US20120228150A1 - Co2 decomposition via oxygen deficient ferrite electrodes using solid oxide electrolyser cell - Google Patents
Co2 decomposition via oxygen deficient ferrite electrodes using solid oxide electrolyser cell Download PDFInfo
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- US20120228150A1 US20120228150A1 US13/043,335 US201113043335A US2012228150A1 US 20120228150 A1 US20120228150 A1 US 20120228150A1 US 201113043335 A US201113043335 A US 201113043335A US 2012228150 A1 US2012228150 A1 US 2012228150A1
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
- C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
- C25B9/23—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms comprising ion-exchange membranes in or on which electrode material is embedded
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/02—Hydrogen or oxygen
- C25B1/04—Hydrogen or oxygen by electrolysis of water
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- C—CHEMISTRY; METALLURGY
- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/073—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material
- C25B11/075—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of a single catalytic element or catalytic compound
- C25B11/077—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of a single catalytic element or catalytic compound the compound being a non-noble metal oxide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
Definitions
- the present invention relates to the decomposition of carbon dioxide into carbon/carbon monoxide and oxygen via oxygen deficient ferrite (ODF) electrodes in a continuous process using solid oxide electrolyser cell (SOEC).
- ODF oxygen deficient ferrite
- SOEC solid oxide electrolyser cell
- Another application is the co-electrolysis of CO 2 and water to produce syngas for fuel or further processing.
- the generated O 2 can be re-circulated to the oxy-fuel combustion that will reduce fuel demand and energy requirement for the Air Separator Unit (ASU).
- ASU Air Separator Unit
- CO 2 carbon-dioxide
- CCS Carbon Capture and Storage
- a preferable approach would be to decompose CO 2 into C/CO and oxygen, or co-electrolysis with H 2 O to generate syngas (H 2 +CO) and oxygen (O 2 ) [Qingxi Fu, et al. (2010), Energy Environ. Sci., 3, 1382-1397] as shown in Reaction [1] and Reaction [2].
- Syngas and O 2 can be fed back to the oxyfuel combustion chamber that will reduce fuel demand for combustion and energy requirement for the Air Separator Unit (ASU).
- Syngas can also be further processed into synthetic liquid fuel (synfuel) through the Fischer-Tropsch process as shown in Reaction [3].
- CO can be further processed into methanol by reacting with H 2 that is produced from methane (CH 4 ) thermal pyrolysis [Muradov et al. Catalytic Dissociation of Hydrocarbons: a Route to CO-free Hydrogen] as shown in Reaction [4] and Reaction [5].
- CH 4 methane
- Carbon dioxide (CO 2 ) is electrochemically decomposed into carbon/carbon monoxide (CO) and oxygen (O 2 ) by Oxygen Deficient Ferrites (ODF) electrodes.
- the Solid Oxide Electrolysis Cell (SOEC) consists of a thin Yttria Stabilized Zirconia (YSZ) electrolyte with ODF electrodes on both sides, working as anode and cathode. In order to keep the electrodes active, a small potential bias ( ⁇ 0.5V) is applied across the electrodes. CO 2 and water (H 2 O) can also be electrolyzed simultaneously to produce syngas (H 2 +CO) and O 2 continuously.
- the generated O 2 can be re-circulated to the oxy-fuel combustion that will reduce fuel demand and energy requirement for the Air Separator Unit (ASU) and thus partially offset the energy required in the decomposition process.
- ASU Air Separator Unit
- CO or syngas can be recovered as valuable products that can be further processed into liquid fuel through Fischer-Tropsch process. With this approach, CO 2 can be transformed into a valuable fuel source allowing CO 2 neutral use of the hydrocarbon fuels.
- FIG. 1 shows the principle of ODF reactivity
- FIG. 2 shows a schematic of ODF electrodes in SOEC for CO 2 decomposition into CO and O 2
- FIG. 3 shows the SOEC inside NexTech ProbostatTM Test Apparatus
- ODF oxygen-deficient ferrites
- M x Fe 3-x O 4- ⁇ is formed by the reducing the spinal ferrites (M x Fe 3-x O 4- ⁇ ) with hydrogen gas (H 2 ) as shown in Reaction [6].
- M represents a bivalent metal ion such as Fe(II), Cu(II), Co(II), Mn(II), Ni(II), and so on; the oxygen deficiency ( ⁇ ) expresses the degree of reduction.
- the ODF then decomposed CO 2 into carbon as shown in Reaction [7].
- carbon is deposited on the ODF surface and oxygen is transferred in the form of oxide ions (O 2 ⁇ ) to be incorporated into the vacant lattice sites of ODF.
