EP2173927B1 - Vorrichtung und verfahren zur elektrolytischen verzinnung von stahlstreifen mithilfe einer nichtlöslichen anode - Google Patents

Vorrichtung und verfahren zur elektrolytischen verzinnung von stahlstreifen mithilfe einer nichtlöslichen anode Download PDF

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Publication number
EP2173927B1
EP2173927B1 EP08826511A EP08826511A EP2173927B1 EP 2173927 B1 EP2173927 B1 EP 2173927B1 EP 08826511 A EP08826511 A EP 08826511A EP 08826511 A EP08826511 A EP 08826511A EP 2173927 B1 EP2173927 B1 EP 2173927B1
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EP
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Prior art keywords
zone
tin
installation
electrolyte solution
anode
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EP08826511A
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English (en)
French (fr)
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EP2173927A2 (de
Inventor
Philippe Barbieri
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Clecim SAS
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Siemens VAI Metals Technologies SAS
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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
    • C25D3/00—Electroplating: Baths therefor
    • C25D3/02—Electroplating: Baths therefor from solutions
    • C25D3/30—Electroplating: Baths therefor from solutions of tin
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
    • C25D17/00—Constructional parts, or assemblies thereof, of cells for electrolytic coating
    • C25D17/002—Cell separation, e.g. membranes, diaphragms
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
    • C25D21/00—Processes for servicing or operating cells for electrolytic coating
    • C25D21/16—Regeneration of process solutions
    • C25D21/18—Regeneration of process solutions of electrolytes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
    • C25D7/00—Electroplating characterised by the article coated
    • C25D7/06—Wires; Strips; Foils
    • C25D7/0614—Strips or foils
    • C25D7/0628—In vertical cells

