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EP4123057A1 - Vidange de liquide optimisée des électrolyseurs à membrane - Google Patents

Vidange de liquide optimisée des électrolyseurs à membrane Download PDF

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Publication number
EP4123057A1
EP4123057A1 EP21186388.1A EP21186388A EP4123057A1 EP 4123057 A1 EP4123057 A1 EP 4123057A1 EP 21186388 A EP21186388 A EP 21186388A EP 4123057 A1 EP4123057 A1 EP 4123057A1
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EP
European Patent Office
Prior art keywords
gas
liquid
electrolyzers
electrolysers
outlet
Prior art date
Legal status (The legal status 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 status listed.)
Withdrawn
Application number
EP21186388.1A
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German (de)
English (en)
Inventor
Thorsten Leidig
Marcel Obermeier
Torsten Kern
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Covestro Deutschland AG
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Covestro Deutschland AG
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 Covestro Deutschland AG filed Critical Covestro Deutschland AG
Priority to EP21186388.1A priority Critical patent/EP4123057A1/fr
Priority to EP22751360.3A priority patent/EP4373996A1/fr
Priority to PCT/EP2022/069970 priority patent/WO2023001723A1/fr
Priority to JP2024502610A priority patent/JP2024527791A/ja
Priority to CN202280047082.8A priority patent/CN117616153A/zh
Priority to US18/579,653 priority patent/US20240328002A1/en
Publication of EP4123057A1 publication Critical patent/EP4123057A1/fr
Withdrawn legal-status Critical Current

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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
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • 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
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • C25B1/46—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in diaphragm cells
    • 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
    • C25B11/02—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form
    • C25B11/03—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form perforated or foraminous
    • C25B11/031—Porous electrodes
    • C25B11/032—Gas diffusion electrodes
    • 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
    • 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
    • C25B3/00—Electrolytic production of organic compounds
    • C25B3/20—Processes
    • C25B3/25—Reduction
    • C25B3/26—Reduction of carbon dioxide
    • 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
    • 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
    • C25B9/70—Assemblies comprising two or more cells

