EP4105362A1 - Verfahren zur oxidation von manganspezies in einer behandlungsvorrichtung sowie behandlungsvorrichtung - Google Patents

Verfahren zur oxidation von manganspezies in einer behandlungsvorrichtung sowie behandlungsvorrichtung Download PDF

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Publication number
EP4105362A1
EP4105362A1 EP21179866.5A EP21179866A EP4105362A1 EP 4105362 A1 EP4105362 A1 EP 4105362A1 EP 21179866 A EP21179866 A EP 21179866A EP 4105362 A1 EP4105362 A1 EP 4105362A1
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EP
European Patent Office
Prior art keywords
anode
cathode
housing
present
preferred
Prior art date
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Application number
EP21179866.5A
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English (en)
French (fr)
Inventor
Sebastian Kühne
Guido Klupsch
Ulrich Laudien
Jens Heydecke
Thomas Fischer
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Atotech Deutschland GmbH and Co KG
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Atotech Deutschland GmbH and Co KG
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Publication date
Application filed by Atotech Deutschland GmbH and Co KG filed Critical Atotech Deutschland GmbH and Co KG
Priority to EP21179866.5A priority Critical patent/EP4105362A1/de
Priority to KR1020247001641A priority patent/KR20240021303A/ko
Priority to TW111122141A priority patent/TW202305185A/zh
Priority to PCT/EP2022/066248 priority patent/WO2022263483A1/en
Priority to JP2023577756A priority patent/JP2024522777A/ja
Priority to BR112023026219A priority patent/BR112023026219A2/pt
Priority to CN202280048589.5A priority patent/CN117693611A/zh
Priority to MX2023015333A priority patent/MX2023015333A/es
Publication of EP4105362A1 publication Critical patent/EP4105362A1/de
Pending 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
    • C25B1/21—Manganese oxides
    • 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
    • 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
    • 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

Definitions

  • the present invention relates to a method for oxidizing manganese species in a treatment device (10) comprising at least one anode unit (20) and at least one cathode (30), wherein said unit comprises at least one anode (21) and is confined by a housing (22), the housing defining a free inner volume (V), wherein (i) the housing comprises at least one permeable barrier (23) and the at least one cathode is located outside the anode unit, or (ii) the at least one anode unit comprises at least partly the at least one cathode, wherein the housing does not comprise a permeable barrier, characterized in that in (i) and (ii) the at least one anode and the at least one cathode have a distance (d) ranging from 0.5 mm to 100 mm.
  • the invention furthermore refers to a respective treatment device (10).
  • Metallizing non-metallic substrates such as plastic substrates has a long history in modern technology. Typical applications are found in automotive industry as well as for sanitary articles.
  • etching a surface modification of the substrate's surface
  • compositions comprising environmentally questionable chromium species, such as hexavalent chromium species (e.g. chromic acid). Although these compositions usually provide very strong and acceptable etching results, environmentally friendly alternatives are more and more demanded and to a certain extent already provided in the art. In many cases manganese-based etching compositions are utilized instead.
  • environmentally questionable chromium species such as hexavalent chromium species (e.g. chromic acid).
  • manganese-based etching compositions are either acidic or alkaline.
  • acidic manganese-based etching compositions are inherently more susceptible to degradation, in particular permanganate-based etching compositions.
  • etching compositions require a constant and comparatively high level of replenishment of active manganese species.
  • etching compositions are continually recycled to maintain a comparatively constant level of active manganese species. This is typically either achieved by chemical oxidation or by applying an electrical current.
  • Respective regeneration methods and devices, respectively, are known in the art.
  • CN 109628948 A refers to a regeneration device comprising a ceramic diaphragm for recycling a permanganate ion solution.
  • CN 1498291 A refers to an electrolytic regeneration treatment device for regenerating an etching treatment solution.
  • WO 2013/030098 A1 refers to a device for an at least partial regeneration of a treatment solution comprising permanganate, which is used for treatment and/or etching of plastic parts.
  • WO 01/90442 A1 refers to a cathode for an electrochemical arrangement for regeneration of permanganate etching solutions and a device for electrolytically regenerating permanganate etching solutions.
  • the treatment device (10) allows a very efficient anodic oxidation of manganese species having an oxidation number below +7.
  • the at least one anode unit (20) allows a very compact design, which is the basis for the improved efficiency.
  • the present invention is very suitable for efficiently treating acidic manganese-based etching compositions because the volume needed in the treatment device is relatively low compared to the volume of a corresponding etching composition.
  • a volume in a respective treatment device is about identical to the volume of the utilized etching composition.
  • the volume treated in the treatment device is significantly lower than the volume of the etching composition.
  • the so-called dead volume has been significantly reduced compared to common methods and devices.
  • step (A) Preferred is a method of the present invention, wherein the liquid provided in step (A) has a volume of 50 vol.-% or less of a total liquid utilizing said liquid provided in step (A), preferably 40 vol.-% or less, most preferably 30 vol.-% or less.
  • the at least one cathode is either outside the anode unit or comprised in the housing.
  • the at least one cathode is (at least mainly) built around (in a sense of surrounding) the at least one anode.
  • the at least one cathode at least mainly encircles or circulates the at least one anode, wherein this wording does not limit the ensemble to a circular shape.
  • This essential anode/cathode arrangement can also be described as follows: referenced to the center point in the anode unit, the distance of the at least one anode to the center point is shorter than the corresponding distance of the corresponding at least one cathode.
  • the at least one anode is located more towards the center of the anode unit than the corresponding at least one cathode, preferably the at least one anode is centered in the anode unit.
