Apparatus, system and method for direct capture of carbonaceous gases

Abstract

The present disclosure relates to devices, systems, and methods for selectively recovering carbon-containing gases from an input gas mixture.

Description

[Technical field]

[0001] CROSS-REFERENCE TO RELATED APPLICATIONS [1] This application claims priority to and the benefit of U.S. Provisional Patent Application No. 63 / 179,778, filed April 26, 2021, U.S. Provisional Patent Application No. 63 / 305,544, filed February 1, 2022, and U.S. Provisional Patent Application No. 63 / 318,944, filed March 11, 2022, each of which is incorporated by reference in its entirety herein.

[0002] [2] This disclosure relates to the selective recovery of carbon-containing gases from an input gas mixture. In particular, this disclosure relates to an apparatus, system, and method for selectively recovering carbon-containing gases from an input gas mixture by using an insulating material and a medium having an affinity for the carbon-containing gas. [Background technology]

[0003] [3] Atmospheric carbon dioxide (CO2) concentrations fluctuated periodically between about 235 ± 50 ppm for about 400,000 years until about 1850. Currently, atmospheric CO2 concentrations are about 420 ppm and are rising at a rapid annual rate. Rising concentrations of atmospheric CO2 pose global climate disruption, habitat loss, and various other threats to the Earth. CO2 is considered to be such a stable molecule that converting it to a non-greenhouse gas presents a significant challenge at present.

[0004] [4] It is known that rising atmospheric concentration levels of CO2 can be mitigated by removing CO2 from the air and / or by reducing the rate of CO2 emission into the atmosphere. Known technologies that attempt to remove CO2 from the air that have been investigated are costly, water- and energy-intensive, and have shown little incentive for long-term storage of the removed CO2. For example, concentrated CO2 produced by air capture membrane technology is known to be used to make seltzer water, which re-releases CO2 when consumed.

[0005] [5] In another known example, concentrated CO2 produced by precipitation / calcination is currently injected to release fossil fuels, but because this has limited storage capacity it is re-injected into the air, releasing CO2 into the air when the fossil fuels are consumed.

[0006] [6] Further known examples for mitigating rising atmospheric CO2 concentration levels include the conversion of CO2 to carbon and molten carbonate electrolytes. Useful products produced by this process include carbon nanomaterials. Carbon nanomaterials, including graphitic carbon nanomaterials, have great potential as a material resource, and their applications range from reinforced composites, capacitors, lithium-ion batteries, textiles, nanoelectronics, and catalysts to the main component of lightweight, high-strength building materials due to their excellent strength, electrical conductivity, thermal conductivity, flexibility, and durability. However, technological challenges remain to capture sufficient amounts of CO2 to substantially reduce atmospheric CO2 concentration levels and the associated negative impacts on the planet. Summary of the Invention

[0007] [7] Some embodiments of the present disclosure relate to a system for selectively transferring a carbon-containing gas from an input gas mixture. The system may include an optional permeable insulation that allows net selective passage of the carbon-containing gas from the input gas mixture at a first temperature, and a plenum for containing a medium at a second temperature higher than the first temperature. The medium has a first affinity for carbon in the carbon-containing gas received from the optional insulation, and the medium functions as a carbon sink. The optional insulation, when used, may be disposed between a source of the input gas mixture and the plenum.

[0008] [8] Some embodiments of the present disclosure relate to a method for reducing a carbon-containing gas in an input gas mixture, the method including providing a medium in fluid communication with a source of the input gas mixture, the medium having an affinity for reacting with the carbon-containing gas in the input gas mixture, establishing a temperature differential such that the medium has a higher temperature than the input gas mixture, and reacting the medium and the carbon-containing gas together such that the medium acts as a carbon sink for reducing the carbon-containing gas content of the input gas mixture.

[0009] [9] Some embodiments of the present disclosure relate to an apparatus for recovering carbon dioxide (CO2) from an input gas mixture. The apparatus includes an anode and a cathode disposed within an electrolysis cell, a molten electrolyte medium disposed between the anode and the cathode, the molten electrolyte medium defining a top surface having a first surface area, the top surface in fluid communication with a plenum containing the input gas mixture, and a thermal insulator disposed between the plenum containing the input gas mixture and the top surface, the thermal insulator configured to facilitate net selective passage of CO2 through the thermal insulator to the top surface. The apparatus is configured to selectively heat and electrolytically decompose the recovered CO2.

[0010]

[10] In some embodiments of the apparatus, the input gas mixture is air and the source of the input gas mixture is the Earth's atmosphere.

[0011]

[11] In some embodiments of the apparatus, the input gas mixture is an anthropogenic CO2-containing gas, an industrial exhaust gas stream, gas from a sequestered CO2 reservoir, an exhaust gas from an industrial plant, an exhaust gas from a chemical reactor, an exhaust gas from a power plant, an exhaust gas from a steam generation unit, an exhaust gas from a pyrolysis reactor, a CO2-containing gas product from the combustion of a fossil fuel, a CO2-containing gas product from the conversion of a fossil fuel, a CO2-containing gas product from heating, a CO2-containing gas product from transportation, a CO2-containing gas product from the manufacture of a polymer, a CO2-containing gas product from the manufacture of a plastic, or a combination thereof.

[0012]

[12] In some embodiments of the apparatus, the thermal insulator has a surface area that is 2 to 100 times greater than a first surface area of ​​an upper surface of the molten electrolyte medium in the electrolytic cell.

[0013]

[13] In some embodiments of the apparatus, the apparatus further comprises a housing disposed between the plenum that contains the input gas mixture and the insulation.

[0014]

[14] In some embodiments of the apparatus, the insulation and the housing define an inter-insulation plenum having a first end and a second end, the cell is disposed therebetween, and the inter-insulation plenum receives the input mixed gas at the first end.

[0015]

[15] In some embodiments of the apparatus, the electrolytic cell comprises at least one metal wall that functions as an anode.

[0016]

[16] In some embodiments of the apparatus, the anode and cathode are configured to select the relative amounts of constituent carbon nanostructures within the CNM product.

[0017]

[17] In some embodiments of the apparatus, the electrolysis current and voltage are configured to select the relative amounts of constituent carbon nanostructures in the CNM product.

[0018]

[18] In some embodiments of the present device, metal salts, metals, or other additives are added to the electrolyte to select the relative amounts of constituent carbon nanostructures in the CNM product.

[0019]

[19] In some embodiments of the device, the electrolyte includes one or more carbonates to select the relative amounts of constituent carbon nanostructures in the CNM product.

[0020]

[20] In some embodiments of the device, the electrolyte is configured for enhanced thermal properties that enhance the selective capture of CO2 from the input gas mixture.

[0021]

[21] In some embodiments of the device, the electrolyte may store excess thermal energy.

[0022]

[22] In some embodiments of the device, the input gas mixture is redirected through the device using a wind lens or wind focus.

[0023]

[23] In some embodiments of the device, heat is input to drive a heat engine or to drive the movement of an input gas mixture.

[0024]

[24] Some embodiments of the present disclosure relate to a system for recovering carbon dioxide (CO2) from an input gas mixture. The system includes at least two devices, each of which includes an anode and a cathode disposed within an electrolysis cell, a molten electrolyte medium disposed between the anode and the cathode, the molten electrolyte medium defining a top surface having a first surface area, the top surface in fluid communication with a plenum containing the input gas mixture, and a porous insulation disposed between the plenum containing the input gas mixture and the top surface, the porous insulation configured to facilitate net selective passage of CO2 through the porous insulation to the top surface. Each device of the system is configured to selectively heat and electrolytically decompose the CO2 recovered by the electrolysis process.

[0025]

[25] In some embodiments of the system, at least two devices are arranged in a vertical stack to reduce the physical footprint area of ​​the system.

[0026]

[26] In some embodiments of the system, the system further comprises a heat source and an electrical current source operably coupled to each device.

[0027]

[27] In some embodiments of the system, the system further comprises a heat source and an electrical current source operably coupled to the at least two devices.

[0028]

[28] Some embodiments of the present disclosure relate to a method for direct capture of carbon dioxide (CO2) from an input gas mixture including CO2 in a plenum. The method includes establishing fluid communication between an input gas mixture and an exterior surface of a porous insulation, selectively capturing CO2 from the input gas mixture by passing the CO2 through the insulation into a second plenum, establishing fluid communication between an interior surface of the porous insulation and an electrolyte medium in the second plenum, the electrolyte medium configured to enhance capture of CO2, and recovering a carbon nanomaterial product generated from the captured CO2 from an electrode in the second plenum.

[0029]

[29] In some embodiments of the present apparatus, systems, and / or methods, the input gas mixture comprises at least one carbon-containing gas.

[0030]

[30] In some embodiments of the apparatus, system, and / or method, the input gas mixture is air, an anthropogenic CO2-containing gas, an industrial exhaust gas stream, gas from a sequestered CO2 reservoir, an exhaust gas from an industrial plant, an exhaust gas from a chemical reactor, an exhaust gas from a power plant, an exhaust gas from a steam generation unit, an exhaust gas from a pyrolysis reactor, a CO2-containing gas product from the combustion of a fossil fuel, a CO2-containing gas product from the conversion of a fossil fuel, a CO2-containing gas product from heating, a CO2-containing gas product from transportation, a CO2-containing gas product from the production of a polymer, a CO2-containing gas product from the production of a plastic, or a combination thereof.

[0031]

[31] In some embodiments of the apparatus, systems, and / or methods, the input rate of the input gas mixture or the exit rate of the input gas mixture is accelerated by varying pressure between the first and second sides of the porous insulation through the use of a diaphragm pump.

[0032]

[32] In some embodiments of the apparatus, systems, and / or methods, the input velocity of the input gas mixture or the exit velocity of the input gas mixture is accelerated by varying the pressure between the first and second sides of the porous insulation through the use of a blower or fan.

[0033]

[33] Some embodiments of the apparatus, systems, and / or methods further comprise a compressor mechanism for compressing the input gas mixture to a pressure greater than ambient pressure.

[0034]

[34] In some embodiments of the present devices, systems, and / or methods, the input gas mixture is pressurized.

[0035]

[35] In some embodiments of the present apparatus, systems, and / or methods, the off-gas produced in the second plenum is hotter than the input gas mixture.

[0036]

[36] In some embodiments of the present apparatus, systems, and / or methods, the off-gas generated in the second plenum is oxygen (O2).

[0037]

[37] In some embodiments of the present apparatus, systems, and / or methods, the off-gas products compensate or enhance the input rate of the input gas mixture and / or the CO2 capture in the internal second medium.

[0038]

[38] In some embodiments of the method, the method further includes transferring thermal energy from the off-gas products to the input gas mixture.

[0039]

[39] In some embodiments of the present apparatus, systems, and / or methods, the porous insulation is substantially completely porous and open to the input gas mixture.

[0040]

[40] In some embodiments of the apparatus, systems, and / or methods, the porous insulation is an open flow path insulation that inhibits heat transfer between the second plenum and the input gas mixture.

[0041]

[41] In some embodiments of the present apparatus, systems, and / or methods, the porous insulation is adjustable to adjust gas flow rate and heat transfer through the porous insulation.

[0042]

[42] In some embodiments of the present devices, systems, and / or methods, the porous insulation has a surface area that is 1 to 100 times greater than the surface area of ​​the internal second medium. In some embodiments of the present devices, systems, and / or methods, the porous insulation has a surface area that is 2 to 20 times greater than the surface area of ​​the internal second medium.

[0043]

[43] In some embodiments of the present devices, systems, and / or methods, the ratio of the surface area of ​​the porous insulation to the surface area of ​​the electrolyte surface of the electrolyte medium is adjustable.

[0044]

[44] In some embodiments of the present devices, systems, and / or methods, the inner surface of the porous insulation directly contacts the electrolyte medium.

[0045]

[45] In some embodiments of the present devices, systems, and / or methods, the inner surface of the porous insulation is proximate to the electrolyte medium with a gas space disposed therebetween.

[0046]

[46] In some embodiments of the method, the method further includes a third step of disposing a non-porous housing about the porous insulation to define an inter-insulation plenum, also referred to as a flow path, having a first end and a second end, the inter-insulation plenum configured to receive the input mixed gas at the first end.

[0047]

[47] In some embodiments of the present devices, systems, and / or methods, the non-porous housing is a thermal insulator.

[0048]

[48] ​​In some embodiments of the present devices, systems, and / or methods, excess heat generated by the methods is used to heat or power an external device.

[0049]

[49] In some embodiments of the present apparatus, systems and / or methods, a heat pump or heat engine is used to heat the input gas mixture, the internal second medium, or a combination thereof.

[0050]

[50] In some embodiments of the apparatus, systems and / or methods, Joule heat, industrial waste heat, solar heat, geothermal heat, exhaust heat, or combinations thereof are used to heat the input gas mixture, the internal second medium, or combinations thereof.

[0051]

[51] Some embodiments of the apparatus, systems, and / or methods further comprise a vortex tube, a heat pump, a heat engine, and combinations thereof, for increasing the concentration of the carbon-containing gas in the input gas mixture, for increasing the flow rate of the input gas mixture, or combinations thereof.

[0052]

[52] In some embodiments of the present apparatus, systems, and / or methods, the insulation is configured to enhance exhaust flow of off-gas products from the molten electrolyte medium, to increase the velocity at which carbon-containing gas passes through the insulation, or a combination thereof.

[0053]

[53] In some embodiments of the apparatus, systems, and / or methods, the insulation is configured to selectively pass a greater amount of carbon-containing gas through the insulation than other non-carbon-containing gases that are constituents of the input gas mixture.

[0054]

[54] In some embodiments of the apparatus, systems, and / or methods, the system further comprises one or more shiftable members that shift to shift their position to direct the flow of gas in a first direction or a second direction within the flow path, the first direction being toward the input opening and the second direction being opposite and toward the output opening.

[0055]

[55] Some embodiments of the apparatus, systems, and / or methods further include disposing a cover configured to regulate access to the captured CO2.

[0056]

[56] In some embodiments of the present devices, systems, and / or methods, one or more components of the selectively captured CO2 are mixed in the electrolyte medium via mechanical mixing, agitation, stirring, convection, aeration, or combinations thereof.

[0057]

[57] In some embodiments of the present devices, systems, and / or methods, the input gas mixture includes a carbon-containing gas other than CO2, and the electrolyte medium has an affinity for the carbon-containing gas other than CO2.

