CN1829825A - Electrochemical cell - Google Patents
Electrochemical cell Download PDFInfo
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- CN1829825A CN1829825A CNA2004800214734A CN200480021473A CN1829825A CN 1829825 A CN1829825 A CN 1829825A CN A2004800214734 A CNA2004800214734 A CN A2004800214734A CN 200480021473 A CN200480021473 A CN 200480021473A CN 1829825 A CN1829825 A CN 1829825A
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- gap
- cell
- electrolytic solution
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- gas diffusion
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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
Abstract
The invention relates to an electrochemical cell (1) which consists at least of an anode half cell (2) having an anode (21), a cathode half cell (3) having a cathode (31) and an ion exchange membrane (4) arranged between the anode half cell (2) and the cathode half cell (3), wherein the anode (21) and/or the cathode (31) is a gas diffusion electrode and a gap (32) is arranged between the gas diffusion electrode (31) and the ion exchange membrane (4), and the half cell (2, 3) having the gas diffusion electrode (31) has an electrolyte feed pipe (33) and an electrolyte discharge pipe (34) and a gas inlet (35) and a gas outlet (36), characterized in that the electrolyte feed pipe (33) and the gap (32) are connected in a sealing manner.
Description
The present invention relates to a kind of electrochemical cell, it is at least by having the anodic anodic half-cell, have the cathode half-cell of negative electrode and be provided in anodic half-cell and cathode half-cell between ion-exchange membrane form, wherein anode and/or negative electrode are gas diffusion electrodes.The present invention relates to a kind of method that is used for aqueous solution of electrolytic alkali metallic chloride in addition.
A porous layer wherein is equipped with from WO-A 01/57290 known a kind of electrolyzer, in the gap between gas diffusion electrode and the ion-exchange membrane with gas diffusion electrode.Described electrolytic solution from top to bottom flows through this gap through porous layer under action of gravity.The porous layer of WO 01/57290 can be made of foam, wire screen etc.
In US 6 117 286, put down in writing the electrolyzer that is used for the electrolytic chlorination sodium solution equally, wherein had the water wetted material layer in the gap between gas diffusion electrode and ion-exchange membrane with gas diffusion electrode.The layer that this water wetted material is made preferably has vesicular structure, and it contains corrosion resistant metal or resin.Can use for example net, fabric or foam as vesicular structure.Electrolytic solution sodium hydroxide arrives the bottom of electrolyzer through this water wetted material sulfate layer flows downhill under action of gravity.
In addition by EP-A 1 033 419 known a kind of be used for the electrolytic chlorination sodium solution have the electrolyzer of gas diffusion electrode as negative electrode.(wherein electrolytic solution separates with gas compartment by gas diffusion electrode), described electrolytic solution was downward through the hydrophilic porous material that is provided in this cathode half-cell in cathode half-cell.Can consider metal, metal oxide or organic materials as porous material, as long as they are corrosion resistant.
Be that by the shortcoming with electrolyzer of gas diffusion electrode well known in the prior art because described porous material, the gap between gas diffusion electrode and the anion-exchange membrane can not be filled by electrolytic solution fully.In this gap, exist gas to form therein and the cumulative zone thus.No current circulation in this zone.Electric current only flows through the zone of being filled by electrolytic solution in the gap, makes the part have higher current density, causes higher electrolysis voltage.If gas is accumulated on ion-exchange membrane, ion-exchange membrane may damage owing to lacking electrolytic solution so.Porous layer has following shortcoming in addition, that is, in case gas appears in the vesicular structure, so only can therefrom leave on difficult ground again.Gas can accumulate in this porous layer, produces above-mentioned shortcoming thus.Gas from gas compartment also can enter this gap by gas diffusion electrode from gas compartment under operational condition.
Therefore task of the present invention is to provide a kind of electrolyzer of avoiding the shortcoming of prior art.
