NO135855B - - Google Patents
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- Publication number
- NO135855B NO135855B NO3979/69A NO397969A NO135855B NO 135855 B NO135855 B NO 135855B NO 3979/69 A NO3979/69 A NO 3979/69A NO 397969 A NO397969 A NO 397969A NO 135855 B NO135855 B NO 135855B
- Authority
- NO
- Norway
- Prior art keywords
- particles
- fluid
- particle
- electrolyte
- flow
- Prior art date
Links
- 239000002245 particle Substances 0.000 claims description 42
- 238000000034 method Methods 0.000 claims description 16
- 230000008569 process Effects 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 13
- 239000003792 electrolyte Substances 0.000 claims description 12
- 230000004888 barrier function Effects 0.000 claims description 5
- 239000000376 reactant Substances 0.000 claims description 2
- 210000004027 cell Anatomy 0.000 description 14
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000004744 fabric Substances 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 229910000792 Monel Inorganic materials 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229920004933 Terylene® Polymers 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 210000000170 cell membrane Anatomy 0.000 description 1
- 229910010293 ceramic material Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 150000001879 copper Chemical class 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- ZOMNIUBKTOKEHS-UHFFFAOYSA-L dimercury dichloride Chemical class Cl[Hg][Hg]Cl ZOMNIUBKTOKEHS-UHFFFAOYSA-L 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000003487 electrochemical reaction Methods 0.000 description 1
- 239000007772 electrode material Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000011133 lead Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 239000005020 polyethylene terephthalate Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 230000027756 respiratory electron transport chain Effects 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000012798 spherical particle Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- H—ELECTRICITY
- H01—ELECTRIC ELEMENTS
- H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
- H01M8/00—Fuel cells; Manufacture thereof
- H01M8/08—Fuel cells with aqueous 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
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
-
- 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
-
- 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
- C25B9/40—Cells or assemblies of cells comprising electrodes made of particles; Assemblies of constructional parts thereof
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/50—Fuel cells
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Electrochemistry (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Metallurgy (AREA)
- Manufacturing & Machinery (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- General Chemical & Material Sciences (AREA)
- Inert Electrodes (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Electrolytic Production Of Metals (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Elektrokjemisk prosess. Electrochemical process.
Oppfinnelsen vedrører en elektrokjemisk prosess, ved hvis gjennomføring minst en av elektrodene består av en masse av fluidiserte, adskilte partikler, hvorved de adskilte partikler, The invention relates to an electrochemical process, during the implementation of which at least one of the electrodes consists of a mass of fluidized, separated particles, whereby the separated particles,
i hvert fall delvis, er elektrisk ledende og under driften holdes i bevegelse ved hjelp av en oppoverrettet og gjennom en fluidumpermeabel bunn ført fluidstrøm, og hvorved fluidumet består av elektrolytten, og/eller en reaktant. . De elektrokjemiske prosesser som foreliggende oppfinnelse vedrører omfatter prosesser med elektronoverføring i grense-flaten mellom et fast stoff og et fluidum og hvor en kjemisk forandring finner sted, og omfatter prosesser hvori oksydasjon eller reduksjon av kjemiske stoffer oppnås ved å påføre en posi-tiv eller negativ ladning til den elektrode som.dannes av den faste skilleflate samt prosesser.hvori en kjemisk reaksjon anvendes for å produsere elektrisitet, som f. eks. i brenselscel-ler ... at least partially, is electrically conductive and during operation is kept in motion by means of a fluid flow directed upwards and through a fluid-permeable bottom, and whereby the fluid consists of the electrolyte and/or a reactant. . The electrochemical processes to which the present invention relates include processes with electron transfer at the interface between a solid and a fluid and where a chemical change takes place, and include processes in which oxidation or reduction of chemical substances is achieved by applying a positive or negative charge to the electrode which is formed by the solid separation surface as well as processes in which a chemical reaction is used to produce electricity, such as e.g. in fuel cells...