[0058]

[58] In some embodiments of the method, the electrolyte medium is a molten electrolyte medium.

[0059]

[59] In some embodiments of the method, the method additionally includes the steps of heating the electrolyte to obtain a molten electrolyte medium; disposing the molten electrolyte medium between an anode and a cathode in an electrolysis cell; selectively heating the CO2 in the input gas mixture with at least the molten electrolyte medium; applying an electric current to the cathode and anode in the cell to electrolytically decompose (decompose by an electrolytic process) the selectively heated CO2; and recovering carbon nanomaterial product from the cathode of the cell.

[0060]

[60] In some embodiments of the method, the method further includes generating an oxygen (O2) product within the molten electrolyte medium.

[0061]

[61] In some embodiments of the present devices, systems, and / or methods, the O2 production enhances convection within the molten electrolyte medium to mix the molten electrolyte medium.

[0062]

[62] In some embodiments of the present devices, systems, and / or methods, the carbon nanomaterial product comprises one or more forms of graphitic nanocarbon, such as, but not limited to, carbon nanotubes, carbon nano-onions, platelets, nanoscaffolds, nanohelices, nanoflowers, nanotrees, nanobelts, graphene, doped carbon nanomaterials, magnetic carbon nanomaterials, amorphous carbon, or combinations thereof.

[0063]

[63] In some embodiments of the present devices, systems, and / or methods, the morphology of the carbon nanomaterial product can be tuned by varying the temperature of the electrolyte medium, the CO rate, the current, the voltage, the composition of the cathode, the composition of the anode, or the composition of the electrolyte medium.

[0064]

[64] In some embodiments of the present devices, systems, and / or methods, the molten electrolyte medium comprises a carbonate.

[0065]

[65] In some embodiments of the devices, systems, and / or methods, the electric current is provided by non-fossil energy sources, including, but not limited to, solar, wind, hydroelectric, geothermal, tidal, wave, nuclear, or combinations thereof.

[0066]

[66] In some embodiments of the method, the method further comprises activating the electrolyte medium.

[0067]

[67] In some embodiments of the present devices, systems, and / or methods, the electrolyte medium includes an added oxide.

[0068]

[68] In some embodiments of the present devices, systems, and / or methods, the electrolyte medium is melted and recycled to enhance the degree of CO2 conversion to different chemicals.

[0069]

[69] In some embodiments of the present devices, systems, and / or methods, the electrolyte medium is melted and allowed to equilibrate for a period of time to enhance the degree of CO2 conversion.

[0070]

[70] In some embodiments of the present devices, systems, and / or methods, an upper surface of the electrolyte medium is disposed near a lower surface of an internal second medium to enhance the degree of CO2 conversion.

[0071]

[71] In some embodiments of the present devices, systems, and / or methods, the current is low to enhance the degree of CO2 conversion.

[0072]

[72] In some embodiments of the present devices, systems, and / or methods, the electrolytic cell is metal to enhance the degree of CO2 conversion.

[0073]

[73] In some embodiments of the apparatus, systems, and / or methods, multiple CO2 capture units are stacked vertically to reduce the horizontal footprint area of ​​the method per unit of input mixed gas processed.

[0074]

[74] In some embodiments of the method, the method further comprises sequentially repeating steps a, b, c, and d.

[0075]

[75] In some embodiments of the method, the method further comprises repeating steps a, b, c, and d and replacing the internal medium.

[0076]

[76] In some embodiments of the present devices, systems, and / or methods, the input gas mixture is accelerated using wind. In some embodiments of the present devices, systems, and / or methods, the input gas mixture is redirected using a wind lens or wind focus.

[0077]

[77] Some embodiments of the apparatus, systems, and / or methods further include a second insulation layer disposed between the source of input gas mixture and the first side of the insulation, the second insulation layer being substantially non-porous and / or impermeable to the input gas mixture.

[0078]

[78] In some embodiments of the present devices, systems, and / or methods, the electrolytic cell comprises at least one metal wall that functions as an anode.

[0079]

[79] In some embodiments of the present devices, systems, and / or methods, the electrolytic cell anode and cathode are each adjusted to form different carbon nanomaterials or to increase the amount of a desired carbon nanomaterial morphology within the carbon nanomaterial product.

[0080]

[80] In some embodiments of the present devices, systems, and / or methods, the electrolytic cell anode and cathode are each adjusted to form different carbon nanomaterials or to increase the amount of a desired carbon nanomaterial morphology within the carbon nanomaterial product.

[0081]

[81] In some embodiments of the present devices, systems, and / or methods, metal salts, metals, or other additives are added to the electrolyte to form different carbon nanomaterials or to increase the amount of a desired carbon nanomaterial morphology in the carbon nanomaterial product.

[0082]

[82] In some embodiments of the present devices, systems, and / or methods, the electrolyte medium includes one or more carbonate salts to form different carbon nanomaterials or to increase the amount of a desired carbon nanomaterial morphology in the carbon nanomaterial product.

[0083]

[83] In some embodiments of the present devices, systems, and / or methods, the electrolyte is tailored to enhance thermal properties.

[0084]

[84] In some embodiments of the present devices, systems, and / or methods, the electrolyte is adjusted to vary the absorption rate of various gases from the input gas mixture.

[0085]

[85] In some embodiments of the present devices, systems, and / or methods, an electrolyte may be used to store excess thermal energy.

[0086]

[86] Without being bound by any particular theory, embodiments of the present disclosure provide an economical, scalable, and robust approach for selectively recovering a carbon-containing gas from an input gas mixture by creating a temperature differential between the input gas mixture and a medium that has an affinity for reacting with the carbon-containing gas. In some embodiments, the source of the input gas mixture can be one or more anthropogenic sources of a carbon-containing gas, such as CO2. [Brief description of the drawings]

[0087] BRIEF DESCRIPTION OF THE DRAWINGS [Figure 1A]

[87] Figure 1 shows three schematic diagrams of a system according to an embodiment of the present disclosure: Figure 1A shows a first system. [Figure 1B]

[87] Figure 1 shows three schematic diagrams of a system according to an embodiment of the present disclosure: Figure 1B shows a second system. [Figure 1C]

[87] Figure 1 shows three schematic diagrams of systems according to embodiments of the present disclosure. Figure 1C shows a third system. [Figure 1D]

[87] Figure 1 shows three schematic diagrams of systems according to embodiments of the present disclosure. Figure 1D shows a third system. [Figure 2A]

[88] Figure 2 shows schematics and experimental data. Figure 2A shows a schematic of the electrolytic decomposition of CO2 in an electrolysis process. [Figure 2B]

[88] Schematic and experimental data are shown in Figure 2. Figure 2B shows a line graph of data showing the diffusion coefficient (DCO2) and velocity (VCO2) of carbon dioxide in air as a function of temperature. [Figure 3A]

[89] Data and schematic diagrams are shown in Figure 3. Figure 3A shows a line graph of data representing the experimental rate of CO2 absorption during the electrolysis reaction at 770 °C for lm Li2O (mol / kg) in Li2CO3 at three different flow rates. [Figure 3B]

[89] Figure 3 shows data and schematic diagrams. Figure 3B shows a schematic diagram of a configuration according to an embodiment of the present disclosure. [Figure 4A]

[90] Figure 4 illustrates two configurations according to an embodiment of the present disclosure: Figure 4A shows a sealed configuration. [Figure 4B]

[90] Figure 4 illustrates two configurations according to an embodiment of the present disclosure: Figure 4B illustrates a non-sealing configuration. [Figure 5A]

[91] Figure 5 shows three schematic diagrams of devices according to embodiments of the present disclosure: Figure 5A shows a first device. [Figure 5B]

[91] Figure 5 shows three schematic diagrams of devices according to embodiments of the present disclosure. Figure 5B shows a second device. [Figure 5C]

[91] Figure 5 shows three schematic diagrams of devices according to embodiments of the present disclosure. Figure 5C shows a third device. [Figure 6A]

[92] Figure 6 shows two schematic diagrams of a system according to an embodiment of the present disclosure: Figure 6A shows a top view of the first system. [Figure 6B]

[92] Figure 6 shows two schematic diagrams of a system according to an embodiment of the present disclosure. Figure 6B shows a side elevation view of the second system. [Figure 7A]

[93] Figure 7 shows two schematic diagrams each illustrating a method according to an embodiment of the present disclosure: Figure 7A shows steps of a first method. [Figure 7B]

[93] Figure 7 shows two schematic diagrams each illustrating a method according to an embodiment of the present disclosure: Figure 7B shows steps of a second method. [Figure 8]

[94] Figure 8 is a scanning electron microscope (SEM) image of a first material for use as an insulator according to an embodiment of the present disclosure. Panel A has a scale bar of 300 μm, panel B has a scale bar of 100 μm, panel C has a scale bar of 100 μm, panel D has a scale bar of 10 μm, panel E has a scale bar of 10 μm, and panel F has a scale bar of 10 μm. [Figure 9]

[95] Figure 9 is an SEM image of a second material for use as an insulator according to an embodiment of the present disclosure. Panel A has a 500 μm scale bar, panel B has a 100 μm scale bar, panel C has a 20 μm scale bar, panel D has a 5 μm scale bar, panel E has a 1 μm scale bar, and panel F has a 500 nm scale bar. [Figure 10A]

[96] Figure 10 is a schematic diagram of device configurations according to embodiments of the present disclosure and experimental data obtained therefrom. Figure 10A shows two device configurations. [Figure 10B]

[96] Figure 10 is a schematic diagram of device configurations and experimental data obtained therefrom according to embodiments of the present disclosure. Figure 10B has top and bottom panels showing device configurations and line graphs showing percent CO2 (CO2%) over time, respectively. [Figure 10C]

[96] Figure 10 is a schematic diagram of an apparatus configuration according to an embodiment of the present disclosure and experimental data obtained therefrom. Figure 10C has top, middle, and bottom panels showing the apparatus configuration and the change in CO2 content (parts per million CO2 (ppm)) over time, respectively. [Figure 11]

[97] Figure 11 shows the surface area enhancement that promotes the net selective passage of CO2 through the insulation. [Figure 12A]

[98] Figure 12 is a schematic diagram of an apparatus configuration for increasing the interaction path length of an input gas with insulation, according to an embodiment of the present disclosure. Figure 12A shows a flow path having an extended length that may be further extended by one or more peaks and / or valleys defined by the insulation and / or housing. [Figure 12B]

[98] Figure 12 is a schematic diagram of an apparatus configuration for increasing the interaction path length of the input gas with the insulation according to an embodiment of the present disclosure. Figure 12B shows a conduit for collecting and separating the hot off-gas product stream. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0088]

[99] Embodiments of the present disclosure relate to one or more devices, one or more systems, and one or more methods useful for selectively capturing carbon dioxide (CO2) from an input gas. The input gas may be a substantially pure gas, a pure gas, or a combination of different gases, and thus the terms "input gas" and "input gas mixture" may be used interchangeably herein. According to embodiments of the present disclosure, the captured CO2 may undergo an electrolysis process, also referred to herein as an electrosynthesis process, to generate carbon nanomaterial (CNM) products from the carbon in the CO2. The terms "carbon nanomaterial products" and "CNM products" are used herein to refer to one or more forms of nanocarbon aggregates, which may also be referred to as nanoscale carbon. The term "nanocarbon" is used herein to refer to carbon arranged in specific structures, such as graphitic nanocarbon structures, within the nanoscale. In particular, the CO2 selectively captured from the input gas mixture may be decomposed into carbon and oxygen using a molten electrolyte medium and various electrolysis process configurations. The electrolysis process may cause mass transfer of carbon from the gas phase to the molten electrolyte medium, to the solid CNM products, or both. The CNM product can be a substantially pure or pure carbon nanomaterial (CNM) that includes carbon nanotubes (CNTs). The CNM product can include one or more forms of CNM structures, such as carbon nanotubes, carbon nano-onions, nanoflowers, nanotrees, nanobelts, platelets, nanoscaffolds, helical carbon nanomaterials, graphene, doped carbon nanomaterials, amorphous carbon, or combinations thereof. Optionally, one or more parameters of the electrolytic process can be adjusted to alter the relative amount of a given form within the CNM product.

[0089]

[0100] FIG. 1 illustrates an implementation of a system according to an embodiment of the present disclosure. FIG. 1A illustrates a system 1000 comprising a vessel 1002 housing a medium 1004 having an affinity for a carbon-containing gas in an input gas 1006. The vessel 1002 may also be more generally referred to as a "plenum," a term used herein to refer to any space that may be filled with a substance, whether liquid, gas, solid, or a combination thereof. The plenum may be open, closed, substantially sealed to restrict fluid inflow or outflow, or fluid-tight to prevent fluid inflow or outflow. The term "affinity" is used herein to refer to the tendency of a medium to absorb, react with, chemically bond with, or bind to the carbon-containing gas in the input gas 1006. As such, in many cases, the medium 1004 absorbs, reacts with, chemically bonds with, or binds to the carbon-containing gas, for example, by participating in one or more chemical reactions with the carbon-containing gas, one or more electrochemical reactions with the carbon-containing gas, preferentially absorbing the carbon-containing gas, binding with the carbon-containing gas, or a combination thereof, without being bound by any limitation or theory. In some embodiments of the present disclosure, the affinity of the medium 1004 to react with the carbon-containing gas results in the production of different chemicals. As used herein, the term "different chemicals" refers to chemicals that would not otherwise be produced in the absence of the medium having an affinity to react with the carbon-containing compound.

[0090]

[0101] The vessel 1002 shown in FIG. 1A is opened to fluid communication with a source of input gas 1006. The medium 1004 has a higher temperature than the input gas 1006. The medium also has an affinity to react with the carbon-containing gas in the input gas. In FIG. 1A, the input gas is enriched with the carbon-containing gas, which in this scenario is CO2. Due to the affinity of the hot medium 1004 for the carbon-containing gas, at least a portion, substantially all, or all of the carbon-containing gas exits the input gas 1006 and enters the medium 1004 in the vessel 1002. The medium 1004 also has an affinity to react with other gases in the input gas 1006, but the affinity to react with the carbon-containing gas is higher than the affinity to react with non-carbon-containing gases. In this manner, the medium 1004 may act as a carbon sink such that as the carbon-containing gas enters and reacts with the medium 1004, the amount of carbon in the input gas 1006 is reduced, substantially depleted, or completely depleted, while the amount of non-carbon-containing gas in the input gas 1006 remains largely unchanged or not at all.

