermore, in embodiments, the desorption stage may comprise exposing the loaded sorbent to a desorption gas at a desorption temperature Td to provide a regenerated sorbent and a gaseous product. In embodiments, the desorption gas may comprise H2 or water vapor. Furthermore, in embodiments, Td may be selected from the range of250 - 700 °C.

[0021] Hence, in embodiments, the invention may provide a method for separating carbon monoxide from a gaseous mixture using a sorbent, wherein the sorbent has a specific surface area (As) of at least 10 m2per gram, wherein the sorbent comprises 0.001 - 25 mg / m2of a first element, wherein the first element comprises an alkali metal or alkaline earth metal selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof, and wherein the method comprises a sorption cycle comprising: (A) a sorption stage comprising exposing the sorbent to the gaseous mixture at a sorption temperature Tsto provide a loaded sorbent, wherein Tsis selected from the range of 250 - 700 °C; and (B) a desorption stage comprising exposing the loaded sorbent to a desorption gas at a desorption temperature Ta to provide a regenerated sorbent and a gaseous product, wherein the desorption gas comprises H2 or water vapor, wherein Ta is selected from the range of 250 - 700 °C.

[0022] Such a method provides the benefit that separation of carbon monoxide from N and complex gaseous mixtures (including O2, H2O, air, CH4, hydrocarbons) may be obtained via a chemisorption-based process. The method may especially provide a selective carbon monoxide chemisorption-based separation and reutilization process.

[0023] Compared to the traditional CO separation methods, the advantage of this chemisorption-based technology are multiple. For example, the method of the invention may enable operation of the desorption stage (i.e. a (sorbent) regeneration step) at the same temperature and pressure conditions as for the sorption (i.e. separation) stage (i.e. the stages may be performed under isothermal and isobaric conditions). Therewith, the method may provide a simplified process, potentially lowering the operational costs. Moreover, the method of the invention may not require execution of pressure swing operation. In addition, compared to physisorption-based methods, chemisorption-based CO sequestration may be achieved in a wide range of operational conditions, while being robust against moisture and / or O2 in the feed.

[0024] Furthermore, the method may be executed under medium-high temperature conditions as compared to temperatures common to exhaust combustion systems. Therefore, the method may thus be easily implemented for carbon capture in exhaust combustion streams. Besides effectively separating CO from complex streams, the technology of the invention also enables the direct conversion of CO into value-added products (i.e. synthesis gas, CFU, hydrocarbons) that may be readily marketed.

[0025] Furthermore, the method of the invention provides the opportunity to reintegrate CO into the production cycle, therewith reducing the carbon footprint, which may contribute to meeting environmental and regulatory requirements. Moreover, the method of the invention may be applied to capture carbon dioxide (CO2) from gaseous waste streams in addition to carbon monoxide (CO).

[0026] The invention may thus provide a carbon monoxide separation technology, especially a method for separating carbon monoxide from a gaseous mixture. The term “gaseous mixture” may herein especially refer to a mixture of various constituents in the gaseous phase, especially comprising at least carbon monoxide and one other gaseous constituent. For example, in embodiments, the gaseous mixture may comprise an exhaust gas or flue gas.

[0027] In embodiments, the gaseous mixture may comprise at least 0.1 ppm carbon monoxide, such as at least 0.5 ppm carbon monoxide, like at least 1 ppm carbon monoxide, especially at least 5 ppm carbon monoxide. Moreover, in embodiments, the gaseous mixture may comprise at most 99 vol.% carbon monoxide, such as at most 98 vol.%, like at most 95 vol.%, especially at most 90 vol.%. Especially, the gaseous mixture may comprise carbon monoxide selected from the range of 0.5 ppm - 80 vol.%, such as selected from the range of 0.5 ppm - 60 vol%, like from the range of 1 ppm - 50 vol.%, especially from the range of 1 ppm - 20 vol.%.

[0028] Moreover, in embodiments, the gaseous mixture may comprise dinitrogen (N2). Especially, the gaseous mixture may comprise at least 0.5 vol.% dinitrogen, especially at least 1 vol.% dinitrogen, such as at least 2 vol.% dinitrogen, like at least 5 vol.% dinitrogen. In specific embodiments, the gaseous mixture may comprise 1 ppm - 20 vol.% carbon monoxide and at least 1 vol.% dinitrogen. The method of the invention may provide the benefit of selectively separating carbon monoxide from dinitrogen using chemisorption even from relatively dilute gas streams (i.e. CO concentration ranging from ppm to 20 vol%). Furthermore, the sorbent may selectively sequestrate carbon monoxide from complex gaseous mixtures, such as mixtures including one or more of N2, O2, H2O, air, CH4, and hydrocarbons. Therewith, the method may be applied to purify a gaseous stream, such as a waste stream, a complex gas stream at a reactor outlet, or an exhaust combustion stream. The method may especially provide improved (even up to full, i.e., 100%,) removal of carbon monoxide from the gaseous mixture. Especially, the method may comprise using a sorbent having a sorption capacity (see also further below) selected such that at least 70% removal of carbon monoxide from the gaseous mixture may be obtained before saturation of the sorbent (using the method of the invention), such as at least 80% removal of carbon monoxide, like at least 90% removal of carbon monoxide, including essentially 100% removal of carbon monoxide may be obtained before saturation of the sorbent (using the method of the invention).

[0029] The method may thus make use of a sorbent. Herein the term “sorbent” may refer to an material that may either absorb or adsorb liquids and / or gases. The term “to absorb” may refer to the incorporation of a substance in one state into another of a different state. For example, in embodiments, the method may comprise the absorption of a gaseous component (i.e. carbon monoxide) in a solid-state or liquid sorbent. Hence, in embodiments, the sorbent may comprise a solid-state or a liquid sorbent. Conversely, the term “to adsorb” may refer to the physical adherence or bonding of ions and molecules onto the surface of another phase. For example, in embodiments, the method may comprise adsorption of a gaseous component (i.e. carbon monoxide) on the surface of a solid-state sorbent. Hence, in embodiments, the sorbent may comprise a solid-state sorbent.

[0030] Especially, in embodiments, the sorbent may comprise a material that may adsorb gases. Hence, in embodiments, the method may comprise separating carbon monoxide from a gaseous mixture using an adsorbent.

[0031] In embodiments, the sorbent may have a sorption capacity Ccox for (selectively) sorbing the carbon monoxide (and potentially present carbon dioxide). Herein, the sorption capacity Ccox may refer to a total sorption capacity for COXspecies that are present in the gaseous mixture, such as the total sorption capacity for carbon monoxide (CO) and carbon dioxide (CO2) combined, in case of their copresence. Especially, the sorbent may have a sorption capacity Ccox for sorbing the carbon monoxide (and potentially present carbon dioxide) in the gaseous mixture of at least 0.05 mmol / g, such as at least 0.075 mmol / g, like at least 0.1 mmol / g, especially at least 0.2 mmol / g. Moreover, in embodiments, the sorbent may have a sorption capacity Ccox for sorbing the carbon monoxide of at most 1 mmol / g, such as at most 0.8 mmol / g, like at most 0.6 mmol / g, especially at most 0.4 mmol / g. Especially, in embodiments, the sorption capacity Ccox may be selected from the range of 0.05 - 1 mmol / g, like from the range of 0.1 - 0.7 mmol / g, such as from the range of 0.2 - 0.5 mmol / g. The sorption capacity Ccox may especially be determined using a technique such as e.g., volumetric analysis. manometric analysis, and gravimetric analysis. As may be clear to the skilled person, the sorption capacity CCO. may depend on the specific composition of the sorbent.

[0032] The sorbent may, in embodiments, comprise an adsorbent and a support material. In embodiments, the support material may have a relatively high specific surface area (As). Herein, a specific surface area may especially be defined as the total surface area of a material per unit mass (m2 / g). The specific surface area may be determined through the application of the Brunauer-Emmett-Teller (N2-BET) adsorption method on the support material prior to the addition of the first and second elements (hence on the bare support material).

[0033] In embodiments, the specific surface area (As) may be at least 10 m2per gram, such as at least 15 m2per gram, like at least 25 m2per gram. Especially, in embodiments, the specific surface area (As) may be at least 50 m2per gram, especially at least 100 nf per gram, such as at least 250 m2per gram, like at least 500 m2per gram. Moreover, in embodiments, the specific surface area (As) may be at most 2500 m2per gram, such as at most 2000 nf per gram, like at most 1500 n per gram Especially, in embodiments, the specific surface area (As) may be selected from the range of 10 - 1200 m2 / g, such as from the range of 20 - 1000 nf / g, like from the range of 30 - 800 nf / g.

[0034] In specific embodiments, the sorbent may comprise a support material selected from the group comprising metal oxides and carbon-based materials. In embodiments, the support material may comprise a metal oxide selected from the group comprising: y-AhOi, ZrCh, a hydrotalcite, and a zeolite. Additionally or alternatively, in embodiments, the support material may comprise a carbon-based material selected from the group comprising: a carbon fiber, a granular carbon, and an activated carbon. Hence, in embodiments, the sorbent may comprise a support material selected from the group comprising (i) metal oxides, such as y- Al2O3, Z1O2, a hydrotalcite, and a zeolite; and (ii) carbon-based materials, such as a carbon fiber, a granular carbon, and an activated carbon. Such embodiments may be beneficial as these support materials have relatively high surface areas. Furthermore, such support materials may be conveniently functionalized with a metallic component (i.e. the second element, see also further below) and an alkaline or alkaline earth component (i.e. the first element, see also further below), therewith providing a solid base for a bifunctional chemisorption system.

[0035] Further, in embodiments, the sorbent may comprise a sorbent surface. In embodiments, (the sorbent surface of) the sorbent may comprise a first element.

[0036] The first element may, in embodiments, be selected from: an alkali metal, an alkaline earth metal, and a combination thereof. Especially, the first element may be selected from the group comprising: Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof. Such embodiments may be beneficial as the alkali metal or alkaline earth metal may act as the active component for capturing the carbon monoxide on the sorbent. The term “first element” may thus also refer to a plurality of different first elements selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, and Sr. In specific embodiments, the first element may comprise a single element selected from the group comprising: Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, and Sr.

[0037] In embodiments, (the sorbent surface of) the sorbent may comprise 0.001 - 40 mg / m2of the first element, i.e., per unit area m2of the sorbent, the sorbent comprises 0.001 -40 mg of the first element. Especially, (the sorbent surface of) the sorbent may comprise 0.001 - 25 mg / m2, like 0.002 - 25 mg / m2of the first element. In specific embodiments, (the sorbent surface of) the sorbent may comprise 0.05 - 25 mg / m2of the first element. The amount of first element (i.e. alkali metal or alkaline earth metal) per gram of the sorbent may be determined using an analysis technique such as inductively coupled plasma mass spectroscopy (ICP-MS). This amount of first element per gram of sorbent may then be divided by the surface area per gram of sorbent to determine a final composition of first element in mg / m2.