Fra norsk patent nr. 117v536 er det kjent en elektro-deanordning i elektrokjemiske celler hvor minst en elektrode består av fluidiserte enkeltpartikler, hvorved fluidiseringen frembringes ved hjelp av en oppoverrettet fluidumstrøm. Man har her imidlertid den ulempe at det ikke er noen begrensning av bevegelsen oppover for partiklene i fluidumstrømmen. Plaser-ingen av den øvre flate på det fluidiserte sjikt vil derfor bare bestemmes av de grenser som bestemmes.av strømningshastigheten som vil ekspandere sjiktet til det kan sammenlignes med en koken-de væskemasse. Norwegian patent no. 117v536 discloses an electrode arrangement in electrochemical cells where at least one electrode consists of fluidized individual particles, whereby the fluidization is produced by means of an upwardly directed fluid flow. However, one has the disadvantage here that there is no restriction of the upward movement of the particles in the fluid flow. The placement of the upper surface on the fluidized layer will therefore only be determined by the limits determined by the flow rate which will expand the layer until it can be compared to a boiling liquid mass.
Foreliggende oppfinnelse har til hensikt å tilveie-bringe en elektrokjemisk prosess hvor denne ulempe unngås-. • The present invention aims to provide an electrochemical process in which this disadvantage is avoided. •
Dette oppnås .ved en elektrokjemisk prosess av den Inn-ledningsvis nevnte type som.er kjennetegnet ved det som fremgår av kravene. This is achieved by an electrochemical process of the type mentioned in the introduction which is characterized by what appears in the requirements.
"Ved oppfinnelsen vil den øvre flate av partikkelsjik-tet alltid være linder den øvre grense for et virkelig fluidisert sjikt som benytter den samme gitte partikkelmasse, idet en ytter-ligere sjiktekspansjon begrenses av den porøse barriere som er partikkelugjennomtrengelig, men fluidumgjennomtrengelig. Ved oppfinnelsen kan de fluidiserte partikler som danner elektroden holdes i et nøyaktig definert rom også hvis strømningshastigheten for fluidumet svinger eller blir relativt høy. Resultatet er at cellestrømmens styrke er vidtgående uavhengig av strømningshas-tigheten til fluidumet. "With the invention, the upper surface of the particle layer will always be closer to the upper limit of a truly fluidized layer that uses the same given particle mass, as further layer expansion is limited by the porous barrier which is particle impermeable but fluid permeable. With the invention, the fluidized particles that form the electrode are kept in a precisely defined space even if the flow rate of the fluid fluctuates or becomes relatively high.The result is that the strength of the cell current is widely independent of the flow rate of the fluid.
De partikler som danner elektroden kan i sin helhet bestå av. elektrisk ledende materiale, såsom metall, eller kan f. eks. bestå av en dårlig ledende kjerne, såsom glass, keramisk materiale eller plastmateriale med en flate som er ledende eller som Kar partier med god'ledeevne. Alternativt kan partiklene -være halvledermateriale, såsom grafitt. Fortrinnsvis kan partiklene være helt ledende og bestå av faste metaller•eller<;>legerin-ger, såsom f. eks. kobber, nikkel, bly eller Monel. (MONEL er registrert varemerke.}. Partiklene kan selv delta i den elektrokjemiske reaksjon. The particles that form the electrode may consist entirely of electrically conductive material, such as metal, or can e.g. consist of a poorly conductive core, such as glass, ceramic material or plastic material with a surface that is conductive or as parts with good conductivity. Alternatively, the particles can be semiconductor material, such as graphite. Preferably, the particles can be completely conductive and consist of solid metals•or<;>alloys, such as e.g. copper, nickel, lead or Monel. (MONEL is a registered trademark.} The particles themselves can participate in the electrochemical reaction.
De partikler som danner elektroden og har en størrel-se på 70 - 1000 um kan beskrives som pulvere. Partiklene kan fortrinnsvis være i størrelsesområdet 100' - 250 ym. The particles that form the electrode and have a size of 70 - 1000 µm can be described as powders. The particles can preferably be in the size range 100' - 250 ym.