  • embodiments are present, (i) and (ii), wherein embodiment (i) comprises at least one permeable barrier and embodiment (ii) is free thereof.
  • embodiment (i) due to the presence of the at least one permeable barrier, a catholyte is formed/present around the at least one cathode and an anolyte around the at least one anode, respectively. They are permeably separated from each other by the at least one permeable barrier.
  • the housing comprises at least one permeable barrier and the at least one cathode is located outside the anode unit.
  • This embodiment is preferably also referred to as the membrane-approach (if the at least one permeable barrier comprises a membrane). It denotes that the at least one cathode is not directly part of the anode unit or its housing but is located (i.e. positioned, arranged) outside the anode unit (but within the treatment device). However, by means of the permeable barrier the current can flow despite the housing such that anodically the at least one manganese species is oxidized to a manganese species having the oxidation number +7.
  • the liquid is (i.e. corresponds to) the anolyte.
  • the maximum volume of the liquid i.e. preferably the anolyte present in embodiment (i)
  • the liquid is an etching composition, i.e. preferably means is provided as an utilized etching composition in step (A) and returned as refreshed/recycled etching composition after step (C).
  • the free inner volume (V) corresponds to the total inner housing volume subtracted by at least the volume (i.e. the tare volume) of the at least one anode (including e.g. its parts for installation) which is located inside the housing and, thus, is reducing the total inner housing volume.
  • the free inner volume (V) is more preferably the volume that the liquid can maximally occupy within the at least one anode unit.
  • the catholyte comprises an inorganic acid, preferably phosphoric acid, more preferably 20 wt.-% to 90 wt.-% phosphoric acid, even more preferably 30 wt.-% to 80 wt.-%, most preferably 40 wt.-% to 70 wt.-% phosphoric acid.
  • the catholyte comprises an inorganic acid, preferably phosphoric acid, more preferably 20 wt.-% to 90 wt.-% phosphoric acid, even more preferably 30 wt.-% to 80 wt.-%, most preferably 40 wt.-% to 70 wt.-% phosphoric acid.
  • all manganese species are preferably separated from the at least one cathode.
  • the at least one permeable barrier is an ion-selective permeable barrier, preferably an ion-selective permeable membrane.
  • the at least one permeable barrier is a cation-selective permeable barrier, preferably a cation-selective permeable membrane.
  • the at least one permeable barrier is a cation-selective permeable barrier, preferably a cation-selective permeable membrane.
  • the at least one permeable barrier is organic. More preferred is a method of the present invention, wherein the at least one permeable barrier is organic and comprises fluorine (preferably is fluorinated), most preferably is organic and perfluorinated. Most preferred, the at least one permeable barrier is a Nafion-type-membrane, although the at last one membrane is not particularly limited to this particular brand.
  • the aforementioned preferably applies likewise to the preferred ion-selective (preferably cation-selective) permeable barrier, preferably the ion-selective (preferably cation-selective) permeable membrane.
  • Membranes, preferably said organic membranes are very thin and therefore positively contribute to the comparatively short distance (d), and, thus, to the compact design of the at least one anode unit.
  • step (C) of the method of the present invention a current is applied, preferably an electrical current.
  • This current and the electrical field related thereto typically affect the migration direction of the respective ions present in the liquid. As a result, negatively charged manganese species are forced to migrate to the at least one anode.
  • the permeable barrier present in embodiment (i), in combination with said current typically brings about that negatively charged manganese species are even more fully prevented from contacting the at least one cathode.
  • the permeable barrier preferably significantly suppresses/reduces the mixing of anolyte and catholyte with each other (preferably a transport of anions into the catholyte).
  • the permeable barrier most preferably the cation-selective permeable membrane, suppresses/avoids an anion transport from the anolyte into the catholyte.
  • the transport of negatively charged manganese species e.g.
  • MnO 4 - , PO 4 3- , HPO 4 2- , H 2 PO 4 - is significantly suppressed, without and even more with the current. Furthermore, also a transport of particulate, non-charged MnO 2 is preferably avoided or at least significantly suppressed.
  • the permeable barrier freely and primarily allows transport/migration of water molecules, preferably of water and hydronium ions.
  • the at least one cathode is at least partly integrated in the housing, preferably is at least partly penetrating the housing from the outside into the inside towards the at least one anode.
  • the housing comprises (preferably integrates) at least partly the at least one cathode, wherein the housing does not comprise (i.e. is free of) a permeable barrier.
  • This embodiment is preferably also referred to as the membrane-free approach.
  • the entire housing does not comprise a permeable barrier.
  • the at least one cathode is, preferably at least partly, integrated in the housing. This also means that the at least one cathode (preferably at least partly) is preferably itself part of the housing and is therefore (preferably at least partly) preferably confining the at least one anode unit as part of the housing.
  • the at least one cathode (preferably at least partly) is comprised (preferably integrated) in the housing and preferably at least partly exposes cathodic areas into the inside of the housing.
  • no distinct catholyte and anolyte are formed but rather only the liquid.
  • all manganese species are basically in contact with the at least one anode and the at least one cathode.
  • embodiment (i) provides a great advantage if the liquid comprises besides manganese species further metal ions such as silver ions.
  • an undesired cathodic silver deposition can be prevented or at least reversed such that silver (or possibly other metal ions besides manganese) remains permanently dissolved or is re-dissolved at least in certain time intervals.
  • (d) is ranging from 1 mm to 90 mm, preferably from 2 mm to 80 mm, more preferably from 3 mm to 70 mm, even more preferably from 4 mm to 60 mm, most preferably from 5 mm to 50 mm.
  • the distance (d) is defined as the shortest distance between the at least one anode and the closest (preferably corresponding) at least one cathode.