[0091]

[0102] FIG. 1B illustrates a system 1000A that includes a vessel 1002, a medium 1004, and an insulation 1008 disposed between a top surface of the medium 1004 and a source of an input gas 1006. The medium 1004 is at a higher temperature than the input gas 1006. The insulation 1008 is porous and allows the carbon-containing gas to pass through. In some embodiments of the present disclosure, the insulation 1008 may be permeable to the carbon-containing gas and to other constituent gases of the input gas 1006 that do not contain carbon. In some embodiments of the present disclosure, the insulation 1008 may have a greater permeability to the carbon-containing gas compared to the carbon-free gas in the input gas 1006, meaning that under the same or substantially similar thermodynamic parameters, a greater net amount of the carbon-containing gas passes through the insulation than the carbon-free gas. In some embodiments of the present disclosure, the insulation 1008 may be impermeable or less permeable to the carbon-free gas in the input gas 1006.

[0092]

[0103] In some embodiments of the present disclosure, the affinity of the medium to react with carbon-containing gases and the permeability properties of the insulating material 1008 may cooperate to deplete the carbon-containing gas content of the input gas 1006 and increase the carbon content of the medium 1004. Similar to Figure 1A, the medium 1004 in Figure 1B may function as a carbon sink.

[0093]

[0104] FIG. 1C illustrates system 1000B having many of the same features as system 1000A (shown in FIG. 1B) with the additional feature that the particular input gas is air and the space defined between the inner / lower surface of insulation 1008 and the upper surface of medium 1004A is also hotter than the input gas 1006 and may contain and enclose air that is also hotter than the input gas 1006. In system 1000B, medium 1004A is also hotter than the input gas 1006. For example, medium 1004A may be a molten carbonate electrolyte, optionally supplemented with an oxide, such that the upper surface of medium 1004A forms a gas-liquid interface. In system 1000B, medium 1004A has a high affinity to react with carbon-containing gases in input gas 1006 and a relatively low affinity to react with other carbon-free constituent gases in input gas 1006, such as nitrogen, oxygen, and water. In some embodiments of the present disclosure, the insulation 1008 and the medium 10004A may reduce the carbon content of the input gas 1006 by facilitating a reaction between the medium 1004A and a carbon-containing gas, such as CO. In this manner, the system 1000B acts as a carbon sink by selectively reducing the carbon content of the input gas 1006.

[0094]

[0105] 1D shows system 1000C, which has many of the same features as system 1000B, but with the additional feature of electrodes 1010A and 1010B immersed in a molten carbonate electrolyte medium 1004A (at a temperature of about 750° C.). When a current is applied between the electrodes, a carbon-containing gas, in this example CO2, is transferred (decomposed electrolytically), new carbon material is produced, and oxygen is produced. The details of these electrochemical reactions between medium 1004A and the carbon-containing gas are described in more detail later in this specification.

[0095]

[0106] 7A shows a schematic diagram of the steps of a method 2000 for reducing the carbon-containing gas content of an input gas mixture. The method 2000 includes step 2002 of providing a medium in fluid communication with a source of the input gas mixture, the medium having an affinity for reacting with the carbon-containing gas of the input gas mixture, step 2004 of establishing a temperature differential such that the medium has a higher temperature than the input gas mixture, and step 2006 of reacting the medium and the carbon-containing gas together such that the medium acts as a carbon sink for reducing the carbon-containing gas content of the input gas mixture.

[0096]

[0107] CO2 is rapidly absorbed from the air and naturally concentrated by reacting with oxides in the molten salt in an exothermic reaction with the molten electrolyte medium, which continually regenerates the molten carbonate electrolyte medium, as represented by the following equations 1, 2, and 3, without being bound to any particular theory:

[0097]

[0108] CO 2(gas) +O2 - fi CO3 2- (Formula 1)

[0098]

[0109] The electrolytic reaction follows the following equation (2):

[0099]

[0110] CO3 2- fi C+O2+O 2- (Formula 2)

[0100]

[0111] In this process, CO2 is decomposed by melt electrolysis to produce CNM carbon products and high-temperature oxygen, and carbon is the CNM product, as represented by equation (3).

[0101]

[0112] CO2fi CNM 生成物 +O2 (Formula 3)

[0102]

[0113] As shown in Figure 3A, molten Li2CO3 electrolyte rapidly absorbs and reacts with gaseous CO2, but is poorly soluble in the major atmospheric gases N2, O2, and H2O. Experimental CO2 absorption rates in 1 mole Li2O per kg Li2CO3 at 770 °C are fast, significantly faster than the rate required to sustain the electrolytic decomposition of CO2.

[0103]

[0114] FIG. 2A shows a schematic diagram of the electrolytic decomposition of CO in a molten carbonate medium 1004A. The molten Li2CO3 electrolyte medium 1004A has an affinity for carbon to rapidly absorb and react with gaseous CO2, but has a low affinity due, at least in part, to its poor solubility in N2, O2, and H2O, the primary gases in atmospheric air. The gray arrows extending into the medium indicate the net mass transfer of carbon into the medium 1004A, and the yellow arrows with red Xs indicate the absence of mass transfer of other constituent gases in the carbon-enriched atmospheric air that was the input gas mixture in FIG. 2A.

[0104]

[0115] The rapid CO2 absorption rate in molten lithium carbonate medium at 770°C with 1 molar lithium oxide obtained in the experiment is shown in Figure 3A. Figure 2A shows a schematic diagram depicting one physicochemical feature of the electrolysis process that results in CO2 from the input gas mixture reacting with the medium 1004A. CO2 is readily absorbed into the electrolyte medium via an exothermic reaction characterized by equations 4a and 4b, while N2, O2, and H2O from air are poorly soluble in molten Li2CO3. Note that the rapid rate of CO2 reactive absorption was measured after the oxide was chemically mixed with Li2CO3, which is in a chemical environment rather than an electrochemical environment. Instead, during electrolysis, not only is an oxide formed at the cathode, but O2 is generated at the anode (Figure 2A and equation 3) and floats to the surface. CO3 2- fi C ナノマテリアル +O 2_ +O2 (Equation 4a) CO2+O 2- fi CO32- ;CO2+Li2O fi Li2CO3△H(770℃)=-158,000J / mol (Formula 4b)

[0105]

[0116] With reference to Equation 4a, the high absorption rate of CO2 is due to the exothermic chemical reaction of CO2 with one of the chemical species in the electrolyte medium. Without being bound by any theory, the oxide that drives the fast reaction with CO2 is formed by chemical equilibrium and by electrolysis of the carbonate in the formation of the CNM product.

[0106]

[0117] With reference to Equation 4b, and without being bound by any theory, the oxide reacts exothermically with CO2 to continuously regenerate the carbonate in the electrolyte medium, such as Li2CO3, and the reaction enthalpy is calculated from the reaction enthalpy of the individual reacting species using thermodynamic data available through the NIST Webbook and NIST-JANAF Thermochemical Tables.

[0107]

[0118] The O2 product that is evolved rises through the electrolyte, enhancing convection in the electrolyte medium, helping to mix the incoming CO2 and increasing the reaction rate. The reaction rate of CO2 from air to the electrolyte is very fast, but slow compared to gas mixtures containing high levels of CO2, such as exhaust gas. Alternatively, the rate of reactive absorption of CO2 with oxides in a molten carbonate electrolyte medium can be further increased by convection enhancements such as mechanical stirring or flow of the electrolyte, with or without electrolysis, or electrode rotation, agitation, or bubbling of hot gases through the electrolyte.

[0108]

[0119] FIG. 3A shows that the experimental CO2 absorption rate at 1 mole Li2O per kg Li2CO3 at 770 °C is fast, significantly faster than the rate required to sustain the decomposition of CO2 by electrolysis. Without being bound to any particular theory, it is believed that the selective CO2 sink for binding, capture, reaction, or consumption of CO2 combined with the lack of solubility by the main gases in air results in a diffusion coefficient of CO2 in air (DCO2 ), D in air CO2 can help separate CO from other components of the input gas mixture and maintain a desired rate of electrolysis reactions occurring within a molten electrolyte medium such as LiCO (melting point = 723 °C) or other electrolyte medium mixture of binary or ternary carbonates.

[0109]

[0120] An additional physicochemical feature that allows the CO2 fraction in the input gas mixture to be selectively heated independently of other constituents of the ambient air is the traditional rate of CO2 diffusion in air, which is fast compared to the rate at which CO2 is consumed during electrolysis. Figure 2B shows the known CO2 diffusion in air, extrapolated in blue over the range of 0°C to 400°C, to the high temperature region relevant to CO2 electrolysis. The extrapolation is based on Fick's law of diffusion, T(K) 3 / 2 The change in the diffusion coefficient exponent is shown in R 2 Used with conformance > 0.9996.

[0110]

[0121] Diffusion is conventionally described by Fick's law. Without being bound to any particular theory, a fundamentally equivalent, but simpler, starting point is the Einstein-Smoluchowski equation, which describes the relationship between mean square displacement and diffusion: The mean square displacement due to Brownian motion of a species i due to diffusion at time t is <x 2 > is given by Equation 5 in one, two, or three dimensions. <x 2 >=qD i t (Equation 5)

[0111]

[0122] where q is the dimensionality factor (q=2, 4, or 6 for one-, two-, or three-dimensional diffusion), Di is the diffusion coefficient, and t is time. Note that molecular motion at the interface may differ from this ideal case.

[0112]

[0123] This translational displacement is the average diffusion rate of CO2 as a function of temperature. <x 2 > / t (see Equation 6): n CO2 = <x 2 > 0.5 / t=(qxD CO2 (T) 0.5 / t u (Formula 6) In the above formula, T is the temperature and t u is a unit of time consistent with the diffusion coefficient.

[0113]

[0124] Figure 3A shows CO2 and the translational displacement, i.e. velocity, of CO2 in air, calculated as a function of temperature using Equation 6. The diffusion coefficient of CO2 in air (D CO2 ) and the translational displacement of the CO2 velocity (n CO2 ) depends on temperature. In Figure 2B, D CO2 The value is the dark blue dotted line) and the 1D, 2D, or 3D velocities of CO2 are shown as the red, yellow, and light blue (top) lines, respectively. As shown in Figure 2A, in electrolysis, the total number of moles of gas leaving the electrolyte medium consists of the O2 product in equation 1. Similarly, this is the same total number of moles of gas entering the electrolyte medium as the reactant CO2 in equation 2. Thus, to the extent that the gas volume matches the ideal molar volume, the volume of CO2 entering from above the electrolyte medium is replaced by the volume of O2 leaving the electrolyte medium, with no net change in the gas volume above the electrolyte medium. Note that although the volumes displaced are the same, O2, being a lighter molecule, moves faster in the gas phase than CO2.

[0114]

[0125] Without being bound to any particular theory, the hot O2 produced by the electrolysis process, which may also be referred to as an off-gas product, may itself be used to generate oxidants for various applications, including, but not limited to, sterilants for various industrial processes and oxy-fuel processes. Additionally, the hot O2 may be used to transfer some of its energy back into the absorbed CO2 or to pull more reactants into the system, such as in a heat engine process. Some embodiments of the present disclosure relate to isolating the O2 off-gas product from the electrolysis cell, for example, by a conduit in fluid communication with the gas space above the gas-liquid interface of the carbonate electrolyte medium in the electrolysis cell.

[0115]

[0126] Adding porous insulation surrounding the electrolysis cell can help retain heat within the electrolyte medium. Also, note that oxygen contained in the air within the gas space of the electrolysis cell above the top surface of the electrolyte medium and within the porous insulation increases in concentration as the electrolysis process progresses.

[0116]

[0127] The addition of a porous insulation cover above the molten carbonate electrolyte medium allows gas phase CO2 to diffuse from the input gas mixture into the molten lithium carbonate electrolyte medium, an additional physicochemical feature by which the CO2 portion of the input gas mixture can be selectively heated. Without being bound by any theory, in the absence of convection, the maximum rate at which CO2 arrives as a reactant for electrolysis is limited by the maximum one-dimensional velocity of CO2 in a direction perpendicular to the insulation surface as it travels toward the interior of the kiln housing the electrolysis cell. Without being bound by any theory, the one-dimensional average displacement per second and velocity of CO2 in the air trapped in the insulation closest to the ambient air side at 20°C is n CO2-断熱材 =n CO2 (20℃)=0.56cmCO2s -1 It is.

[0117]

[0128] When the input gas mixture is air supplied from the atmosphere, CO2 originates from the ambient air, arrives as a reactant, and passes into the porous insulation for electrolysis. * C) Molar volume concentration of CO2 V M (CO2 in air) is calculated from its 0.04% molar concentration and the molar volume of the gas, V M (CO in air 2 )=V M (20℃) / 0.04%CO2=6.0×10 7 cm 3 The amount of CO2 passing through the outer surface of the porous insulation is calculated as 1 mole of CO2 per cm of air. 2 The molar flux of CO2 per unit volume is f(CO2) 断熱材 is given as:

[0118]

[0129] The average wind speed (wind speed) of the Earth's air is n 空気-平均 =330 cm / s (=11.9 kph=7.4 mph) and has been increasing at a rate of 0.8% per year since 2010. In the examples, 0.33%, 10%, or 100% of this wind speed range (1, 33, or 330 cm / s) were considered to demonstrate that natural wind, rather than artificial blowers, is sufficient to maintain CO2 for embodiments of the present disclosure. Without being bound by any theory, to a first approximation, it is believed that 2 The wind at the air velocity of the air hitting the four sides at right angles displaces the depleted CO2 by the diffusion mean square displacement Z=n 空気 (cm / s) / nCO2. In principle, air velocity can be increased by forcing more air through a smaller area, or by a diaphragm pressurizing the air. As air velocity increases, the molar concentration of CO2 impinging on that area increases by Z×V M (CO2 in air). The CO2 flux is driven by the concentration gradient between the concentration at the outer surface of the insulation and the concentration at the surface of the electrolyte medium. The uptake of CO2 by the electrolyte medium during electrolysis is rapid, the reaction rate is fast, and the mass transfer of carbon into the electrolyte medium is promoted.