Definitions

  • the invention relates to the provision of electrolysis devices with membrane electrolyzers with an optimized liquid flow, and a method for operating these electrolysis devices.
  • Electrolysis processes for the production of basic chemicals have to be developed for production on a large industrial scale (several 1000 t/a). Large-area electrolytic cells and electrolyzers with a large number of electrolytic cells are necessary in order to produce industrial quantities of product using electrolysis methods.
  • electrolytic cells with an electrode area of more than 2m 2 per electrolytic cell are usually used.
  • the electrolysis cells are combined in groups of up to 100 in an electrolysis frame.
  • Several racks then form an electrolyser.
  • the capacity of an industrial electrolyser, for example for chlorine production, is currently up to 30,000 t/a of chlorine and the respective equivalents of caustic soda or hydrogen.
  • At least one of the electrode half-reactions liberates a gaseous product, such as oxygen and hydrogen in water electrolysis, or chlorine and optionally hydrogen in chlor-alkali electrolysis.
  • a gaseous product such as oxygen and hydrogen in water electrolysis, or chlorine and optionally hydrogen in chlor-alkali electrolysis.
  • This formation of gas often results in a pressure difference between the operating pressure of the electrolyzer and the operating pressure of the liquid discharge line from the electrolyzer.
  • the products chlorine, aqueous alkali metal hydroxide solution (lye) and hydrogen are produced by electrolysis of an aqueous alkali metal salt solution.
  • the reaction equation for the production of sodium hydroxide lye is given here as an example: 2NaCl + 2H2O ⁇ Cl2 + 2NaOH + H2
  • the pressure difference described above is also observed when operating electrolysers with gas diffusion electrodes, in which the operating pressure of the electrolyser is at least influenced by the reactant gas introduced or its residual gas removed (e.g. oxygen when operating an oxygen-consuming cathode or, for example, carbon dioxide when operating a CO 2 electrolysis with Gas diffusion electrode) is optionally influenced in combination with the product gas formed during the electrolysis.
  • the reactant gas introduced or its residual gas removed e.g. oxygen when operating an oxygen-consuming cathode or, for example, carbon dioxide when operating a CO 2 electrolysis with Gas diffusion electrode
  • electrolysis devices electrolysis devices
  • electrolyzers include, for example, in DE19641125 described, each in turn several individual electrolytic cells connected hydraulically in parallel, through which electric current flows in an electrical series connection (“bipolar electrolyzers”) or also in an electrical parallel connection (“monopolar electrolyzers”).
  • the supply of the electrolysers with the operating media e.g. brine for the anode side, lye for the cathode side
  • the removal of the products e.g. chlorine gas and depleted brine "anolyte” from the anode side and hydrogen and enriched lye "catholyte” from the cathode side
  • the electrolysers and piping systems in an electrolysis cell room can, for example Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Chlorins ", to be taken.
  • the electrolysers are usually operated at elevated temperature and elevated pressure, typical values are approx. 40 - 90 °C and an operating pressure of approximately atmospheric pressure to 200 - 500 mbar overpressure.
  • An operating overpressure in the electrolytic cell offers the advantage that the subsequent processing steps of the gaseous products, such as chlorine and hydrogen (condensation of moisture), run more easily, especially on the anolyte side of the electrolysers, and the subsequent compression has better starting conditions and intermediate compressors that may be required are not required be able.
  • the additional measures described below are necessary in order to achieve normal operation at increased pressure/temperature between a depressurized standstill and start-up and shut-down operation.
  • the operating media are usually fed to the electrolytic cells from below; the products leave the electrolytic cells in overflow.
  • the electrolytic cells are always filled with liquid when they are switched on or off, or with a liquid/gas mixture during normal operation due to the gases that are produced.
  • the electrolysers For commissioning, the electrolysers must be heated up from the ambient conditions (atmospheric pressure, room temperature) to the operating temperature and pressurized to the operating pressure, and for decommissioning they must be cooled down and expanded accordingly. Exemplary procedures for start-up and shut-down are described, for example, in the Handbook of Chlor-Alkali Technology, Chapter 13 "Plant Commissioning and Operation".
  • a common technical solution for these start-up processes is to connect the electrolysers to start-up circuits via separate start-up piping systems, so that individual electrolysers can be switched on or off independently of the others that are in operation.
  • a typical start-up process is as follows: An electrolyser is filled with the operating media via the separate start-up circuits. The operating media are then circulated and heated up until the target temperature for operation is reached. Now the circulation is stopped via the start-up circuit. The anode and cathode sides of the electrolyser are pressurized (e.g. by adding nitrogen) to the operating pressures. After the connection to the operational piping systems has been opened and the circulation through these operational piping systems has been restarted, the electric current (hereinafter referred to as electrolysis current) can be switched on and the electrolyzer can thus be put into operation.
  • electrolysis current electric current
  • a typical decommissioning process runs the other way around, analogously to commissioning: After the electrolysis current has been switched off, the circulation via the operational piping systems is stopped and the electrolyser is separated from these operational piping systems. Anode and cathode spaces are relieved. It should be noted that the differential pressure between the anode and cathode chambers remains within the specified operating parameters. The circulation is restarted via the start-up piping system and the electrolyser is cooled down.