- oxide ions O 2 ⁇
- This process has been demonstrated to have high efficiency (nearly 100%) to decompose CO 2 to atomic carbon at the decomposition rate of 2.9-3.5 mmol per min per gram. (Tamaura, et al., Nature 346, 255-256 (1990); Tamaura, et al., Carbon 33 (10), 1443-1447 (1995)).
- the deposited carbon powder can be separated by mechanical or chemical processes, or can be converted into methane or syngas.
- FIG. 2 shows the schematic of the SOEC utilized in the present invention to decompose CO 2 electrochemically.
- a laboratory scale setup is also depicted in FIG. 3 .
- the electrolyser unit cell consists of a dense electrolyte as ionic-oxygen (O 2 ⁇ ) conductor and ODF-based anode and cathode electrodes.
- the electrolyte may be ceria-based electrolyte (eg. Gadolinium-doped Ceria (GDC or CGO), Samarium-doped Ceria (SDC)) or zirconia-based electrolyte (eg.
- YSZ Yttrium stabilized zirconia
- Scandium-doped zirconia ScSZ
- ODF e.g. nickel ferrite, copper ferrite
- perovskite electrode materials e.g. Lanthanum strontium cobalt ferrite (LSCF), lanthanum strontium ferrite (LSF), Lanthanum strontium cobalt oxide (LSC), lanthanum strontium manganite (LSM)
- electrolyte materials eg. LSCF/GDC, LSM/GDC, ODF/GDC, LSM/YSZ
- electrolyte materials eg. LSCF/GDC, LSM/GDC, ODF/GDC, LSM/YSZ
- electrolyte materials eg. LSCF/GDC, LSM/GDC, ODF/GDC, LSM/YSZ
- electrolyte materials eg. LSCF/GDC, LSM/GDC, O
- a feed which may contain CO 2 or CO 2 +H 2 O flows from a feed source 1 through the cathode side channel 2 and react with the ODF electrode 3 .
- a small potential bias is applied from the external source 4 that keep the ODF electrodes active.
- the electrode decomposes CO 2 into CO and oxide ions O 2 ⁇ as shown in Reaction [9].
- the generated oxide ions migrate thorough the YSZ electrolyte 5 to the anode electrode 6 and thus complete the cell internal circuit.
- the oxide ions combine to generate oxygen and shown in Reaction [10], which flow through the anode side channel 7 .
- a preliminary test was performed according to the embodiments of the invention to establish the feasibility of the inventive process.
- the test set is shown in FIG. 3 .
- a button cell 8 manufactured according to the description in FIG. 2 .
- the button cell was mounted inside the NexTech ProbostatTM 9 button cell test apparatus using AREMCO-516 high temperature cement.
- AlicatTM mass flow controllers (MFCs) were used to control the flow rates, pressure and compositions.
- the electrochemical performances were measured using Reference 300TM Potentiostat/Galvanostat/ZRA (Gamry Instruments, Warminster, Pa.) 10.
- the button cell was heated from room temperature to 750° C. at a rate of 1° C./min. During this period, the anode and cathode were exposed to 50 sccm of N 2 . After that, 100 sccm H 2 was provided to anode and cathode side, respectively, to reduce NiFe 2 O 4 into ODF at 750° C. Once the reduction of electrodes was completed, the cathode was supplied with 60 sccm of CO 2 . The experiment investigation was carried out at 750° C.
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
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- Inorganic Chemistry (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
Oxygen Deficient Ferrites (ODF) electrodes integrated with Yttria Stabilized Zirconia (YSZ) electrolyte, electrochemically decompose carbon dioxide (CO2) into carbon (C)/carbon monoxide (CO) and oxygen (O2) in a continuous process. The ODF electrodes can be kept active by applying a small potential bias across the electrodes. CO2 and water (H2O) can also be electrolyzed simultaneously to produce syngas (H2+CO) and O2 continuously that can be fed back to the oxy-fuel combustion. With this approach, CO2 can be transformed into a valuable fuel source allowing CO2 neutral use of the hydrocarbon fuels.
Description
- 1. Field of Invention
- The present invention relates to the decomposition of carbon dioxide into carbon/carbon monoxide and oxygen via oxygen deficient ferrite (ODF) electrodes in a continuous process using solid oxide electrolyser cell (SOEC). Another application is the co-electrolysis of CO2 and water to produce syngas for fuel or further processing. The generated O2 can be re-circulated to the oxy-fuel combustion that will reduce fuel demand and energy requirement for the Air Separator Unit (ASU).
