WO2024120928A1 - Procédé et installation pour produire un mélange de gaz de départ contenant ou étant constitué d'hydrogène et d'azote - Google Patents

Procédé et installation pour produire un mélange de gaz de départ contenant ou étant constitué d'hydrogène et d'azote Download PDF

Info

Publication number
WO2024120928A1
WO2024120928A1 PCT/EP2023/083533 EP2023083533W WO2024120928A1 WO 2024120928 A1 WO2024120928 A1 WO 2024120928A1 EP 2023083533 W EP2023083533 W EP 2023083533W WO 2024120928 A1 WO2024120928 A1 WO 2024120928A1
Authority
WO
WIPO (PCT)
Prior art keywords
water vapor
heat exchanger
hydrogen
countercurrent heat
soec stack
Prior art date
Application number
PCT/EP2023/083533
Other languages
German (de)
English (en)
Inventor
Michael Gallwitz
Gregor Herz
Paul Adam
Erik Reichelt
Original Assignee
Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V. filed Critical Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V.
Publication of WO2024120928A1 publication Critical patent/WO2024120928A1/fr

Links

Classifications

    • 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
    • C25B1/042—Hydrogen or oxygen by electrolysis of water by electrolysis of steam
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/025—Preparation or purification of gas mixtures for ammonia synthesis
    • 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
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/081—Supplying products to non-electrochemical reactors that are combined with the electrochemical cell, e.g. Sabatier reactor
    • 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
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/083—Separating products