  • an auxiliary rectifier is switched on when a certain temperature is reached during commissioning low polarization current (order of magnitude: a few 10 A), which protects the electrode coating from damage; when decommissioning, it is switched off again when the temperature falls below a certain level and as soon as the anode chamber has been rinsed free of chlorine.
  • the polarization rectifier can remain switched on during the short interruption of the circulation when switching over from the start-up to the operating circuits during start-up or vice versa during decommissioning. Since the electrolytic cells of conventional design are filled with liquid during these processes, no damage can be caused by the polarization current.
  • an additional catalyst arranged on the electrode-side current distributor of the electrolysis cells is used.
  • GDE gas diffusion electrode
  • oxygen is used as the educt gas
  • the gas diffusion electrode is also referred to as an oxygen-depleting cathode (SVK) or oxygen depolarized cathode (ODC).
  • SVK oxygen-depleting cathode
  • ODC oxygen depolarized cathode
  • This is used, for example, in chlor-alkali electrolysis, whereby lye (OH - ) is produced instead of hydrogen (H 2 ) in a modified cathode reaction with the addition of oxygen.
  • This altered cathode reaction is associated with a lower electrolysis voltage and corresponding energy savings.
  • the following reaction equation results for the example of the production of sodium hydroxide lye: 4NaCl + O2 + 2H2O ⁇ 2Cl2 + 4NaOH
  • a gas diffusion electrode is described below as an example for chlor-alkali electrolysis.
  • an oxygen-consuming cathode is used as a gas diffusion electrode.
  • the oxygen supply to the electrolysers which is necessary to maintain the oxygen consumption reaction, can be carried out by simply flowing through the electrolytic cells, as for example in DE 102013011298 A described or contain an additional recycling step as in DE 10149779 A intended.
  • this is done in the context of a chlor-alkali electrolysis, as for example in the published application EP 2746429 A described in such a way that the alkali metal hydroxide lye trickles down as a liquid film in front of the catalyst layer and runs out of the bottom of the electrolytic cell, while the oxygen gas is introduced from the back of the catalyst layer.
  • the volume of liquid on the cathode side of the electrolytic cell is very small compared to conventional chlor-alkali membrane electrolysis and, since the liquid no longer drains via an overflow, in contrast to conventional electrolysis, but directly through an outlet at the bottom of the electrolytic cell, the If the liquid circulation is interrupted, the liquid content drains out of the cells within a very short time.
  • a polarization current applied to protect the electrode coating and the catalyst of the oxygen-consuming cathode during startup/shutdown would have to be switched off immediately if the liquid circulation is interrupted, e.g. to avoid short circuits in an electrolytic cell that has run dry on the cathode side.
  • the electrolysers are connected in parallel to the operating and start-up pipeline systems, analogously to conventional electrolysis technology.
  • the electrolysers of said electrolysis device can be operated with conventional electrodes. It is important that during operation the operating pressure of at least one liquid discharge is set lower than the operating pressure of the electrolysers. It has been found to be particularly suitable according to the invention if the electrolysis device operated by the method is operated on the anode side and/or cathode side with gas diffusion electrodes and a gas supply provided for this purpose.
  • the operated electrolysis device contains several electrolyzers selected from membrane electrolyzers with gas diffusion electrodes, in particular with oxygen-consuming cathodes, these electrolyzers at least having a gas supply on the gas diffusion electrode side, a liquid supply on the gas diffusion electrode side as liquid supply, a residual gas discharge on the gas diffusion electrode as gas discharge and a liquid discharge on the gas diffusion electrode side are connected to each other as a liquid drain.
  • the electrolyzers are selected from alkali metal chloride membrane electrolyzers with an oxygen-consuming cathode as the gas diffusion electrode.
  • a suitable alkali metal chloride that can be used for this embodiment is, for example, at least one alkali metal chloride selected from lithium chloride, sodium chloride and potassium chloride, sodium chloride being preferred.
  • the liquid circulation on the electrode side preferably the gas diffusion electrode side
  • the gas pressure on the electrode side preferably the gas diffusion electrode side
  • the liquid level in the leg of the pipeline siphon facing the electrolyte outlet of the electrolyser adjusts itself automatically to the changed operating pressure of the electrolyser if the drain side of the siphon drains into a piping system with a lower operating pressure.
  • the operating pressure on the electrode side, preferably the gas diffusion electrode side, of the electrolyzer is between atmospheric pressure and 1 bar overpressure, preferably in a range from 100 to 500 mbar overpressure.
  • the reference pressure for specifying an overpressure is, unless explicitly defined otherwise, the atmospheric pressure.
  • the operating pressure on the electrode side is the gas pressure in the gas space of the electrolytic cells on the electrode side, preferably on the gas diffusion electrode side.
  • gas and liquid are separated by their density difference in a pipeline which is connected to the discharge collecting line and is preferably routed vertically with a tolerance of ⁇ 15° and is discharged separately.
  • the gas flows upwards in the direction of the pressure control associated with each electrolyser; the liquid drains down into the pipeline siphon.