[0119]

[0130] Heat (-Q in) is generated during electrolysis and, without being bound by any theory, is generated by (i) the heat of reaction with Li2O as CO2 reforms the electrolyte medium, ΔH=-158,000 J / mol (Eq. 4), and (ii) resistive heating due to electrolysis overpotential. The reaction heat released is the exothermic reaction of CO2 with electrolytic Li2O, -ΔH (Eq. 4), according to the number of moles of CO2 consumed. Resistive heating due to the product of electrolysis overpotential h and electrolysis current. The residual potential for electrolytic decomposition of CO2 in a molten carbonate electrolyte is about 0.8 V and varies with electrolyte medium composition and electrolysis electrodes. The additional overpotential to drive a constant current density I varies with electrolyte medium composition, electrode composition, and texturing and has been measured for planar electrodes. Heat loss from the system P out is given by the thermal conductivity, the surface area of ​​thermal contact A, the temperature difference ΔT between the two sides of the insulation, and the thickness of the insulation. The thermal conductivity k is often expressed in metric units (W / (mK)), and the thermal resistance R is often expressed in English units (ft2 hr °F / Btu), including the thickness of the insulation in inches. Pout=kA△T / =A△T / R (Equation 7)

[0120]

[0131] The dual properties of the material, allowing CO2 to enter the kiln and retain heat in the electrolysis chamber, are possible with porous insulation. Such materials (i) have open porosity (as opposed to closed porosity or grain), (ii) have a high insulation coefficient, and (iii) can withstand the temperatures of the electrolysis conditions in the appropriate temperature range. The porosity dependence of thermal conductivity for high temperature resistant materials has been studied. Porous insulation materials that can withstand high temperatures (>1150°C) are alumina silicate and alumina calcium silicate blankets. Examples include various products including "ceramic fiber insulation for furnaces", "alumina silica ceramic fiber", "Durablanket®", or "Cerablanket®". Related thermal commercial products often revert to imperial rather than metric units, with similar available compositions (e.g., 46% Al2O3 and 54% SiO), thicknesses (0.5, 1, or 2 inches thick), and density ranges (4, 6, or 8 lb / ft3 = pcf).

[0121]

[0132] Even the densest of these alumina-silica fiber blankets are lightweight due to their high porosity. As an example, the porosity of a Cerablanket® blanket with a density of 8 pcf (=0.128 g / cm3) is approximately 100% of the solid (nonporous) average d 固体 Using a density of d = 3.2 g / cm, the porosity can be estimated from 46% for alumina with a density of 4.0 g / cm and 54% for SiO with a density of 2.6 g / cm. The porosity is calculated from the open space (d 空気 = 0.001225 g / cm3) is estimated as follows: p = 100% × (d solid - d ceramic blanket) / (d solid - d air) (where d air = 0.001225 g / cm 3 ) p (8pcf alumina silicate example) = 96% (Equation 8)

[0122]

[0133] A readily available alumina-silica fiber is a 2-inch thick, 8 pcf thermal fiber blanket with nominal thermal insulation values ​​of k and (R) at 0°C (extrapolated), 200°C, 400°C, 600°C, and 800°C of 0.028 (10), 0.05 (5.7), 0.08 (3.6), 0.19 (2.2), and NS 0.20 (1.4), respectively, and T 電解 From T 空気 The average thermal coefficient for the temperature range from 15.2 ft2 hr to 3.8 ft2 hr is k = 0.52 W / (mK) (and R = 3.8 ft2 hr F°Btu-1). The mathematical convenience of expressing thermal resistance as "R" is its approximate additivity with the insulation layer. Thus, if this insulation were 8 inches thick instead of 2 inches, the R-value would be about 15.2 ft2 hr. 2 hr F°Btu -1 It becomes.

[0123]

[0134] The outer layer of insulation may utilize a porous insulation that is more compatible with lower temperatures (less expensive and has a higher R-value), such as bare fiberglass insulation. Such insulation is available from a variety of commercial manufacturers. The example used here is one with R=16.7 and 1.5 pcf, or 0.024 g / cm, composed of woven glass fibers. 3 It is a 4-inch thick, unpolished Corning 710 fiber insulation with a density of 2.5 gcm -3 With a density of solid glass fiber, the porosity of this insulation is p(4 inches of C701) = 99%. Combined, the thermal performance of the 8 inches of 8 pcf alumina silicate facing out from the interior of the kiln and the 4 inches of C701 exposed fiberglass insulation extending to the ambient air are approximately additive, i.e., they have an approximately combined R = (15.2 + 16.7) = 31.9 ft 2 hr F°Btu -1 It becomes.

[0124]

[0135] Some embodiments of the present disclosure relate to an apparatus for selectively capturing CO2 from a carbon-containing input gas mixture and generating a CNM product from the captured CO2. The apparatus includes a pair of electrodes, a cathode and an anode, that define an interelectrode space, which may be referred to as an electrolytic space, that may receive and contain an electrolyte medium. The apparatus also includes an insulating material disposed between a source of input gas mixture and the electrolyte medium. The insulating material is porous and configured to aid in selectively capturing CO2 from the input gas mixture. The apparatus may further include a source of electrical current, a heat source, and a case that contains the electrodes and the electrolyte medium and is in fluid communication with the source of carbon-containing input gas mixture.

[0125]

[0136] FIG. 5A shows an example of an apparatus 10A according to an embodiment of the present disclosure. The apparatus 10A includes a case 12, which may be referred to as an electrolysis chamber or electrolysis cell, for housing a cathode 18, and an anode 16 may form at least a portion of the inner surface of the wall of the case 12. The two electrodes together define an electrolysis space B between them. Optionally, the anode 16 may be separate from the wall of the case 12, as will be understood by those skilled in the art. The case 12 is configured to house an electrolyte medium 21 (shown in a molten state in FIG. 5A, with a top surface designated 21A). The electrolysis space B, including the top surface 21A, may be in fluid communication with a plenum D that contains an input gas mixture including CO2. The case 12 may be supported on a base 14 within an insulated housing 20, such as a kiln, that defines an insulated plenum A. The apparatus 10 further includes insulation 22 disposed between the electrolysis space B and the plenum D that contains the input gas mixture. In some embodiments of the present disclosure, the insulating plenum A may also be in fluid communication with a plenum D that contains the input mixed gas.

[0126]

[0137] The plenum D containing the input gas mixture can be the Earth's atmosphere (CO2 content about 420 ppm CO2) or it can be a plenum containing concentrated anthropogenic CO2-containing gas such as an industrial exhaust gas stream or a reservoir of sequestered CO2. For example, the plenum D contains or is a source of the input gas mixture, which can be any gas containing CO2 and optionally other carbon-containing gases. For example, the source of the input gas mixture can be various industrial plants including, but not limited to, cement manufacturing plants, iron smelting plants, steel manufacturing plants, plants that produce or use one or more of ammonia, ethanol, magnesium, hydrogen, polymers, plastics, glass, wastewater treatment plants, food processing plants. The source of the input gas mixture can also be chemical reactors including internal combustion engines and the combustion of carbonaceous materials for heating or cooking. Exhaust gas from power plants, steam generating facilities, or pyrolysis reactors can also be sources of the input gas mixture. CO2-containing gas emitted from these sources or from the production of high carbon footprint materials may also contribute to or constitute the input gas mixture. In addition, CO2-containing gas products of combustion or conversion of fossil fuels for heating, transportation, carbon products such as polymers or plastics may also contribute to or constitute the input gas mixture. The temperature of the input gas mixture may range from about -90°C to about 400°C. For example, if the source of the input gas mixture is atmospheric, the temperature range may range from about -90°C to about 75°C. If the source of the input gas mixture is anthropogenic, the temperature range may range from about 50°C to about 400°C. The case 12 is configured in fluid communication with the plenum D to receive the input gas mixture into the interelectrode space B.

[0127]

[0138] In some embodiments of the present disclosure, the anode 16 may be formed as a planar structure, a wire structure, a screen, a porous structure, a conductive plate, a flat or folded shim, a coiled structure, or the anode may form at least a portion of the inner wall of the case 12. The anode 16 may be formed from a variety of conductive materials such that the anode 16 may or may not generate oxygen. Such anode-forming materials include, but are not limited to, any conductive material that has a stable layer or establishes a highly stable oxide outer layer that supports oxygen generation in the electrolytic reaction carried out according to embodiments of the present disclosure, Ni, Ni alloys, galvanized (zinc-coated) steel, titanium, graphite, iron, and a wide variety of metals that establish a highly stable oxide outer layer that supports oxygen generation. Further examples of suitable materials for forming the anode 16 include nickel alloy 36 (nickel with iron but no chromium), nichrome (nickel chromium based alloy) with stainless steel such as SS304 or SS316, and Inconel alloys such as Inconel 600, 625, and 718, alloy C-264, or nichrome such as Chromium A, B, or because simultaneous nucleation of the alloy components is known to produce high quality CNTs. Binary and ternary transition metal nucleating agents including, but not limited to, Ni, Cr, Sn, In, Fe, and Mo may also be useful and may affect CNM product growth.

[0128]

[0139] In some embodiments of the present disclosure, a transition metal may be added onto the anode 16, from which it may dissolve and migrate through the electrolyte medium 21 onto the cathode 18. The added transition metal may function as a nucleating agent and may be selected from nickel, iron, cobalt, copper, titanium, chromium, manganese, zirconium, molybdenum, silver, cadmium, tin, ruthenium, zinc, antimony, vanadium, tungsten, indium, gallium, or non-transition metals such as germanium or silicon, or mixtures thereof. The transition metal may also be introduced directly into the electrolyte medium 21 as a dissolved transition metal salt and migrated onto the cathode 18. It is also possible to add a transition metal nucleating agent directly onto the cathode 18.

[0129]

[0140] In some embodiments of the present disclosure, the cathode 18 may be formed as a planar structure, a wire structure, a screen, a porous structure, a conductive plate, a flat or folded shim, a sheet, a coiled structure, or the cathode may form at least a portion of the inner wall of the case 12. The cathode 18 may be formed from a variety of conductive materials reflecting the need for nucleation sites and variations in the CNM products that form on the cathode 18. Such cathode forming materials include, but are not limited to, any conductive material, galvanized (zinc coated) steel, titanium, graphite, iron, alloys including copper and zinc, Monel (Ni400, Ni / Cu alloy), Inconel, stainless steel, iron, nichrome, pure Cu, and brass alloys may also be suitable materials for making the cathode 18.

[0130]

[0141] The anode 16 and the cathode 18 may be aligned substantially parallel to one another within a case 12, such as a stainless steel case or a case made of substantially pure or pure alumina. The case 12 may be made of any material suitable for containing the molten electrolyte medium 21 and for maintaining the temperature achieved by the apparatus 10A. The electrodes may be spaced apart from one another in any orientation, such as, but not limited to, substantially horizontally or substantially vertically, to define an electrolysis space B therebetween. In some embodiments of the present disclosure, the electrolysis space B is about 0.1 cm to about 10 cm. In some embodiments of the present disclosure, the electrolysis space B is about 1 cm. As will be appreciated by those skilled in the art, the dimensions of the electrolysis space B are determined by the scale of the apparatus 10A, such as the size of each electrode, the plenum defined within the case, the amount of current applied, and combinations thereof.

[0131]

[0142] The anode 16 and the cathode 18 are operably connected to a current source (not shown), the current source having a current of approximately 0.001 A / cm 2 ~10A / cm 2The current density provided between the electrodes may be any AC or DC current source, either constant or non-constant, that provides a current density of at least 0.02 A / cm. In some embodiments of the present disclosure, the current density provided between the electrodes is at least 0.02 A / cm. 2 , 0.05A / cm 2 , 0.1A / cm 2 , 0.2A / cm 2 , 0.3A / cm 2 , 0.4A / cm 2 , 0.5A / cm 2 , 0.6A / cm 2 , 0.7A / cm 2 , 0.8A / cm 2 , 0.9A / cm2, 1.0A / cm 2 The power for the current source can be any source or combination of sources, including electric power sources, solar power sources, and the like.

[0132]

[0143] The heat source (not shown) can be any heat source that raises the temperature within the case 12 to a temperature that transitions the electrolyte medium 21 to a molten phase. For example, the heat source can achieve a temperature within the case 12 of about 500°C to about 850°C or higher. In some embodiments of the present disclosure, the heating achieves a temperature of about 700°C to about 800°C, about 720°C to about 790°C, or about 750°C to about 780°C. In some embodiments of the present disclosure, the heating achieves a temperature of 749-750°C, 751-752°C, 753-754°C, 755-756°C, 757-758°C, 759-760°C, 761-762°C, 763-764°C, 765-766°C, 767-768°C, 769-770°C, 771-772°C, 773-774°C, 775-776°C, 777-778°C, or 779-780°C. In some embodiments of the present disclosure, the temperature within the case 12 can be increased to about 800°C or higher. In some embodiments of the present disclosure, the heat source is provided by or supplemented by the exothermic reaction of CO2 absorption and conversion to carbonate (mass transfer from gas phase to solid phase CNM product), or by an overpotential of the applied electrolysis current.

[0133]

[0144] In some embodiments of the present disclosure, the electrolyte medium may include a carbonate that may be heated by a heat source until it transitions to a molten phase. For example, the carbonate may be lithium carbonate or lithium carbonate. Molten carbonates such as lithium carbonate (Li2CO3) with a melting point of 723°C, or lower melting point lithium carbonate such as LiBaCaCO3 with a melting point of 620°C, sustain rapid absorption of CO2 from the space above the molten electrolyte medium if the oxides they contain include native oxide formation that occurs upon melting or is the result of electrolysis or mixing with highly soluble oxides such as Li2O, Na2O, and BaO. Suitable carbonates include alkali and alkaline earth carbonates. Alkaline carbonates include lithium, sodium, potassium, rubidium, cesium, or francium carbonates, or mixtures thereof. Alkaline earth carbonates include beryllium, magnesium, calcium, strontium, barium, or radium carbonates, or mixtures thereof. In some embodiments of the present disclosure, the electrolyte may be a mixed composition, for example, a mixture of alkali and alkaline earth carbonates with one or more of oxides, borates, sulfates, nitrates, chlorides, chlorates, or phosphates.