[0038] Further, in embodiments, (the sorbent surface of) the sorbent may comprise a second element. Especially, the second element may be a transition metal. In embodiments, the second element may be selected from the group comprising: Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof. Such embodiments may be beneficial as the transition metal (i.e. metallic component) may intervene in product formation during the desorption stage (i.e. during regeneration of the sorbent). In other words, the choice of transition metal for the second element may define the gaseous product that may be obtained using the method. The term “second element” may thus also refer to a plurality of different second elements selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, and Zn. In specific embodiments, the second element may comprise a single element selected from the group comprising: Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, and Zn.

[0039] For example, in embodiments, the second element may be selected from the group comprising Cu, Pt, and Pd. Such embodiments may be beneficial as the use of such second elements may result in the production of synthetic gas (or “syngas”, i.e., a combination of hydrogen and carbon monoxide) through application of the method, which may be a key component for the production of ammonia or ethanol as well as being a useful fuel gas. Additionally or alternatively, in embodiments, the second element may be selected from the group comprising Ni, Cr, and Ru. Such embodiments may be beneficial as the use of such second elements may result in the production of methane (or “CH4”) through application of the method, which may be used as fuel gas or chemical feedstock for further chemical processes.

[0040] Additionally or alternatively, in embodiments, the second element may be selected from the group comprising Fe and Co. Such embodiments may be beneficial as the use of such second elements may result in the production of a C1-C3 hydrocarbon (such as e.g. one or more of ethane, ethene, propane, and propene) through application of the method, which may be key components for various further chemical (synthesis) processes.

[0041] In embodiments, (the sorbent surface of) the sorbent may comprise 0.005 - 25 mg / m2of the second element, such as 0.01 - 15 mg / m2, especially 0.01 - 10 mg / m2of the second element. In other words, (the sorbent surface of) the sorbent may comprise 0.01 - 10 mg / m2of the second element per unit area m2of the sorbent

[0042] Through incorporation of a transition metal in the sorbent, the desorption (and thus sorbent regeneration) kinetics may be less hindered and thus a lower desorption temperature (Ta, see also further below) may be used, which may reduce energy expenditure. Hence, in embodiments, (the sorbent surface of) the sorbent may comprise 0.01 - 10 mg / m2of a second element, wherein the second element may comprise a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof. In specific embodiments, (the sorbent surface of) the sorbent may comprise 0.01 - 5 mg / m2of the second element. Hence, in embodiments, (the sorbent surface of) the sorbent may comprise 0.05 - 25 mg / m2of the first element and 0.01 - 5 mg / m2of the second element. The amount of second element (i.e. transition metal) per gram of the sorbent may be determined using an analysis technique such as inductively coupled plasma mass spectroscopy (ICP-MS). The determined amount of second element per gram of sorbent may then be divided by the surface area per gram of sorbent to determine a final composition of second element in mg / m2.

[0043] Alternatively, in some embodiments, (the sorbent surface of) the sorbent may comprise <0.005 mg / m2of the second element, like <0.001 mg / m2of the second element, such as <0.0005 mg / m2of the second element, including essentially zero mg / m2of the second element. Hence, in embodiments, the sorbent is devoid of a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof. Such embodiments may be particularly suitable for separating carbon monoxide from gaseous mixtures containing traces of contaminant gases, such as sulfur-comprising compounds, without poisoning of the transition metal and thus reduction of performance. In such embodiments it may be beneficial to apply a relatively higher desorption temperature (Ta, see also further below) to improve the desorption (and thus sorbent regeneration) kinetics.

[0044] Furthermore, in embodiments, the sorbent may comprise 2 -40 wt.% of the first element, such as 3 - 35 wt.%, like 4 - 30 wt.%, especially 5 - 25 wt.% of the first element. Moreover, in embodiments, the sorbent may comprise 5 - 20 wt.% of the first element, such as 10 - 20 wt.%. Conversely, in embodiments, the sorbent may comprise 0.05 - 25 wt.% of the second element, such as 0.1 - 20 wt.%, like 0.1 - 15 wt.%, especial ly 0.5 - 10 wt.% of the second element. Moreover, in embodiments, the sorbent may comprise 0.3 - 10 wt.% of the second element, such as 0.2 - 5 wt.%. Further, in embodiments, the sorbent may comprise 70 - 95 wt.% of the support material, such as 80 - 95 wt.%, like 80 - 90 wt.%, especially 85 - 90 wt.% of the support material. Hence, in embodiments, the sorbent may comprise at least the support material, the first element and the second element. In specific embodiments, the sorbent may comprise 5 - 25 wt.% of the first element and 0.1 - 15 wt.% of the second element. Such embodiments may be beneficial as the sorbent, comprising both the first element and the second element, may comprise a bifunctional material. Hence, the sorbent may both capture carbon monoxide and may be tunable to produce different value-added carbon-based gaseous products. By properly choosing the metallic component of the bifunctional sorbent material, different products can be directly achieved in the regeneration steps including synthesis gas, CH4, and higher hydrocarbons.

[0045] The method may thus comprise separating carbon monoxide from a gaseous mixture using a sorbent. Therefore, in embodiments, the method may comprise a sorption cycle. The sorption cycle may especially comprise a sorption stage and a desorption stage. Through sequential execution of the sorption stage and the desorption stage (in the same reactor or in multiple sequentially fluidically connected reactors) a sorption cycle may be provided.

[0046] In embodiments, the sorption stage (or sorption step) may comprise exposing the sorbent to the gaseous mixture. Especially, the gaseous mixture may be provided to (and forced or allowed to propagate through) a container comprising the sorbent. For example, in embodiments, the gaseous mixture may be fed to a chemical device or reactor comprising the sorbent. Especially, in embodiments, the method may comprise flowing gas over static solvent particles (packed bed configuration) in a reactor. Alternatively, in embodiments, the method may comprise permitting the movement of gaseous particles in a single reactor (e.g. a fluidized bed reactor, a basked mixed flow reactor, etc....) or among multiple reactors (e.g. a circulating fluidized bed reactor, a riser reactor, or an entrained flow reactor). Providing the gaseous mixture to a container comprising the sorbent may be beneficial as effective gas-solid contact may be provided, which may improve the sorption of carbon monoxide onto the sorbent.

[0047] The gaseous mixture may thus be provided to the sorbent. In embodiments, the sorbent may be configured to adsorb at least part of the carbon monoxide in the gaseous mixture to provide a loaded sorbent. Hence, in embodiments, the sorption stage may comprise exposing the sorbent to the gaseous mixture to provide the loaded sorbent.

[0048] Further, in embodiments, the sorption stage may comprise exposing the sorbent to the gaseous mixture at a sorption temperature Ts. In embodiments, the sorption temperature Tsmay be at least 250 °C, such as at least 350 °C, like at least 450 °C. Moreover, in embodiments, the sorption temperature Tsmay be at most 750 °C, such as at most 650 °C, like at most 550 °C. Especially, the sorption temperature Tsmay be selected from the range of 250 - 700 °C. In specific embodiments, the sorption temperature Tsmay be selected from the range of350 - 600 °C.

[0049] In embodiments, the desorption stage (or desorption step) may comprise exposing the loaded sorbent to a desorption gas. Especially, the desorption gas may be provided to (and forced or allowed to propagate through) a container comprising the loaded sorbent. For example, in embodiments, the desorption gas may be fed to a chemical device or reactor comprising the loaded sorbent.

[0050] The desorption gas may thus be provided to the loaded sorbent. In embodiments, the loaded sorbent may be configured to desorb at least part of the carbon monoxide captured in the sorption stage to provide a regenerated sorbent. Hence, in embodiments, the desorption stage may comprise exposing the loaded sorbent to the desorption gas to provide the regenerated sorbent.

[0051] Further, in embodiments, the desorption stage may comprise exposing the loaded sorbent to the desorption gas at a desorption temperature Td. In embodiments, the desorption temperature Ta may be at least 250 °C, such as at least 350 °C, like at least 450 °C. Moreover, in embodiments, the desorption temperature Ta may be at most 750 °C, such as at most 650 °C, like at most 550 °C. Especially, the desorption temperature Ta may be selected from the range of 250 - 700 °C, In specific embodiments, the desorption temperature Ta may be selected from the range of 350 - 600 °C.

[0052] The sorption temperature Tsand the desorption temperature Td may be different temperatures, i.e., T,4T(I. In such embodiments, the following may apply: |TS-Ta|>l 5°, such as |TS-Td|>25°, like |Ts-Td|>50°, especially |Ts-Td|>100°. Alternatively, in embodiments, the sorption stage and the desorption stage may be executed at essentially the same temperature, i.e., the method may be isothermal. An isothermal method, i.e., a method where different operations may be performed under the same temperature condition, may be more energy efficient as less energy is required for heating and / or cooling the process. Furthermore, an isothermal method may provide the advantage that the risk of thermal expansion and / or shrinkage may be reduced. Hence, in embodiments, the sorption temperature Tsand the desorption temperature Ta may be relatively similar temperatures. In such embodiments, |TS- Td| < 75 °C, such as |TS-Td< 50 °C, like |TS-Td| < 20 °C, especially |TS-Td| < 10 °C, including Ts=Td.

[0053] Referring back to the desorption stage, in embodiments, the desorption gas may comprise a gas selected from the group comprising: hydrogen gas (H? (g)), water vapor (II2O (g)), and a combination thereof. For example, in embodiments, the desorption gas may comprise hydrogen gas (II2 (g)). In embodiments, the desorption gas may comprise at least 70 vol.% of H?, such as at least 80 vol.% of H2, like at least 90 vol.% of H2, especially at least 95 vol.% of H2, including essentially 100% of Ffc. Further, in embodiments, the desorption gas may comprise at most 100 vol.% of Fl?, such as at most 80 vol.% of Hz, like at most 60 vol.% of H?, especially at most 50 vol.% of H2. In specific embodiments, the desorption gas may comprise at least 90 vol.% of H? and the gaseous product may comprise hydrogen gas (H2) and carbon monoxide (CO). In other words, in specific embodiments, the desorption gas may comprise at least 90 vol.% of II2 and the gaseous product may comprise syngas.

[0054] As briefly indicated above, the gaseous product may comprise syngas when the second element, in embodiments, is selected from the group comprising copper (Cu), platinum (Pt), and palladium (Pd). Hence, in specific embodiments, (the desorption gas may comprise at least 90 vol.% of H2,) the second element may be selected from the group comprising Cu, Pt, and Pd, and the gaseous product may comprise syngas (i.e. hydrogen gas (Ha) and carbon monoxide (CO)).