  • the operating pressure on the outlet side of the pipeline siphon is lower than the operating pressure on the inlet side of this pipeline siphon, preferably between atmospheric pressure and 100 mbar overpressure.
  • the operating pressure on the outlet side of the pipeline siphon is the gas pressure in the gas space of the system parts following the outlet side of the siphon.
  • the operating pressure on the inlet side of the pipeline siphon is the gas pressure in the outlet manifold of the electrolyzer, which is connected on the one hand to the gas space of the electrolysis cells and on the other hand to the inlet of the siphon.
  • the invention Expensive controls for automating a changeover from the start-up to the operating pipeline system are avoided by the invention.
  • a separate piping system for liquid and gas removal when starting up is no longer required.
  • the remaining necessary fittings can be dimensioned smaller because only the liquid flow at the pipeline siphon and no longer the two-phase flow of liquid and gas at the outlet header of the electrolyser has to be adjusted/shut off. Possible operating errors and consequential damage to the electrolyser with a manual switchover at the process header are eliminated.
  • the liquid is preferably removed in each operating mode of the electrolysis device according to step a. of the method according to the invention, in particular when starting up, shutting down and during operation of the electrolysis device.
  • a "fluid connection” to be a connection between at least two parts of a plant, through which a substance, which can be present in any physical state, can be transported as a material flow from one part of the plant (e.g. pipe siphon) to another part of the plant (e.g. residual gas discharge), for example a pipe .
  • the electrolysis device has gas diffusion electrodes on the anode side and/or on the cathode side, particularly preferably on the cathode side, with at least one outflow manifold on the gas diffusion electrode side being present in each electrolyzer, which is in fluid communication with the gas space and the liquid on the gas diffusion electrode side, and which branches into at least one gas discharge line on the gas diffusion electrode side with a control valve and at least one liquid discharge line on the gas diffusion electrode side with a pipeline siphon.
  • This Branching can be implemented very particularly preferably by a pipeline that is routed perpendicularly with a tolerance of ⁇ 15°.
  • the electrolyzers of the electrolysis device each have a device for pressure regulation, which regulates the operating pressure on the inlet side of the pipeline siphon via the individual control valve of the gas discharge line, preferably on the gas diffusion electrode side, in such a way that a There is overpressure, preferably so that the operating pressure on the outlet side of the pipeline siphon is lower than the operating pressure on the inlet side of the pipeline siphon, preferably between atmospheric pressure and 100 mbar overpressure.
  • the necessary dimensioning of the pipeline siphon can be determined without further ado by a person skilled in the art for use according to the invention.
  • the height of the pipeline siphon results from the maximum pressure difference between the outlet side of the pipeline siphon, where the pressure is preferably between 0 mbar and 100 mbar overpressure, and the inlet side of the pipeline siphon, where the operating pressure is preferably between 0 mbar and 1 bar overpressure is between 0 mbar and 500 mbar overpressure, as well as the minimum density of the circulation liquid discharged via the pipe siphon on the electrode side.
  • the diameter of the siphon is characterized in that the pressure losses occurring in the siphon can be neglected.
  • Another object of the invention is the use of a pipeline siphon on the electrode side, preferably on the gas diffusion electrode side, liquid outlet of membrane electrolyzers of an electrolyzer containing several electrolyzers in the form of membrane electrolyzers (preferably with gas diffusion electrodes, in particular with oxygen-consuming cathodes), with at least each electrolyzer has at least one liquid outlet and at least one gas outlet on the anode side, and at least one liquid outlet and at least one gas outlet on the cathode side, and the anode chambers of these electrolyzers are connected to one another and separately the cathode chambers of these electrolyzers are connected to one another via at least one liquid inlet, one gas outlet and one liquid outlet are, to decouple the operating pressure of the electrolysers from the operating pressure of the liquid outlet side the piping system.
  • gas space of the pipeline siphon is in fluid communication with the gas outlet of the electrolysis device via a control valve that can be controlled.
  • the electrolyzers have at least one liquid outlet and at least one gas outlet each on the anode side, and separately on the cathode side at least one liquid outlet and at least one each a gas discharge line, and on the gas diffusion electrode side via a gas supply line, the anode chambers of these electrolyzers being connected to one another and separately the cathode chambers of these electrolyzers to one another being connected to one another at least via said gas inlet, via a liquid inlet, via a gas outlet and via a liquid outlet.
  • the operating pressure of at least one liquid discharge is lower than the operating pressure of the electrolyzers.
  • FIG. 2a illustrates an example of an electrolysis device according to the invention, which contains a number of n membrane electrolyzers shown as “electrolyzer 1" to “electrolyzer 2...n”, which are each equipped with a normal electrode (not shown), ie no gas diffusion electrode, on the anode side and cathode side.
  • a normal electrode not shown
  • ie no gas diffusion electrode on the anode side and cathode side.
  • the electrolyzers are further connected to one another at least via a liquid supply 2.2, gas discharge 2.4 and a liquid discharge 2.5.