Definitions

  • a process and a plant for producing a reactant gas mixture containing or consisting of hydrogen and nitrogen is provided.
  • the process and the system are characterized by the fact that only a maximum of two solid oxide electrolysis cell stacks (SOEC stacks) connected in series are used, no air is supplied to the first SOEC stack, and a burner between the two SOEC stacks is supplied with air on the one hand and steam on the other at a temperature in the range of 100 °C to 150 °C.
  • SOEC stacks solid oxide electrolysis cell stacks
  • the process and the system make it possible to produce a reactant gas mixture that contains or consists of hydrogen and nitrogen in a small space and in a more energy-efficient and cost-effective manner, while also minimizing the risk of downtime.
  • NH3 ammonia
  • both low-temperature and high-temperature electrolysis processes can be used to integrate renewable energy using electrolysis.
  • an additional process step for the provision of N2 may be necessary.
  • a known solution approach in the state of the art for electrolysis-based feedstock gas production is based on the separate production of H2 from H2O and N2 from air, followed by combining and reacting the material flows to form NH3.
  • the processes of alkaline electrolysis, PEM electrolysis and high-temperature electrolysis can be used for H2O electrolysis.
  • N2 is obtained directly from the air in an air separation unit using cryogenic air separation unit (ASU), pressure swing adsorption (PSA) or membrane technology.
  • ASU cryogenic air separation unit
  • PSA pressure swing adsorption
  • the subsequent purification of the feedstock gas is limited to the removal of unreacted H2O due to the high purity of the gases produced by electrolysis or air separation.
  • a very low proportion of inert gas results in the downstream synthesis cycle.
  • Feedstock gas production designed in this way can be operated entirely with electrical energy. If this is obtained from renewable sources, emission-free NHs production is possible.
  • a simplified flow diagram of this known process is shown in Figure
  • a mixture is fed to the first SOEC stack which contains not only water vapor but also air, which increases the energy consumption of the process.
  • the SOEC stacks have to be brought to a very high temperature during high-temperature electrolysis and kept at this temperature, which, with a large number of stacks, results in a high heat input and, due to a high temperature gradient with the environment, high heat losses during the process.
  • the implementation of the process could thus be more energy-efficient and cost-effective (ie more economical and ecological).
  • the object of the present invention was to provide a process and a plant for producing hydrogen (Hz) and nitrogen (Nz) which do not have the disadvantages of the prior art.
  • the process and the plant should allow H2 and N2 to be produced in a more energy-efficient and cost-effective manner (i.e. more ecological and economical).
  • a method for producing a reactant gas mixture containing or consisting of hydrogen and nitrogen comprising the following steps: a) introducing a gas which contains or consists of water vapor, but not air, into a cathode of a first SOEC stack which has an anode and has a cathode, wherein in the first SOEC stack, oxygen and hydrogen are partially produced from the water vapor and oxygen and hydrogen are spatially separated, wherein at least 20 vol.% of the water vapor, in relation to a total volume of the water vapor, is not converted to oxygen and hydrogen; b) discharging the oxygen from the anode of the first SOEC stack as exhaust gas; c) discharging a mixture which contains or consists of hydrogen and unreacted water vapor from the cathode of the first SOEC stack into a burner, wherein additional air and additional water vapor are introduced into the burner, wherein the additionally introduced water vapor has a temperature in the range of 100 °C to 150 °C, wherein
  • SOEC stack refers to a stack of solid oxide electrolysis cells, i.e. a solid oxide electrolysis cell stack. In the process according to the invention, only two SOEC stacks are used, which makes it possible to produce an approximately stoichiometric reactant gas mixture in a merely two-stage arrangement, ie with a low system complexity and the smallest possible cell area.
  • a first essential feature of the process is that a gas is fed to the first SOEC stack that contains or consists of water vapor, but not air. This reduces the proportion that has to be returned from the already generated reactant gas to a technically necessary minimum, which is advantageous both in terms of energy and in terms of the dimensioning of the components.
  • nitrogen is therefore only integrated after the first SOEC stack (i.e. between the two SOEC stacks in a burner) by supplying air.
  • a second key feature of the process is that in addition to air, water vapor, which has a temperature in the range of 100 °C to 150 °C, is introduced into the burner, which is arranged between the first and second SOEC stacks.
  • This additional water vapor makes it possible to efficiently cool (i.e. "quench") the gas mixture produced in the burner, which has a very high temperature due to the combustion of hydrogen with the oxygen from the air, and at the same time to heat up the supplied water vapor so that the resulting gas mixture is conditioned to an ideal working temperature for the second SOEC stack (i.e. a temperature of 700 °C to 900 °C).
  • this measure allows the first SOEC stack and/or second SOEC stack to be operated exothermically.
  • the advantage of this is that the first and second SOEC stacks require a significantly smaller cell area for electrolysis than in prior art processes (e.g. the process of WO 2019/072608 Al), which can greatly reduce process costs and minimize downtime.
  • this measure allows a gas mixture with a high nitrogen content to be produced upstream of the second SOEC stack, since the cooling effect of the water vapor introduced into the burner allows more air to be introduced into the burner than with known processes from the state of the art.
  • the reason for this is that when hydrogen is burned with a large amount of air (or the oxygen content of the air), a large amount of thermal energy is generated, but this thermal energy is absorbed by the water vapor, which is also fed into the burner and has an inlet temperature in the range of 100 to 150 °C, so that even with a very large air supply (and thus nitrogen supply), the gas can be tempered to an optimal operating temperature of the second SOEC stack.