[0055] Conversely, in embodiments, the gaseous product may comprise methane when the second element is selected from the group comprising nickel (Ni), chromium (Cr), and ruthenium (Ru). Hence, in specific embodiments, (the desorption gas may comprise at least 90 vol.% of H?,) the second element may be selected from the group comprising Ni, Cr, and Ru, and the gaseous product may comprise methane (i.e. CH4).

[0056] Yet, in embodiments, the gaseous product may comprise a C1-C3 hydrocarbon when the second element is selected from the group comprising iron (Fe) and cobalt (Co). Hence, in specific embodiments, the second element may be selected from the group comprising Fe and Co, and the gaseous product may comprise a Cj-C3 hydrocarbon (such as e.g. one or more of ethane, ethene, propane, and propene). In further embodiments, the desorption gas may comprise at least 90 vol.% of I E.

[0057] Referring back to the desorption gas, in embodiments, the desorption gas may comprise water vapor (H2O (g)). In embodiments, the desorption gas may comprise at least 3 vol.% of H2O, such as at least 5 vol.% of H2O, like at least 10 vol.% of H2O, especially at least 15 vol.% of H2O. In such embodiments, the desorption gas may further comprise an inert gas, such as e.g. one or more of helium, neon, nitrogen (N2), and argon. Hence, in embodiments, the desorption gas may essentially consi st of water vapor in an inert gas such as helium. Further, in embodiments, the desorption gas may comprise at most 100 vol.% of H2O, such as at most 75 vol.% of II2O, like at most 50 vol.% of H? O, especially at most 25 vol.% of H2O. In such embodiments (where the desorption gas comprises water vapor), the gaseous product may comprise carbon dioxide. Especially, the gaseous product may comprise at least 1 vol.% of carbon dioxide, especially at least 2 vol.%, such as at least 3 vol.%, especially at least 5 vol.% carbon dioxide (when the desorption gas comprises water vapor). Moreover, in embodiments, the gaseous product may comprise up to 100 vol.% of carbon dioxide, such as at most 80 vol.%, especially at most 60 vol.% carbon dioxide (when the desorption gas comprises water vapor). Yet, in embodiments, the gaseous product may comprise at most 75 vol.% of carbon dioxide, such as at most 50 vol.%, especially at most 25 vol.% carbon dioxide (when the desorption gas comprises water vapor). In embodiments, the method may comprise transforming carbon monoxide captured by the sorbent into carbon dioxide using water vapor as desorption gas. In such embodiments, essentially no carbon monoxide evolution may occur, therewith providing essential ly full transformation of carbon monoxide to carbon dioxide. Hence, in embodiments, the desorption gas may comprise at least 5 vol.% of H2O, and the gaseous product may comprise at least 2 vol.% of carbon dioxide. Such embodiments may be beneficial as the regeneration step may be accomplished using water vapor at isothermal / isobaric conditions, therewith simplifying the required system and reducing operation costs. Moreover, the regeneration step does not necessarily include the execution of pressure swing operation. In such embodiments, the adsorbed CO may be converted to CO2 and II2 upon its reaction with water, through a water gas shift reaction process. A further advantage of such embodiments may be that water vapor is a relatively inexpensive regeneration agent.

[0058] As briefly indicated above, the gaseous product may comprise syngas when the second element is selected from the group comprising copper (Cu), platinum (Pt), and palladium (Pd). Hence, in specific embodiments, (the desorption gas may comprise at least 90 vol.% of H2,) the second element may be selected from the group comprising Cu, Pt, and Pd, and the gaseous product may comprise syngas (i.e. hydrogen gas (Fb) and carbon monoxide (CO)).

[0059] As described above, the sorption stage and the desorption stage may both be performed at their respective sorption and desorption temperatures (Ts, T<i). Moreover, in embodiments, the method may comprise executing the sorption stage at a sorption pressure pi. In embodiments, the sorption pressure pi may be selected from the range of >1 bar, such as >1.5 bar, like >2 bar. Further, in embodiments, the sorption pressure pi may be selected from the range of <200 bar, such as <100 bar, like <50 bar.

[0060] Similarly, in embodiments, the method may comprise executing the desorption stage at a desorption pressure p2. In embodiments, the desorption pressure p2 may be selected from the range of >1 bar, such as >1.5 bar, like >2 bar. Further, in embodiments, the desorption pressure p2 may be selected from the range of <200 bar, such as <100 bar, like <50 bar.

[0061] In embodiments, the sorption pressure pi and the desorption pressure ps may be different pressures, i.e., p p2. In such embodiments, the following may apply: |pj-p2|> I bar, such as |pj-p2|>2 bar, like |pj- 2|>5 bar, especially |pj-p2|>10 bar. Alternatively, in embodiments, the sorption stage and the desorption stage may be executed at essentially the same pressure, i.e., the sorption cycle may be isobaric. Especially, in embodiments, the sorption pressure pi and the desorption pressure p2 may be relatively similar pressures. In such embodiments, |pi-p2| < 2.5 bar, such as |pi-p2| < 2 bar, like |pi-p2| < 1.5 bar, especially |pi-p2| < 1 bar, including pi=p2. In specific embodiments, the method may comprise executing the sorption stage at a sorption pressure pi and executing the desorption stage at a desorption pressure p2, wherein |pi-p2| < 1 bar.

[0062] The method may thus comprise a sorption cycle comprising a sorption stage and a desorption stage as described above. Further, in embodiments, the method may comprise a plurality of sorption cycles. For example, in embodiments, the method may comprise between n (successive) sorption cycles. In embodiments, n may be selected from the range of 1 - 500 sorption cycles, such as selected from the range of 2 - 250 sorption cycles, like selected from the range of 5 - 100 sorption cycles. Especially, in embodiments, the method may comprise at least 25 sorption cycles (i.e., n>25), such as at least 50 sorption cycles (i.e., n>50), like at least 100 sorption cycles (i.e., n>100), especially at least 1000 sorption cycles (i.e., n>1000). In embodiments, the regenerated sorbent in one sorption cycle may be used as the sorbent in a subsequent sorption cycle. The method, especially the sorption cycles, may comprise a first sorption cycle and a second sorption cycle. As such, in embodiments, the regenerated sorbent of the first sorption cycle may be used as the sorbent in the second sorption cycle. Moreover, in embodiments, the regenerated sorbent of the second sorption cycle may be used as the sorbent in a subsequent (e.g. a third) sorption cycle, etc. etc.... Hence, in embodiments, the method may comprise a plurality of sorption cycles, wherein the sorption cycles may comprise a first sorption cycle and a second sorption cycle, wherein the regenerated sorbent of the first sorption cycle may be used as the sorbent in the second sorption cycle. Such embodiments may be beneficial as reusing the sorbent of a first sorption cycle in subsequent sorption cycles may reduce chemical waste and therewith the wasteful impact and carbon footprint of the method on the environment. Furthermore, by reusing the sorbent the costs of the method may be significantly reduced.

[0063] In a further aspect, the invention provides a system for separating carbon monoxide from a (carbon monoxide containing) gaseous mixture. In embodiments, the system may comprise an inlet, a gas supply, a sorbent container, and a temperature control system. Further, in embodiments, the system may comprise both the inlet and an outlet. The inlet may be fluidical ly connected to the sorbent container. Furthermore, in embodiments, the gas supply may be configured to provide a desorption gas to the sorbent container. In embodiments, the desorption gas may comprise H2 or water vapor. Further, in embodiments, the temperature control system may be configured to control a temperature of the sorbent container. Further, in embodiments, the system may be configured to execute an operational mode wherein the sorbent container may host a sorbent. Especially, the sorbent (may comprise a support material, wherein the support material) may have a specific surface area (As) of at least 10 m2per gram. Furthermore, in embodiments, the sorbent may comprise 0.001-40 mg / m2of a first element. In embodiments, the first element may comprise an alkali metal or alkaline earth metal. Especially, the first element may be selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof. Further, in embodiments, the system may be configured to execute a soiption cycle comprising a sorption stage and a desorption stage. In embodiments, in the sorption stage, the inlet may be configured to receive the gaseous mixture and to provide the gaseous mixture to the sorbent container. Furthermore, in embodiments, in the sorption stage, the temperature control system may be configured to control the temperature of the sorbent container at a sorption temperature Ts. Especially, Tsmay be selected from the range of 250-700 °C. In embodiments, in the desorption stage, the gas supply may be configured to provide the desorption gas to the sorbent container. Furthermore, in embodiments, in the desorption stage, the temperature control system may be configured to control the temperature of the sorbent container at a desorption temperature Ta. Especial ly, Ta may be selected from the range of 250-700 °C.

[0064] Hence, in embodiments, the invention may provide a system for separating carbon monoxide from a (carbon monoxide containing) gaseous mixture, wherein the system comprises an inlet, a gas supply, a sorbent container, and a temperature control system, wherein the inlet is fluidically connected to the sorbent container, wherein the gas supply is configured to provide a desorption gas to the sorbent container, wherein the desorption gas comprises H2 or water vapor, and wherein the temperature control system is configured to control a temperature of the sorbent container, wherein the system is configured to execute an operational mode wherein: (A) the sorbent container hosts a sorbent, wherein the sorbent (comprises a support material, wherein the support material) has a specific surface area (As) of at least 10 m2per gram, wherein the sorbent comprises 0.001-40 mg / m2of a first element, wherein the first element comprises an alkali metal or alkaline earth metal selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof; and (B) the system executes a sorption cycle comprising: (i) a sorption stage wherein (a) the inlet is configured to receive the gaseous mixture and to provide the gaseous mixture to the sorbent container, and (b) the temperature control system is configured to control the temperature of the sorbent container at a sorption temperature Ts, wherein Tsis selected from the range of 250-700 °C; (ii) a desorption stage wherein (a) the gas supply is configured to provide the desorption gas to the sorbent container, and (b) the temperature control system is configured to control the temperature of the sorbent container at a desorption temperature Td, wherein Td is selected from the range of 250-700 °C. Moreover, in embodiments, the invention may provide a system for separating carbon monoxide from a (carbon monoxide containing) gaseous mixture, wherein the system comprises an inlet, a gas supply, a sorbent container, and a temperature control system, wherein the inlet is fluidically connected to the sorbent container, wherein the gas supply is configured to provide a desorption gas to the sorbent container, wherein the desorption gas comprises H2 or water vapor, and w'herein the temperature control system is configured to control a temperature of the sorbent container, wherein the sorbent container hosts a sorbent, wherein the sorbent (comprises a support material, wherein the support material) has a specific surface area (As) of at least 10 m2per gram, wherein the sorbent comprises 0.001-40 mg / m2of a first element, wherein the first element comprises an alkali metal or alkaline earth metal selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof; and the system is configured to execute, in an operational mode, a sorption cycle comprising: (i) a sorption stage wherein (a) the inlet is configured to receive the gaseous mixture and to provide the gaseous mixture to the sorbent container, and (b) the temperature control system is configured to control the temperature of the sorbent container at a sorption temperature Ts, wherein Tsis selected from the range of 250-700 °C; (ii) a desorption stage wherein (a) the gas supply is configured to provide the desorption gas to the sorbent container, and (b) the temperature control system is configured to control the temperature of the sorbent container at a desorption temperature Ta, wherein Ta is selected from the range of 250-700 °C.