[0134]

[0145] An embodiment of the present disclosure relates to providing insulation 22 between the plenum D containing the input gas mixture and the interior of the case 12 containing the molten electrolyte medium 21. The insulation 22 is configured to aid in the net selective passage of CO2 from the first side 22C to the second side 22D through the insulation 22. Other gases are inhibited from having a net selective passage through the insulation due to the presence of a sink in the hotter medium that has no affinity for its consumption. In some embodiments of the present disclosure, the insulation 22 is made from a material that promotes the flow of CO2 through the insulation 22 and contributes to maintaining the temperature within the insulated housing 20. In some embodiments of the present disclosure, the insulation 22 material (i) has an open pore structure, (ii) has a high insulating coefficient, and (iii) can withstand the high temperatures achieved within the case 22 and the insulated housing 20, if possible. Non-limiting examples of materials suitable for the insulation 22 include those that can withstand high temperatures (>1150° C.), such as alumina silicate and alumina calcium silicate blankets. Examples of readily available materials for use as insulation 22 include, but are not limited to, fibrous or granular permeable batts, mats, or blankets, flexible or rigid boards or panels, and permeable rigid blocks or bricks that allow the passage of gases. Several insulation products used in construction may also be suitable for use as insulation 22, including, but not limited to, low and medium temperature insulation (used in exterior walls) such as fiberglass, cellulose, cotton, or woven fabrics, medium temperature insulation (used in exterior or interior walls) such as mineral wool, and high temperature insulation (used in exterior, interior, or interior walls) such as aluminates (including carbonates), silicates (including calcium alumina silicates), derivatives thereof, and combinations thereof, cements, and ceramics. Examples of various readily available and suitable high temperature ceramic products include, but are not limited to, "furnace ceramic fiber insulation," "alumina-silica ceramic fiber," "Durablanket®," "Cerablanket®," or "Superwool®."Suitable insulation products are available in a range of similar compositions (e.g., about 46% Al2O3 and about 54% SiO), thicknesses (0.5 inch, 1 inch, or 2 inch thick), and densities (4 lb / ft. 3 =pcf, 6pcf, or 8pcf).

[0135]

[0146] Even the densest alumina-silica fiber materials can be lightweight due to their high porosity. For example, 8 pcf (=0.128 g / cm 3 The porosity of a Cerablanket® with a density of 100 mm is the solid (nonporous) average d 固体 =3.2g / cm 3 Using a density of 4.0 g / cm 3 46% of alumina with a density of 2.6g / cm 3 The porosity can be estimated from the open space (d 空気 =0.001225g / cm 3 It is estimated as follows: p=100%×(d 固体 -d cerablanket ) / (d 固体 -d 空気 ) (where d 空気 =0.001225g / cm 3 ). (8 pcf alumina silicate example) = 96% (open space). A readily available alumina silica fiber is a 2 inch thick, 8 pcf thermal fiber blanket with nominal thermal insulation values ​​of k and (R) at 0°C (extrapolated), 200°C, 400°C, 600°C, and 800°C of 0.028(10), 0.05(5.7), 0.08(3.6), 0.19(2.2), and NS 0.20(1.4), respectively, and T 電解 From T 空気 The average thermal coefficient for the temperature range is k = 0.52 W / (mK) (and R = 3.8 ft 2 hr F°Btu -1 ) The mathematical convenience of the "R" representation of thermal resistance is its approximate additivity with the insulation layer. Thus, if this insulation were 8 inches thick instead of 2 inches, the R-value would be approximately 15.2 ft 2 hr F°Btu -1The porosity and spacing between the insulating fibers are evident in scanning electron microscope images of the first material, Durablanket®, and the second material, Superwool®, shown in Figures 8 and 9, respectively. Figure 8 shows that the first material has fibers with diameters of about 5.8 μm (panel D), 4.4 μm (panel E), and 3.3 μm (panel F). Figure 9 shows that the second material has fibers with diameters of about 2.5 μm (panel D), 0.49 μm (panel E), and 0.24 μm (panel F).

[0136]

[0147] In some embodiments of the present disclosure, the surface area of ​​the insulation 22 is 1-100 times greater than the surface area of ​​the top surface 21A of the molten electrolyte medium 21. In some embodiments of the present disclosure, the surface area of ​​the insulation 22 is 2-20 times greater than the surface area of ​​the top surface 21A of the molten electrolyte medium 21. In some embodiments of the present disclosure, the surface area of ​​the insulation 22 is greater on the outside (first surface 22C) facing the input gas mixture than on the inside (second surface 22D) exposed to the hotter medium to maximize net inward CO2 diffusion and minimize outward heat flow.

[0137]

[0148] In some embodiments of the present disclosure, the density and / or thickness of the insulation material may be subjected to a modification process for use with embodiments of the present disclosure. For example, the insulation material may be compressed or modified by other simple mechanical, chemical, or structural means to alter, increase, or decrease the net passage of carbon-containing gas through the insulation material compared to unmodified insulation material.

[0138]

[0149] FIG. 5B shows an apparatus 10B according to an embodiment of the present disclosure. The apparatus 10B has many similar or identical features to the apparatus 10 described above. The main difference between the two apparatuses 10, 10B is that the apparatus 10B has a frame 22A with one or more walls and a ceiling made of insulation 22 that define an insulating plenum C, which contains CO2 captured from the input gas mixture in a plenum D outside the frame 22A. These walls and ceiling of the frame 22A increase the surface area of ​​interaction between the input gas and the porous insulation, which can increase the net CO2 diffusion rate inward (through the insulation from the first surface 22C to the second surface 22D). The plenum A may or may not be in fluid communication with the insulating plenum C, as shown in FIG. 5B. Each wall and ceiling of the frame 22A was made from a 20 cm x 20 cm, 2 inch thick section of insulation 22. The second surface 22D of the insulation 22 is spaced a predetermined distance from the top surface 21A of the molten electrolyte medium 21 based on the size of the frame 22A and the volume of the molten electrolyte medium 21 in the cells 12. Thus, by varying the size of the frame 22A, the predetermined distance can be increased or decreased to increase or decrease the volume of the molten electrolyte medium 21 in the cells 12. The concentration of CO2 in the insulating plenum C can be higher than the concentration of CO2 in the incoming gas mixture in plenum D. Additionally, the CO2-containing gas in the insulating plenum C can also be at a higher temperature than the input gas mixture in plenum D.

[0139]

[0150] FIG. 5C shows an apparatus 10C according to an embodiment of the present disclosure. The apparatus 10C has many similar or identical features as the apparatus 10B described above. The main difference between the two apparatuses 10B, 10C is that the apparatus 10C further comprises a housing 24 defining a plenum D in which the frame 22B is disposed. The housing 24 may be constructed of a material that is substantially impermeable to gas and has low thermal conductivity (e.g., firebrick). In other words, the housing 24 may be made of a material that has thermal insulation properties. The housing 24 may define two openings, an input opening 26A at a first end and an output opening 26B at a second end, such that the flow of gas in the plenum D travels from the input opening 26A into the housing 24 and exits the housing 24 through the output opening 26B. The gas content of the plenum D may be substantially the same inside the housing 24 as outside. Similar to the apparatus 10B, the gas content and properties of plenum D are different from those of insulated plenum C due to the insulation 22, on a net basis, due to carbon-containing gases migrating from plenum D through insulation 22 into plenum C and selectively through interface 21A into media 21. Plenum C may have a higher temperature than plenum D. Optionally, the housing 24 may also include one or more shiftable members that may shift their position depending on whether the input gas mixture enters the housing through input opening 26A or output opening 26B, such as when the wind direction changes. The shiftable members may be sliding doors, ports, baffles, or any other mechanism configured to shift their position to change the direction the input gas mixture travels through the housing 24. The shiftable members may also be configured to shift their position to change the direction the input gas mixture travels through the housing 24. Additionally or alternatively, the shiftable member may shift the input gas mixture toward or away from a hot spot based on a hot spot occurring within any of the devices described herein. As shown, plenum C is in fluid communication with a top surface 21A of electrolyte medium 21 within cell 12.In some embodiments of the present disclosure, the apparatus may include a convoluted flow path between the first surface 22C and the second surface 22D to increase the contact path length, and therefore the contact time, between the input mixed gas and the insulation material 22.

[0140]

[0151] Frame 22B, shown in FIG. 5C, may have one or more walls made of insulation layer 22, for example, a 20 cm by 20 cm, 4 inch thick section of insulation 22, and the same ceiling as frame 22A.

[0141]

[0152] The apparatus 10A may also be configured to establish a gas pressure differential between the electrolysis space B above the upper surface 21A and the plenum D. The gas pressure in the cells 12 may be lower than in the plenum D such that the established gas pressure differential may enhance the flow of the carbon-containing gas through the insulation 22 and into the cells 12. The pressure differential may be caused by various mechanisms, such as a diaphragm pump, that reduces the relative gas pressure in the cells 12 compared to the plenum D. Alternatively or additionally, a blower or fan may also be used to increase the gas pressure in the plenum D.

[0142]

[0153] In some embodiments of the present disclosure, apparatus 10B and 10C are configured to establish a gas pressure differential between plenum D and plenum C to enhance the movement of the carbon-containing gas through insulation 22 and into plenum C. For example, the gas in the plenum may be pressurized to a level higher than the gas pressure in plenum C. A diaphragm pump, blower, or fan may be used to help establish the gas pressure differential between plenum D and plenum C.

[0143]

[0154] In some embodiments of the present disclosure, the cell 12 may be configured to cause mixing of gas present between the inner surface 22C of the insulation 22 and the top surface 21A of the molten electrolyte medium 21. For example, the cell 12 may include one or more mechanisms for mechanical mixing, agitation, stirring, convection, aeration, or combinations thereof to aid in mixing of the gas above the top surface 21A and the electrolyte medium 21.

[0144]

[0155] In some embodiments of the present disclosure, the apparatuses 10A, 10B, and 10C may further comprise a mechanism for concentrating the input gas mixture. For example, the apparatuses 10A, 10B, and 10C may further comprise a vortex tube, a heat pump, or a heat engine to increase the concentration of the carbon-containing gas in the input gas mixture.

[0145]

[0156] Some embodiments of the present disclosure relate to one or more systems configured to selectively recover carbon-containing gas from an input gas mixture and generate CNM products from the recovered gas. FIG. 6 shows two examples of systems according to embodiments of the present disclosure. FIG. 6A shows a non-limiting example of a system 200A comprising at least two devices 10D and a component 10E. Device 10D represents any device configured to selectively recover CO2 from an input gas mixture and generate CNM products from the recovered CO2 using an electrolysis process, including devices 10A, 10B, 10C, and combinations thereof. Component 10E represents a heat source and a power source for providing electrical current to device 10D. Although FIG. 6A shows three devices 10D, it should be understood that there may be more or fewer individual devices 10D that make up system 200A. Such devices 10D may share individual components 10E, or there may be more than one component 10E in system 200A.

[0146]

[0157] 6B shows a non-limiting example of a system 200B comprising at least two devices 10D, with one device 10D vertically positioned above another device 10D to form a stack 10F comprised of at least two devices 10D. The at least two devices 10D may be operatively coupled to a component 10E, and there may be more than one component 10E in the system 200B. Although FIG. 6B shows one stack 10F, it should be understood that the system 200B may comprise more than one stack 10E. One or more stacks 10F may be operatively coupled to a given component 10E, and each of the one or more stacks 10F may be operatively coupled to a dedicated component 10E.

[0147]

[0158] Some embodiments of the present disclosure relate to one or more methods for selectively recovering carbon-containing gas from an input gas mixture and producing CNM products from the recovered gas. In some embodiments of the present disclosure, the methods described herein may be operated using the devices and systems described herein, although various embodiments of the methods are not limited to such devices and systems.

[0148]

[0159] FIG. 7 shows a schematic diagram depicting a method 300 for selectively capturing CO2 from an input gas mixture in a plenum. The method 300 includes establishing 302 fluid communication between the input gas mixture and an outer surface of a porous insulation, and selectively capturing 304 CO2 from the input gas mixture by passing CO2 through the insulation into a second plenum. The method 300 further includes establishing 306 fluid communication between an inner surface of the porous insulation and an electrolyte medium in the second plenum, the electrolyte medium being configured to enhance the capture of CO2. The method 300 further includes recovering 308 carbon nanomaterial products generated from the captured CO2 from an electrode in the second plenum. The method 300 may further include an optional step of removing off-gas products generated during the CO2 capture. In some embodiments of the present disclosure, the method 300 further includes selectively removing or adding heat to balance the heat generated or required in the capture of CO2.

[0149]

[0160] According to some embodiments of the present disclosure, the method 300 may further include establishing a gas pressure difference between the two sides of the insulation such that the gas pressure of the input gas mixture is higher than the collected gas in the second plenum. The gas pressure difference may be established using a diaphragm pump, a blower, or a fan. Additionally or alternatively, the input gas mixture may be pressurized to establish the gas pressure difference. In some embodiments of the present disclosure, the generated off-gas in the second plenum may be at a higher temperature than the input gas mixture. In some embodiments of the present method, the off-gas product is O2. In some embodiments of the present disclosure, the off-gas product compensates or enhances the input rate of the input gas mixture and / or the selective capture and transfer of CO2 into the second plenum. Some embodiments of the method 300 include transferring thermal energy from the off-gas product to the input gas mixture. In some embodiments of the method 300, the porosity of the porous insulation is adjustable to change the rate at which CO2 is selectively captured by moving through the insulation and the rate at which heat may be transferred through the insulation.

[0150]

[0161] In some embodiments of the method 300, the inner surface of the porous insulation may directly contact the electrolyte medium. In other embodiments of the method 300, the method 300 further includes positioning the inner surface of the porous insulation a predetermined distance from a top surface of the electrolyte medium.

[0151]

[0162] Some embodiments of the present disclosure include a method step of disposing a non-porous exterior wall medium around a porous insulation to define an inter-insulation plenum having a first end and a second end, the inter-insulation plenum configured to receive an input mixed gas at the first end. Optionally, the non-porous exterior wall medium is also an insulating material.

[0152]

[0163] In some embodiments of the present disclosure, the method 300 further includes using the heat generated in the second plenum to heat or power an external device, such as a heat pump or heat engine being used to heat the input gas mixture, the electrolyte medium, or a combination thereof. Additionally or alternatively, Joule heat, industrial waste heat, solar heat, geothermal heat, exhaust heat, or a combination thereof may be used to heat the input gas mixture, the electrolyte medium, or a combination thereof.

[0153]

[0164] In some embodiments of the present disclosure, the method 300 further includes mixing the gas contents of the second plenum with the electrolyte medium via mechanical mixing, agitation, stirring, convection, aeration, or combinations thereof.