  • the distance (d) is preferably the shortest outer distance between the at least one anode and the closest (preferably corresponding) at least one cathode.
  • the term "outer” preferably refers to the outermost of the at least one anode directly facing towards the outermost of the closest at least one cathode.
  • the distance (d) is the shortest average outer distance between the at least one anode and the closest (preferably corresponding) at least one cathode. This is preferably the case if the at least one anode and the at least one cathode have a parallel alignment towards each other.
  • Fig. 1 to 3 For a supportive understanding, reference is made to Fig. 1 to 3 .
  • a method of the present invention is preferred, wherein (d) is ranging from 9 mm to 70 mm, preferably from 10 mm to 60 mm, more preferably from 11 mm to 50 mm, even more preferably from 12 mm to 30 mm, most preferably from 13 mm to 20 mm.
  • the minimum of distance (d) is typically larger compared to embodiment (ii) because the at least one cathode is located outside the anode unit (i.e. outside the housing) such that the housing is in between the at least one cathode and the at least one anode.
  • the distance (d) has a minimum distance with the proviso that the minimum distance in (i) is higher compared to the minimum distance (d) in embodiment (ii).
  • the at least one permeable barrier is between the at least one anode and the at least one cathode without getting in direct contact to said anode and cathode.
  • the thickness of the permeable barrier is preferably neglectable and therefore does not substantially contribute to the distance (d).
  • a method of the present invention is preferred, wherein (d) is ranging from 1 mm to 70 mm, preferably from 2 mm to 60 mm, more preferably from 3 mm to 50 mm, even more preferably from 4 mm to 30 mm, most preferably from 5 mm to 20 mm.
  • a comparatively low distance (d) is maintained because the housing comprises at least partly the at least one cathode.
  • the minimum of distance (d) is comparatively low. This has the advantage that less voltage is needed compared to embodiment (i), which preferably has a higher minimum of distance (d).
  • the at least one anode comprises a layer stack (25) of anode layers, preferably of 3 or more than 3 anode layers, more preferably the layer stack comprises 3 to 300 anode layers, even more preferably 4 to 200 anode layers, yet even more preferably 6 to 100 anode layers, most preferably 8 to 60 anode layers, even most preferably 9 to 30 anode layers.
  • an anode having a very compact design e.g. designed as a layer stack of multiple anode layers
  • provides a sufficiently high current efficiency/turnover most preferably if the space between individual anode segments is very small; for example if the number of individual anode layers in a layer stack is comparatively high and therefore the space between them comparatively small.
  • a very high and detrimental shielding effect occurs, e.g. in particular the more individual anode segments are consecutively placed towards the at least one cathode.
  • the layer stack preferably comprises at least one inner anode layer and at least one outer anode layer.
  • the at least one inner anode layer is either facing another inner anode layer or at least on one side the at least one outer layer.
  • the layer stack comprises exactly two anode layers, they are at the same time the at least one outer anode layer. This likewise applies if the at least one anode comprises or is a single anode layer.
  • the at least one anode comprises or is a single anode layer providing also a huge total effective anode surface area, preferably equivalent to the huge total effective anode surface area obtained by means of the preferred layer stack.
  • the distance (d) is defined as the shortest distance between the at least one anode and the closest (preferably corresponding) at least one cathode. More preferred is a method of the present invention, wherein the distance (d) is defined as the shortest distance between an outermost anode layer of a layer stack and the closest (preferably corresponding) at least one cathode.
  • distance (d) is a constant distance. This preferably means, (d) denotes a distance between the at least one anode and the at least one cathode, which are aligned to each other in parallel.
  • the at least one anode is preferably oriented horizontally or vertically (compare Fig. 1 and 2 ). More preferred is a method of the present invention, wherein the at least one anode is vertically oriented (compare Fig. 1 ). This most preferably applies to the anode layers of a layer stack (25). However, in some other cases a method of the present invention is preferred, wherein the at least one anode is horizontally oriented (compare Fig. 2 ). This most preferably also applies to the anode layers in a layer stack (25). Own experiments have shown that a vertical orientation provides in many cases an improved current efficiency and is therefore preferred. It is assumed that in such a case the liquid has an improved perfusion through the at least one anode unit and formed gas can easily escape without adsorbing on an anode surface. Furthermore, this approach is also related to lower costs.
  • the at least one anode comprises a layer stack (25) of 2 to 100 anode layers, preferably of 3 to 80 anode layers, more preferably of 4 to 60 anode layers, even more preferably of 5 to 40 anode layers, most preferably of 6 to 30 anode layers.
  • the at least one anode comprises a layer stack (25) of 2 to 300 anode layers, preferably of 5 to 260 anode layers, more preferably of 7 to 220 anode layers, even more preferably of 9 to 170 anode layers, most preferably of 12 to 130 anode layers.
  • the number of anode layers is preferably as defined above for embodiment (i).
  • the distance (m) is fixed by means of a spacer (26). More preferably, (m) is (essentially) constant, most preferably is (essentially) constant between all anode layers in the layer stack.
  • a very preferred distance (m) is ranging from 1 mm to 6 mm, preferably from 1.5 mm to 4 mm.
  • the at least one anode preferably the layer stack, comprises a sheet, a mesh, a woven web, and/or an expanded metal (i.e. a metal lath).
  • the at least one anode In the context of the present invention it is generally preferred to provide the at least one anode with a comparatively high total effective anode surface area.
  • the aforementioned forms of the at least one anode (most preferably the layer stack) preferably fulfill this very desired and preferred characteristic.