Theme of the present invention is a kind of electrochemical cell, its at least by have the anodic anodic half-cell, have the cathode half-cell of negative electrode and be provided in anodic half-cell and cathode half-cell between ion-exchange membrane form, wherein anode and/or negative electrode are gas diffusion electrodes, the gap is equipped with between gas diffusion electrode and ion-exchange membrane,, and the half-cell with gas diffusion electrode has electrolytic solution feed-pipe and electrolytic solution discharge tube and gas inlet and pneumatic outlet, it is characterized in that the electrolytic solution feed-pipe is connected with clearance seal.
In the operating process of electrochemical cell of the present invention, the electrolytic solution in the gap between gas diffusion electrode and the ion-exchange membrane flows through half-cell from top to down.This gap is filled by electrolytic solution fully thus.The remaining space of this half-cell is that gas compartment is filled with gas, and gas enters by the gas inlet and discharges by pneumatic outlet.According to the present invention, the electrolytic solution feed-pipe is connected with clearance seal.Avoided gas to enter in the gap through the electrolytic solution feed-pipe thus by gas compartment.Because being tightly connected between electrolytic solution feed-pipe and the gap, electrolytic solution can make electrolyte stream can the mode with free-falling not flow along gas diffusion electrode in the gap by pump delivery by this gap.The volumetric flow rate of electrolytic solution in gap of flowing through can be regulated by pump.Preferred this volumetric flow rate of regulating makes the flow velocity of electrolytic solution be lower than the flow velocity of free-falling.
Flow-guiding structure is equipped with in a preferred implementation, in this gap.This flow-guiding structure has been avoided electrolytic solution free-falling in the gap equally, makes flow velocity reduce with respect to the flow velocity of free-falling.Simultaneously because this flow-guiding structure also makes electrolytic solution can not accumulate in the gap.Select flow-guiding structure to make that the pressure-losses of statics of fluids liquid column is compensated in this gap.If be equipped with flow-guiding structure, flow-guiding structure can be born the function (that is, being reduced in the flow velocity in the gap) of pump fully so, and making does not need pump.But also can use the combination of pump and flow-guiding structure.
Described flow-guiding structure is made of thin plate, film etc., and it has opening so that electrolyte circulation.Flow-guiding structure is placed to being laterally (promptly vertical or inclination) with respect to electrolyte stream in the gap.Tabular flow-guiding structure preferably is inclined relative to horizontal, wherein its can be only axle tilt or two axles all tilt.If described flow-guiding structure tilts to install with respect to flowing to, it both can also can tilt to the gas diffusion electrode direction to the ion-exchange membrane direction so.Corresponding to the inclination around an axle, this axle is parallel to gas diffusion electrode or ion-exchange membrane and is horizontal alignment to the inclination of gas diffusion electrode or ion-exchange membrane direction.This flow-guiding structure can also tilt at the electrochemical cell width in addition.This inclination is corresponding to the inclination around an axle, and this axle orientation is perpendicular to gas diffusion electrode or ion-exchange membrane.This inclination can be 0-45 °, is preferably 3-15 °.
Because in electrochemical cell operation, often still have (promptly from the chamber of gas diffusion electrode back, the half-cell chamber of ion-exchange membrane dorsad) a small amount of gas, enter into the through-flow gap of electrolytic solution by gas diffusion electrode, from this gap, discharge so must guarantee gas.The content of gas is high more in electrolytic solution, and the resistance of electrolytic solution is high more.If there is flow-guiding structure in the gap, gas can upwards be overflowed or carried secretly downwards by electrolyte stream by the opening in flow-guiding structure so.The inclination of this flow-guiding structure especially impels bubble upwards to discharge.