[0154]

[0165] In some embodiments of the present disclosure, the method 300 further includes heating the electrolyte to obtain a molten electrolyte medium; disposing the molten electrolyte medium between an anode and a cathode of an electrolytic cell in the second plenum; selectively heating the CO2 in the input gas mixture with at least the molten electrolyte medium; applying an electric current to the cathode and anode in the cell to electrolytically decompose the selectively heated CO2; and recovering carbon nanomaterial product from the cathode of the cell.

[0155]

[0166] In some embodiments of the present disclosure, the method 300 further includes generating an O2 product within the molten electrolyte medium, which can enhance convection within the molten electrolyte medium to mix the molten electrolyte medium.

[0156]

[0167] In some embodiments of the present disclosure, the CNM product of method 300 comprises carbon nanotubes, carbon nano-onions, nanoflowers, nanotrees, nanobelts, platelets, nanoscaffolds, helices, graphene, doped carbon nanomaterials, magnetic carbon nanomaterials, amorphous carbon, or combinations thereof. In some embodiments of the present disclosure, method 300 further comprises selecting the relative amounts of constituent carbon nanostructures in the CNM product by varying the temperature, CO2 rate, current, voltage, composition of the electrolyte medium, composition of the cathode, composition of the anode, or composition of the electrolyte medium.

[0157]

[0168] As used herein, "selecting the relative amounts of constituent carbon nanostructures in the CNM product" refers to any step that contributes to controlling the morphology of the electrosynthesized CNM product. In some embodiments of the present disclosure, the selected morphology of the CNM includes the following CNM morphologies: carbon nano-onion, carbon nano-scaffold, carbon nanosphere, carbon nano-helix, carbon nanoplatelet, graphene, or combinations thereof. In some embodiments of the present disclosure, the step of selecting the nanomaterial morphology may result in an electrosynthesized CNM product that is partially, mostly, substantially all, or all a single CNM morphology. For example, the step of selecting the nanomaterial morphology may produce an electrosynthesized CNM product that is partially, mostly, substantially all, or all carbon nano-onion, carbon nano-scaffold, carbon nanosphere, carbon nano-helix, carbon nanoplatelet, or graphene.

[0158]

[0169] In some embodiments of the present disclosure, the step of selecting the nanomaterial morphology includes applying an electric current to the cathode and the anode as an alternating current (AC). For example, an AC electrolytic current may select for CNM products having a nano-onion morphology.

[0159]

[0170] In another embodiment, the step of selecting the nanomaterial morphology includes adding ZnO to a molten carbonate electrolyte and applying an AC electrolysis current that can select for CNM products having graphene platelet morphology.

[0160]

[0171] In another embodiment, the step of selecting the nanomaterial morphology includes adding MgO to a molten carbonate electrolyte and selecting an electrical current for hollow carbon nanosphere production.

[0161]

[0172] Transition metal nucleation growth, such as the addition of nickel powder, can result in clearly observable CNT walls. However, if these nucleation additives are intentionally omitted in the synthesis, high yield synthesis of carbon nanoonions and graphene is achieved. These differences in the parameters of the electrosynthesis process are just a few examples of how the electrosynthesized CNM products can be selected.

[0162]

[0173] In some embodiments of the present disclosure, the method 300 further includes a step of supplying electrical current to the cell by a non-fossil energy source, including, but not limited to, solar, wind, hydroelectric, geothermal, tidal, wave, nuclear, or a combination thereof.

[0163]

[0174] In some embodiments of the present disclosure, the method 300 further includes one or more of activating the molten electrolyte medium by pre-heating the electrolyte medium, adding an oxide to the electrolyte medium, reusing the electrolyte medium for multiple electrolysis processes, and time-equilibriuming the molten electrolyte medium. EXAMPLES

[0164] Working Example

[0175] The examples and experiments described below relate to the direct capture of CO2 from an input gas mixture by net selective passage of CO2 through a porous insulation and the production of CNM products from the captured CO2. Without being bound to any particular theory, the net selective passage of CO2 is due, at least in part, to the media's affinity for carbon, which may be higher than the media's affinity for other constituent gases of the input gas mixture. These examples are provided to illustrate embodiments of the present disclosure and are not to be construed as limiting the scope of the present disclosure in any manner.

[0165]

[0176] Example 1 - CO2 passage through insulation

[0177] FIG. 10 shows a schematic diagram of the device configuration and data obtained in an experiment demonstrating the ease of CO2 flow through the insulation of the present disclosure. FIG. 10A shows a fluid-tight vessel 100 with a diameter of about 4 inches (1 inch is equal to about 2.54 cm) separated into upper and lower chambers 100A and 100B by a lower porous open channel insulation 122B. Optionally, the upper chamber 100A was also provided with an upper insulation 122A in fluid communication with the air outside the vessel 100. Unless otherwise noted, the insulation 122A and 122B are each a porous insulating separator that is 2 inches thick and has a density of 8 lb pounds per cubic foot, Durablanket®. The upper chamber 100A received an input gas mixture via a gas supply line 102. The lower chamber 100B contained a CO2 sensor 104 (such as a type commercially available from CO2meter.com) for measuring and reporting the CO2 level within the lower chamber 100B. The lower chamber 100B initially contained only pure N2 and no CO2.

[0166]

[0178] FIG. 10B shows two experimental setups, the setup shown in the top panel received 100% CO2 into the upper chamber 100A via the supply line 102. In the top panel of FIG. 10B, the upper chamber 100A was equipped with top insulation 122A, while in the bottom panel, the upper chamber 100A did not have top insulation 122A. The sensor 104 used in the experimental setup of FIG. 10B was a CO2 sensor with a sensitivity of 0-100%. In the bottom panel of FIG. 10B, the upper chamber 100A was initially filled with 100% CO2. Each of the top and bottom panels of FIG. 10B also includes a line graph showing the experimental CO2 levels measured over time in the bottom chamber 100B.

[0167]

[0179] As shown in the top panel of FIG. 10B, when an input gas mixture of pure CO2 was introduced into the upper chamber 100A at a flow rate of 1 L / min, the CO2 concentration in the lower chamber 100B increased from 0 to 100% in about 15 minutes, and the CO2 concentration gradually decreased when the flow was stopped. As shown in the bottom panel of FIG. 10B, when the upper chamber was filled with 100% CO2, the CO2 concentration in the lower chamber increased from 0 to about 62% in about 24 minutes. CO2 is denser than N2, which may promote the increased concentration in the lower chamber 100B compared to the upper chamber 100A. The relative gas density of N2 to 1 mole of CO2 is given by the ratio of their formula weights, which is 28 / 44=63.6%.

[0168]

[0180] FIG. 10C shows three experimental setups, two of which received compressed air (with a CO2 level of approximately 418 ppm) at various flow rates via supply line 102 and used CO2 sensors with sensitivity between 0 and 1%. The top panel of FIG. 10C shows only the lower chamber 100B, lower insulation 122B, and delivered compressed air at a rate of 6.2 L / min (equivalent to a wind speed of 330 cm / s) over the insulation 102. As shown in the top panel of FIG. 10C, the concentration of CO2 in the chamber increased from 0 (pure N2) to approximately 410 ppm in approximately 29 minutes.

[0169]

[0181] In the middle panel of FIG. 10C, the experimental setup included an upper chamber 100A separated from a lower chamber 100B by an upper insulation 122A and a lower insulation 122B. The top line graph in the middle panel of FIG. 10C shows the CO2 levels detected over time in the lower chamber 100A when air was introduced at a rate of 0.624 L / min (corresponding to a wind speed of 33 cm / s). The CO2 concentration in the lower chamber increased from 0 to about 395 ppm in about 45 minutes. The bottom line graph in the middle panel of FIG. 10C shows the CO2 levels detected over time in the lower chamber 100A when air was introduced at a rate of 6.2 L / min. The CO2 concentration in the lower chamber increased from 0 to about 395 ppm in about 10 minutes.

[0170]

[0182] Without being bound to any particular theory, it is believed that a thicker, more porous layer of insulation may slow the rate of increase in CO2 concentration. Interestingly, the opposite phenomenon was observed to occur. In the same test chamber, the 2 inches of insulation was replaced with 8 inches (four 2 inch layers) of insulation to separate the upper and lower chambers (not shown). CO2 from the air in the upper compartment reached 395 ppm levels in approximately 20 minutes or 2.5 minutes, respectively, at flow rates of 0.624 or 6.2 L air / min. Without being bound to any particular theory, it is believed that the observed increase in CO2 concentration in the lower chamber 100B in a shorter time when the thicker insulation was used may be related to the substantial reduction in the height of the lower chamber 100B, which in turn reduced the volume of the lower chamber 100B, allowing for a more rapid exchange of the original N2.

[0171]

[0183] The bottom panel of FIG. 10C shows a further experimental setup in which the sealed upper chamber 100A was filled with 100% air, and then the CO2 concentration in the lower chamber 100B was increased from 0 to about 240 ppm in about 18 minutes.

[0172]

[0184] Without being bound to any particular theory, all experimental set-ups shown in FIG. 10 demonstrate the passage of CO2 from air or pure CO2 through porous open channel insulation.

[0173]

[0185] For each of the electrolysis processes described hereinafter, the theoretical mass change before and after electrolysis is calculated using: Q = measured applied electrolytic charge in ampere-hours (Ah); n=4. The electrons transferred in the electrolysis of Eq. F = Faraday constant = 96485 C per mole of electrons = 26.801 Ah per mole of electrons; FW(C), FW(O2), and FW(CO2) = formula weight of carbon, O2, or CO2, i.e., 12.01, 32.00, or 44.01 g / mol, respectively.

[0174]

[0186] Example 2 - Carbonate electrolysis in the absence and presence of CO2

[0187] The experimental demonstration consisted of two electrolysis configurations. As shown in FIG. 4A, in the first configuration 400, an electrolysis chamber 402 containing a molten carbonate electrolyte medium 404 and an electrolysis electrode 406 was sealed by a seal member 408. The electrolysis chamber 402 was housed in a housing 405 made of solid insulation. During electrolysis, air was not allowed to enter the chamber, and no additional CO2 was available to regenerate the carbonate electrolyte medium 404 during the electrolysis process. A pressure relief valve allowed O2 to be released during the electrolysis process through a pipe 410 that extended below the seal member 408 and above the housing 405. In the absence of additional CO2, the level of the carbonate electrolyte medium dropped in the electrolysis cell 402 during the electrolysis process, according to Equation 2. The total measured mass of the electrodes 406 and electrolyte medium 404 was measured before and after the passage of an electrolysis charge. In the absence of CO2, the total mass was observed to decrease as oxygen was evolved.

[0175]

[0188] Specifically, experiments were performed without CO. Configuration 400 was run with the following operating parameters (as shown in FIG. 4A): Case: 4" x 6" stainless steel 304 crucible. The inner wall acts as the anode. Anode / electrode: Nichrome C, approx. 6cm x 6cm Cathode / electrode: Brass, approx. 6cm x 6cm ·Electrolyte medium: Li2CO3 ·Temperature: 750℃ ·Current: 8.4 Amps (Current density=0.2A / cm 2 ) Electrolysis time: 20 hours

[0176]

[0189] The combined mass of the cell, electrolyte, and electrodes was measured before and after passing an electrolytic charge of 8.4 amps x 20 hours = 168 Ah. 168 Ah was calculated by mass = Q / nF according to equation 2, where n = 4 and F = 9.6485 x 10 4Using As, 1.567 moles of carbonate can be reduced. In a closed cell of configuration 400, without the exchange of CO2, the closed cell should lose approximately 50 g of mass due to loss of O2, as 1.567 mol x 32 g (O2 per mole) according to Equation 2. After electrolysis in the closed cell, the measured cell mass loss was approximately 48 g, 96% of the theoretical loss of 50 g.

[0177]

[0190] Without being bound by any theory, the increase in oxides according to Equation 3 may make it more difficult to generate the last remaining traces of O2. For example, a competing equilibrium may develop in which O2+ combines with oxides or carbonates to generate species that inhibit the continued release of O2.

[0178]

[0191] In the second configuration 400A (shown in FIG. 4B), CO2 from the air was allowed to flow into the electrolysis chamber 402 through the porous insulation 412. Specifically, the top of the electrolysis chamber 402 was not sealed, and the porous insulation 412, with 10 times the surface area of ​​the electrolyte medium 404, was exposed in the electrolysis chamber 402 as the top surface. Experiments were also performed using the non-sealed configuration 400A (as shown in FIG. 5B), with the same type of electrodes and the same Li2CO3 electrolyte medium at 750° C. in a stainless steel 304 case as the cell 402, also with a current density of 0.2 A / cm2, with a porous top. The cover was made of 2-inch thick porous Durablanket®, which allows the passage of CO2 from the air into the electrolysis cell 402.

[0179]

[0192] With the non-sealed configuration 400A having porous insulation 412, the measured mass of the electrolysis cell 402, electrodes 406, and carbonate electrolyte medium 404 is equal to: CO 2was absorbed and reacted to regenerate the electrolyte medium 404. From the input CO2, only O2 exits the system. The electrolytically decomposed CO2 remains as a solid CNM product on the cathode and is evolved as oxygen from the anode. During this electrolysis process, the outside of the porous insulation was observed to remain cool, near the ambient air temperature, preventing the loss of 48 g of cell mass after the electrolysis process performed with configuration 400.

[0180]

[0193] Example 3 - CO2 capture and CNM product generation

[0194] Further experiments investigating the capture of CO2 from air and the production of CNM products by electrolytic decomposition of CO2 were carried out with the following operating parameters: Case: 1.2" x 4" x 6" stainless steel 304 crucible. The inner wall acts as the anode. Cathode / electrode: Brass 5cm x 6cm (2 sides active) · Electrolyte medium: Li2CO3, the electrolyte was heated for 24 hours prior to electrode immersion. ·Temperature: 750℃ Current: 2 amps (current density = 0.04A / cm 2 ) Electrolysis time: 9 hours

[0181]

[0195] These experiments consisted of measuring the mass of the cell before and after electrolysis, which included the mass of the cell, electrolyte, and electrodes.

[0182]

[0196] Ambient air temperature varied from 21 to 23 °C. Mass was measured using a Radwag R Series Precision balance with 0.01 g resolution. Although the cell mass was elevated above the balance platform by insulation, the balance is heat sensitive and accounted for a few percent error in mass change in the experiment.