  • a method of the present invention is preferred, wherein the at least one anode comprises an expanded metal (metal laths; also called "Streckmetall").
  • the layer stack (25) comprises expanded metal as anode layers.
  • the at least one anode preferably the individual anode layer in the layer stack, has a surface factor of 1 or more, preferably of 1.4 or more, even more preferably of 1.7 or more, yet even more preferably of 2 or more, most preferably of 2.1 or more, even most preferably of 2.2 or more.
  • the surface factor denotes a parameter defining the total effective surface area per geometric area.
  • a plate i.e. a surface, geometrically of 1 m 2 typically has a surface factor of 2 (for the sake of simplicity, the area of the cutting edges is neglected), which results in a total effective surface area of 2 m 2 (including front side and back side).
  • the surface factor is without any dimensions/units.
  • a surface factor below or even above 2 is typically obtained if e.g. a plate has holes and a mesh has openings, respectively, in a defined number and with defined dimensions.
  • the surface factor of commercially available meshes today is typically not exceeding 2.5.
  • the surface factor as defined above most preferably applies to the individual anode layers in a layer stack.
  • the at least one anode is, preferably additionally to anodes mentioned already above, selected from the group consisting of 3D-printed anodes, woven fabric anodes, foam anodes, and packed bed anodes.
  • anodes typically have a comparatively high effective surface area per volume, most preferably of 6 m 2 /L or more, based on the total volume of the at least one anode. This is also known as surface density, which denotes the total effective surface area per geometric volume.
  • the surface density is in a range from 6 m 2 /L to 100 m 2 /L, preferably from 8 m 2 /L to 70 m 2 /L, more preferably from 10 m 2 /L to 50 m 2 /L, even more preferably from 12 m 2 /L to 40 m 2 /L, yet even more preferably from 14 m 2 /L to 30 m 2 /L, most preferably from 16 m 2 /L to 22 m 2 /L.
  • the woven fabric anodes comprise woven metallic wires and/or woven metallized filaments.
  • the woven fabric anodes comprise flat woven fabric anodes and/or pile fabric anodes.
  • the 3D-printed anodes comprise 3D-printed lattice anodes and/or 3D-printed lamella anodes.
  • the packed bed anodes comprise a package compartment selected from the group consisting of raschig ring, lessing ring, pall ring, bialecki ring, dixon ring, net balls, and Hex-X compartments.
  • the at least one anode comprises platinum, titanium, niobium, lead, gold, alloys comprising at least one thereof, oxides thereof, and/or mixtures thereof; preferably at least one of platinum, titanium, and gold.
  • the at least one anode (and its respective material) must be carefully selected. A minimum requirement is that a respective material is (electro-)chemically inert towards the liquid.
  • the aforementioned anodes are resistant, at least for a certain time.
  • the at least one anode comprises a platinized anode and/or a platinum anode, preferably a platinized titanium anode, and/or a platinized niobium anode.
  • a method of the present invention is preferred, wherein the at least one anode comprises lead and/or lead alloys.
  • Preferred lead alloys comprise tin and/or silver as alloying elements.
  • own experiments have shown that an excellent efficiency is obtained with at least one anode comprising platinum, preferably the at least one anode comprises a platinized anode and/or a platinum anode. This preferably applies likewise to embodiment (i) and (ii), respectively.
  • the at least one cathode comprises titanium, platinum, niobium, lead, alloys comprising at least one thereof, oxides thereof, stainless steel, and/or mixtures thereof.
  • the at least one cathode is of a wide variety of materials as long as a respective material is preferably acid resistant, sufficiently stable against hydrogen embrittlement, and/or chemically resistant to the liquid (depending on the utilized embodiment).
  • a method of the present invention is preferred, wherein the at least one cathode is identical to the at least one anode, preferably in embodiment (ii). However, in other cases, preferably, the at least one cathode is different from the at least one anode, preferably in embodiment (i) but also in cases of embodiment (ii).
  • the at least one cathode comprises platinum, titanium, lead, nickel, alloys comprising at least one thereof, oxides thereof, stainless steel, and/or mixtures thereof.
  • the at least one cathode comprises platinum, titanium, lead, nickel, alloys comprising at least one thereof, oxides thereof, stainless steel, and/or mixtures thereof.
  • stainless steel it shows a very desired resistance in phosphoric acid, which is the most preferred catholyte in this embodiment.
  • the cathodic current protects the at least one cathode such that even less resistant materials can be utilized. This general principle of cathodic protection preferably also applies to embodiment (ii).
  • an electro-chemically very inert cathode material is needed.
  • the at least one cathode comprises titanium, platinum, niobium, lead, alloys comprising at least one thereof, oxides thereof, stainless steel, and/or mixtures thereof.
  • a method of the present invention is preferred, wherein the at least one cathode comprises a platinized cathode and/or a platinum cathode, preferably a platinized titanium cathode, and/or a platinized niobium cathode.
  • a method of the present invention is preferred, wherein the at least one cathode comprise stainless steel.
  • Stainless steel is in some cases preferably used due to the cathodic protection and therefore can be used in embodiment (ii) according to the method of the present invention.
  • the at least one cathode comprises one cathode layer or a layer stack of two, three or more than three cathode layers, preferably of two cathode layers.
  • a cathode layer stack, preferably of two cathode layers, is more preferred in embodiment (ii) of the method of the present invention.
  • each cathode layer in the layer stack is electrically separated from each other. This preferably allows that each cathode layer has a distinct current source.
  • the at least one cathode comprises a sheet, a mesh, a woven web, and/or an expanded metal. This most preferably applies to embodiment (i).
  • At least one cathode and the at least one anode are vertically oriented, preferably vertically oriented and in parallel to each other.