  • the process according to the invention therefore makes it possible to produce a reactant gas mixture containing or consisting of hydrogen and nitrogen in a compact space in a more energy-efficient, more cost-effective and less error-prone manner (i.e. more economical and ecological).
  • the process is suitable as a starting process for the sustainable production of ammonia (NH3).
  • Ammonia is currently one of the most important bulk chemicals and will continue to play an important role in the future as a starting material for the chemical industry and fertilizer production, as well as a carbon-free energy source.
  • the gas introduced into the cathode of the first SOEC stack can have a temperature of >800 °C.
  • the material flow of the gas introduced into the cathode of the first SOEC stack can be approximately 17.5% of the material flow of a reactant gas mixture that is to be (or is) provided by the process (standardized material flow).
  • the gas that is introduced into the cathode of the first SOEC stack can be introduced into the cathode of the first SOEC stack via a first countercurrent heat exchanger, preferably also via a second countercurrent heat exchanger, particularly preferably also via a first heating device, wherein gas is heated in the first countercurrent heat exchanger, the second countercurrent heat exchanger and/or the first heating device, preferably to a temperature of at least 800 °C.
  • a first countercurrent heat exchanger preferably also via a second countercurrent heat exchanger, particularly preferably also via a first heating device, wherein gas is heated in the first countercurrent heat exchanger, the second countercurrent heat exchanger and/or the first heating device, preferably to a temperature of at least 800 °C.
  • the first SOEC stack and/or the second SOEC stack can have a temperature of 700 °C to 900 °C, preferably 750 °C to 850 °C, in particular 800 °C.
  • a temperature in this range is advantageous for the partial production of oxygen and hydrogen from the water vapor and in order not to convert at least 20 vol.% of the water vapor into oxygen and hydrogen.
  • the oxygen can be discharged as exhaust gas from the anode of the first SOEC stack and/or from the anode of the second SOEC stack via a second countercurrent heat exchanger, optionally also via a third countercurrent heat exchanger, wherein the oxygen is cooled in the second and/or third countercurrent heat exchanger, wherein the countercurrent heat exchangers preferably each have a temperature of 100 K.
  • the advantage here is that the waste heat of the oxygen can be used to preheat the gas that is introduced into the cathode of the first SOEC stack and/or can be used to preheat the additional water vapor that is additionally introduced into the burner.
  • the mixture containing or consisting of hydrogen and unreacted water vapor may be supplied to the burner at a temperature from 700 to 900 °C, preferably 750 °C to 850 °C, in particular 800 °C.
  • additional air can be supplied to the burner at a temperature of 20 °C to 30 °C.
  • the material flow of the additional air can be approximately 33% of the material flow of the reactant gas mixture that is to be (or is) provided by the process (standardized material flow).
  • the material flow of the additional steam can be approximately 83% of the material flow of the reactant gas mixture that is to be (or is) provided by the process (standardized material flow).
  • the additional steam (which has a temperature in the range of 100 °C to 150 °C) can be supplied to the burner via a fourth countercurrent heat exchanger, particularly preferably also a third countercurrent heat exchanger, in particular also via a second heating device, wherein the additional steam is heated in the fourth countercurrent heat exchanger, the third countercurrent heat exchanger and/or the second heating device, particularly preferably from a temperature of 100 °C to a temperature in the range of >100 °C to 150 °C.
  • a fourth countercurrent heat exchanger particularly preferably also a third countercurrent heat exchanger, in particular also via a second heating device, wherein the additional steam is heated in the fourth countercurrent heat exchanger, the third countercurrent heat exchanger and/or the second heating device, particularly preferably from a temperature of 100 °C to a temperature in the range of >100 °C to 150 °C.
  • the gas from the burner which is introduced into the cathode of the second SOEC stack can have a temperature in the range of 700 to 900 °C, preferably 750 °C to 850 °C, in particular 800 °C.
  • the discharge of the mixture containing or consisting of hydrogen, nitrogen and at least 20 vol.% water vapor, in relation to the total volume of the gas, from the cathode of the second SOEC stack can be carried out via a first
  • the heat exchange can be carried out via a first countercurrent heat exchanger, optionally also via a fourth countercurrent heat exchanger, the mixture being cooled in the first and/or fourth countercurrent heat exchanger, the countercurrent heat exchangers preferably each having a temperature of 100 K.
  • a portion of the mixture discharged from the cathode of the second SOEC stack (in particular its proportion of hydrogen and nitrogen) can be fed back into the cathode of the first SOEC stack, preferably via a first countercurrent heat exchanger, particularly preferably also via a second countercurrent heat exchanger, very particularly preferably also via a first heating device, wherein the mixture is heated in the first countercurrent heat exchanger, the second countercurrent heat exchanger and/or the first heating device, preferably to a temperature of at least 800 °C.
  • This procedure ensures a reducing atmosphere at the inlet of the first SOEC stack, which may be technically necessary to prevent oxidation of the first SOEC stack. Without recirculation, an additional supply of hydrogen may be necessary.
  • a mixture of hydrogen, nitrogen and ammonia that has been discharged from a Haber-Bosch cycle can be fed to the anode of the first SOEC stack, preferably via a third heating device, wherein the mixture of hydrogen, nitrogen and ammonia is heated in the third heating device, preferably to a temperature of > 750 °C.
  • the chemically bound energy of the purge current of the Haber-Bosch cycle is converted into thermal energy within the first SOEC stack.