- 2. State of the Art
- The attenuation of carbon-dioxide (CO2) concentration in the atmosphere has been an important ecological issue associated with the global warming. In order to mitigate this effect, Carbon Capture and Storage (CCS), and CO2 decomposition technologies are being developed. Currently, CO2 is captured from flue gas by amine scrubbing or cryogenic separation. Amine scrubbing involves two steps: absorption of CO2 at lower temperature and release the captured CO2 to a storage unit at higher temperature [Advanced Research Projects Agency—Energy, IMPACCT 2009]. This process consumes a significant portion of the power plant energy output. Moreover, the captured CO2 must be compressed and transported to a permanent place which is also an energy consuming process.
- A preferable approach would be to decompose CO2 into C/CO and oxygen, or co-electrolysis with H2O to generate syngas (H2+CO) and oxygen (O2) [Qingxi Fu, et al. (2010), Energy Environ. Sci., 3, 1382-1397] as shown in Reaction [1] and Reaction [2].
-
CO2→CO+½O2ΔH600° C. =283kJ/mole [1] -
H2O→H2+½ O2ΔH600° C. =247kJ/mole [2] - Syngas and O2 can be fed back to the oxyfuel combustion chamber that will reduce fuel demand for combustion and energy requirement for the Air Separator Unit (ASU). Syngas can also be further processed into synthetic liquid fuel (synfuel) through the Fischer-Tropsch process as shown in Reaction [3].
-
(2n+1)H2+nCO→CnH(2n+2)+nH2O [3] - CO can be further processed into methanol by reacting with H2 that is produced from methane (CH4) thermal pyrolysis [Muradov et al. Catalytic Dissociation of Hydrocarbons: a Route to CO-free Hydrogen] as shown in Reaction [4] and Reaction [5].
-
CH4→C+2H2ΔH800° C.92kJ/mole [4] -
CO+2H2→CH3OHΔH250° C.=−128kJ/mole [5] - Thus, CO2 can be chemically transformed into a valuable energy source and its storage will not be a concern. Moreover, the generated O2 will reduce the ASU energy requirement [McCutchen, et al. U.S. Pat. App. No. 201010146927 (published Jun. 17, 2010)].
- Carbon dioxide (CO2) is electrochemically decomposed into carbon/carbon monoxide (CO) and oxygen (O2) by Oxygen Deficient Ferrites (ODF) electrodes. The Solid Oxide Electrolysis Cell (SOEC) consists of a thin Yttria Stabilized Zirconia (YSZ) electrolyte with ODF electrodes on both sides, working as anode and cathode. In order to keep the electrodes active, a small potential bias (<0.5V) is applied across the electrodes. CO2 and water (H2O) can also be electrolyzed simultaneously to produce syngas (H2+CO) and O2 continuously. The generated O2 can be re-circulated to the oxy-fuel combustion that will reduce fuel demand and energy requirement for the Air Separator Unit (ASU) and thus partially offset the energy required in the decomposition process. Moreover, CO or syngas can be recovered as valuable products that can be further processed into liquid fuel through Fischer-Tropsch process. With this approach, CO2 can be transformed into a valuable fuel source allowing CO2 neutral use of the hydrocarbon fuels.
-
FIG. 1 shows the principle of ODF reactivity -
FIG. 2 shows a schematic of ODF electrodes in SOEC for CO2 decomposition into CO and O2 -
FIG. 3 shows the SOEC inside NexTech Probostat™ Test Apparatus - CO2 can be actively decomposed into carbon on the oxygen-deficient ferrites (ODF) surface. The principle of ODF reactivity is shown in
FIG. 1 . ODF (MxFe3-xO4-δ) is formed by the reducing the spinal ferrites (MxFe3-xO4-δ) with hydrogen gas (H2) as shown in Reaction [6]. Here M represents a bivalent metal ion such as Fe(II), Cu(II), Co(II), Mn(II), Ni(II), and so on; the oxygen deficiency (δ) expresses the degree of reduction. -
Reduction H2+O2−+2Fe3+→H2O+Vo+2Fe2+[6] -
Decomposition CO2+2Vo+4Fe2+→C+2O2−+4Fe3+ [7] -
Methanation C+2H2→CH4 [8] - The ODF then decomposed CO2 into carbon as shown in Reaction [7]. In this step, carbon is deposited on the ODF surface and oxygen is transferred in the form of oxide ions (O2−) to be incorporated into the vacant lattice sites of ODF. This process has been demonstrated to have high efficiency (nearly 100%) to decompose CO2 to atomic carbon at the decomposition rate of 2.9-3.5 mmol per min per gram. (Tamaura, et al., Nature 346, 255-256 (1990); Tamaura, et al., Carbon 33 (10), 1443-1447 (1995)). The deposited carbon powder can be separated by mechanical or chemical processes, or can be converted into methane or syngas. During methanation, the carbon deposited by CO2 decomposition can be readily reacted with H2 to form CH4 (Tsuji, et al., Journal of Materials Science 29, 5481-5484 (1994); Tsuji, et al., Journal of Catalysis 164, 315-321 (1996)). Recently, a growing interest has been developed for electrochemical conversion of CO2 to produce syngas and O2 using Solid Oxide Electrolyser Cell (SOEC) [Zhan et al. Energy & Fuel 2009, 23, 3089-3096].