Partikler av enhver form kan anvendes. Det foretrek-kes imidlertid å anvende partikler av noenlunde jevne hoveddi-mensjoner, og granulære klumper,foretrekkes derfor fremfor nåle-formede partikler, og overveiehde kuleformede partikler er å foretrekke fremfor granulære klumper. Particles of any shape can be used. However, it is preferred to use particles of roughly uniform main dimensions, and granular lumps are therefore preferred to needle-shaped particles, and predominantly spherical particles are preferred to granular lumps.
De partikler som danner elektroden vil normalt anvendes i forbindelse med et elektrisk ledende element, som kan danne en effektiv kontakt med partikkelmassen og som er i stand til å lede en elektrisk ladning mellom partiklene og det ytre av cellen eller halvcellen hvori den elektrokjemiske prosess finner sted. Det nevnte ledende, element kan selv danne veggen eller en del av veggen som omgir elektroden. The particles that form the electrode will normally be used in connection with an electrically conductive element, which can form an effective contact with the particle mass and which is capable of conducting an electrical charge between the particles and the outside of the cell or half-cell in which the electrochemical process takes place . The aforementioned conductive element can itself form the wall or part of the wall that surrounds the electrode.
Det fluidum- som danner elektrolytten og/eller reak-sjpnsmediet vil vanligvis være en væske og vil vanligvis pumpes gjennom elektroden. Det bemerkes imidlertid at i enkelte reak-sjoner kan en eller flere av realIcs jons stoffene være i gassform. Det kan Benyttes anordninger for å regulere hastigheten hvormed fluidumet strømmer gjennom elektroden. The fluid that forms the electrolyte and/or the reaction medium will usually be a liquid and will usually be pumped through the electrode. It is noted, however, that in some reactions one or more of the real ion substances may be in gaseous form. Devices can be used to regulate the speed at which the fluid flows through the electrode.
Foreliggende oppfinnel&e vil i det følgende bli beskrevet nærmere ved" hjelp av et utførelseseksempel som er vist på tegningen. The present invention will be described in more detail in the following by means of an embodiment shown in the drawing.
Fig. 1 jviser et skjematisk riss av en.membraneelle som anvendes ved oppfinnelsen., og Fig. 1 shows a schematic view of a membrane cell used in the invention, and
fig. 2 viser de oppnådde resultater og er en grafisk fremstilling av cellestrømmen som funksjon av strømningshastig-heten ved .reduksjon av meta-nitrobenzensulfonsyre ved en kobber-pulverelektrode ved konstant katodepotensial. fig. 2 shows the results obtained and is a graphical presentation of the cell current as a function of the flow rate during the reduction of meta-nitrobenzenesulfonic acid at a copper powder electrode at constant cathode potential.
Den spesielle elektrokjemiske prosess som er beskrevet som et eksempel er reduksjon av meta-nitrobenzen-sulsonsyre The particular electrochemical process described as an example is the reduction of meta-nitrobenzene-sulsonic acid
i vandig oppløsning. Reaksjonen foregår ved et elektrisk poten-sial lavere enn -0,8 volt i forhold.til en mettet kalomel-elektrode, avhengig av elektrodematerialet, i en oppløsning som inneholder 0,125 molar meta-nitrobenzensulfonsyre og molar svovelsyre ved romtemperatur. Strømtettheten for de enkelte partikler er ca."22 A/m . Virkningsgraden er høyest ved lavere strømtettheter og når elektrolytt-temperaturen heves. in aqueous solution. The reaction takes place at an electric potential lower than -0.8 volts relative to a saturated calomel electrode, depending on the electrode material, in a solution containing 0.125 molar meta-nitrobenzenesulfonic acid and molar sulfuric acid at room temperature. The current density for the individual particles is approx. 22 A/m. The efficiency is highest at lower current densities and when the electrolyte temperature is raised.