  • an anode depolarization takes place, which increases the electrical efficiency of the electrolysis.
  • a mixture of hydrogen, nitrogen and ammonia which has been discharged from a Haber-Bosch cycle, can be fed to the anode of the second SOEC stack, preferably via a fourth Heating device, wherein the mixture of hydrogen, nitrogen and ammonia is heated in the fourth heating device, preferably to a temperature of > 750 °C.
  • the chemically bound energy of the purge current of the Haber-Bosch cycle is converted into thermal energy within the second SOEC stack.
  • an anode depolarization takes place, which increases the electrical efficiency of the electrolysis.
  • the material flow of the mixture of hydrogen, nitrogen and ammonia can be approximately 5.5% of the material flow of the reactant gas mixture that is to be provided (or is provided) by the process (standardized material flow).
  • the material flow of the exhaust gas (oxygen) can be approximately 47% of the material flow of the reactant gas mixture that is to be provided (or is provided) by the process (standardized material flow) and the material flow of water (which exits the cooling device) can be approximately 26.5% of the material flow of the reactant gas mixture that is to be provided (or is provided) by the process (standardized material flow).
  • a system for producing a reactant gas mixture containing or consisting of hydrogen and nitrogen comprising a) a first SOEC stack, which has an anode and a cathode and is configured to produce oxygen and hydrogen partially from water vapor and to separate them spatially and not to convert at least 20 vol. % of the water vapor, in relation to a total volume of the water vapor, into oxygen and hydrogen; b) a burner, which is configured to produce a gas from a mixture discharged from the first SOEC stack and additional air and additional water vapor, which contains or consists of water vapor, nitrogen and at least 5 vol.
  • a second SOEC stack which has an anode and a cathode and is configured to produce oxygen and hydrogen partially from water vapor to produce and spatially separate them and not convert at least 20 vol.% of the water vapor, in relation to a total volume of the water vapor, into oxygen and hydrogen; d) a cooling device that is configured to condense water from a mixture that is discharged from the second SOEC stack and to produce a reactant gas that contains or consists of hydrogen and nitrogen; wherein the system contains no more than two SOEC stacks, wherein the system is configured, optionally controlled via a control unit of the system, to introduce a gas that contains or consists of water vapor, but not air, into the cathode of the first SOEC stack,
  • the plant has the advantage that it can be used to produce a reactant gas mixture containing or consisting of hydrogen and nitrogen in a compact space (i.e. in a compact design) in a more energy-efficient, more cost-effective and less error-prone manner (i.e. more economical and ecological).
  • the system is configured (optionally controlled via a control unit of the system) to operate the first SOEC stack and/or second SOEC stack exothermically.
  • the system can be configured to feed the gas containing or consisting of water vapor, but not air, at a temperature of >800 °C into the cathode of the first SOEC stack.
  • the gas may have originated from a mixture of water and steam that was heated to such an extent that the water contained in it completely evaporated into steam.
  • the system can be configured to introduce the gas, which contains or consists of water vapor but not air, into the cathode of the first SOEC stack with a material flow that amounts to approximately 17.5% of the material flow of a reactant gas mixture that is to be provided (or is provided) with the system.
  • the system can be configured to introduce the gas, which contains or consists of water vapor but not air, into the cathode of the first SOEC stack via a first countercurrent heat exchanger, preferably also via a second countercurrent heat exchanger, particularly preferably also via a first heating device, of the system, wherein the first countercurrent heat exchanger, the second countercurrent heat exchanger and/or the first heating device are configured to heat the gas, preferably to a temperature of at least 800 °C.
  • the first SOEC stack and/or the second SOEC stack of the system can be configured to have a temperature of 700 °C to 900 °C, preferably 750 °C to 850 °C, in particular 800 °C.
  • the system can be configured to discharge the oxygen from the anode of the first SOEC stack and/or from the anode of the second SOEC stack as exhaust gas via a second countercurrent heat exchanger, optionally also via the third countercurrent heat exchanger, of the system, wherein the second countercurrent heat exchanger and/or third countercurrent heat exchanger is configured to cool the oxygen, wherein the countercurrent heat exchangers preferably each have a temperature of 100 K.
  • the system can be configured to supply the mixture from the first SOEC stack to the burner at a temperature of 700 to 900 °C, preferably 750 °C to 850 °C, in particular 800 °C. Furthermore, the system can be configured to supply the burner with additional air at a temperature of 20 °C to 30 °C.
  • the system can be configured to supply the additional air to the burner with a material flow that is approximately 33% of the material flow of a reactant gas mixture that is to be provided (or is provided) by the system.
  • the system can be configured to supply the additional steam (i.e. the steam having a temperature in the range of 100 °C to 150 °C) to the burner with a material flow that is approximately 83% of the material flow of a reactant gas mixture that is to be provided (or is provided) by the system.
  • the additional steam i.e. the steam having a temperature in the range of 100 °C to 150 °C
  • the system can be configured to supply the additional water vapor (i.e. the water vapor having a temperature in the range of 100 °C to 150 °C) to the burner via a fourth countercurrent heat exchanger, particularly preferably also via a third countercurrent heat exchanger, in particular also via a second heating device, wherein the fourth countercurrent heat exchanger, the third countercurrent heat exchanger and/or the second heating device are configured to heat a mixture containing water and water vapor such that water contained in the mixture completely evaporates to water vapor, particularly preferably is heated to a temperature of >100 °C to 150 °C.