  • total effective surface area refers to the area available for participation in electrochemical redox-reactions.
  • the at least one cathode is at least partly (preferably partly) penetrating the housing from the outside into the inside such that a plurality of cathode spots (31) are exposed into the inside towards the at least one anode and A 2 is formed by said spots.
  • Such spots effectively minimize the total effective cathode surface area if only these spots are exposed into the anode unit towards the at least one anode.
  • the spots are equally distributed over at last a part of the housing.
  • the A 2 is homogeneously distributed within the anode unit.
  • a method of the present invention is preferred, wherein the plurality of cathode spots is planar with the inside of the housing.
  • the at least one cathode which is at least partly (preferably partly) penetrating the housing from the outside into the inside towards the at least one anode comprises a layer stack of at least two cathode layers (compare Fig. 3 ).
  • the plurality of cathode spots is forming a first and a second set of cathode spots (32 and 33, respectively, compare Fig. 3 ), each set preferably having its own current.
  • This preferably means that the first and second set are electrically separated from each other.
  • This preferably furthermore allows to temporarily switch off one of the sets, to run both with different currents, or to reverse the current in one of the sets compared to the other set. Own experiments have shown that this is of great benefit to avoid deposition of e.g. metallic silver if silver ions are utilized in the liquid.
  • a 1 : A 2 is ranging from 5:1 to 100:1, preferably from 10:1 to 85:1, more preferably from 15:1 to 70:1, even more preferably from 20:1 to 60:1, most preferably from 30:1 to 50:1.
  • a 1 : A 2 is ranging from 5:1 to 30:1, preferably from 6:1 to 25:1, more preferably from 7:1 to 20:1.
  • a method of the present invention is preferred, wherein A 1 : A 2 is at least 10:1, preferably at least 20:1, more preferably at least 30:1, most preferably at least 40:1.
  • a 1 : A 2 is ranging from 10:1 to 100:1, preferably from 20:1 to 70:1, more preferably from 30:1 to 50:1, most preferably from 35:1 to 45:1.
  • This is preferably required to perform embodiment (ii) with a preferably high current efficiency and to sufficiently suppress undesired cathodic side-reactions breaking down desired manganese species.
  • an optimal balance between current efficiency and energy consumption is provided.
  • a 1 is ranging from 10 dm 2 /dm 3 to 100 dm 2 / dm 3 , based on the free inner volume (V), preferably from 15 dm 2 /dm 3 to 85 dm 2 / dm 3 , more preferably from 20 dm 2 / dm 3 to 70 dm 2 / dm 3 , even more preferably from 25 dm 2 / dm 3 to 60 dm 2 /dm 3 , most preferably from 30 dm 2 / dm 3 to 50 dm 2 / dm 3 .
  • the aforementioned parameter denotes an anode density (i.e. total effective anode surface area per dm 3 of the free inner volume of the at least one anode unit).
  • anode density i.e. total effective anode surface area per dm 3 of the free inner volume of the at least one anode unit.
  • the aforementioned anode densities in particular the preferred and most preferred ones, are typically considered as high.
  • the treatment device and/or the at least one anode unit preferably the at least one anode unit
  • has at least one inner surface comprising or consisting of a fluorinated plastic, preferably polyvinylidene fluoride (PVDF) and/or polytetrafluoroethylene (PTFE).
  • PVDF polyvinylidene fluoride
  • PTFE polytetrafluoroethylene
  • step (A) the at least one manganese species having an oxidation number below +7 is provided in a liquid.
  • step (A) the liquid is obtained from an etching compartment for etching a non-metallic substrate, preferably a plastic substrate.
  • the liquid is preferably an etching composition, most preferably after being in contact with a non-metallic substrate, preferably a plastic substrate.
  • step (A) in said liquid the at least one manganese species having an oxidation number below +7 comprises manganese species having an oxidation number of +IV, preferably MnO 2 .
  • manganese species having an oxidation number of +IV constitutes more than 50 mol-% of all manganese species in the liquid prior to step (C), preferably at least 75 mol-%.
  • the MnO 2 is particulate, preferably is present as colloidal particles. This preferably includes optional agglomerates thereof.
  • the plastic substrate comprises acrylonitrile butadiene styrene (ABS), acrylonitrile butadiene styrene - polycarbonate (ABS-PC), polypropylene (PP), polyamide (PA), polyurethane (PU), polyepoxide (PE), polyacrylate, polyetherimide (PEI), a polyetherketone (PEK), mixtures thereof, and/or composites thereof; preferably acrylonitrile butadiene styrene (ABS), acrylonitrile butadiene styrene - polycarbonate (ABS-PC), polyamide (PA), polyurethane (PU), polyepoxides (PE), polyacrylate, mixtures thereof, and/or composites thereof.
  • Such plastic substrates are typically used in decorative applications such as automotive parts, in particular ABS and ABS-PC.
  • step (C) the manganese species having the oxidation number +7 comprises permanganate ions, most preferably are permanganate ions.
  • etching a plastic substrate with e.g. permanganate reduces permanganate to manganese species with lower oxidation numbers while the material of the plastic is at least partly oxidized.
  • step (A) the at least one manganese species having an oxidation number below +7 have a total concentration ranging from 0.1 g/L to 4 g/L, based on the element manganese and the total volume of the liquid, preferably ranging from 0.2 g/L to 3 g/L, more preferably ranging from 0.3 g/L to 2 g/L, most preferably 0.4 g/L to 1.5 g/L.
  • step (C) of the method of the present invention a current is applied to anodically oxidize at least a portion of manganese species having an oxidation number below +7.