[0065] The system of the invention may provide the benefit of selectively separating carbon monoxide from dinitrogen using chemisorption even from relatively dilute gas streams (i.e. CO concentration ranging from ppm to 20 vol%). Furthermore, the sorbent may selectively sequestrate carbon monoxide from complex gaseous mixtures, such as mixtures including one or more of N2, O2, argon, H2O, air, CH4, and hydrocarbons. Therewith, the system may be applied to purify a gaseous stream, such as a waste stream, a complex gas stream at a reactor outlet, or an exhaust combustion stream. The system may especially be applied to recover purified and concentrated carbon monoxide streams from such complex gaseous mixtures. Furthermore, the system may be used to capture carbon dioxide.

[0066] The gas supply, configured to provide the desorption gas, may further provide the advantage of regeneration of the sorbent through the facilitation of the desorption gas to the sorbent, therewith increasing the lifetime of the system. Hence, with the system of the invention a plurality of cycles may be run without the requirement of replacing the sorbent. In other words, the system may provide the benefit of reusability and may thus be a sustainable and cost efficient system. Furthermore, the system may be operated at a medium-high temperature range and may thus be easily implemented for carbon capture in exhaust combustion streams.

[0067] The invention may thus provide a system for separating carbon monoxide from a (carbon monoxide containing) gaseous mixture. The system may, in embodiments, comprise an inlet, a gas supply, a sorbent container, and a temperature control system.

[0068] In embodiments, the inlet may be fluidically connected to the sorbent container. Herein, the term “fluidically connected” or “fluidically coupled” may refer to two components being configured such that a fluid, such as a liquid or a gas, may be configured in contact with both components and / or may migrate between the two components. The inlet may, in embodiments, be configured to provide the gaseous mixture from a gaseous mixture source (see also further below) to the system, especially to the sorbent container.

[0069] Further, in embodiments, the system may comprise an outlet. The outlet may especially be fluidically connected to the sorbent container. In embodiments, the outlet may be configured to provide a gaseous product (see also above and further below) generated in the sorbent container during the desorption stage to a storage container or a subsequent (chemical) reactor / process.

[0070] The sorbent container may, in embodiments, be configured to receive the gaseous mixture (from the gaseous mixture source via the inlet). In embodiments, the sorbent container may be configured to adsorb carbon monoxide from the gaseous mixture. Therefore, in embodiments, the sorbent container may host a sorbent. In other words, the sorbent container may be configured to host a sorbent. The sorbent container may, in embodiments, comprise one or more of a chemical device, a reactor, a column, an adsorption tower or adsorber, etc.... The sorbent container may especially comprise a chemically inert material (as opposed to the sorbent hosted by the sorbent container).

[0071] In embodiments, the sorbent container may comprise one or more of (a) static solvent particles (e.g. a packed bed configuration), (b) a reactor that permits the movement of particles in that single reactor (e.g. a fluidized bed, basked mixed flow reactor, etc...), and (c) multiple reactors that permit the movement of particles between said reactors (e.g. a circulating fluidized bed reactor, riser reactor, entrained flow reactor). Hosting the sorbent in a sorbent container and configuring the system to provide the gaseous mixture to the sorbent container may facilitate providing an effective gas-solid contact, in turn leading to effective sorption and / or desorption.

[0072] In embodiments, the sorbent may comprise a material that may adsorb gases, especially carbon monoxide. Embodiments of the sorbent described above for the method may mutatis mutandis apply for the sorbent hosted in the system. In short, the sorbent may, in embodiments, comprise an adsorbent and a support material. In embodiments, the support material may have a relatively high specific surface area (As). Especially, the specific surface area (As) may be at least 10 m2per gram, such as at least 15 m2per gram, like at least 25 m2per gram. In embodiments, the specific surface area (As) may be at least 50 m2per gram, especially at least 100 m2per gram, such as at least 250 m2per gram, like at least 500 m2per gram. Moreover, in embodiments, the specific surface area (As) may be at most 2500 m2per gram, such as at most 2000 m2per gram, like at most 1500 m2per gram Especially, in embodiments, the specific surface area (As) may be selected from the range of 10 - 1200 m2 / g, such as from the range of 20 - 1000 m2 / g, like from the range of 30 - 800 m2 / g.

[0073] In specific embodiments, the sorbent may comprise any type of support material, such as e.g. a support material selected from the group comprising metal oxides and carbonbased materials. Further, in embodiments, the sorbent may comprise a sorbent surface. In embodiments, (the sorbent surface of) the sorbent may comprise a first element. The first element may, in embodiments, be selected from: an alkali metal, an alkaline earth metal, and a combination thereof. Especially, the first element may be selected from the group comprising: Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof. Such embodiments may be beneficial as the alkali metal or alkaline earth metal may act as the active component for capturing the carbon monoxide on the sorbent.

[0074] In embodiments, (the sorbent surface of) the sorbent may comprise 0.001 - 40 mg / m2of the first element, i.e., per unit area m2of the sorbent, the sorbent comprises 0.001 -40 mg of the first element. Especial ly, (the sorbent surface of) the sorbent may comprise 0.001 - 25 mg / m2, like 0.002 - 25 mg / m2of the first element. In specific embodiments, (the sorbent surface of) the sorbent may comprise 0.05 - 25 mg / m2of the first element.

[0075] Additionally, in embodiments, (the sorbent surface of) the sorbent may comprise a second element. The second element may especially be a transition metal. Especially, the second element may be selected from the group comprising: Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof. For example, in embodiments, the second element may be selected from the group comprising Cu, Pt, and Pd. Additionally or alternatively, in embodiments, the second element may be selected from the group comprising Ni, Cr, and Ru. Additionally or alternatively, in embodiments, the second element may be selected from the group comprising Fe and Co.

[0076] In embodiments, (the sorbent surface of) the sorbent may comprise 0 - 25 mg / m2of the second element, such as 0 - 15 mg / m2, i.e., per unit area m2of the sorbent, the sorbent comprises 0 - 15 mg of the second element. Especially, (the sorbent surface of) the sorbent may comprise 0.01 - 15 mg / m2of the second element, such as 0.01 - 10 mg / m2of the second element. In specific embodiments, (the sorbent surface of) the sorbent may comprise 0.01 - 5 mg / m2of the second el ement. Hence, in embodiments, (the sorbent surface of) the sorbent may comprise 0.05 - 25 mg / m2of the first element and 0.01 - 5 mg / m2of the second element.

[0077] Alternatively, in some embodiments, (the sorbent surface of) the sorbent may comprise <0.005 mg / m2of the second element, like <0.001 mg / m2of the second element, such as <0.0005 mg / m2of the second element, including essentially zero mg / m2of the second element. Hence, in embodiments, the sorbent is devoid of a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof. Such embodiments may be particularly suitable for separating carbon monoxide from gaseous mixtures containing traces of contaminant gases, such as sulfur- comprising compounds, without poisoning of the transition metal and thus reduction of performance. In such embodiments it may be beneficial to apply a relatively higher desorption temperature (Ta, see also further below) to improve the desorption (and thus sorbent regeneration) kinetics.

[0078] However, in embodiments, the sorbent may comprise 5-25 wt.% of the first element and 0.1-15 wt.% of the second element. Such embodiments may be beneficial as the sorbent, comprising both the first element and the second element, may comprise a bifunctional material. Hence, the system may be configured (i) to capture carbon monoxide using the sorbent and (ii) tunable through carefid selection of the sorbent to produce different value-added carbon-based gaseous products. By selecting different metallic components for the bifunctional sorbent material, during operation of the system different products can be achieved in the regeneration steps including synthesis gas, CITj, and higher hydrocarbons.

[0079] The system may further comprise a gas supply. In embodiments, the gas supply may be configured fluidically connected to the sorbent container. The gas supply may, in embodiments, be configured to provide a desoiption gas to the system, especially to the sorbent container. The desorption gas may, in embodiments, comprise a gas selected from the group comprising: hydrogen gas (H2 (g)), water vapor (ITO (g)), and a combination thereof. For example, in embodiments, the desorption gas may comprise hydrogen gas (H2 (g)). In embodiments, the desorption gas may comprise at least 70 vol.% of Hz, such as at least 80 vol.% of H2, like at least 90 vol.% of H2, especially at least 95 vol.% of H2, including essentially 100% of H2. Further, in embodiments, the desorption gas may comprise at most 100 vol.% of Hz, such as at most 80 vol.% of H2, like at most 60 vol.% of Hz, especially at most 50 vol.% of H2.

[0080] Additionally or alternatively, in embodiments, the desorption gas may comprise water vapor (H2O (g)). In embodiments, the desorption gas may comprise at least 3 vol.% of HzO, such as at least 5 vol.% of H2O, like at least 10 vol.% of H2O, especially at least 15 vol.% of H2O. In such embodiments, the desorption gas may further comprise an inert gas, such as e.g. one or more of helium, neon, and argon. Hence, in embodiments, the desorption gas may essentially consist of water vapor in an inert gas such as helium. Further, in embodiments, the desorption gas may comprise at most 100 vol.% of H2O, such as at most 75 vol.% of II2O, like at most 50 vol.% of H2O, especially at most 25 vol.% of H2O.

[0081] In embodiments, the desoiption gas may comprise both hydrogen gas (H2 (g)) and water vapor (H2O (g)). However, in alternative embodiments, the desorption gas may comprise hydrogen gas with very little or even no water vapor. In such embodiments, the desorption gas may comprise hydrogen gas and at most 0.5 vol.% water vapor, such as at most 0.1 vol.% water vapor, like at most 0.05 vol.% water vapor, especially at most 0.01 vol.% water vapor. Conversely, in embodiments, the desorption gas may comprise water vapor with very little or even no hydrogen gas. In such embodiments, the desorption gas may comprise water vapor and at most 0.5 vol.% hydrogen gas, such as at most 0.1 vol.% hydrogen gas, like at most 0.05 vol.% hydrogen gas, especially at most 0.01 vol.% hydrogen gas.