  • a fourth countercurrent heat exchanger particularly preferably also via a third countercurrent heat exchanger, in particular also via a second heating device, wherein the fourth countercurrent heat exchanger, the third countercurrent heat exchanger and/or the second heating device are configured to heat a mixture containing water and water vapor such that water contained in the mixture completely evaporates to water vapor, particularly preferably is heated to a temperature of >100 °C to 150
  • the system can be configured to introduce the gas from the burner into the cathode of the second SOEC stack at a temperature in the range of 700 to 900 °C, preferably 750 °C to 850 °C, in particular 800 °C.
  • the system can be configured to discharge the mixture containing or consisting of hydrogen, nitrogen and water vapor from the cathode of the second SOEC stack via a first countercurrent heat exchanger, optionally also via a fourth countercurrent heat exchanger, of the system, wherein the first countercurrent heat exchanger and/or fourth countercurrent heat exchanger are preferably configured to cool the mixture, wherein the Counterflow heat exchangers preferably have a temperature of 100 K each.
  • the system can be configured to conduct a portion of the hydrogen and nitrogen discharged from the cathode of the second SOEC stack back into the cathode of the first SOEC stack, preferably via a first countercurrent heat exchanger, particularly preferably also via a second countercurrent heat exchanger, most preferably also via a first heating device of the system, wherein the first countercurrent heat exchanger, the second countercurrent heat exchanger and/or the first heating device are configured to heat the hydrogen and nitrogen, preferably to a temperature of at least 800 °C.
  • the system may be configured to supply a mixture of hydrogen, nitrogen and ammonia, which has been discharged from a Haber-Bosch cycle, to the anode of the first SOEC stack, preferably via a third heating device of the system, wherein the third heating device is configured to heat the mixture of hydrogen, nitrogen and ammonia, preferably to a temperature of > 750 °C.
  • the system can be configured to supply a mixture of hydrogen, nitrogen and ammonia, which has been discharged from a Haber-Bosch cycle, to the anode of the second SOEC stack, preferably via a fourth heating device of the system, wherein the fourth heating device of the system is configured to heat the mixture of hydrogen, nitrogen and ammonia, preferably to a temperature of > 750 °C.
  • the system is particularly configured to carry out the method according to the invention.
  • Figure 1 shows a flow diagram of a process known in the prior art for electrolysis-based reactant gas production and reactant gas purification with separate provision of H2 and N2 for the downstream synthesis of NH3.
  • the downstream synthesis of NH3 is no longer shown.
  • Figure 2 shows a flow diagram of a method according to the invention for producing a reactant gas mixture containing or consisting of hydrogen and nitrogen.
  • a gas which contains or consists of water vapor 1 but no air is introduced into a cathode of a first SOEC stack 2, which has an anode and a cathode, wherein in the first SOEC stack 2 oxygen and hydrogen are partially produced from the water vapor 1 and oxygen and hydrogen are spatially separated, wherein at least 20 vol.% of the water vapor, in relation to a total volume of the water vapor, is not converted to oxygen and hydrogen.
  • Oxygen 3 is discharged from the anode of the first SOEC stack 2 as exhaust gas.
  • a mixture 4 containing or consisting of hydrogen and unreacted water vapor is introduced from the cathode of the first SOEC stack 2 into a burner 5, wherein air 6 and additional water vapor 7 are additionally introduced into the burner 5, wherein the additional water vapor 7 has a temperature in the range from 100 °C to 150 °C.
  • the mixture 4, the air 6 and the additional water vapor 7 are converted into a gas 8 which contains or consists of water vapor, nitrogen and at least 5 vol. % hydrogen, in relation to the total volume of the gas.
  • This gas 8 is introduced from the burner 5 into a cathode of a second SOEC stack 9, which has an anode and a cathode, wherein in the second SOEC stack 9 oxygen and hydrogen are produced from the water vapor of the gas 8 and oxygen and hydrogen are spatially separated.
  • the oxygen 10 is discharged as exhaust gas from the anode of the second SOEC stack 9 and a mixture 11 which contains or consists of hydrogen, nitrogen and unreacted water vapor is discharged from the cathode of the second SOEC stack 9.
  • the mixture 11 is introduced into a cooling device 20, wherein water vapor condenses to water in the cooling device 20 and the condensed water is separated from the mixture, whereby a reactant gas mixture containing or consisting of hydrogen and nitrogen is formed.
  • Figure 2 also shows the arrangement and use the first countercurrent heat exchanger 12, the second countercurrent heat exchanger 13, the third countercurrent heat exchanger 14 and the fourth countercurrent heat exchanger 15 are illustrated. Furthermore, the arrangement and use of the first heating device 16, the second heating device 17, the third heating device 18 and the fourth heating device 19 are shown. Apart from that, the optional embodiment is apparent in which a mixture 21 of hydrogen, nitrogen and ammonia, which was discharged from a Haber-Bosch cycle process, is fed to the anode of the first SOEC stack 2 via the third heating device 18 and is fed to the anode of the second SEOC stack 9 via a fourth heating device 19.
  • Figure 3 shows an evaluation-based comparison of the specific energy requirement (E), the investment costs (TCI) and the production costs (TPC) between the process according to the invention, which only requires two SOEC stacks, and a known prior art process that uses eight SOEC stacks (see WO 2019/072608 Al) for the case of production of an amount of hydrogen and nitrogen that allows a production capacity of 1000 tNHs/day.
  • the evaluation included both a process simulation and a profitability calculation for a so-called "2050 scenario”.
  • the methodology used to assess the profitability is described in detail in Herz, G. et al. (Economic assessment of Power-to-Liquid processes - Influence of electrolysis technology and operating conditions, Applied Energy, Vol. 292, 116655) and in Jacobasch, E.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)