  • the liquid discharge takes place on the cathode side of each electrolyzer via a pipeline siphon 2.14 for the liquid discharge-side decoupling of the operating pressure of the electrolyzers from the operating pressure of the subsequent pipeline system of the liquid discharge 2.5. Furthermore, the gas is discharged from all electrolyzers equipped with the aforementioned pipeline siphon 2.14 into the common gas outlet 2.4 via an individual control valve 2.16 provided for each individual electrolyzer. On the anode side, the electrolyzers are also connected to one another at least via a liquid inlet, gas outlet and liquid outlet (not shown).
  • Figure 2b shows an example of an electrolysis device within the meaning of the invention, which contains a number of n membrane electrolyzers shown as “electrolyzer 1" to "electrolyzer 2...n” with a gas diffusion electrode connected on the cathode side (not shown), the electrolyzers at least having the gas diffusion electrode side Gas supply 2.1, a gas diffusion electrode-side liquid supply 2.2, a gas diffusion electrode-side residual gas discharge 2.4 and a gas diffusion electrode-side liquid discharge 2.5 are connected to one another. Only two electrolysers have been shown for simplicity. For further simplification, in Fig.2b only the gas and liquid connections of the gas diffusion electrode side (ie the cathode side) are shown.
  • the liquid outflow of an electrolyzer on the gas diffusion electrode side takes place via a pipeline siphon 2.14 for decoupling the operating pressure of the electrolyzer from the operating pressure of the subsequent pipeline system 2.5 on the liquid outflow side. Furthermore, the gas discharge on the gas diffusion electrode side of all electrolysers equipped with the aforementioned pipeline siphon 2.14 takes place into the common gas diffusion electrode side residual gas discharge 2.4 via an individual control valve 2.16 provided for each individual electrolyser. On the anode side, the electrolyzers are also connected to one another at least via a liquid inlet, gas outlet and liquid outlet (not shown).
  • Fig.2a and 2 B drain side as in Fig.3 shown initially gas (product gas or residual gas) and liquid in the horizontally running discharge manifold 3.1 of the electrolyzer together in the direction of the further piping systems. Gas and liquid then separate due to their density difference in a subsequent branch with an almost vertical pipe run (preferably ⁇ 15°); Gas flows upwards through the discharge of residual gas 3.3 in the direction of the pressure control 2.16 assigned to each electrolyzer. The liquid is discharged downwards into the liquid discharge line 3.2.
  • electrolyzers electrolyzer 1, electrolyzer 2...n
  • electrolyzer 1 electrolyzer 1
  • electrolyzer 2...n electrolyzer 2
  • Fig.1 only two electrolysers shown.
  • up to 10 or more electrolysers were operated in parallel.
  • Fig.1 only the gas and liquid connections of the cathode side are shown.
  • the raw materials oxygen (1.1) and diluted caustic soda (1.2, 1.3) were distributed from the upstream plants to the electrolyzers via piping systems. On the liquid side, there were separate systems for normal operation (1.2) and start-up/shutdown (1.3), since the start-up/shutdown processes generally follow a pressure/temperature profile that differs from normal operation.
  • the operating pressure was generally controlled via a central pressure control for the exhaust gas (1.8).
  • the pipe system for liquid removal during normal operation was under the same operating pressure as the electrolysers.
  • the start-up/shutdown operation was generally carried out without pressure at atmospheric pressure.
  • valves (1.14, 1.15) arranged on the electrolyzer. Since gas and liquid were initially discharged through the same line in the outlet of the electrolysers, the gas and liquid were separated after the valves on the outlet side (1.14, 1.15) by pipes leading away upwards and downwards.
  • An electrolyser was switched from start-up to normal operation in analogy to conventional chlor-alkali electrolysis by first stopping the liquid and gas circulation by closing the valves to the start-up/shutdown systems (1.11, 1.13, 1.15). The pressure was then raised to the operating pressure, e.g. via the gas supply 1.11 or an additional auxiliary gas supply. After that, the liquid and gas circulation on the operating systems (1.11, 1.12, 1.14) could be started again. The descent was carried out analogously in reverse order.
  • this mode of operation involves the risk of damage to the oxygen-depleting cathode.
  • the alternative automation with mechanically driven fittings would be expensive since it would be required separately for each electrolyser.
  • the products of the electrolysis process, the residual gas of the oxygen-depleted cathode reaction (2.4) and the caustic soda strengthened in the electrolyser (2.5) were collected in pipeline systems analogously to the product feed and discharged into the downstream plants.
  • the liquid could always drain freely in the direction of the draining pipeline system (3.4), regardless of the operating pressure that was set in each case.
  • the liquid level on the inlet side of the siphon was at the same level (3.5) as on the outlet side.
  • the liquid level in the inlet side of the siphon was lower in accordance with the ratio of operating pressure to liquid density (3.6). Intermediate states could occur freely when the operating pressure was increased from start-up to normal operation or vice versa when shutting down.
  • the height of the siphon had to be selected in such a way that no gas could penetrate through the lower end, even at the maximum possible operating pressure.
  • the further piping system (3.4) was dimensioned in such a way that the liquid can drain freely. Overpressure was avoided, as was underpressure, which could arise, for example, from lifting effects. It is advantageous to design the discharging line as a free level line or an additional ventilation (3.7) that avoids negative pressure.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
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  • Metallurgy (AREA)
  • Inorganic Chemistry (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
EP21186388.1A 2021-07-19 2021-07-19 Vidange de liquide optimisée des électrolyseurs à membrane Withdrawn EP4123057A1 (fr)