Flow-guiding structure is set in addition makes its gentle on the one hand bulk diffusion electrode contact, and contact with ion-exchange membrane on the other hand.The electrolytic solution opening of guide frame of only flowing through thus.Flow-guiding structure can be connected with ion-exchange membrane with gas diffusion electrode regularly or removedly.Preferably this flow-guiding structure is clipped between gas diffusion electrode and the ion-exchange membrane.This flow-guiding structure is fixed in perpendicular (promptly being arranged essentially parallel to gas diffusion electrode and ion-exchange membrane) and is installed on the supporting structure in the gap in an especially preferred embodiment.This supporting structure is for example extended at the middle part in gap, makes this flow-guiding structure stretch to the direction of ion-exchange membrane on the one hand, and stretches to the direction of gas diffusion electrode on the other hand.This supporting structure for example is made of thin plastic bar, and this shank diameter is less than the gap width between gas diffusion electrode and the ion-exchange membrane.At the gas diffusion electrode length upper support structure form of plastic bar (for example with) thus quantity and the quantity of the flow-guiding structure material thickness that depends on flow-guiding structure because plastic bar is for example playing stable effect in the electrolyzer assembling.
Flow-guiding structure can be smooth.In order to be easy to that flow-guiding structure is clipped between gas diffusion electrode and the ion-exchange membrane, this flow-guiding structure can have for example Z type, L type, T type, double-T shaped or trapezoidal profile.This flow-guiding structure is knuckle or bending arbitrarily also.It preferably is made of the elastic plate of being wider than gap width.By being clipped between gas diffusion electrode and the ion-exchange membrane and effect by electrolyte stream in the gap makes this elastic plate be bent downwardly.Flow-guiding structure is bent downwardly then.But also can use the flow-guiding structure that is bent upwards.Flow-guiding structure through bending is favourable, because it has offset the manufacturing tolerance of electrochemical cell, this tolerance for example influences the width in gap.
Opening in the flow-guiding structure can have arbitrary shape, for example circle or dihedral.These stacked placements up and down of opening in stacked up and down flow-guiding structure, promptly opening is overlapping.Described electrolyte stream is substantially perpendicularly by this gap.But described opening also can be positioned opposite to each other, makes that electrolyte stream is not that the gap is crossed in rectilinear flow, but for example with broken line form or the back-shaped gap of flowing through.Reduced the formation of dead zone like this.
Flow-guiding structure can be prepared by alkaline-resisting liquid material, especially metal or the plastics by alkaline-resisting liquid.For example can use nickel or PTFE as material.
Select quantity and the number of openings and the cross-sectional area of flow-guiding structure, make the flow velocity of electrolytic solution less than the flow velocity of free-falling.In the electrolyte content of the electrolyzer height of for example 1.3m and for example 1801/h, can use 26 flow-guiding structures with 64 openings.Opening has for example diameter of 1mm.Perhaps, also can use 6 flow-guiding structures of 127 openings with 0.5mm diameter to this.Depend on throughput, can reach corresponding pressure compensation by the diameter of adjusting opening and the quantity of quantity and flow-guiding structure.
The electrolytic solution that flows downward in the gap does not allow to accumulate on the flow-guiding structure.Therefore must guarantee that for all flow-guiding structures the cross-sectional area summation size of all openings of flow-guiding structure is identical.This can obtain by changing open amount or cross-sectional area.
Do not rely on whether electrolytic solution flow through the gap by pump or whether flow-guiding structure exists or the two, (gap width for example for 3mm time) preferred electrolytic solution volume flow is 100-3001/h in the gap.The preferred maximum of volumetric flow rate is 5001/h.This flow velocity is preferably and is 1cm/s to the maximum.
With porous layer well known in the prior art, the advantage of flow-guiding structure is to have improved the bubble discharge that enters into the gap by gas diffusion electrode relatively.In addition, through the gap between gas diffusion electrode and the ion-exchange membrane, this thus gap is by the electrolytic solution completely filled by pump delivery for electrolytic solution.The vesicular structure that electrolytic solution passes through in the free-falling mode according to prior art often is not to be filled by electrolytic solution fully, it is characterized in that higher electrolysis voltage.