Abstract

L'invention concerne un procédé et une installation pour produire un mélange de gaz de départ contenant ou étant constitué d'hydrogène et d'azote. Le procédé et l'installation sont caractésisés en ce que l'on n'utilise qu'un maximum de deux piles de cellules d'électrolyse à oxyde solide (en anglais : solid oxide electrolysis cell stack = SOEC stack) montées l'une après l'autre, que l'on n'alimente pas la première pile SOEC en air et que l'on alimente un brûleur situé entre les deux piles SOEC en air d'une part et en vapeur d'eau d'autre part, à une température comprise entre 100 °C et 150 °C. Le brûleur est équipé d'un système d'alimentation en vapeur d'eau. Ce procédé et cette installation permettent de produire un mélange de gaz de départ contenant ou étant constitué d'hydrogène et d'azote dans un espace réduit et d'une manière plus efficace sur le plan énergétique et plus économique, tout en minimisant en outre le risque de temps d'arrêt.
PCT/EP2023/083533 2022-12-08 2023-11-29 Procédé et installation pour produire un mélange de gaz de départ contenant ou étant constitué d'hydrogène et d'azote WO2024120928A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102022213277.7A DE102022213277B3 (de) 2022-12-08 2022-12-08 Verfahren und Anlage zur Herstellung eines Eduktgasgemisches enthaltend oder bestehend aus Wasserstoff und Stickstoff
DE102022213277.7 2022-12-08

Publications (1)

Publication Number Publication Date
WO2024120928A1 true WO2024120928A1 (fr) 2024-06-13

Family

ID=89030001

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2023/083533 WO2024120928A1 (fr) 2022-12-08 2023-11-29 Procédé et installation pour produire un mélange de gaz de départ contenant ou étant constitué d'hydrogène et d'azote

Country Status (2)

Country Link
DE (1) DE102022213277B3 (fr)
WO (1) WO2024120928A1 (fr)

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3054932A1 (fr) * 2016-08-03 2018-02-09 Commissariat A L'energie Atomique Et Aux Energies Alternatives Systeme de regulation de temperature et de pression d'un electrolyseur a haute temperature (soec) fonctionnant de maniere reversible en pile a combustible (sofc)
WO2019072608A1 (fr) 2017-10-11 2019-04-18 Haldor Topsøe A/S Procédé de génération de gaz de synthèse pour la production d'ammoniac
EP3978651A1 (fr) * 2019-05-27 2022-04-06 Panasonic Intellectual Property Management Co., Ltd. Dispositif électrochimique et procédé de génération d'hydrogène