Priority Applications (6)

Application Number Priority Date Filing Date Title
EP21186388.1A EP4123057A1 (fr) 2021-07-19 2021-07-19 Vidange de liquide optimisée des électrolyseurs à membrane
EP22751360.3A EP4373996A1 (fr) 2021-07-19 2022-07-17 Évacuation optimisée de liquide provenant d'électrolyseurs à membrane
PCT/EP2022/069970 WO2023001723A1 (fr) 2021-07-19 2022-07-17 Évacuation optimisée de liquide provenant d'électrolyseurs à membrane
JP2024502610A JP2024527791A (ja) 2021-07-19 2022-07-17 膜電解槽からの最適な液体流出
CN202280047082.8A CN117616153A (zh) 2021-07-19 2022-07-17 膜电解槽的液体流出的优化
US18/579,653 US20240328002A1 (en) 2021-07-19 2022-07-17 Optimised liquid outflow from membrane electrolysers

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP21186388.1A EP4123057A1 (fr) 2021-07-19 2021-07-19 Vidange de liquide optimisée des électrolyseurs à membrane

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EP4123057A1 true EP4123057A1 (fr) 2023-01-25

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EP21186388.1A Withdrawn EP4123057A1 (fr) 2021-07-19 2021-07-19 Vidange de liquide optimisée des électrolyseurs à membrane
EP22751360.3A Pending EP4373996A1 (fr) 2021-07-19 2022-07-17 Évacuation optimisée de liquide provenant d'électrolyseurs à membrane

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US (1) US20240328002A1 (fr)
EP (2) EP4123057A1 (fr)
JP (1) JP2024527791A (fr)
CN (1) CN117616153A (fr)
WO (1) WO2023001723A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2025061916A1 (fr) * 2023-09-20 2025-03-27 Robert Bosch Gmbh Système d'électrolyse

Citations (8)

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