Can be used for various electrolysis processs according to electrochemical cell of the present invention, wherein at least one electrode is a gas diffusion electrode.Preferably gas diffusion electrode plays cathodic process, and especially preferably as oxygen diffusion cathode, the gas that wherein imports this electrochemical cell is for example air, oxygen-rich air or oxygen of oxygen-containing gas itself.
Battery of the present invention is preferred for the electrolysis of alkali metal halide aqueous solution, especially sodium chloride aqueous solution.
Under the situation of electrolytic sodium chloride aqueous solution, gas diffusion electrode is for example pressed surface construction: this gas diffusion electrode is made of conductive carrier and electrochemical activity coating at least.This conductive carrier preferably by metal, especially by net, fabric, grid, fabric, nonwoven fabric or the foam of nickel, silver or the preparation of silver plated nickel.The electrochemical activity coating preferably at least by catalyzer for example silver (I) oxide compound and tackiness agent for example polytetrafluoroethylene (PTFE) constitute.The electrochemical activity coating can be made of one deck or laminated coating.Can apply gas diffusion layers (for example the mixture by carbon and tetrafluoroethylene forms) to this base material in addition.
Can for example use the titanium electrode that applies with ruthenium-iridium oxide or ru oxide as anode.
Can use commercially available film as ion-exchange membrane, for example the Nafion NX2010 of Dupont company.
The electrolyzer that is suitable for electrolytic sodium chloride aqueous solution of the present invention has that the width order of magnitude is the gap of 3mm between gas diffusion electrode and ion-exchange membrane.Described flow-guiding structure is preferably prepared and is had the thickness of 0.1-0.5mm by the thin plate of PTFE or PVDF.
Described electrolytic solution feed-pipe is passage (a for example pipe), and it extends on the whole length of gas diffusion electrode.In this case electrolytic solution by the electrolytic solution feed-pipe of channel form can be equably in make progress gap between inflow gas diffusion electrode and the ion-exchange membrane of its whole length.Substitute this electrolytic solution feed-pipe that on the whole length of gas diffusion electrode, extends, charging also can be only in a zone for example in these gas diffusion electrode two ends first zone of an end carry out.By at the flow-guiding structure of an axle, play electrolytic solution equally distributed effect on the whole length in this gap in this case perpendicular to gas diffusion electrode or ion-exchange membrane inclination.
Another theme of the present invention is the method for electrolysis alkali metal halide aqueous solution in electrochemical cell, this electrochemical cell is at least by having the anodic anodic half-cell, have the cathode half-cell of negative electrode and be provided in anodic half-cell and cathode half-cell between ion-exchange membrane form, wherein anode and/or negative electrode are gas diffusion electrodes and are equipped with the gap between gas diffusion electrode and ion-exchange membranees, and this half-cell with gas diffusion electrode has electrolytic solution feed-pipe and electrolytic solution discharge tube and gas inlet and pneumatic outlet, it is characterized in that electrolytic solution from top to bottom flows through in the gap by pump, wherein this gap is by the electrolytic solution completely filled.
Following the present invention is elaborated with reference to accompanying drawing.
Fig. 1 is according to the cross sectional representation of first embodiment of electrochemical cell of the present invention, does not have guiding device in the gap between gas diffusion electrode and ion-exchange membrane in this embodiment.
Fig. 2 is according to the cross sectional representation of second embodiment of electrochemical cell of the present invention, has guiding device in the gap between gas diffusion electrode and ion-exchange membrane in this embodiment.