  • the method of the present invention is a recycling method for permanganate ions.
  • recycling refers to a re-oxidation of (preferably already utilized) manganese species to the oxidation number +7 with subsequent re-utilization thereof for etching.
  • a method of the present invention is preferred, wherein the method is carried out continually.
  • a method of the present invention is preferred, wherein the treatment device is external relative to the etching compartment. This means that the treatment device is outside the etching compartment. This is typically preferred. However, in other cases a method of the present invention is preferred, wherein the treatment device is at least partly integrated into the etching compartment. This preferably means that the treatment device is internal relative to the etching compartment.
  • step (C) the current has a current density ranging from 0.1 A/dm 2 to 10 A/dm 2 , preferably from 0.2 A/dm 2 to 8 A/dm 2 , more preferably from 0.3 A/dm 2 to 6 A/dm 2 , even more preferably from 0.4 A/dm 2 to 4 A/dm 2 , yet even more preferably from 0.5 A/dm 2 to 2.8 A/dm 2 , most preferably from 0.6 A/dm 2 to 1.5 A/dm 2 .
  • This is the anodic current density preferably based on the effective anode surface area.
  • the anodic current density is comparatively low in order to avoid/reduce undesired anodic oxygen gas production, which in turn reduces the current efficiency.
  • step (C) the at least one cathode has a cathodic current density ranging from 2 A/dm 2 to 70 A/dm 2 , preferably from 3 A/dm 2 to 60 A/dm 2 , more preferably from 4 A/dm 2 to 50 A/dm 2 , even more preferably from 5 A/dm 2 to 40 A/dm 2 , yet even more preferably from 6 A/dm 2 to 30 A/dm 2 , most preferably from 7 A/dm 2 to 20 A/dm 2 .
  • This is the cathodic current density.
  • a comparatively low anodic current density it is desired to have a comparatively high cathodic current density. This typically leads to hydrogen gas production. Although this is generally not desired, in the context of the present invention, it suppresses undesired cathodic decomposition reactions of desired manganese species. This most preferably applies to embodiment (ii).
  • a method of the present invention is preferred, wherein in step (C) the at least one cathode has a cathodic current density ranging from 2 A/dm 2 to 30 A/dm 2 , preferably from 3 A/dm 2 to 25 A/dm 2 , more preferably from 4 A/dm 2 to 20 A/dm 2 , even more preferably from 5 A/dm 2 to 15 A/dm 2 , most preferably from 6 A/dm 2 to 12 A/dm 2 .
  • a method of the present invention is preferred, wherein in step (C) the at least one cathode has a cathodic current density ranging from 10 A/dm 2 to 70 A/dm 2 , preferably from 12 A/dm 2 to 65 A/dm 2 , more preferably from 14 A/dm 2 to 60 A/dm 2 , most preferably from 16 A/dm 2 to 50 A/dm 2 . In some cases, a cathodic current density is preferred ranging from 18 A/dm 2 to 35 A/dm 2 .
  • the liquid comprises an acid, preferably an inorganic acid, most preferably phosphoric acid.
  • liquid comprises, preferably after step (C),
  • the liquid utilized in the method of the present invention comprises water.
  • the manganese species having the oxidation number +7, preferably the permanganate ions have a concentration ranging from 0.004 mol/L to 0.09 mol/L, based on the total volume of the liquid, preferably from 0.005 mol/L to 0.075 mol/L, more preferably from 0.006 mol/L to 0.06 mol/L, even more preferably from 0.007 mol/L to 0.045 mol/L, yet even more preferably from 0.008 mol/L to 0.03 mol/L, most preferably from 0.009 mol/L to 0.019 mol/L.
  • step (A) in the liquid all manganese species together have a total concentration ranging from 0.02 mol/L to 0.3 mol/L, based on the total volume of the liquid, preferably from 0.03 mol/L to 0.25 mol/L, most preferably from 0.035 mol/L to 0.2 mol/L.
  • phosphoric acid is the only (mineral) acid in the liquid. It is in particular phosphoric acid and preferably the absence of other strong mineral acids that significantly slows down further reduction of manganese species having an oxidation number of +IV (such as MnO 2 ) to an oxidation number below +IV. This is very preferred. This is preferably also the reason that the liquid comprises comparatively low amounts of manganese (II) ions.
  • a method of the present invention is preferred, wherein in the liquid the phosphoric acid has a concentration ranging from 9.2 mol/L to 10.5 mol/L, based on the total volume of the liquid, preferably from 9.3 mol/L to 10.4 mol/L, more preferably from 9.4 mol/L to 10.3 mol/L.
  • a method of the present invention is preferred, wherein the liquid comprises silver (I) ions.
  • Silver ions are preferably needed in order to better catalyze the electrolytic re-oxidation.
  • the silver (I) ions have a concentration ranging from 0.0001 mol/L to 0.09 mol/L, preferably from 0.0002 mol/L to 0.07 mol/L, more preferably from 0.0005 mol/L to 0.05 mol/L, even more preferably from 0.0007 mol/L to 0.03 mol/L, most preferably from 0.001 mol/L to 0.01 mol/L.
  • the liquid is substantially free of, preferably does not comprise, manganese (II) ions.
  • the concentration thereof is preferably comparatively low, most preferably not exceeding 10 ppm, based on the total volume of the liquid. This preferably applies generally to the liquid utilized in the method of the present invention.
  • the liquid comprises alkali ions, most preferably sodium ions, preferably in a total concentration ranging from 0.002 mol/L to 0.5 mol/L, based on the total volume of the liquid, preferably from 0.004 mol/L to 0.3 mol/L.