- In the present invention, ODF electrode are integrated with YSZ electrolyte to decompose CO2 into C/CO and O2.
FIG. 2 shows the schematic of the SOEC utilized in the present invention to decompose CO2 electrochemically. A laboratory scale setup is also depicted inFIG. 3 . The electrolyser unit cell consists of a dense electrolyte as ionic-oxygen (O2−) conductor and ODF-based anode and cathode electrodes. The electrolyte may be ceria-based electrolyte (eg. Gadolinium-doped Ceria (GDC or CGO), Samarium-doped Ceria (SDC)) or zirconia-based electrolyte (eg. Yttrium stabilized zirconia (YSZ), Scandium-doped zirconia (ScSZ)). ODF (e.g. nickel ferrite, copper ferrite) particles and/or several perovskite electrode materials (eg. Lanthanum strontium cobalt ferrite (LSCF), lanthanum strontium ferrite (LSF), Lanthanum strontium cobalt oxide (LSC), lanthanum strontium manganite (LSM)) combined with corresponding electrolyte materials (eg. LSCF/GDC, LSM/GDC, ODF/GDC, LSM/YSZ) serve as electrodes for anode and cathode respectively. Analogous to the fuel cell technology, the proposed setup can be easily scaled up. - A feed which may contain CO2 or CO2+H2O flows from a
feed source 1 through thecathode side channel 2 and react with theODF electrode 3. A small potential bias is applied from the external source 4 that keep the ODF electrodes active. The electrode decomposes CO2 into CO and oxide ions O2−as shown in Reaction [9]. -
CO2+2e−→CO+O2− [9] -
O2−→½O2+2e− [10] - The generated oxide ions migrate thorough the YSZ electrolyte 5 to the
anode electrode 6 and thus complete the cell internal circuit. At the anode electrode the oxide ions combine to generate oxygen and shown in Reaction [10], which flow through theanode side channel 7. - A preliminary test was performed according to the embodiments of the invention to establish the feasibility of the inventive process. The test set is shown in
FIG. 3 . Abutton cell 8 manufactured according to the description inFIG. 2 . The button cell was mounted inside the NexTech Probostat™ 9 button cell test apparatus using AREMCO-516 high temperature cement. Alicat™ mass flow controllers (MFCs) were used to control the flow rates, pressure and compositions. Concurrently, the electrochemical performances were measured using Reference 300™ Potentiostat/Galvanostat/ZRA (Gamry Instruments, Warminster, Pa.) 10. - The button cell was heated from room temperature to 750° C. at a rate of 1° C./min. During this period, the anode and cathode were exposed to 50 sccm of N2. After that, 100 sccm H2 was provided to anode and cathode side, respectively, to reduce NiFe2O4 into ODF at 750° C. Once the reduction of electrodes was completed, the cathode was supplied with 60 sccm of CO2. The experiment investigation was carried out at 750° C. and the cell electrochemical performances were measured using Reference 300 Potentiostat/Galvanostat/ZRA (Gamry Instruments, Warminster, Pa.), and exhaust gases were analyzed via Gas Chromatography (GC) 11. This test confirmed the feasibility of CO2 electrolysis via ODF electrodes in a continuous process as shown in Table 1.
-
TABLE 1 Gas Chromatography Analysis Description After After After After decomposition decomposition decomposition decomposition for 6 hrs for 150 hrs for 461 hrs for 531 hrs Cathode Anode Cathode Anode Cathode Anode Cathode Anode Side Side Side Side Side Side Side Side Compound (%) (%) (%) (%) (%) (%) (%) (%) CO2 44.72 3.04 49.48 5.06 47.23 3.41 44.20 5.05 CO ND ND ND ND 1.16 ND 0.52 0.14 O2 13.35 79.32 13.16 94.16 14.05 56.08 13.94 84.48 H2 ND ND ND ND ND ND ND ND Ar 8.17 ND 8.45 ND 4.84 8.94 3.79 9.55 N2 33.76 17.64 28.91 0.78 32.72 31.58 37.34 0.77
Claims (1)
1. A method to decompose CO2 into C/CO and O2 using Oxygen Deficient Ferrites (MxFe3-xO4-δ, M represents a bivalent metal ion such as Fe(II), Cu(II), Co(II), Mn(II), Ni(II), and so on) electrodes integrated with solid oxide electrolyser cell.