[0082] The system may further comprise a temperature control system. In embodiments, the temperature control system may be configured to control a temperature of the sorbent container. Especially, the temperature control system may be configured to control a temperature of the sorbent e.g., by controlling the temperature of the gaseous mixture.

[0083] The term “controlling” and similar terms especially refer at least to determining the behavior or supervising the running of an element. Hence, herein “controlling” and similar terms may e.g. refer to imposing behavior to the element (determining the behavior or supervising the running of an element), etc., such as e.g. measuring, displaying, actuating, opening, shifting, changing temperature, etc.. Beyond that, the term “controlling” and similar terms may additionally include monitoring. Hence, the term “controlling” and similar terms may include imposing behavior on an element and also imposing behavior on an element and monitoring the element. The controlling of the element can be done with a (temperature) control system, which may also be indicated as “controller”. The (temperature) control system and the element (e.g. the sorbent container) may thus at least temporarily, or permanently, functionally be coupled. The element may comprise the control system. In embodiments, the control system and element may not be physically coupled. Control can be done via wired and / or wireless control. The term “control system” may also refer to a plurality of different control systems, which especially are functionally coupled, and of which e.g. one control system may be a master control system and one or more others may be slave control systems. A control system may comprise or may be functionally coupled to a user interface.

[0084] The control system may also be configured to receive and execute instructions from a remote control. In embodiments, the control system may be controlled via an App on a device, such as a portable device, like a Smartphone or I-phone, a tablet, etc..

[0085] In embodiments, the system may further comprise a control system. In embodiments, the control system may be configured to control the temperature control system (and the pressure control unit, see also further below). Additionally or alternatively, in embodiments, the control system may be configured to control a gas flow at the inlet and / or from the gas supply. Especially, in embodiments, the control system may be configured to control subsequent (or successive) feeding of the gaseous mixture and the desorption gas, respectively, to the sorbent container.

[0086] The system may be configured to separate carbon monoxide from a gaseous mixture using a sorbent. Therefore, in embodiments, the system may be configured to execute an operational mode wherein the system executes a sorption cycle. Especially, in embodiments, the control system may be configured to have the system execute the operational mode, i.e., to execute the sorption cycle. The system may execute an action in a “mode” or “operation mode” or “mode of operation” or “operational mode”. The term “operational mode” may also be indicated as “controlling mode”. Likewise, in a method an action or stage, or step may be executed in a “mode” or “operation mode” or “mode of operation” or “operational mode”. This does not exclude that the system may also be adapted for providing another controlling mode, or a plurality of other controlling modes. Likewise, this may not exclude that before executing the mode and / or after executing the mode one or more other modes may be executed.

[0087] The system may thus, in an operational mode, be configured to execute a sorption cycle. The sorption cycle may especially comprise a sorption stage and a desorption stage. Through sequential execution of the sorption stage and the desorption stage (in the same reactor or in multiple sequentially fluidically connected reactors) a sorption cycle may be provided.

[0088] In embodiments, in the sorption stage (or sorption step) the inlet may be configured to receive the gaseous mixture and to provide the gaseous mixture to the sorbent container. As such, in embodiments, the system may be configured to expose the sorbent to the gaseous mixture. Especially, the gaseous mixture may be provided to (and forced or allowed to propagate through) the sorbent container via the inlet. In embodiments, the sorbent may be configured to adsorb at least part of the carbon monoxide in the gaseous mixture to provide a loaded sorbent. Hence, in embodiments, the sorption stage may comprise exposing the sorbent to the gaseous mixture to provide the loaded sorbent.

[0089] Further, in embodiments, in the sorption stage the temperature control system may be configured to control the temperature of the sorbent container at a sorption temperature Ts. In embodiments, the sorption temperature Tsmay be at least 250 °C, such as at least 350 °C, like at least 450 °C. Moreover, in embodiments, the sorption temperature Tsmay be at most 750 °C, such as at most 650 °C, like at most 550 °C. Especially, the sorption temperature Tsmay be selected from the range of 250 - 700 °C. In specific embodiments, the sorption temperature Tsmay be selected from the range of 350 - 600 °C. In embodiments, in the desorption stage (or desorption step) the gas supply may be configured to provide the desorption gas to the sorbent container. As such, in embodiments, the system may be configured to expose the loaded sorbent to the desorption gas. Especially, the desorption gas may be provided to (and forced or allowed to propagate through) the sorbent container via the gas supply. In embodiments, the loaded sorbent may be configured to desorb at least part of the carbon monoxide captured in the sorption stage to provide a regenerated sorbent. Hence, in embodiments, the desorption stage may comprise exposing the loaded sorbent to the desorption gas to provide the regenerated sorbent.

[0090] Further, in embodiments, in the desorption stage the temperature control system may be configured to control the temperature of the sorbent container at a desorption temperature Ta. In embodiments, the desorption temperature Ta may be at least 250 °C, such as at least 350 °C, like at least 450 °C. Moreover, in embodiments, the desorption temperature Ta may be at most 750 °C, such as at most 650 °C, like at most 550 °C. Especially, the desorption temperature Ta may be selected from the range of 250 - 700 °C. In specific embodiments, the desorption temperature Ta may be selected from the range of 350 - 600 °C.

[0091] The sorption temperature Tsand the desorption temperature Ta may be different temperatures, i.e., T Td. In such embodiments, the following may apply: |TS-Td|>15°, such as |Ts-Ta|>25o, like jTs-Td|>50°, especially |Ts-Td|>100°. Alternatively, in embodiments, the sorption stage and the desorption stage may be executed at essentially the same temperature, i.e., the sorption cycle may be isothermal. Especially, in embodiments, the sorption temperature Tsand the desorption temperature Td may be relatively similar temperatures. In such embodiments, |TS-Td|<75 °C, such as |Ts-Td|<50 °C, like |Ts-Td|<20 °C, especially |TS-Td| <10 °C, including Ts=Td.

[0092] As described above, the sorption stage and the desorption stage may both be performed at their respective sorption and desorption temperatures (Ts, Td). Moreover, in embodiments, the system may be configured to execute the sorption stage a sorption pressure pi. In embodiments, the sorption pressure pi may be selected from the range of >1 bar, such as >1.5 bar, like >2 bar. Further, in embodiments, the sorption pressure pj may be selected from the range of <200 bar, such as <100 bar, like <50 bar.

[0093] Similarly, in embodiments, the system may be configured to execute the desorption stage at a desorption pressure ps. In embodiments, the desorption pressure p2 may be selected from the range of >1 bar, such as >1.5 bar, like >2 bar. Further, in embodiments, the desorption pressure p? may be selected from the range of <200 bar, such as <100 bar, like <50 bar. In embodiments, the sorption pressure pi and the desorption pressure p2 may be different pressures, i.e., pi p2. In such embodiments, the following may apply: |pi-p2|>l bar, such as |pj-p2|>2 bar, like |pi-p2|>5 bar, especially |pj-p2|>10 bar. Alternatively, in embodiments, the sorption stage and the desorption stage may be executed at essentially the same pressure, i.e., may be isobaric. Especially, in embodiments, the sorption pressure pi and the desorption pressure p2 may be relatively similar pressures. In such embodiments, |pi-p2j < 2.5 bar, such as |pi-p2|<2 bar, like |pi-p2|<l.5 bar, especially |pi-p2|<l bar, including pi=p2.

[0094] The system may further comprise a pressure control unit. In embodiments, the pressure control unit may be configured to control a pressure in the sorbent container. Especially, the pressure control unit may be configured to control a pressure in the sorbent container at the sorption pressure pi during the sorption stage. Additionally, the pressure control unit may be configured to control a pressure in the sorbent container at the desorption pressure p2 during the desorption stage.

[0095] The system, in the operational mode, may thus be configured to execute a sorption cycle comprising a sorption stage and a desorption stage as described above. Further, in embodiments, the system may be configured to execute a plurality of (successive) sorption cycles in the operational mode. For example, in embodiments, the system may be configured to execute n (successive) sorption cycles. In embodiments, n may be selected from the range of 1 - 500 sorption cycles, such as selected from the range of 2 - 250 sorption cycles, like selected from the range of 5 - 100 sorption cycles. Especially, in embodiments, the system may be configured to execute at least 25 sorption cycles (i.e., n>25), such as at least 50 sorption cycles (i.e., n>50), like at least 100 sorption cycles (i.e., n>100), especially at least 1000 sorption cycles (i.e., n>1000). In embodiments, the regenerated sorbent in one sorption cycle may be used as the sorbent in a subsequent sorption cycle. Especially, (the method, especially) the sorption cycles may comprise a first sorption cycle and a second sorption cycle. As such, in embodiments, the regenerated sorbent of the first sorption cycle may be used as the sorbent in the second soiption cycle. Moreover, in embodiments, the regenerated sorbent of the second sorption cycle may be used as the sorbent in a subsequent (e.g. a third) sorption cycle, etc. etc....

[0096] In embodiments, the sorption stage and the desorption stage may be executed in the same (single) sorbent container (e.g. chemical reactor). In such embodiments, the different gases (especially the (CO rich) gaseous mixture and the desorption (or regeneration) gas) may be fed to the sorbent container sequentially, therewith resulting in a cyclical operation. Alternatively, in embodiments, the sorption stage and the desorption stage may be executed in the separate (first and second) sorbent containers (e.g. chemical reactors). In such embodiments, the system may comprise a first sorbent container and a second sorbent container. In embodiments, in the operational mode of the system, the (CO rich) gaseous mixture may be fed into the first sorbent container. Hence, the first sorbent container may comprise the sorbent during the sorption stage. Between the sorption stage and the desorption stage the (now loaded) sorbent may be transferred from the first sorbent container to the second sorbent container. As such, in embodiments, the second sorbent container may comprise the sorbent during the desorption stage. Moreover, in such embodiments, the desorption (or regeneration) gas may be fed to the second sorbent container. Hence, in such embodiments, the system may comprise two (or more) chemical reactors. Here, cyclical operation may thus be ensured by, in this case, transferring the sorbent from one reactor to the other one.

[0097] In embodiments, in the operational mode, the system may be configured to generate a gaseous product during the desorption stage. In embodiments, the gaseous product may comprise a gas selected from the group comprising: l b, CO, CO2, O2, syngas, CH4, a Ci- C3 hydrocarbon, and a larger hydrocarbon. In specific embodiments, the gaseous product may comprise a gas selected from the group comprising: II2, CO, CO2, syngas, CII4, and a C1-C3 hydrocarbon. The gaseous product may, in embodiments, essentially consist of a single gas compound, such as e.g. pure CO. Alternatively, in embodiments, the gaseous product may comprise a combination of gases selected from the group comprising: H2, CO, CO2, CH4, and a C1-C3 hydrocarbon. For example, the gaseous product may especially comprise syngas, i.e., a combination of II2 and CO. Alternatively, in embodiments, the gaseous product may comprise a combination of H and CO2. Yet alternatively, in embodiments, the gaseous product may comprise a combination of H2 and a C1-C3 hydrocarbon The system may therefore, in embodiments, comprise an outlet fluidically connected to the sorbent container. The outlet may especially be configured to provide the gaseous product generated in the sorbent container during the desorption stage to a storage container or a subsequent (chemical) reactor / process.