[0183]

[0197] The theoretical mass gain due to CNM production is nF x FW(C), according to Equations 2 and 3. This is the same as the theoretical cell mass gain of a complete cell including electrodes and electrolyte, only under the condition that there is sufficient CO2 present to regenerate all of the consumed carbonate, according to Equation 1. The theoretical mass loss due to O2, according to Equation 2, is nF x FW(O2), which is the same as the theoretical cell mass loss, only under the condition that there is no CO2 present to regenerate the consumed carbonate, according to Equation 1.

[0184]

[0198] Example 3A

[0199] FIG. 5A shows the configuration of the apparatus 10A used for the above-described recovery and CNM production experiments. The apparatus 10A included a cell 12, an anode 16 forming at least a portion of the inner wall surface of the cell 12, and a cathode 18. The anode 16 and the cathode 18 defined an electrolytic space B that contained an electrolyte medium 21 in a molten state, thereby defining an upper surface 21A of the electrolyte medium 21. The cell 12 was supported on a base 14 of insulation that rested on a scale, such as a Radwag R Series Precision balance with a resolution of 0.01 g, to measure the cell mass. The cell 12 was contained within an insulating plenum A of an insulating housing 20. The insulation 22 was a 2-inch thick piece of Durablanket® having a density of 8 pcf. The apparatus 10A was placed in an ambient air plenum D such that the upper surface 21A was in fluid communication with the plenum D through a portion of the insulation 22.

[0185]

[0200] Electrolysis experiments that measure the relative reactions due to CO2 ingress and decomposition (reactions in Eq. 3 from the net balance of Eqs. 1 and 2) as well as carbonate decomposition (Eq. 2) can be analyzed as total CO2 absorbed (Eq. 3) or total CO2 blocked, the latter resulting in a mass loss of O2 evolution (Eq. 2). This is the change in cell mass before and after electrolysis, Dm セル It is measured as:

[0186]

[0201] The degree of dominance of CO2 decomposition relative to carbonate decomposition is expressed here in two different ways. The first, represented by Eqs. 9a and 9b, is the ratio of Dm to the measured electrolytic charge converted to the negative mass expected from carbon (CO2 uptake) or oxygen evolution (carbonate decomposition). セル The second part of Equation 10 measures the percentage of absorbed CO2 compared to the CO2 required for electrolysis. This is the maximum possible O2 loss combined with Dm compared to the electrolytic charge converted to carbon plus oxygen (CO2). セル Equations 4a, 4b, and 5 are given below. DC = 100 × Dm セル / (nF×FW(C) (Equation 9a) DO2 = -100 × Dm セル / (nF×FW(O2) (Equation 9b) DCO2 = 100 × (Dm セル +(nF×FW(O2)) / (nF×FW(CO2) (Equation 10)

[0187]

[0202] In the open configuration of device 10A, the expected result was net electrolysis and loss of cell mass in response to insufficient CO in the absence of sufficient CO input (see Equation 11): Li2CO3→CNM 生成物 (y) + Li2O(y) + O2↑, y = what stays in the cell, ↑ = gas that leaves the cell (Eq. 11)

[0188]

[0203] In the configuration of Apparatus 10A, where there is a minimal inlet for CO to enter the cell, i.e., only through a small section of porous insulation whose primary function is to allow the electrolysis off-gas product of O to exit the cell, the observed results were a pre-electrolysis cell mass of 2262.50 g and a post-electrolysis cell mass of 2257.50 g. The mass loss after electrolysis was approximately 5 g lower than the pre-electrolysis cell mass.

[0189]

[0204] With minimal CO2 input, the theoretical mass loss as O2 is: Loss of 32.00g x 2A x 9h / 4F = 5.37g per mole of O2 (due to the evolution of O2)

[0190]

[0205] The change in oxygen, DO2, was about 93% (indicating oxygen evolution).

[0191]

[0206] The theoretical mass of CO2 is: 44.01g x 2A x 9h / 4F = 7.38g per mole of CO2

[0192]

[0207] The change in CO2 DCO462 was about 5% (indicating slight 46 absorption of CO2). Without being bound to any particular theory, the CNM product remained on the cathode with n(e-)=4, while the anode produced O2 evolved from cell 12.

[0193]

[0208] Example 3B

[0209] FIG. 5B shows a second apparatus 10B that was also used for the capture and CNM production experiments described above. The insulation 22 used was again a 2-inch thick piece of Durablanket® with a density of 8 pcf, but this time with a larger surface area comprised of walls and a ceiling disposed between the input gas mixture source and the electrolyte surface 21A to enhance CO2 access and absorption into the electrolyte medium 21. In the apparatus 10B shown in FIG. 5B with the frame 22A, the expected result is net electrolysis with CO2 diffusing through the insulation to increase cell mass due to at least partial regeneration of carbon in the electrolyte medium 21 according to Equations 12, 13, and 14. Li2CO3→C CNT (y) + Li2O(y) + O2↑ (outgassing), y = what remains in the cell (Eq. 12) CO2(air) + Li2O(y) → Li2CO3 (Eq. 13) Net: CO2(air) → C CNT (y)+O2↑ (Eq. 14)

[0194]

[0210] In the open configuration of the apparatus 10B with frame 22A, the observed results were a pre-electrolysis cell mass of 2137.67 g and a post-electrolysis cell mass of 2138.81 g. In contrast to the measured mass loss that occurred in Example 3A, a mass gain was measured in this example, with the post-electrolysis mass being approximately 1.14 g more than the pre-electrolysis cell mass. The theoretical mass gain as C is: Increase of 12.01g x 2A x 9h / 4F = 2.01g per mole of C (as CNM product) Compared to the theoretical value, the change in carbon DC was about 57%.

[0195]

[0211] Furthermore, the conversion of CO2 DCO2 was about 88% compared to the theoretical mass of CO2 calculated in Example 3A. Without being bound to any particular theory, Li2CO3 in the electrolyte medium 21 is regenerated using carbon from the CO2 remaining in the cell 12. The CNM product remains on the cathode 18 due to n(e-)=4, which is the main cause of the increase in cell mass.

[0196]

[0212] Example 3C

[0213] FIG. 5C shows a third apparatus 10C used in the above capture and CNM production experiments. The insulation 22 was a 2-inch thick piece of 8 pcf density Durablanket® with an expanded surface, which now formed air channels. By flowing air through the channels formed by the solid insulation wall and the inner porous insulation wall, net contact of the porous insulation with the air and its CO2 can be improved. For apparatus 10C with housing 24 and frame 22B, the expected result was net electrolysis similar to Example 2B.

[0197]

[0214] In the open configuration of device 10C, the observed results were a pre-electrolysis cell mass of 2241.13 g and a post-electrolysis cell mass of 2243.16 g. The post-electrolysis mass was about 2.03 g more than the pre-electrolysis cell mass. The change in carbon conversion DC was about 101% and the change in CO2 DCO2 was about 100%. Without being bound by any theory, it is believed that the diffusion rate of CO2 through insulation increases approximately linearly with decreasing insulation thickness and increases approximately linearly with decreasing insulation density. Thus, by using equivalent insulation but 4 pcf instead of 8 pcf and a thickness of 0.5 inches instead of 2 inches, the sustainable current at high DCO2 may be increased to about 16 amps instead of 2 amps.

[0198]

[0215] Without being bound to any particular theory, the increased cell mass may result because the Li2CO3 in the electrolyte medium 21 is at least partially regenerated by the CO2 drawn into cell 12, and carbon from that CO2 remains in cell 12 to generate CNM product. The increased cell mass is due to increased CNM product originating from the CO2 in plenum D, plenum C, and ultimately electrolytic space B.

[0199]

[0216] Example 4 - Activation of the medium

[0217] The electrolyte medium may require activation to begin consuming the CO2 recovered from the input gas mixture. At 750°C, equilibrium was reached with pure Li2CO3 at approximately 0.3 molar Li2O concentration in Li2CO3, and no mass change was measured for pure Li2CO3 mixed with 0.33 molar Li2O over a 4 hour period. Thus, without being bound by any theory, equilibrium is maintained according to Equation 15:

[0200] [ka]

[0201]

[0219] This consumption may be driven by the transfer of CO2 from the gas phase to the molten lithium carbonate electrolyte medium, for example, according to Equation 1 and electrolytic consumption. Without being bound by any theory, if CO2 is not consumed, the electrolyte medium is consumed and not regenerated by CO2, according to Equation 2. The electrolyte medium may electrolytically decompose and lose weight as oxygen is evolved, according to Equation 2 (rather than following the net balance of Equations 1 and 2).

[0202]

[0220] In an example without electrolyte activation, molten Li2CO3 contained in a high purity alumina (Al2O3) crucible acted as inactive for CO2 absorption during electrolysis in the molten electrolyte. Specifically, fresh molten Li2CO3 exhibited the need to be activated to initiate the continuous electrolytic consumption of incoming gaseous CO2 in the air into the molten electrolyte. In one example, molten lithium carbonate exposed to hot air in a high purity alumina (Al2O3) crucible was inactive for CO2 absorption during electrolysis, regardless of whether or not the molten electrolyte contained metal (12.5% ​​cast iron). Specifically, fresh electrolyte was activated at 750° and 0.2 A / cm between a NiCrC anode and a Muntz brass cathode. 2 After 4 hours of electrolysis at 200 K, the cell showed good carbon deposition on the cathode, as predicted by Equation 2, but the total mass of the cell measured before and after electrolysis decreased rather than increasing as would be expected with sufficient CO2 absorption. The change in CO2 was either due to a lack of oxygen absorption, as shown in Equation 1, or due to the regeneration of CO2 per carbonate electrolyte.

[0203]

[0221] Repeating the 4-hour electrolysis in the cell while reusing the same electrolyte (which may be considered to be in the first stage of equilibration activation) resulted in a small absorption of CO2 (a 3% increase as measured by DCO2). This 3% indicated the beginning of the incomplete electrolyte CO2 continuous activation that regenerates carbonate during electrolysis. However, the pure Li2CO3 electrolyte was substantially activated when the electrolyte was heated at 750 °C for 24 hours (equilibration time) prior to electrode immersion and electrolysis. This activation step increased the CO2 conversion to about 81%. Similarly, when Li2CO3 and sufficient Li2O (5 wt%) were mixed in a stainless steel 304 crucible rather than alumina without waiting for equilibration after the electrolysis time, the CO2 conversion in the new molten electrolyte increased to about 99%, indicating nearly complete CO2 absorption. Similar to the electrolysis without time equilibration activation with pure Li2CO3, fresh Li2CO3 mixed with 10 wt% Na2CO3, or fresh Li2CO3 mixed with 3 wt% and 1.3 wt% CaO, showed no mass-based evidence of CO2 absorption during 4 h of electrolysis. The electrolyte can be modified with metal salts, metals, and other additives to affect both the CO2 absorption rate and the CNM products.

[0204]

[0222] Two other examples of CO2 absorption by electrolyte activation are described here. Electrolyte reuse may allow longer electrolyte equilibration times, presumably resulting in the observed increase in CO2 absorption; specifically, after electrolysis in Li2CO3 at 750 °C with 1 wt% Li2O, electrolyte reuse increased the CO2 change from 38% to 91%. Second, the top surface of the electrolyte relative to the top of the cell and in close proximity to the inward flow of CO2 is directly related to the measured change in observed CO2. When the gas phase interacted with the electrolysis electrodes immersed in the low electrolyte (below the top of the cell), very low values ​​of CO2 change were observed, suggesting a CO2-depleted "dead zone" just above the top surface of the molten electrolyte medium. Without being bound by any theory, this dead zone may be related to the flow of gas (up from the surface) leaving during electrolysis without access to gas-phase CO2 during electrolysis. In some cases, this depletion was observed to be so great that electrolyte decomposition apparently occurred beyond that resulting from electrolysis in Equation 2, and the CO2 concentration became so low above the surface of the electrolyte medium that, without being bound by any theory, the carbonate could be further decomposed according to Equation 11. This further carbonate decomposition could lead to further mass loss and loss of CO2, rather than the electrolyte using the CO2 to produce the CNM product. For electrolysis where the electrolyte was lowered in the crucible, the change in CO2 was measured to be -39%.

[0205]

[0223] Example 5 - Varying the Input Gas Flow

[0224] Inducing or enhancing the flow of input gas (e.g., by directing wind, adding additional fans, blowers, wind lenses, wind focuses, or driving convection) over a porous insulation material separated from the electrolyte medium can also affect the consumption of carbon-containing input gas such as CO2 in air by the electrolysis process. Thus, as a relevant example, a configuration as in FIG. 5C was used with an electrolyte medium containing Li2CO3 at 750° C. with 1 wt% Li2O equilibrated for 24 hours in a stainless steel 304 crucible. The electrolysis process was then carried out at air velocities of either 0 m / s, 1.5 m / s, or 2.5 m / s, with CO2 changes of 38%, 89%, and 100%, respectively. The cases of higher wind velocities showed virtually complete absorption of CO2.

[0206]

[0225] Note that in another example, the presence of a combination of (i) air sparging, (ii) a metal crucible, and (iii) a low level of added LiO (3 1 / 3 wt%), but using a fresh rather than time-equilibrated electrolyte, still resulted in a relatively low CO uptake of about 8%.

[0207]

[0226] Example 6 - Varying current density

[0227] J is the current density of the electrolysis 電解 can also affect the magnitude of the change in CO2. The higher the J, the greater the inflow velocity of CO2. Thus, under the previous conditions, if the inflow air velocity is 2.5 m / s, J 電解 is 0.042A / cm 2 The CO2 absorption rate was about 100% at the same air velocity, but 電解 is 0.15A / cm 2 The CO2 absorption rate was measured at 55%.

[0208]

[0228] Example 7 - Increasing the insulation surface area

[0229] Increasing the surface area of ​​the first side 22C of the insulation 22, for example by contouring the first side 22C, can increase the net passage of CO2 through the insulation 22 and the rate of absorption of CO2 into the medium 21. Maintaining a substantially flat second side 22D of the insulation 22 can have the added benefit of minimizing heat flow from the plenum C to the outside. Increasing the surface area of ​​the first side 22C can be achieved by a wide variety of known contouring techniques, including but not limited to macroscopic (geometric), microscopic (surface roughening), and nanoscopic techniques / methods such as bonding molecular assemblies to the first side 22C. For example, the active surface area of ​​the first side 22C of the insulation 22 can be increased by adding a layer of "loose fill", blown fiberglass, borate coated cellulose, or ceramic insulation. This layer may be distributed loosely on the first surface 22C and then confined by a flat or shaped screen to maximize the surface area of ​​the first surface 22C.