  • the liquid is substantially free of, preferably does not comprise, a methane sulfonic acid and salts thereof, preferably is substantially free of, preferably does not comprise, a C1 to C4 alkyl sulfonic acid and salts thereof, most preferably is substantially free of, preferably does not comprise, a C1 to C4 sulfonic acid and salts thereof.
  • liquid is substantially free of, preferably does not comprise, bromide and iodide anions, preferably is substantially free of, preferably does not comprise, chloride, bromide, and iodide anions, most preferably is substantially free of, preferably does not comprise, halide anions.
  • liquid is substantially free of, preferably does not comprise, trivalent chromium ions and hexavalent chromium compounds, preferably is substantially free of, preferably does not comprise, any compounds and ions comprising chromium.
  • step (C) Preferred is a method of the present invention, wherein during step (C) the liquid has a temperature ranging from 20°C to 65°C, preferably from 30°C to 50°C.
  • step (A) and after step (C) is acidic, preferably has a pH of 2 or below, more preferably of 1 or below, even more preferably of 0.5 or below.
  • step (A) and after step (C) the liquid has a density in a range from 1.2 g/cm 3 to 1.7 g/cm 3 , referenced to a temperature of 20°C, preferably from 1.3 g/cm 3 to 1.6 g/cm 3 , more preferably from 1.4 g/cm 3 to 1.6 g/cm 3 .
  • This density is preferably the result of large amounts of phosphoric acid and particulate and/or colloidal MnO 2 .
  • the present invention furthermore refers to a respective treatment device, preferably for oxidizing manganese species having an oxidation number below +7 to a manganese species having the oxidation number +7, the treatment device comprising at least one anode unit (20) and at least one cathode (30), wherein said unit comprises at least one anode (21) and the unit is confined by a housing (22), the housing defining a free inner volume (V), wherein
  • the aforementioned regarding the method of the present invention applies likewise to the treatment device of the present invention, most preferably features defined as preferred for the treatment device utilized in the method of the present invention apply likewise to the treatment device of the present invention.
  • a liquid comprising approximately 9 to 10 mol/L phosphoric acid, approximately 10 mmol/L permanganate ions, and approximately 2 mmol/L silver (I) ions was used as etching composition for etching ABS and ABS-PC substrates at approximately 40°C.
  • the etching composition was continually provided by actively pumping (not shown) as a liquid to a treatment device (10) for recycling.
  • the treatment device (10) was filled with a catholyte consisting of aqueous, concentrated phosphoric acid (70 wt.-%), wherein the liquid (i.e. the anolyte in this embodiment) was continually pumped through the at least one anode unit (20).
  • the at least one anode unit (20) was a defined compartment comprising at least one anode (21) in the center of the at least one anode unit (20).
  • the at least one anode (21) was provided as a vertically oriented layer stack comprising a plurality of 8 to 20 anode layers (25), which were expanded metals having an individual surface factor of slightly above 2.
  • the at least one anode unit (20) provided a total effective anode surface area A 1 of about 40 dm 2 /dm 3 .
  • the at least one anode unit (20) was confined by a housing (22) comprising at least one permeable barrier (23), which was a Nafion-type membrane. Typically, two of them were used on opposite sides of the housing (22) as shown in Fig. 1 .
  • the distance (m) between the plurality of anode layers was fixed by spacers (26) and was approximately 1 to 2 mm.
  • anode units are utilized in the treatment device to constantly recycle permanganate ions with a performance of about 200 L etching composition recycled per anode unit.
  • 5 anode units in one treatment device were utilized for about 600 to 1000 L etching composition.
  • the volume of the liquid present in the at least one anode unite corresponds to the free inner volume (V) as defined above in the text.
  • At least one cathode (30) was provided, typically around the at least one anode unit (20) on opposite sides relative to the at least one anode unit (20).
  • the at least one cathode (30) provided a total effective cathode surface area A 2 , wherein A 1 was significantly larger than A 2 .
  • the distance (d) between the at least one anode (21) and the at least one cathode (30) was approximately 15 mm.
  • An electrical current was applied to said at least one anode (21) and said at least one cathode (30).
  • the anodic current density was approximately 1 A/dm 2
  • the cathodic current density was approximately 10 A/dm 2 .
  • the liquid While flowing through the at least one anode unit (20), the liquid was in contact with the anode layers of layer stack (25) and manganese species having an oxidation number below +7 were continually re-oxidized to permanganate ions (i.e. a manganese species having the oxidation number +7).
  • silver (I) ions were replenished from time to time to compensate not only drag out but also an undesired minor precipitation.
  • no permeable barriers (23) were used in housing (22).
  • the at least one cathode was at least partly integrated in the housing (22) on opposite sides in such a way that that the at least one cathode (30) partly penetrates the housing (22) into the inside towards the at least one anode (21).
  • a plurality of cathode spots (31) was formed, approximately 16 to 60 spots per side on two opposite inner sides of the housing (22) of the at least one anode unit (20).
  • cathodes (30) were utilized such that a first set (32) and a second set (33) of cathode spots (from said plurality of cathode spots) were present inside the at least one anode unit (20) towards the at least one anode (21). Both cathodes were electrical separated from each other. The electrical cathodic current was repeatedly reversed such that silver precipitation was dissolved and therefore basically avoided. Only a loss due to drag out was compensated in time intervals. As a result, significantly less silver was consumed.
  • the cathodic current density was approximately 50 A/dm 2 and thus, significantly higher than in embodiment (i).
  • the distance (d) between the at least one anode (21) and the at least one cathode (30) was approximately 10 mm.
  • the liquid comprising re-oxidized permanganate ions was returned as etching composition.