Membrancellen vist på .fig. 1 som ble brukt ved forsø-kene besto av en seng 1 av kobberpartikler som dannet cellens katode, idet sengens bredde var 12,7 mm og høyden 38,1 mm. - Katodestrømbæreren 2 i form av en kobberduk var plasert 5 mm fra cellemembranen ft som var ay terylenduk. En piatinadukanode 3 var plasert. 5 mm vekk fra membranen 4"på den annen side av denne. Katodepartikkelsengen hvilte på en permeabel bæreanord-ning eller diffusor 6. Sengen hadde en tykkelse på ca. 25,4 mm. The membrane cell shown in .fig. 1 which was used in the experiments consisted of a bed 1 of copper particles which formed the cathode of the cell, the width of the bed being 12.7 mm and the height 38.1 mm. - The cathode current carrier 2 in the form of a copper cloth was placed 5 mm from the cell membrane ft which was a terylene cloth. A piatina cloth anode 3 was placed. 5 mm away from the membrane 4" on the other side thereof. The cathode particle bed rested on a permeable carrier or diffuser 6. The bed had a thickness of approximately 25.4 mm.
Anolyttvæsken var molar svovelsyre i vann. The anolyte liquid was molar sulfuric acid in water.
CeIlestrømmen ble så målt ved -forskjellige økende . strømningshast.igheter av 'elektrolytten gjennom cellen ved konstant elektrodepotenaial. Resultatene er vist som kurve A på fig.' 2. Man: ser at når partiklene- i katodesengen fritt kan be-vege, seg i e 1 e k t r o 1 y t ts t r ømme n,. får man en optimal, strøm ved en viss- strømningshastighet, idet .strømmen avtar sterkt etter-som strømningshastigheten enten avtar eller øker i forhold til den optimale hastighet. The cell current was then measured at -different increasing . flow rates of the electrolyte through the cell at constant electrode potential. The results are shown as curve A in fig.' 2. One: sees that when the particles in the cathode bed can move freely, they e 1 e c t r o 1 y t t s flow n,. you get an optimal current at a certain flow rate, as the current decreases strongly as the flow rate either decreases or increases in relation to the optimal rate.
I en videre eksperimentserie: ble det plasert en porøs barriére 5-over part.ikkelsengen: for å'begrense- den frie bevegelse av partiklene i eléktrolyttstrømmen. Man fant at mari på denne måte kunne opprettholde en optimal cellestrøm ved høyere strøm-ningshastigheter, som vist på kurve B- på fig. 2. In a further series of experiments: a porous barrier was placed 5 above the particle bed in order to limit the free movement of the particles in the electrolyte flow. It was found that in this way mari could maintain an optimal cell flow at higher flow rates, as shown on curve B- in fig. 2.
En viktig fordel ved prosessen i henhold til foreligg- An important advantage of the process according to existing
ende oppfinnelse, som eksempelvis beskrevet ovenfor, er at celle-strømmen er mindre avhengig av elektrolyttens hastighet gjennom elektrodene enn ved prosesser hvori partikkelsengen er fullt fluidisert og hvor partikkeIsengén ikke er holdt tilbake. Det bemerkes imidlertid at grensetilfellet der'partikkélsengen er" fullstendig stasjonær ikke faller innenfor oppfinnelsens ramme. end of the invention, as for example described above, is that the cell current is less dependent on the speed of the electrolyte through the electrodes than in processes in which the particle bed is fully fluidized and where the particle bed is not held back. It is noted, however, that the limit case where the 'particle bed is' completely stationary does not fall within the scope of the invention.
Prosessen i foreliggende oppfinnelse kan imidlertid finne sted'f. eks. ved å forandre elektrolyttens hastighet på en pulserende måte, slik at i en viss periode er partiklene i elek-trolyttsengen fysisk holdt1 tilbake ved en høy strømnihgshastig- The process in the present invention can, however, take place'f. e.g. by changing the speed of the electrolyte in a pulsating manner, so that for a certain period the particles in the electrolyte bed are physically held back1 at a high current rate
het og deretter gjort stasjonære ved å redusere strømningshastig-JTeten til under det nivå hvorved partiklene påvirkes av strøm- hot and then made stationary by reducing the flow velocity below the level at which the particles are affected by current
ningen. nothing.