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT368749B (de) 1981-02-25 1982-11-10 Bbc Brown Boveri & Cie Verfahren zur kontinuierlichen herstellung von stickoxyd (no) und vorrichtung zur durchfuehrung des verfahrens
DE102016213360A1 (de) 2016-07-21 2018-01-25 Thyssenkrupp Ag Verfahren zur elektrochemischen Herstellung von Ammoniak

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR3054932A1 (fr) * 2016-08-03 2018-02-09 Commissariat A L'energie Atomique Et Aux Energies Alternatives Systeme de regulation de temperature et de pression d'un electrolyseur a haute temperature (soec) fonctionnant de maniere reversible en pile a combustible (sofc)
WO2019072608A1 (fr) 2017-10-11 2019-04-18 Haldor Topsøe A/S Procédé de génération de gaz de synthèse pour la production d'ammoniac
EP3978651A1 (fr) * 2019-05-27 2022-04-06 Panasonic Intellectual Property Management Co., Ltd. Dispositif électrochimique et procédé de génération d'hydrogène

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
HERZ, G. ET AL.: "Economic assessment of Power-to-Liquid processes - Influence of electrolysis technology and operating conditions", APPLIED ENERGY, vol. 292, pages 116655
JACOBASCH, E. ET AL.: "Economic evaluation of low-carbon steelmaking via coupling of electrolysis and direct reduction", JOURNAL OF CLEANER PRODUCTION, vol. 328, pages 129502

Also Published As

Publication number Publication date
DE102022213277B3 (de) 2024-01-04

Similar Documents

Publication Publication Date Title
EP3158111B1 (fr) Procédé d'électrolyse et système d'électrolyse à fluides de balayage remis en circulation
EP3472370B1 (fr) Production de gaz de synthèse à partir de co2 et h2o dans une co-électrolyse
DE4032993C1 (fr)
DE69917117T2 (de) Festelektrolyt-Brennstoffzellenstromversorgungssystem
EP3491172B1 (fr) Procédé et installaton de production de méthane
EP0704109B1 (fr) Installation de piles a combustible a haute temperature
EP4097045A1 (fr) Méthode et installation de production d'hydrogène
WO1992000614A1 (fr) Centrale electrique a piles a combustible
WO2018228642A1 (fr) Procédé et système pour éviter et/ou réduire la quantité de suie
DE69721072T2 (de) Verfahren zur durchführung von katalytische oder nichtkatalytische verfahren, mit einem mit sauerstoff angereichertem reaktant
WO2024120928A1 (fr) Procédé et installation pour produire un mélange de gaz de départ contenant ou étant constitué d'hydrogène et d'azote
EP0490925B1 (fr) Installation pour produire de l'energie electrique
EP2598618B1 (fr) Procédé de production de gaz naturel de substitution
DE102005025345A1 (de) Kraftwerk mit CO2-Heißgasrückführung sowie Verfahren zum Betreiben desselben
DE102019128882B3 (de) Verfahren zur prozessintegrierten Sauerstoff-Versorgung eines Wasserstoff-Kreislaufmotors mit Kreislaufführung eines Edelgases
DE102007018311A1 (de) Zweistufiger Reformer und Verfahren zum Betreiben eines Reformers
WO2024032928A1 (fr) Méthode et système d'obtention d'un produit contenant de l'hydrogène à l'aide d'ammoniac
BE1030199B1 (de) Ammoniaksynthese und Harnstoffsynthese mit reduziertem CO2-Fußabdruck
BE1030221B1 (de) Verfahren und Anlage zur Herstellung von Wasserstoff aus Ammoniak
BE1030201B1 (de) Ammoniaksynthese und Harnstoffsynthese mit reduziertem CO2-Fußabdruck
BE1030273B1 (de) Elektrochemische und chemische Synthese von Ammoniak
WO2024074221A1 (fr) Procédé et système de production d'un produit d'hydrogène
DE102020109016B4 (de) Verfahren und Vorrichtung zur Synthese von Ammoniak
EP4324787A1 (fr) Procédé et installation d'obtention d'au moins un produit selon le procédé
EP0300151B2 (fr) Procédé de préparation d'ammoniac à partir de gaz naturel