Described among Fig. 1 according to electrochemical cell 1 of the present invention, it is by the anodic half-cell 2 with anode 21 and have gas diffusion electrode 31 and constitute as the cathode half-cell 3 of negative electrode.Two half- cells 2,3 are separated from each other by ion-exchange membrane 4.Gas diffusion electrode 31 is separated by gap 32 with ion-exchange membrane 4.Sealing member 39 makes half-cell 3 and external isolation.Negatively charged ion half-cell 3 has electrolytic solution feed-pipe 33 and electrolytic solution discharge tube 34 and gas inlet 35 and pneumatic outlet 36.This electrolytic solution feed-pipe 33 is tightly connected with gap 32.Electrolytic solution through electrolytic solution feed-pipe 33 be fed in the half-cell 3 and in gap 32 to dirty, with after electrolytic solution discharge tube 34 discharge from half-cell 3.Gap 32 was filled by electrolytic solution fully in 1 operating period of electrolyzer.Gas is 35 gas compartments 37 that enter into half-cell 3 through the gas inlet, in gas compartment 37 to the upper reaches and go out 36 through gas and discharge from half-cell 3.Being tightly connected of electrolytic solution feed-pipe 33 and gap 32 makes that electrolytic solution can be by flow through gap 32 and regulate ideal electrolytic solution volume flow or ideal electrolyte flow rate thus in gap 32 of pump.Sealing connects must avoid gas to flow into the gap 32 from gas compartment 37.Completely filled electrolytic solution feed-pipe 33 for this reason.Select the size of balance openings 38, make the electrolytic solution of very low volumetric flow rate flow to gas compartment 37 through opening 38.Preferably flow into the volumetric flow rate of chamber, back less than 5% of total volumetric flow rate through opening 38.Simultaneously balance openings 38 makes gas to discharge, this gas 1 operating period of electrolyzer to enter gap 32 and upwards rise through gas diffusion electrode 31 from gas compartment 37 on a small quantity with bubble form.32 balance openings 38 through electrolytic solution feed-pipe 33 enter gas compartment 37 to gas from the gap by this way.
Compare with the embodiment that proposes among Fig. 1, the electrolyzer 1 in Fig. 2 also has flow-guiding structure 51,52,53,54 in gap 32 except being tightly connected of electrolytic solution opening for feed 33 and gap 32.With respect to the flow velocity of electrolytic solution free-falling, flow-guiding structure 51,52,53,54 has reduced the flow velocity of electrolytic solution in gap 32.Flow-guiding structure 51,52,53,54 allows the thin plate of the through-flow opening 56 of electrolytic solution to constitute by having.These flow-guiding structures are clipped between ion-exchange membrane 4 and the gas diffusion electrode 31 in the above-described embodiment.Flow-guiding structure 51 in gap 32 substantially in horizontal direction the flow direction of electrolytic solution (that is, transverse to) be provided with.Flow-guiding structure 53 can tilt equally (that is, at an angle to flow direction for example the direction of ion-exchange membrane 4 tilt) be provided with.Flow-guiding structure 53 V-shaped structures in another embodiment.Flow-guiding structure 54 is for being bent downwardly.
Claims (6)
1. electrochemical cell (1), it is at least by the anodic half-cell with anode (21) (2), have the cathode half-cell (3) of negative electrode (31) and be provided in anodic half-cell (2) and cathode half-cell (3) between ion-exchange membrane (4) form, wherein anode (21) and/or negative electrode (31) are gas diffusion electrodes and are equipped with gap (32) between gas diffusion electrode (31) and ion-exchange membranees (4), and this has the half-cell (2 of gas diffusion electrode (31), 3) have electrolytic solution feed-pipe (33) and electrolytic solution discharge tube (34) and gas inlet (35) and pneumatic outlet (36), it is characterized in that electrolytic solution feed-pipe (33) and gap (32) are tightly connected.
2. the electrochemical cell of claim 1 is characterized in that in gap (32) flow-guiding structure (51 being installed; 52; 53; 54).
3. claim 1 or 2 electrochemical cell is characterized in that described flow-guiding structure (51; 52; 53; 54) be clipped between gas diffusion electrode (31) and the ion-exchange membrane (4).
4. each electrochemical cell among the claim 1-3 is characterized in that flow-guiding structure (51; 52; 53; 54) be inclined relative to horizontal.