Prosessene i foreliggende oppfinnelse kan være spesi- The processes in the present invention can be speci-
elt anvendbare i celler med ét nedre parti som. er konisk eller kileformet og hvori elektrolytten s-om kommer inn i cellen har høyere hastighet enn når de;n strømmer gjennom sengen. Det kan i slike tilfeller være unødvendig å anvende en elektrolyttdiffu- otherwise applicable in cells with a lower part which. is conical or wedge-shaped and in which the electrolyte as it enters the cell has a higher speed than when it flows through the bed. In such cases, it may be unnecessary to use an electrolyte diffuser
sor under partikkélsengen. sor under the particle bed.
Claims (1)
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GB47406/68A GB1239983A (en) | 1968-10-07 | 1968-10-07 | Electrochemical processes |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| NO135855B true NO135855B (en) | 1977-03-07 |
| NO135855C NO135855C (en) | 1977-06-15 |
Family
ID=10444847
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NO3979/69A NO135855C (en) | 1968-10-07 | 1969-10-06 |
Country Status (7)
| Country | Link |
|---|---|
| CH (1) | CH511059A (en) |
| DE (1) | DE1950379C3 (en) |
| FR (1) | FR2020055A1 (en) |
| GB (1) | GB1239983A (en) |
| NL (1) | NL144995B (en) |
| NO (1) | NO135855C (en) |
| SE (1) | SE349483B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU568388B2 (en) * | 1983-08-10 | 1987-12-24 | National Research Development Corp. | Purifying a mixed cation electrolyte |
| GB8508726D0 (en) * | 1985-04-03 | 1985-05-09 | Goodridge F | Purifying mixed-cation electrolyte |
| FR2599758B1 (en) * | 1986-06-06 | 1990-10-26 | Toulouse Inst Nat Polytech | PROCESS AND INSTALLATION OF PERCOLATING ELECTROLYSIS THROUGH ONE OR MORE POROUS VOLUME ELECTRODES |
| GB8900557D0 (en) * | 1989-01-11 | 1989-03-08 | Atomic Energy Authority Uk | Electrochemical cell |
| CN100404726C (en) * | 2004-09-01 | 2008-07-23 | 上海氯碱化工股份有限公司 | Process for electrolytic reduction preparation of metanilic acid |
| EP1870494A1 (en) * | 2006-06-23 | 2007-12-26 | ETH Zürich, ETH Transfer | Electrochemical reactor |
| US11753730B2 (en) | 2018-11-30 | 2023-09-12 | Sedo Engineering Sa | Leucodye (such as leucoindigo) as dispersing aid |
| WO2020109595A1 (en) | 2018-11-30 | 2020-06-04 | Sedo Engineering Sa | Electrochemical reactor and its cleaning or regeneration |
| EP3887577B1 (en) | 2018-11-30 | 2022-12-07 | Sedo Engineering SA | By-products (impurity) removal |
-
1968
- 1968-10-07 GB GB47406/68A patent/GB1239983A/en not_active Expired
-
1969
- 1969-10-06 CH CH1500869A patent/CH511059A/en not_active IP Right Cessation
- 1969-10-06 SE SE13707/69A patent/SE349483B/xx unknown
- 1969-10-06 FR FR6934080A patent/FR2020055A1/fr not_active Withdrawn
- 1969-10-06 NL NL696915100A patent/NL144995B/en not_active IP Right Cessation
- 1969-10-06 DE DE1950379A patent/DE1950379C3/en not_active Expired
- 1969-10-06 NO NO3979/69A patent/NO135855C/no unknown
Also Published As
| Publication number | Publication date |
|---|---|
| DE1950379A1 (en) | 1970-09-10 |
| SE349483B (en) | 1972-10-02 |
| NL6915100A (en) | 1970-04-09 |
| CH511059A (en) | 1971-08-15 |
| DE1950379B2 (en) | 1980-10-23 |
| NO135855C (en) | 1977-06-15 |
| NL144995B (en) | 1975-02-17 |
| FR2020055A1 (en) | 1970-07-10 |
| DE1950379C3 (en) | 1981-11-05 |
| GB1239983A (en) | 1971-07-21 |
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