[0098] In further embodiments, the system may comprise a gaseous mixture source. In embodiments, the gaseous mixture source may be selected from the group comprising a combustion system (, such as an internal combustion engine), an industrial plant(, such as a hydrocarbon processing plant), a refinery system, a biomass gasification system, a lignocellulosic gasification system, and a pyrolysis system. Especially, the gaseous mixture source may be configured to provide the gaseous mixture to the inlet (during the sorption stage). Further, in embodiments, the gaseous mixture source (especially the combustion system) may be configured to provide the gaseous mixture with a gaseous mixture temperature Tg. In embodiments, Tgmay be selected from the range of 100 - 1200 °C, such as from the range of 200 - 1000 °C, like from the range of 350 - 900 °C, especially from the range of 350 - 700 °C. Moreover, in embodiments, Tgmay be selected from the range of 250 - 600 °C, such as from the range of 400 - 600 °C.

[0099] In specific embodiments, the gaseous mixture source may comprise a combustion system. In such embodiments, the gaseous mixture may comprise an exhaust gas.

[0100] BRIEF DESCRIPTION OF THE DRAWINGS

[0101] Embodiments of the invention will now be described, by way of example only, with reference to the accompanying schematic drawings in which corresponding reference symbols indicate corresponding parts, and in which: Fig. 1A schematically depicts embodiments of the system of the invention. Fig. 1 B schematically depicts an embodiment of the method of the invention. Figs. 2A-E schematically depict experimental results obtained with the method of the invention. The schematic drawings are not necessarily on scale.

[0102] DETAILED DESCRIPTION OF THE EMBODIMENTS

[0103] Fig. 1 A schematically depicts an embodiment of the system 100 for separating carbon monoxide 11 from a (carbon monoxide containing) gaseous mixture 10. The gaseous mixture 10 may comprise at least carbon monoxide 11. Furthermore, in embodiments such as depicted in Fig. 1 A, the gaseous mixture 10 may further comprise dinitrogen 12. For example, in embodiments, the gaseous mixture 10 may comprise an exhaust gas.

[0104] In the depicted embodiment, the system 100 may comprise an inlet 110, a gas supply 120, an outlet 130, a sorbent container 140, and a temperature control system 150.

[0105] In embodiments, the inlet 110 may be fluidically connected to the sorbent container 140. As depicted, the inlet 110 may be configured to provide (or feed) the gaseous mixture 10 to the sorbent container 140. The gaseous mixture 10 may for example be sourced from a gaseous mixture source 200. The gaseous mixture source 200 may especially be selected from the group comprising a combustion system 210, such as an internal combustion engine, an industrial plant, such as a hydrocarbon processing plant, a refinery system, a biomass gasification system, a lignocellulosic gasification system, and a pyrolysis system. Especially, the gaseous mixture source 200 may be configured to provide the gaseous mixture 10 to the inlet 110. Further, in embodiments, the gaseous mixture source 200 may be configured to provide the gaseous mixture 10 with a gaseous mixture temperature Tg. Especially, Tgmay be selected from the range of 200-1000 °C. As depicted here, the gaseous mixture source 200 may comprise a combustion system 210 configured to provide the gaseous mixture 10 (which may comprise an exhaust gas) to the sorbent container 140 via the inlet 110.

[0106] Further, in embodiments, the gas supply 120 may be configured to provide (or feed) a desorption gas 20 to the sorbent container 140. In embodiments, the desorption gas 20 may comprise lb 21 or water vapor 22.

[0107] The inlet 110 and the gas supply 120 may be operated successively so as to create a sorption cycle 50 (see also further below) in the sorbent container 140. Hence, in embodiments, the system 100 may be configured to execute an operational mode. Especially, in the operational mode, the system 100 may be configured to execute a sorption cycle 50 comprising a sorption stage 58 and a desorption stage 59, see especialty Fig. IB. The system 100 may especially be configured to execute a plurality of (successive) sorption cycles 50 in the operational mode.

[0108] In the left schematic of Fig. 1A, the system 100 is depicted during operation of the sorption stage 58 of the sorption cycle 50. In embodiments, in the sorption stage 58 the inlet 110 may be configured to receive the gaseous mixture 10 and to provide the gaseous mixture 10 to the sorbent container 140. Additionally, in the sorption stage 58 the temperature control system 150 may be configured to control the temperature of the sorbent container 140 at a sorption temperature Ts. In embodiments, Tsmay be selected from the range of 250 -700 °C.

[0109] In embodiments, the system 100 may further comprise a control system 300. The control system 300 may especially be configured to control a gas flow from the inlet 110 to the sorbent container 140. Therefore, in embodiments, as depicted here, the control system 300 may comprise or be configured to control a valve 310 configured to control a flow (or feed) of gaseous mixture 10 from (the gaseous mixture source 200 via) the inlet 110 to the sorbent container 140. Hence, in the sorption stage 58 the valve 310 is configured to provide the gaseous mixture 10 from the inlet 110 to the sorbent container 140.

[0110] In the right schematics of Fig. 1 A, the system 100 is depicted during operation of a desorption stage 59 of the sorption cycle 50. In said desorption stage 59 the valve 310 is configured to provide the desorption gas 20 from the gas supply 120 to the sorbent container 140.

[0111] Hence, similarly to the sorption stage 58, in embodiments, in the desorption stage 59 the gas supply 120 may be configured to provide the desorption gas 20 to the sorbent container 140. Additionally, in the desorption stage 59 the temperature control system 150 may be configured to control the temperature of the sorbent container 140 at a desorption temperature Ta. In embodiments, Ta may be selected from the range of 250-700 °C. Furthermore, in embodiments, |TS-Td| < 50 °C. Moreover, in embodiments, the control system 300 may be configured to control a gas flow from the gas supply 120 to the sorbent container 140. Especially, as depicted here, the valve 310 may be configured to control a flow (or feed) of desorption gas 20 from the gas supply 120 to the sorbent container 140. Hence, in the desorption stage 59 the valve 310 is configured to provide the desorption gas 20 from the gas supply 120 to the sorbent container 140.

[0112] As described above, in embodiments, the temperature control system 150 may be configured to control a temperature of the sorbent container 140. Furthermore, in embodiments, the control system 300 may be configured to control the temperature control system 150.

[0113] Furthermore, in embodiments, the system 100 may be configured to execute the sorption stage 58 at a sorption pressure pi and to execute the desorption stage 59 at a desorption pressure p2. Furthermore, in embodiments, |pi-p2| < 1 bar. Therefore, in embodiments, the system 100 may comprise a pressure control unit 160 to control a pressure in the sorbent container 140 at the sorption pressure pi during the sorption stage 58 and at the desorption pressure p2 during the desorption stage 59.

[0114] The system 100 may be configured such that during operation the sorbent container 140 may host a sorbent 40. In embodiments, the sorbent 40 may comprise a support material 45. The (support material 45 comprised by the) sorbent 40 may have a specific surface area (As) of at least 10 m2per gram.

[0115] Furthermore, in embodiments, the sorbent 40 may comprise 0.001 - 25 mg / m2of a first element 41. The first element 41 may comprise an alkali metal or alkaline earth metal selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof. Additionally, in embodiments, the sorbent 40 may comprise 0.01 - 10 mg / m2of a second element 42. Especially, the second element 42 may comprise a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof.

[0116] Reference 30 may herein refer to a gaseous product provided by the system 100 during the operational mode. The gaseous product 30 may, in embodiments, comprise one or more of carbon monoxide 11, dihydrogen gas 21, carbon dioxide 13, and syngas 35 (see also further below). Especially, in some embodiments, as depicted in Fig. 1A top right schematic, the desorption gas 20 may comprise at least 90 vol.% of Eb 21. In such embodiments, the gaseous product 30 may comprise H? 21 and carbon monoxide 11. Especially when the desorption gas 20 comprises IE, the second element 42 may especially be selected from the group comprising Cu, Pt, and Pd. As such, the gaseous product 30 may comprise syngas 35.

[0117] Alternatively, especially when the desorption gas 20 comprises FE, the second element 42 may be selected from the group comprising Ni, Cr, and Ru. In such embodiments, the gaseous product 30 may comprise methane.

[0118] Yet alternatively, in embodiments, especially when the desorption gas 20 comprises IE, the second element 42 may be selected from the group comprising Fe and Co. In such embodiments, the gaseous product 30 may comprise a C1-C3 hydrocarbon.

[0119] As depicted in Fig. 1 A bottom right schematic, in some embodiments, the desorption gas 20 may comprise at least 5 vol.% of H2O 22. Hence, in such embodiments, the desorption gas 20 may comprise water vapor 22. In such embodiments, the gaseous product 30 may comprise at least 2 vol.% of carbon dioxide 13.

[0120] Fig. IB schematically depicts an embodiment of the method for separating carbon monoxide 11 from a gaseous mixture 10 using a sorbent 40.

[0121] The method may comprise a sorption cycle 50 comprising a sorption stage 58 and a desorption stage 59. The figure especially schematically depicts the sorption cycle 50 comprising the sorption stage 58 and the desorption stage 59.

[0122] The four vertically stacked blocks in Fig. 1 B each represent the sorbent container 140 at different times. In particular, the top block of the schematic represents the initiation of the sorption cycle 50 by introducing a feed stream of gaseous mixture 10 comprising 1 ppm- 20 vol.% carbon monoxide 11 to the sorbent container 140. Furthermore, in embodiments, the gaseous mixture 10 may comprise at least 1 vol.% dinitrogen 12.

[0123] In embodiments, the sorption stage 58 may comprise exposing the sorbent 40 to the gaseous mixture 10 at a sorption temperature Tsto provide a loaded sorbent 48. In embodiments, Tsmay be selected from the range of 250 - 700 °C, such as from the range of 350 - 600 °C. Hence, at this stage, the sorbent 40 comprised by the sorbent container 140 may be configured to capture the carbon monoxide 11 from the gaseous mixture 10 to provide the loaded sorbent 48, which is depicted in the second block from the top. Furthermore, the sorbent container 140, especially the system 100 (e.g. through an outlet 130), may be configured to release a non-adsorbed gaseous mixture part 15.