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Cited By (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2014154253A1 (en) | 2013-03-26 | 2014-10-02 | Haldor Topsøe A/S | A process for producing co from co2 in a solid oxide electrolysis cell |
WO2014170200A1 (en) | 2013-04-19 | 2014-10-23 | Gunnar Sanner | Methods for production of liquid hydrocarbons from energy, co2 and h2o |
US20150299871A1 (en) * | 2014-04-21 | 2015-10-22 | University Of South Carolina | Partial oxidation of methane (pom) assisted solid oxide co-electrolysis |
EP2940773A1 (en) | 2014-04-29 | 2015-11-04 | Haldor Topsøe A/S | Ejector for solid oxide electrolysis cell stack system |
DE102014009531A1 (en) | 2014-06-26 | 2015-12-31 | Linde Aktiengesellschaft | Process and Vorrichtuntg for reacting at least one reactant in a gaseous feed stream to at least one product |
US9238598B2 (en) | 2013-01-04 | 2016-01-19 | Saudi Arabian Oil Company | Carbon dioxide conversion to hydrocarbon fuel via syngas production cell harnessed from solar radiation |
US9364791B1 (en) | 2015-02-12 | 2016-06-14 | Gas Technology Institute | Carbon dioxide decomposition |
KR20180052412A (en) * | 2016-11-10 | 2018-05-18 | 한국에너지기술연구원 | Solid Oxide Electrolysis Cells for Production of Synthesis Gas from CO2-Containing Biogas |
CN113012842A (en) * | 2019-12-20 | 2021-06-22 | 中国科学院福建物质结构研究所 | Isotope of carbon monoxide14C curing method |
CN114555865A (en) * | 2019-10-08 | 2022-05-27 | 于利希研究中心有限公司 | Carbon monoxide production |
US11401165B2 (en) | 2016-02-26 | 2022-08-02 | Haldor Topsøe A/S | Carbon monoxide production process optimized by SOEC |
US11905173B2 (en) | 2018-05-31 | 2024-02-20 | Haldor Topsøe A/S | Steam reforming heated by resistance heating |
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WO2014154253A1 (en) | 2013-03-26 | 2014-10-02 | Haldor Topsøe A/S | A process for producing co from co2 in a solid oxide electrolysis cell |
WO2014170200A1 (en) | 2013-04-19 | 2014-10-23 | Gunnar Sanner | Methods for production of liquid hydrocarbons from energy, co2 and h2o |
US9574274B2 (en) * | 2014-04-21 | 2017-02-21 | University Of South Carolina | Partial oxidation of methane (POM) assisted solid oxide co-electrolysis |
US20150299871A1 (en) * | 2014-04-21 | 2015-10-22 | University Of South Carolina | Partial oxidation of methane (pom) assisted solid oxide co-electrolysis |
EP2940773A1 (en) | 2014-04-29 | 2015-11-04 | Haldor Topsøe A/S | Ejector for solid oxide electrolysis cell stack system |
DE102014009531A1 (en) | 2014-06-26 | 2015-12-31 | Linde Aktiengesellschaft | Process and Vorrichtuntg for reacting at least one reactant in a gaseous feed stream to at least one product |
US9364791B1 (en) | 2015-02-12 | 2016-06-14 | Gas Technology Institute | Carbon dioxide decomposition |
US11401165B2 (en) | 2016-02-26 | 2022-08-02 | Haldor Topsøe A/S | Carbon monoxide production process optimized by SOEC |
KR20180052412A (en) * | 2016-11-10 | 2018-05-18 | 한국에너지기술연구원 | Solid Oxide Electrolysis Cells for Production of Synthesis Gas from CO2-Containing Biogas |
KR101963172B1 (en) * | 2016-11-10 | 2019-07-31 | 한국에너지기술연구원 | Solid Oxide Electrolysis Cells for Production of Synthesis Gas from CO2-Containing Biogas |
US11905173B2 (en) | 2018-05-31 | 2024-02-20 | Haldor Topsøe A/S | Steam reforming heated by resistance heating |
CN114555865A (en) * | 2019-10-08 | 2022-05-27 | 于利希研究中心有限公司 | Carbon monoxide production |
CN113012842A (en) * | 2019-12-20 | 2021-06-22 | 中国科学院福建物质结构研究所 | Isotope of carbon monoxide14C curing method |
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