5. be used for method at electrochemical cell (1) electrolysis alkali metal halide aqueous solution, this electrochemical cell is at least by the anodic half-cell with anode (21) (2), have the cathode half-cell (3) of negative electrode (31) and be provided in anodic half-cell (2) and cathode half-cell (3) between ion-exchange membrane (4) form, wherein anode (21) and/or negative electrode (31) are gas diffusion electrodes and are equipped with gap (32) between gas diffusion electrode (31) and ion-exchange membranees (4), and this has the half-cell (2 of gas diffusion electrode (31), 3) have electrolytic solution feed-pipe (33) and electrolytic solution discharge tube (34) and gas inlet (35) and pneumatic outlet (36), it is characterized in that electrolytic solution from top to bottom flows through in gap (32) by pump, its intermediate gap (32) are by the electrolytic solution completely filled.
6. the method for claim 5 is characterized in that being equipped with flow-guiding structure (51 in described gap; 52; 53; 54).
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE10333853.5 | 2003-07-24 | ||
| DE10333853A DE10333853A1 (en) | 2003-07-24 | 2003-07-24 | Electrochemical cell |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1829825A true CN1829825A (en) | 2006-09-06 |
| CN100549239C CN100549239C (en) | 2009-10-14 |
Family
ID=34088814
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004800214734A Active CN100549239C (en) | 2003-07-24 | 2004-07-13 | Electrochemical cell |
Country Status (8)
| Country | Link |
|---|---|
| US (2) | US20050029116A1 (en) |
| EP (1) | EP1651799B1 (en) |
| JP (1) | JP4680901B2 (en) |
| CN (1) | CN100549239C (en) |
| DE (1) | DE10333853A1 (en) |
| HK (1) | HK1097885A1 (en) |
| TW (1) | TWI351447B (en) |
| WO (1) | WO2005012595A1 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107810291A (en) * | 2015-06-17 | 2018-03-16 | 西门子股份公司 | For synthesizing the electrochemical cell and technique of ammonia |
| CN108779560A (en) * | 2016-03-17 | 2018-11-09 | Hpnow爱普斯学会 | Electrochemical cell for the vapor-phase reactant in liquid environment |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ITMI20060726A1 (en) * | 2006-04-12 | 2007-10-13 | De Nora Elettrodi S P A | ELECTRIC DIFFUSION ELECTRODE FOR CELLS WITH ELECTROLYTE DISCHARGE |
| JP4198726B2 (en) * | 2006-09-06 | 2008-12-17 | クロリンエンジニアズ株式会社 | Ion exchange membrane electrolytic cell |
| DE102008011473A1 (en) * | 2008-02-27 | 2009-09-03 | Bayer Materialscience Ag | Process for the production of polycarbonate |
| DE102009004031A1 (en) * | 2009-01-08 | 2010-07-15 | Bayer Technology Services Gmbh | Structured gas diffusion electrode for electrolysis cells |
| US8273254B2 (en) | 2010-04-19 | 2012-09-25 | Watkins Manufacturing Corporation | Spa water sanitizing system |
| US8266736B2 (en) * | 2009-07-16 | 2012-09-18 | Watkins Manufacturing Corporation | Drop-in chlorinator for portable spas |
| US9478803B2 (en) * | 2011-06-27 | 2016-10-25 | Primus Power Corporation | Electrolyte flow configuration for a metal-halogen flow battery |
| JP2019510885A (en) | 2016-04-07 | 2019-04-18 | コベストロ、ドイチュラント、アクチエンゲゼルシャフトＣｏｖｅｓｔｒｏ Ｄｅｕｔｓｃｈｌａｎｄ Ａｇ | Bifunctional electrode and electrolysis device for chloralkali electrolysis |
| US11407661B2 (en) | 2017-07-17 | 2022-08-09 | Watkins Manufacturing Corporation | Chlorine generator system |