[0124] The sorbent 40 may, in embodiments, comprise a support material 45. Especially, the (support material 45 comprised by the) sorbent 40 may have a specific surface area (As) of at least 10 m2per gram. Further, in embodiments, the sorbent 40 may have a sorption capacity Ccox for sorbing the carbon monoxide 11. Especially, Ccox may be at least 0.1 mmol / g.

[0125] In embodiments, the sorbent 40 may comprise a support material 45 selected form the group comprising metal oxides such as y-A Or, ZrCh, a carbon-based material, a hydrotalcite, and a zeolite, and carbon-based materials such as carbon fibers, granular carbon, and activated carbon. In further embodiments, the specific surface area (As) may be at least 100 2 i

[0126] m / g.

[0127] Furthermore, in embodiments, (a sorbent surface 43 of) the sorbent 40 may comprise 0.001-25 mg / m2of a first element 41 and 0-10 mg / m2of a second element 42. The first element 41 may comprise an alkali metal or alkaline earth metal selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof. Conversely, the second element 42 may comprise a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof.

[0128] In further embodiments, the sorbent 40 may comprise 0.05-25 mg / m2of the first element 41. Further, in embodiments, the sorbent 40 may comprise 0.01-5 mg / m2of the second element 42. In yet further embodiments, the sorbent 40 may comprise 5 - 25 wt.% of the first element 41 and 0.1 - 15 wt.% of the second element 42.

[0129] Returning to the stacked blocks in the schematic drawing of the method, the third block from above schematically depicts the desorption stage 59. Especially, the third block of the schematic represents the initiation of the desorption stage 59 by introducing a feed stream of desorption gas 20 to the sorbent container 140.

[0130] In embodiments, the desorption stage 59 may comprise exposing the loaded sorbent 48 to the desorption gas 20 at a desorption temperature T to provide a regenerated sorbent 49 (depicted in the bottom block of the schematic) and a gaseous product 30. Especially, in embodiments, the desorption gas 20 may comprise EL (g) 21 or FLO (g), i.e. water vapor, 22. Furthermore, in embodiments, Ta may be selected from the range of 250 - 700 °C, such as from the range of 350 - 600 °C. Especially, |TS-Ta| < 50 °C.

[0131] Further, in embodiments, the method may comprise executing the sorption stage 58 at a sorption pressure pi and executing the desorption stage 59 at a desorption pressure p2. Moreover, in embodiments, |pi-pz| < 1 bar.

[0132] After regeneration of the loaded sorbent 48 to provide the regenerated sorbent 49 a new sorption cycle 50 may be initiated. In specific embodiments, the method may comprise a plurality of sorption cycles 50. Especially, the sorption cycles 50 may comprise a first sorption cycle 51 and a second sorption cycle 52. In embodiments, the regenerated sorbent 49 of the first sorption cycle 51 may be used as the sorbent 40 in the second sorption cycle 52, as indicated by the dotted arrow in Fig. I B.

[0133] Experiments

[0134] Set-up and basic protocol - A (bifunctional catalyst comprising) sorbent 40, comprising Cu as the transition metal for the second element 42, was reduced in an EE flow at 450 °C. The process was then operated in two stages (sorption 58 and desorption 59) that were alternated cyclically. For the sorption stage 58, the gaseous mixture 10 was contacted with the sorbent 40, resulting in CO capture by the sorbent 40 and selective CO separation from the gaseous mixture 10. In the desorption stage 59, the sorbent 40 was regenerated using EE (or FEO vapor). The regeneration was performed at isothermal / isobaric conditions.

[0135] In all following experiments, unless indicated otherwise, the sorbent 40 comprised a 200 mg CU-K-Al2O3bifunctional material with a 10:10:80 wt.% composition, i.e., the sorbent 40 comprised 80 wt.% of the support material comprised y-AECh, 10 wt.% of the first element 41 comprised K and 10 wt.% of the second element 42 comprised Cu.

[0136] Effect of temperature - Fig. 2A schematically depicts a typical CO concentration profile during the sorption stage 58 and the desorption stage 59 of the method. The whole process was executed at three different temperatures (450 °C, 400 °C, and 350 °C) under isothermal and isobaric (1 bar) conditions. Full CO separation was achieved before the breakthrough point at all tested temperatures. CO was not released upon exposing the (saturated) loaded sorbent 48 to an inert (helium) gas stream. The regeneration of the sorbent 40 took place under a pure IE 21 stream, resulting into the release of CO and thus yielding syngas 35. Inventors have found that the higher the temperature, the more aggressive adsorption and faster desorption of CO in the presence of IE 21 occurred. This indicated that a relatively strong “chemical” adsorption (chemisorption + reaction) took place, as opposed to a simple physisorption. The data suggested that CO adsorption takes place on the alkaline / alkaline earth component (i.e. the first element 41) of the sorbent 40. The CO separation capacity of the sorbent 40 was calculated from these experimental data, being in the order of 0.15 mmol / g at the three different temperatures (450 °C, 400 °C, and 350 °C) under isothermal and isobaric (1 bar) conditions.

[0137] Throughout Figs. 2A-2D the reference LR refers to a reference line where a blank carbon monoxide signal was obtained in absence of a sorbent 40. The reference Ln refers to an average (averaged over 5 cycles) carbon monoxide concentration profile obtained during (i) the selective adsorption (sorption stage 58, the gaseous mixture 10 comprising 2.5 vol.% CO in He) of carbon monoxide from different mixed gas streams and (ii) the regeneration of the sorbent 40 (desorption stage 59, the desorption gas 20 comprising 100 vol.% H?).

[0138] On the axes in Figs. 2A-2D the carbon monoxide concentration (in vol.%) is depicted with a C, the time (in seconds) is depicted with a t, the temperature (in °C) is depicted with a T, and an intensity (in a.u.) is depicted with an I.

[0139] N? / CO separation - Fig. 2B schematically depicts carbon monoxide separation from an ^-containing gas mixture. Here, the reference Li i refers to an average (averaged over 5 cycles operated at a temperature of 450 °C) carbon monoxide concentration profile obtained during (i) the selective adsorption (sorption stage 58, the gaseous mixture 10 comprising 0.125 vol.% CO in 9 vol.% N2 in He) of carbon monoxide from different mixed gas streams and (ii) the regeneration of the sorbent 40 (desorption stage 59, the desorption gas 20 comprising 100 vol.% H2). The graph to the right depicts an MS profile of the same experiment, where reference Lj 2 refers to dinitrogen (N2).

[0140] As evidenced by the graphs in Fig. 2B, N2 / CO separation was achieved with selectivity higher than 99 % in terms of N2 / CO separation efficiency. During the regeneration phase (i.e. the desorption stage 59), essentially no N2 was released, indicating that N2 was not adsorbed during the CO separation phase (i.e. the sorption stage 58). Hence, essentially pure syngas 35 was obtained as gaseous product 30 during the regeneration phase (i.e. the desorption stage 59). Moreover, the inventors found that the IL'. CO ratio may be tuned by altering the operation conditions.

[0141] Effect of regeneration agent (or desorption gas 20) - Fig. 2C schematically depicts gas concentration profiles for CO and CO2 obtained during execution of the method using H221 (desorption stage 59a) and water vapor 22 (desorption stage 59b), respectively, as desorption gases 20. Here, the reference L13 refers to an average (averaged over 5 cycles operated at a temperature of 450 °C) carbon dioxide concentration profile obtained during (i) the selective adsorption (sorption stage 58, the gaseous mixture 10 comprising 2.5 vol.% CO in He at 25 mL / min) of carbon monoxide and (ii) the regeneration of the sorbent 40 (desorption stage 59, the desorption gas 20 comprising 10 vol.% H? O in He at 50 mL / min followed by 100 vol.% H? at 50 mL / min). As can be observed in Fig. 2D, when introducing a water vapor 22 regeneration step, the adsorbed CO was essentially fully converted to CO2 13 (and H2 12), with no CO release if a further H2 regeneration step (i.e. desorption stage 59b) was applied. In other words, as shown in the top graph in Fig. 2C, the CO of the sorption stage 58 was converted to CO2 in the water vapor-assisted desorption stage 59a, whereas essentially no CO was (left over to be) released in the H2-assisted desorption stage 59b. Conversely, as shown in the bottom graph in Fig. 2C, without the water vapor-assisted desorption stage 59a, regeneration of the sorbent 40 occurred as also demonstrated above with the H?-assisted desorption stage 59b. This demonstrates that water vapor 22 as a desorption gas 20 may effectively regenerate the sorbent 40 and may achieve an (essentially) full conversion in the water gas shift reaction, due to the sorption enhanced features of the present invention.

[0142] Effect of H2O during the CO separation phase - Given that H O is present in many streams, the effect of having such a component present during the sorption stage 58 was examined. Fig. 2D schematically depicts gas concentration profiles for CO and CO? obtained during execution of the method. Here, the reference Ln refers to an average (averaged over 5 cycles operated at a temperature of 450 °C) carbon monoxide concentration profile obtained during (i) the selective adsorption (sorption stage 58, the gaseous mixture 10 comprising 0.13 vol.% CO in 0.3 vol.% H2O in He at 50 mL / min) of carbon monoxide and (ii) the regeneration of the sorbent 40 (desorption stage 59, the desorption gas 20 comprising 100 vol.% H2 at 50 mL / min). Further, the reference L12 refers to an average carbon dioxide concentration profile obtained under similar conditions to that for the carbon monoxide.

[0143] The experimental results corresponding to a three times higher concentration of H2O with respect to CO are shown in Fig. 2D. Full CO separation was achieved in the presence of water. CO was regenerated by H2 treatment, being CO desorbed. At those experimental conditions, a five times higher concentration of CO was obtained in the gaseous product 30 with respect to the concentration of the CO in the gaseous mixture 10. These results highlight the possibility of extending the usage of the present invention for water containing streams.

[0144] Stability of performance - Figure 9 schematically depicts gas concentration profiles for CO during six sorption cycles 50 conducted at 450 °C. In the sorption stage 58 a gaseous mixture 10 comprising a CO / N2 mixture (CO 0.125 vol%, in N2 9 vol% in He) was provided, while in the desorption stage a desorption gas 20 comprising H2 as regenerating agent (H2 100 vol%) was provided. Note that the differences related to the maximum concentration of CO during the regeneration phase among the cycles were due to the time resolution of the analysis system. No trend for the change of this maximum was observed with respect to the cycles. Hence, based on the performed sorption cycles and the resulting CO concentration profiles, the system may be regarded as stable. As evidence by the graph, the sorption and separation capacities were restored at every cycle. The term “plurality” refers to two or more. Furthermore, the terms “a plurality of’ and “a number of’ may be used interchangeably.