[0209]

[0230] Another example of contouring the first surface 22C is a macroscopic "dimple" surface reinforcement. As shown in FIG. 11, the first surface 22C can be contoured by various methods to form a plurality of dimples 500 that define a plurality of inter-dimple channels 502. The dimples 500 shown in FIG. 11 may be convex, meaning that they extend away from the second surface 22D, concave, meaning that they extend toward the second surface 22C, or a combination thereof. The plurality of inter-dimple channels 502 together define a convoluted inter-dimple channel 506 through which the input mixed gas may flow. The plurality of dimples 502 also define an over-dimple channel 508 through which the input mixed gas may flow over the convex or concave dimples, instead of or in addition to flowing through the inter-dimple channels 502 in contact with the permeable insulating material.

[0210]

[0231] The surface area of ​​the two-dimensional first side 22C may also be enhanced by macroscopic, microscopic, or nanoscopic methods. Non-limiting examples of methods for microscopic surface area enhancement include roughening the first side 22C by mechanical, physical, optical, electrical, electrochemical, or thermal methods. Microscopic and nanoscopic increases in surface area may also be achieved by chemical treatment of the first side 22C, such as chemical vapor deposition on the first side 22C, chemical reactions, chemical or electrochemical etching, etc.

[0211]

[0232] Without being bound to any particular theory, increasing the surface area of ​​first side 22C by macroscopic means, microscopic means, or a combination thereof may increase the net selective passage of CO2 from first side 22C to second side 22D and into media 21 by providing a chemical affinity, physical affinity, or both, for CO2 to enter insulation 22. In turn, the increased net passage of CO2 through insulation 22 may increase the amount and / or rate at which CO2 is absorbed into media 21.

[0212]

[0233] Example 8 - Altering the flow path between the insulation and the housing

[0234] FIG. 12A illustrates an apparatus 10D having many of the same features as apparatus 10C (shown in FIG. 5C), with apparatus D defining an extended / longer path length of a flow passage 26C defined between an inner surface 24B of the housing 24 and a first side 22C of the insulation 24. The housing 24 has an outer surface 24A that may take a variety of different shapes to aid in integrating the apparatus into one or more systems described herein. The flow passage 26C begins at an input opening 26A and ends at an output opening 26B. As shown in FIG. 12A, the inner surface 24B may define one or more peaks 24C that extend away from the outer surface 24A and toward the first side 22C. The inner surface 24B may also define one or more valleys 24D that extend away from the first side 22C and toward the outer surface 24A.

[0213]

[0235] Additionally or alternatively, the first side 22C of the insulation 22 may define one or more peaks 22E that extend toward the inner side 24B and away from the second side 22D. The first side 22C may also define one or more valleys 22F that extend away from the inner side 24B and toward the second side 22D.

[0214]

[0236] The presence of peaks and / or valleys in flow path 26C defined by inner surface 24B of housing 24, first side 22C of insulation 22, or both, may enhance the net selective passage of CO2 through insulation 22 and into media 21 by increasing the distance the input gas mixture flows along first side 22C. Due to the circuitous nature of flow path 26C, the flow of input gas mixture in flow path 26C may be redirected one or more times as it travels from input opening 26A (where the input gas mixture may have substantially the same constituent gases as the input gas mixture at the source) over first side 22C of insulation 22 to exit through output opening 26B (where the gas in flow path 26C is depleted of carbon-containing gases such as CO2 and is optionally replenished with off-gas generated in cell 12, such as hot O2). The change of direction provided by circuitous flow path 26C may induce turbulence in the input gas mixture and / or extend the flow path length. The turbulence and extended flow path length, respectively, can enhance the interaction of the input gas mixture with the first surface 22C of the insulation 22 and enhance the net selective passage of the carbon-containing gas to exit the flow path 26A into the plenum C and ultimately into the media 21, as compared to when the first surface 22C and the inner surface 24B are substantially flat or smooth. Various flow paths or pathways that maximize this interaction are contemplated herein, and the flow path 26C shown in FIG. 12A is not intended to be limiting. As will be apparent to one of ordinary skill in the art, the path length of the gas input flow path across the permeable insulation can be increased or extended with various mechanical and geometric configurations. In a further embodiment, the input gas mixture can be compressed by a compressor to flow across the first surface 22C at a pressure higher than ambient pressure to promote the inward flow of CO2 into the hotter media.

[0215]

[0237] FIG. 12A shows how the O2 off-gas products of the electrolysis process pass from the second side 22D to the first side 22C of the insulation 22 to form an exhaust stream (see arrow X in FIG. 12A) that mixes with the CO2-depleted input gas toward the output opening 26B. Above the surface 21A of the medium 21, generation of the O2 electrolysis off-gas products occurs in the region close to the anode 16, and localized collection of the off-gas products can be facilitated. Various techniques for collecting the O2 electrolysis off-gas products and separating them from the input gas mixture can be envisioned by those skilled in the art, and one non-limiting technique for collecting and separating the off-gas products is shown in FIG. 12B.

[0216]

[0238] FIG. 12B illustrates how the O2 off-gas product exhaust stream is collected in exhaust conduit 30 and separated from the CO2 depleted input gas exiting apparatus 10D by exhaust opening 26C. Exhaust conduit 30 provides fluid communication between plenum C and plenum D. Alternatively, exhaust conduit 30 may be coupled to a transport and / or storage system (not shown) to provide fluid communication between plenum C and a system that facilitates further use of the oxygen off-gas product. Exhaust conduit X may be made of a variety of materials that will withstand the chemical and temperature environment in plenum C, including the hot off-gas products in exhaust stream X. In some embodiments of the present disclosure, exhaust conduit 30 may direct hot oxygen off-gas product exhaust stream X through an optional heat exchanger 32 that may extract some, most, substantially all, or all of the thermal energy from the oxygen off-gas product in exhaust conduit 30. Heat exchanger 32 may transfer the recovered thermal energy to plenum B, plenum C, or both. Advantages of recovering and separating the hot O2 off-gas product are that (i) some or all of the heat can be returned to the apparatus via heat exchanger 32, and (ii) the high purity O2 product can be directed to a variety of useful industrial and / or oxy-fuel processes. Those skilled in the art will appreciate that the use of exhaust conduit 30 and optional heat exchanger 32 is not limited to use with apparatus 10D. Recovery and separation of the hot exhaust stream may be employed in the various apparatuses described herein, which may be used in the various systems and methods described herein.

[0217]

[0239] In some embodiments of the present disclosure, the insulation 22 may be modified to preferentially or selectively allow a greater flow rate of carbon-containing gases than other constituent gases of the input gas mixture. For example, the molecular structure of the permeable insulation may be chemically altered to selectively allow carbon-containing gases to pass through the insulation 22 more easily compared to the ease of passage of other non-carbon-containing constituent gases or combinations thereof when the insulation 22 is not so altered. For example, the insulation 22 may be altered to allow certain non-carbon-containing gases to be absorbed or adsorbed into the insulation, thus preventing these non-carbon-containing gases from entering the plenum C to be absorbed into the medium 21. In some embodiments of the present disclosure, the insulation may be altered to incorporate molecular sieves that select which constituent gases of the input gas mixture may pass through the insulation more easily than other constituent gases.

[0218]

[0240] Without being bound by any particular theory, the above examples demonstrate the selective capture of CO2 from the input gas mixture and the use of the captured carbon for the production of CNM products. The experiment was monitored from start to finish, including measuring the cell mass before and after electrolysis. Experiments and calculations were compared. Results were verified. Experiments showed that the cell can robustly access rates without the need to heat all of the input gas mixture. The porous insulation with a high CO2 affinity high temperature medium allowed for a net selective passage / diffusion of CO2, which is at least one mechanism by which the selective capture of CO2 from the input gas mixture occurred. Both surface adsorption and pore size influenced the CO2 diffusion of the CO2 / N2 mixture across the porous insulation. The porous structure of the insulation promoted the interaction of the captured CO2 gas with the electrolyte medium. The high affinity of the molten electrolyte for CO2 resulted in a net selective transfer from the gas phase above the electrolyte medium into the electrolyte medium. The experiments and examples described herein demonstrate that different configurations can affect the extent to which CO2 is absorbed in the cell. Experiments have demonstrated configurations and operating conditions such that CO2 is depleted, as well as configurations and operating conditions such that sufficient CO2 is supplied from the air for given operating conditions of the cell.

[0219]

[0241] As supported by the equations presented earlier in this specification, CO2 can be rapidly absorbed from the input gas mixture by exothermic reaction with the electrolyte medium and naturally concentrated through reaction with oxides in the molten salt of the electrolyte medium. The reaction of CO2 with the electrolyte medium can continuously regenerate the carbonate electrolyte medium as represented by equation 1. The experimental results are consistent with the expected mass gain or loss according to the equation (described in section 2). It is observed that the cell mass gain occurs due to carbon accumulated in the form of CNM products on the cathode as represented by the overall net equation (equation 3). Hot O2 generated in electrolysis can also be used. System features that can increase the extent of CO2 conversion to cathode-associated CNM products in molten carbonate electrolysis include, but are not limited to, increasing air or wind speed, using lower current density, modifying the porous insulation, adjusting the spacing between the insulation and the top surface of the electrolyte medium, activating the electrolyte by increasing the equilibration time, reusing the electrolyte, increasing the oxide concentration, placing the top surface of the electrolyte medium closer to the inner surface of the insulation, using a metal electrolytic cell, or a combination of these features.

Claims

1. 1. A system for selectively transferring a carbon-containing gas from an input gas mixture, the system comprising: (a) an insulation material that permits a net passage of the carbon-containing gas from the input gas mixture at a first temperature; (b) a plenum; and (c) an anode and a cathode disposed within the plenum; (d) a molten electrolyte medium contained within the plenum between the anode and the cathode at a second temperature, the second temperature being greater than the first temperature; 11. A system, comprising: a molten electrolyte medium having a first affinity for carbon in the carbon-containing gas received from the insulation, the molten electrolyte medium acting as a carbon sink, the molten electrolyte medium defining a surface having a first surface area, the surface in fluid communication with a source of the input mixed gas, the insulation assisting in the net passage of the carbon-containing gas to the surface of the molten electrolyte medium, the system configured to selectively heat and electrolytically decompose the carbon-containing gas to produce different chemicals, the insulation being disposed between the source of the input mixed gas and the plenum.

2. 2. The system of claim 1, wherein the first affinity for carbon includes the molten electrolyte medium chemically reacting with the carbon-containing gas received from the insulation, electrochemically reacting with the carbon-containing gas received from the insulation, absorbing the carbon-containing gas received from the insulation, bonding with the carbon-containing gas received from the insulation, or any combination thereof.

3. The system of claim 1 , wherein the first affinity for carbon includes the molten electrolyte medium producing a different chemical with the carbon-containing gas received from the insulation.

4. The system of claim 2 , wherein the first affinity for carbon includes the molten electrolyte medium producing a different chemical with the carbon-containing gas received from the insulation.

5. The system of claim 1 , wherein the carbon-containing gas is carbon dioxide (CO2).

6. 2. The system of claim 1, wherein the input mixed gas is air, an artificial CO2-containing gas, an industrial exhaust gas stream, gas from a sequestered CO2 reservoir, an exhaust gas from an industrial plant, an exhaust gas from a chemical reactor, an exhaust gas from a power plant, an exhaust gas from a steam generation facility, an exhaust gas from a pyrolysis reactor, a CO2-containing gas product from the combustion of a fossil fuel, a CO2-containing gas product from the conversion of a fossil fuel, a CO2-containing gas product from heating, a CO2-containing gas product from transportation, a CO2-containing gas product from the manufacture of a polymer, a CO2-containing gas product from the manufacture of a plastic, or a combination thereof.

7. The system of claim 1 , wherein the insulation is permeable.

8. The system of claim 1 , wherein the insulation is porous.

9. The system of claim 7 , wherein the insulation is porous.

10. 10. The system of claim 1, wherein the insulation material comprises fiberglass, cellulose, cotton, fabric, mineral wool, cement, carbonate, calcium aluminate, calcium silicate, aluminum silicate, chemical derivatives thereof, or any combination thereof.

11. The system of claim 1 , wherein the molten electrolyte medium has a second affinity for other gas constituents of the input gas mixture.

12. The system of claim 11 , wherein the first affinity is greater than the second affinity.

13. The system of claim 1 , wherein the first temperature is between −90° C. and 75° C.

14. The system of claim 1 , wherein the first temperature is between 50° C. and 400° C.

15. The system of claim 1 , wherein the second temperature is between 400° C. and 850° C.

16. The system of claim 1 , wherein the carbon-containing gas comprises CO2.

17. 2. The system of claim 1, wherein the first affinity for carbon includes the molten electrolyte medium chemically reacting with the carbon-containing gas received from the insulation, electrochemically reacting with the carbon-containing gas received from the insulation, absorbing the carbon-containing gas received from the insulation, or bonding with the carbon-containing gas received from the insulation.

18. The system of claim 16 , wherein the different chemical is elemental carbon.

19. The system of claim 16 , wherein the different chemical is a nanocarbon.

20. The system of claim 16 , wherein the different chemical is a graphitic nanocarbon.

21. The system of claim 1 , wherein the thermal insulation defines a surface area greater than the first surface area of ​​the molten electrolyte medium.

22. 2. The system of claim 1, wherein the insulation comprises a first side adjacent the source of the input gas mixture, the first side having a greater surface area than an opposing second side adjacent the molten electrolyte medium.

23. The system of claim 22 , wherein the first surface defines a plurality of dimples.

24. 2. The system of claim 1, further comprising a housing disposed between the insulation and the source of the input mixed gas, the housing and the insulation defining a flow path for passing the input mixed gas along a first side of the insulation.

25. 25. The system of claim 24, wherein the housing, the insulation, or both, define one or more peaks, one or more valleys, or both, to increase the length of the flow path.

26. The system of claim 1 , further comprising a conduit providing fluid communication between a source of an exhaust stream of off-gas products and an exterior of the system.

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