| EP3805429A1 (en) * | 2019-10-08 | 2021-04-14 | Covestro Deutschland AG | Method and electrolysis device for producing chlorine, carbon monoxide and hydrogen if applicable |
Family Cites Families (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2749861B2 (en) * | 1989-03-23 | 1998-05-13 | 三菱重工業株式会社 | Gas diffusion electrode |
| DE4306889C1 (en) * | 1993-03-05 | 1994-08-18 | Heraeus Elektrochemie | Electrode arrangement for gas-forming electrolytic processes in membrane cells and their use |
| DE19646950A1 (en) * | 1996-11-13 | 1998-05-14 | Bayer Ag | Electrochemical gas diffusion half cell |
| JP3553775B2 (en) * | 1997-10-16 | 2004-08-11 | ペルメレック電極株式会社 | Electrolyzer using gas diffusion electrode |
| WO2000011242A1 (en) * | 1998-08-25 | 2000-03-02 | Toagosei Co., Ltd. | Soda electrolytic cell provided with gas diffusion electrode |
| JP3086853B2 (en) * | 1999-02-25 | 2000-09-11 | 長一 古屋 | Electrolytic cell |
| IT1317753B1 (en) * | 2000-02-02 | 2003-07-15 | Nora S P A Ora De Nora Impiant | ELECTROLYSIS CELL WITH GAS DIFFUSION ELECTRODE. |
| JP2001300537A (en) * | 2000-04-25 | 2001-10-30 | Matsushita Electric Works Ltd | Water purifier |
| JP2002275670A (en) * | 2001-03-13 | 2002-09-25 | Association For The Progress Of New Chemistry | Ion exchange membrane electrolytic cell and electrolysis method |
| ITMI20012379A1 (en) * | 2001-11-12 | 2003-05-12 | Uhdenora Technologies Srl | ELECTROLYSIS CELL WITH GAS DIFFUSION ELECTRODES |
| DE10249508A1 (en) * | 2002-10-23 | 2004-05-06 | Uhde Gmbh | Electrolysis cell with an inner channel |
-
2003
- 2003-07-24 DE DE10333853A patent/DE10333853A1/en not_active Withdrawn
-
2004
- 2004-07-13 JP JP2006520729A patent/JP4680901B2/en not_active Expired - Fee Related
- 2004-07-13 WO PCT/EP2004/007713 patent/WO2005012595A1/en active Application Filing
- 2004-07-13 CN CNB2004800214734A patent/CN100549239C/en active Active
- 2004-07-13 EP EP04740955.2A patent/EP1651799B1/en active Active
- 2004-07-23 TW TW093121980A patent/TWI351447B/en not_active IP Right Cessation
- 2004-07-23 US US10/897,430 patent/US20050029116A1/en not_active Abandoned
-
2007
- 2007-02-28 HK HK07102252.2A patent/HK1097885A1/en not_active IP Right Cessation
-
2010
- 2010-12-01 US US12/957,805 patent/US20110073491A1/en not_active Abandoned
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107810291A (en) * | 2015-06-17 | 2018-03-16 | 西门子股份公司 | For synthesizing the electrochemical cell and technique of ammonia |
| CN107810291B (en) * | 2015-06-17 | 2020-03-27 | 西门子股份公司 | Electrochemical cell and process for ammonia synthesis |
| CN108779560A (en) * | 2016-03-17 | 2018-11-09 | Hpnow爱普斯学会 | Electrochemical cell for the vapor-phase reactant in liquid environment |
Also Published As
| Publication number | Publication date |
|---|---|
| US20110073491A1 (en) | 2011-03-31 |
| EP1651799A1 (en) | 2006-05-03 |
| EP1651799B1 (en) | 2015-05-27 |
| TW200519233A (en) | 2005-06-16 |
| JP2006528730A (en) | 2006-12-21 |
| WO2005012595A1 (en) | 2005-02-10 |
| HK1097885A1 (en) | 2007-07-06 |
| TWI351447B (en) | 2011-11-01 |
| JP4680901B2 (en) | 2011-05-11 |
| CN100549239C (en) | 2009-10-14 |
| DE10333853A1 (en) | 2005-02-24 |
| US20050029116A1 (en) | 2005-02-10 |
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