[0145] The terms “substantially” or “essentially” herein, and similar terms, will be understood by the person skilled in the art. The terms “substantially” or “essentially” may also include embodiments with “entirely”, “completely”, “all”, etc. Hence, in embodiments the adjective substantially or essentially may also be removed. Where applicable, the term “substantially” or the term “essentially” may also relate to 90% or higher, such as 95% or higher, especially 99% or higher, even more especially 99.5% or higher, including 100%. Moreover, the terms ’’about” and “approximately” may also relate to 90% or higher, such as 95% or higher, especially 99% or higher, even more especially 99.5% or higher, including 100%. For numerical values it is to be understood that the terms “substantially”, “essentially”, “about”, and “approximately” may also relate to the range of 90%-l 10%, such as 95%-105%, especially 99%-101 % of the values(s) it refers to.

[0146] The term “comprise” also includes embodiments wherein the term “comprises” means “consists of’.

[0147] The term “and / or” especially relates to one or more of the items mentioned before and after “and / or”. For instance, a phrase “item 1 and / or item 2” and similar phrases may relate to one or more of item 1 and item 2. The term "comprising" may in an embodiment refer to "consisting of' but may in another embodiment also refer to "containing at least the defined species and optionally one or more other species".

[0148] Furthermore, the terms first, second, third and the like in the description and in the claims, are used for distinguishing between similar elements and not necessarily for describing a sequential or chronological order. It is to be understood that the terms so used are interchangeable under appropriate circumstances and that the embodiments of the invention described herein are capable of operation in other sequences than described or illustrated herein.

[0149] The devices, apparatus, or systems may herein amongst others be described during operation. As will be clear to the person skilled in the art, the invention is not limited to methods of operation, or devices, apparatus, or systems in operation.

[0150] The term “further embodiment” and similar terms may refer to an embodiment comprising the features of the previously discussed embodiment, but may also refer to an alternative embodiment.

[0151] It should be noted that the above-mentioned embodiments illustrate rather than limit the invention, and that those skilled in the art will be able to design many alternative embodiments without departing from the scope of the appended claim s.

[0152] In the claims, any reference signs placed between parentheses shall not be construed as limiting the claim.

[0153] Use of the verb "to comprise" and its conjugations does not exclude the presence of elements or steps other than those stated in a claim. Unless the context clearly requires otherwise, throughout the description and the claims, the words “comprise”, “comprising”, “include”, “including”, “contain”, “containing” and the like are to be construed in an inclusive sense as opposed to an exclusive or exhaustive sense; that is to say, in the sense of “including, but not limited to”.

[0154] The article "a" or "an" preceding an element does not exclude the presence of a plurality of such elements.

[0155] The invention may be implemented by means of hardware comprising several distinct elements, and by means of a suitably programmed computer. In a device claim, or an apparatus claim, or a system claim, enumerating several means, several of these means may be embodied by one and the same item of hardware. The mere fact that certain measures are recited in mutually different dependent claims does not indicate that a combination of these measures cannot be used to advantage.

[0156] The invention also provides a control system that may control the device, apparatus, or system, or that may execute the herein described method or process. Yet further, the invention also provides a computer program product, when running on a computer which is functionally coupled to or comprised by the device, apparatus, or system, controls one or more control lable elements of such device, apparatus, or system.

[0157] The invention further applies to a device, apparatus, or system comprising one or more of the characterizing features described in the description and / or shown in the attached drawings. The invention further pertains to a method or process comprising one or more of the characterizing features described in the description and / or shown in the attached drawings. Moreover, if a method or an embodiment of the method is described being executed in a device, apparatus, or system, it will be understood that the device, apparatus, or system is suitable for or configured for (executing) the method or the embodiment of the method, respectively.

[0158] The various aspects discussed in this patent can be combined in order to provide additional advantages. Further, the person skilled in the art will understand that embodiments can be combined, and that also more than two embodiments can be combined. Furthermore, some of the features can form the basis for one or more divisional applications.

Claims

CLAIMS:

1. A method for separating carbon monoxide (11) from a gaseous mixture (10) using a sorbent (40), wherein the sorbent (40) has a specific surface area (As) of at least 10 m2per gram, wherein the sorbent (40) comprises 0.001 - 25 mg / m2of a first element (41), wherein the first element (41) comprises an alkali metal or alkaline earth metal selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof, and wherein the method comprises a sorption cycle (50) comprising:a sorption stage (58) comprising exposing the sorbent (40) to the gaseous mixture (10) at a sorption temperature Tsto provide a loaded sorbent (48), wherein Tsis selected from the range of 250 - 700 °C; anda desorption stage (59) comprising exposing the loaded sorbent (48) to a desorption gas (20) at a desorption temperature Ta to provide a regenerated sorbent (49) and a gaseous product (30), wherein the desorption gas (20) comprises H2 (21) or water vapor (22), wherein Ta is selected from the range of 250 - 700 °C.

2. The method according to claim 1, wherein the sorbent (40) comprises 0.01 - 10 mg / m2of a second element (42), wherein the second element (42) comprises a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof.

3. The method according to claim 2, wherein the sorbent (40) comprises a support material (45) selected from the group comprising: (i) metal oxides, such as y-ALCh, Z1O2, a hydrotalcite, and a zeolite; (ii) and carbon-based materials, such as a carbon fiber, a granular carbon, and an activated carbon, wherein the specific surface area (As) is at least 100 m2 / g, wherein the sorbent (40) comprises 0.05 - 25 mg / m2of the first element (41), and wherein the sorbent (40) comprises 0.01 - 5 mg / m2of the second element (42).

4. The method according to any one of the preceding claims 2-3, wherein the sorbent (40) comprises 5 - 25 wt.% of the first element (41) and 0.1 - 15 wt.% of the second element (42).

5. The method according to claim 1, wherein the sorbent (40) comprises <0.001 mg / m2of a second element (42), wherein the second element (42) comprises a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof.

6. The method according to any one of the preceding claims, wherein the desorption gas (20) comprises at least 90 vol.% of H2, and wherein the gaseous product (30) comprises H2 (21) and carbon monoxide (11).

7. The method according to claim 6, wherein the second element (42) is selected from the group comprising Cu, Pt, and Pd, and wherein the gaseous product (30) comprises syngas (35).

8. The method according to claim 6, wherein the second element (42) is selected from the group comprising Ni, Cr, and Ru, and wherein the gaseous product (30) comprises methane.

9. The method according to claim 6, wherein the second element (42) is selected from the group comprising Fe and Co, and wherein the gaseous product (30) comprises a Cj- C3 hydrocarbon.

10. The method according to any one of the preceding claims 1-5, wherein the desorption gas (20) comprises at least 5 vol.% of H?. O, and wherein the gaseous product (30) comprises at least 2 vol.% of carbon dioxide (13).

11. The method according to any one of the preceding claims, wherein |TS-Td| < 50 °C.

12. The method according to any one of the preceding claims, wherein Tsis selected from the range of 350 - 600 °C, and wherein Td is selected from the range of 350 - 600 °C.

13. The method according to any one of the preceding claims, wherein the method comprises executing the sorption stage (58) at a sorption pressure pi and executing the desorption stage (59) at a desorption pressure p2, wherein |pi-pz| < 1 bar.

14. The method according to any one of the preceding claims, wherein the sorbent (40) has a sorption capacity Ccox for sorbing the carbon monoxide (11), wherein Ccox is at least 0.1 mmol / g.

15. The method according to any one of the preceding claims, wherein the gaseous mixture (10) comprises 1 ppm - 20 vol.% carbon monoxide (11), and wherein the gaseous mixture (10) comprises at least 1 vol.% dinitrogen (12).

16. The method according to any one of the precedi ng claims, wherein the method comprises a plurality of sorption cycles (50), wherein the sorption cycles (50) comprise a first sorption cycle (51) and a second sorption cycle (52), wherein the regenerated sorbent (49) of the first sorption cycle (51) is used as the sorbent (40) in the second sorption cycle (52).

17. A system (100) for separating carbon monoxide (11) from a gaseous mixture (11), wherein the system (100) comprises an inlet (110), a gas supply (120), a sorbent container (140), and a temperature control system (150), wherein the inlet (110) is fluidically connected to the sorbent container (140), wherein the gas supply (120) is configured to provide a desorption gas (20) to the sorbent container (1 0), wherein the desorption gas (20) comprises H2 (21) or water vapor (22), and wherein the temperature control system (150) is configured to control a temperature of the sorbent container (140), wherein the system (100) is configured to execute an operational mode wherein:the sorbent container (140) hosts a sorbent (40), wherein the sorbent (40) has a specific surface area (As) of at least 10 m2per gram, wherein the sorbent (40) comprises 0.001 - 25 mg / m2of a first element (41), wherein the first element (41) comprises an alkali metal or alkaline earth metal selected from the group comprising Ba, Be, Ca, Cs, K, Li, Mg, Na, Rb, Sr, and combinations thereof; andthe system (100) executes a sorption cycle (50) comprising:a sorption stage (58) wherein (a) the inlet (110) is configured to receive the gaseous mixture ( 10) and to provide the gaseous mixture ( 10) to the sorbent container (140), and (b) the temperature control system (150) is configured to control the temperature of the sorbent container (140) at a sorption temperature Ts, wherein Tsis selected from the range of 250 - 700 °C; anda desorption stage (59) wherein (a) the gas supply (120) is configured to provide the desorption gas (20) to the sorbent container (140), and (b) the temperature control system (150) is configured to control the temperature of the sorbent container (140) at a desorption temperature Td, wherein Td is selected from the range of 250 - 700 °C.

18. The system (100) according to claim 17, wherein the sorbent (40) comprises 0.01 10 mg / m2of a second element (42), wherein the second element (42) comprises a transition metal selected from the group comprising Ag, Au, Co, Cr, Cu, Fe, Ir, Mn, Ni, Pd, Pt, Re, Rh, Ru, Ti, V, Zn, and combinations thereof.

19. The system (100) according to any one of the preceding claims 17-18, wherein the system (100) is configured to execute the sorption stage (58) at a sorption pressure pi and to execute the desorption stage (59) at a desorption pressure p?, wherein |TS-Td| < 50 °C, wherein |pj-p?.| < 1 bar, and wherein the system (100) is configured to execute a plurality of sorption cycles (50) in the operational mode.

20. The system (100) according to any one of the preceding claims 17-19, wherein the system (100) further comprises a gaseous mixture source (200) selected from the group comprising a combustion system (210), an industrial plant, a refinery system, a biomass gasification system, a lignocellulosic gasification system, and a pyrolysis system, wherein the gaseous mixture source (200) is configured to provide the gaseous mixture (10) to the inlet (110), wherein the gaseous mixture source (200) is configured to provide the gaseous mixture (10) with a gaseous mixture temperature Tg, wherein Tgis selected from the range of 200 -1000 °C.

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