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  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Organic Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Electrodes For Compound Or Non-Metal Manufacture (AREA)
  • Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
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EP21179866.5A 2021-06-16 2021-06-16 Verfahren zur oxidation von manganspezies in einer behandlungsvorrichtung sowie behandlungsvorrichtung Pending EP4105362A1 (de)

Priority Applications (8)

Application Number Priority Date Filing Date Title
EP21179866.5A EP4105362A1 (de) 2021-06-16 2021-06-16 Verfahren zur oxidation von manganspezies in einer behandlungsvorrichtung sowie behandlungsvorrichtung
KR1020247001641A KR20240021303A (ko) 2021-06-16 2022-06-15 처리 디바이스에서 망간 종을 산화시키기 위한 방법 및 처리 디바이스
TW111122141A TW202305185A (zh) 2021-06-16 2022-06-15 在處理裝置中氧化錳物質的方法及處理裝置
PCT/EP2022/066248 WO2022263483A1 (en) 2021-06-16 2022-06-15 Method for oxidizing manganese species in a treatment device and treatment device
JP2023577756A JP2024522777A (ja) 2021-06-16 2022-06-15 処理デバイス内でマンガン種を酸化するための方法及び処理デバイス
BR112023026219A BR112023026219A2 (pt) 2021-06-16 2022-06-15 Método de oxidação de espécies de manganês em um dispositivo de tratamento e dispositivo de tratamento
CN202280048589.5A CN117693611A (zh) 2021-06-16 2022-06-15 在处理装置中氧化锰物质的方法及处理装置
MX2023015333A MX2023015333A (es) 2021-06-16 2022-06-15 Metodo para oxidar especies de manganeso en un dispositivo de tratamiento y dispositivo de tratamiento.

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EP21179866.5A EP4105362A1 (de) 2021-06-16 2021-06-16 Verfahren zur oxidation von manganspezies in einer behandlungsvorrichtung sowie behandlungsvorrichtung

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WO2024223646A1 (en) 2023-04-25 2024-10-31 Atotech Deutschland GmbH & Co. KG Apparatus and method for conducting electrolysis and electrode unit for such an apparatus

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US4911802A (en) * 1988-03-09 1990-03-27 Macdermid, Incorporated Conversion of manganate to permanganate
EP0396252A1 (de) * 1989-05-05 1990-11-07 Macdermid Incorporated Elektrochemische Regenerierung von alkalischer Permanganat-Ätzlösung
US5062930A (en) * 1990-07-24 1991-11-05 Shipley Company Inc. Electrolytic permanganate generation
JPH0417688A (ja) * 1990-05-08 1992-01-22 Mitsui Eng & Shipbuild Co Ltd 電極板シート
US5660712A (en) * 1995-06-07 1997-08-26 Carus, Iii; Paul Electrolytic production of potassium permanganate using a cationic membrane in an electrolytic cell
WO2001090442A1 (en) 2000-05-19 2001-11-29 Atotech Deutschland Gmbh Cathode for electrochemical regeneration of permanganate etching solutions
CN1498291A (zh) 2002-02-06 2004-05-19 新光电气工业株式会社 电解再生处理装置
WO2013030098A1 (en) 2011-08-26 2013-03-07 Atotech Deutschland Gmbh Method for treating of plastic substrates and a device for an at least partial regeneration of a treatment solution
CN109628948A (zh) 2019-01-04 2019-04-16 苏州创峰光电科技有限公司 再生装置
WO2020162772A1 (en) * 2019-02-08 2020-08-13 Felicitas A-C - Radosław Droździk Electrolyzer for hydrogen and oxygen production

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US3062734A (en) * 1957-01-09 1962-11-06 Carus Chemical Company Electrolytic cell and electrode therefor
US3293160A (en) * 1962-12-19 1966-12-20 E J Lavino & Co Electrolytic manufacture of manganates and/or permanganates
US4006067A (en) * 1973-03-05 1977-02-01 Gussack Mark C Oxidation-reduction process
US4911802A (en) * 1988-03-09 1990-03-27 Macdermid, Incorporated Conversion of manganate to permanganate
EP0396252A1 (de) * 1989-05-05 1990-11-07 Macdermid Incorporated Elektrochemische Regenerierung von alkalischer Permanganat-Ätzlösung
JPH0417688A (ja) * 1990-05-08 1992-01-22 Mitsui Eng & Shipbuild Co Ltd 電極板シート
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US5660712A (en) * 1995-06-07 1997-08-26 Carus, Iii; Paul Electrolytic production of potassium permanganate using a cationic membrane in an electrolytic cell
WO2001090442A1 (en) 2000-05-19 2001-11-29 Atotech Deutschland Gmbh Cathode for electrochemical regeneration of permanganate etching solutions
CN1498291A (zh) 2002-02-06 2004-05-19 新光电气工业株式会社 电解再生处理装置
WO2013030098A1 (en) 2011-08-26 2013-03-07 Atotech Deutschland Gmbh Method for treating of plastic substrates and a device for an at least partial regeneration of a treatment solution
CN109628948A (zh) 2019-01-04 2019-04-16 苏州创峰光电科技有限公司 再生装置
WO2020162772A1 (en) * 2019-02-08 2020-08-13 Felicitas A-C - Radosław Droździk Electrolyzer for hydrogen and oxygen production

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TW202305185A (zh) 2023-02-01
MX2023015333A (es) 2024-02-29
KR20240021303A (ko) 2024-02-16
BR112023026219A2 (pt) 2024-03-05
JP2024522777A (ja) 2024-06-21
CN117693611A (zh) 2024-03-12

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