Definitions

  • the invention generally relates to the insoluble anode electrolytic tinning of steel strips, and more particularly to an insoluble anode electrolytic tinning process and the installation for its implementation.
  • tinplate tin-plated mild steel in the field of food packaging where it is known under the name of "tinplate”.
  • the manufacture of tinplate is generally made from coils ("coils") of mild steel or ultra-soft, which previously undergo a hot rolling operation, followed by a cold rolling operation. At the end of these rolling operations, steel strips of a few tenths of a millimeter thick are obtained. These strips are then annealed, passed after annealing in a cold rolling mill ("skin passed"), degreased, etched and tinned by an electrolytic tinning process (or “electro-tinning”). Tinning is typically followed by finishing operations such as coating remelting, passivation, and oiling.
  • Electro-tinning is a method of electroplating tin on a metal substrate, which consists in establishing the transfer of stannous Sn 2+ ions to the band to be coated according to the equilibrium: Sn 2+ + 2e - ⁇ Sn deposited
  • This reaction involves the availability of stannous ions in the bath.
  • the bath has an acid for lowering the pH and increasing the electrical conductivity. It also contains additives that contribute, inter alia, to stabilize the stannous ions by preventing them from oxidizing, and to prevent the formation of stannic oxide sludge caused by the oxidation of these stannous ions.
  • the first category of processes includes processes using a soluble anode, or so-called “soluble anode” processes
  • the second category of processes includes processes using a insoluble anode, or so-called “insoluble anode” processes.
  • soluble anode electro-tinning processes are used in electrolytic tinning installations which mainly use high purity tin anodes (that is to say anodes comprising at least 99.85% by weight of tin), which dissolve during the electrolysis and charge the bath in stannous Sn 2+ ions.
  • FIG. figure 1 An example of a "soluble anode” electro-tinning installation known to those skilled in the art is shown in FIG. figure 1 . It is a vertical electro-tinning installation 1, in which a strip to be coated 2 dives into a coating tank 3 (or electro-deposition tank) by winding on two conducting rollers 41, 42 and a bottom roll 5, thus forming a downstream strand 21 and a rising strand 22. The two conducting rollers 41, 42 feed the strip 2 with electrical current.
  • the tin soluble anodes 61, 62 are disposed on either side of the falling 21 and up 22 strands of the steel strip 2 to be coated. This steel strip 2 is connected to the negative pole (represented by the symbol "-" on the Fig.
  • an electric power generator (not shown on the figure 1 ) an electric power generator (not shown on the figure 1 ), and the soluble anodes 61, 62 are connected to the positive pole (represented by the symbol "+" on the figure 1 ) of this generator, thus constituting the anode.
  • the anodes 61, 62 and the descending 21 and 22 strands of the steel strip 2 are partially immersed in an electrolyte solution 7 (or electrolyte).
  • insoluble anode electro-tinning processes are therefore distinguished from those called “soluble anode” in that they lead to the formation of acid in the electrolytic bath correlatively to its depletion of tin. These continuous changes therefore require regeneration, the bath also continues.
  • the patent US5,312,539 proposes another "insoluble anode" tinning process, which uses an anionic membrane dialysis cell and a separate tin dissolution unit in which tin is supplied as an oxide directly dissolved in the acid, or as a tin anode, which is dissolved electrolytically.
  • Such a method has certain disadvantages, and in particular the cost of tin oxide and the need to create a strong concentration gradient on either side of the membrane, which imposes the implementation of a unit of concentration.
  • the necessary membrane surface (of the order of several thousand m 2 for continuous tinning installations of steel strips) makes the industrial application very problematic. .
  • the subject of the present invention is therefore an electro-tinning process and an installation for its implementation which remedy the drawbacks of the prior art, by the use of an electrodialysis membrane or cationic electrolysis membrane in the device. tin dissolution.
  • cationic electrodialysis membrane is meant, in the sense of the present invention, a cation permeable membrane and which is typically used in an electrodialysis process.
  • a cationic electrolysis membrane is understood to mean a membrane permeable to cations typically used in a process membrane electrolysis, but which can advantageously be used in the electrodialysis process according to the invention because of its robustness and its ability to withstand higher current densities than a cationic electrodialysis membrane.
  • the tin anode and the insoluble cathode are separated by a cationic electrodialysis or electrolysis membrane, defining a cathode zone integrating the cathode and an anode zone incorporating the tin anode, and a recirculation circuit of the electrolytic solution connects the electroplating tank to the anode zone of the tin dissolution reactor.
  • the presence of a cationic electrodialysis membrane in the dissolution reactor between the soluble anode of tin and the insoluble cathode allows the H + ions of the electrolytic solution to pass through the membrane, from the anode zone to the zone cathodic, while the Sn 2+ ions produced at the anode remain predominantly in the anode zone of the reactor.
  • the electrolytic solution contained therein is then recharged with stannous ions, and can then be directed back to the coating tank.
  • the recirculation circuit of the electrolytic solution between the electroplating tank and the anode zone of the tin dissolution reactor comprises an oxygen degassing tank, which is arranged upstream of the dissolution reactor in the direction of circulation of the electrolyte in this recirculation circuit.
  • This degassing tank makes it possible to effectively eliminate the gaseous oxygen formed at the insoluble anode of the coating tank.
  • the plant according to the invention also further comprises a degassing circuit of the electrolytic solution contained in the cathode zone of the tin dissolution reactor, this degassing circuit incorporating a hydrogen degassing tank.
  • the acid AH is advantageously chosen from sulphonic acids.
  • sulphonic acids that may be used according to the present invention, mention may be made especially of methanesulfonic acid and phenol-sulphonic acid.
  • the preferred sulfonic acid is methanesulfonic acid.
  • the SnA 2 compound will therefore advantageously be a tin sulphonate corresponding to the preferred sulphonic acids according to US Pat. invention: tin phenol sulphonate or tin methane sulphonate.
  • the present invention also relates to a process for the electrolytic tinning of a continuous steel strip in at least one plating tank filled with an electrolytic solution which comprises an acid AH and stannous Sn 2+ ions under form of a compound SnA 2 with A denoting an acid function, said tinning process employing a non-soluble anode and the metal strip constituting a cathode which are immersed in the electrolytic solution and between which a potential difference is applied, and the SnA 2 compound from a tin dissolution reactor, which comprises an insoluble cathode and a tin anode, between which a potential difference is applied.
  • the electro-tinning installation (or electrolytic tinning installation) represented on the figure 1 is a soluble anode electro-tinning installation 1 of the state of the art, which was previously described in the reference to the prior art which precedes.
  • the electro-tinning installation (or electrolytic tinning installation) represented on the figure 2 is an insoluble anode electro-tinning installation 1 of the state of the art, which was previously described in the reference to the prior art which precedes.
  • FIG 3 is represented a block diagram of an example of installation according to the invention, wherein the strip to be coated and an insoluble anode 60 are partially immersed in an electroplating tank (or coating tank) containing an electrolytic solution (or electrolyte) containing Sn 2+ stannous ions as a SnA compound 2 and an acid AH, A being an acidic radial.
  • an electroplating tank or coating tank
  • electrolytic solution or electrolyte
  • the compound SnA 2 comes from a tin dissolution reactor 10, which comprises an insoluble cathode 120 and a soluble tin anode 160, which are immersed in a tank 130 also containing the same electrolytic solution as the coating tank 30
  • a cationic electrodialysis or electrolysis membrane 140 is disposed between the electrodes 120, 160 of the reactor 10, so that the reservoir 130 of the reactor 10 is divided into a cathode zone 1200 containing the insoluble cathode 120 and an anode zone 1600 containing the soluble anode 160.
  • the anode 160 of the reactor 10 is constituted by tin granules 161 contained in a basket 162 (called “tin dissolution basket”).
  • This basket 162 filled with granules 161 is connected to the positive pole (represented by the symbol “+” on the figure 3 ) a source of electrical power (not shown on the figure 3 ), the tin aggregates 161 playing the role of soluble anode.
  • the insoluble cathode 120 of the tin dissolution reactor 10 is connected to the negative pole (represented by the symbol "-" on the figure 3 ) from the same source of electrical power.
  • a soluble anode 160 it is also possible to use, in the tin dissolution reactor 10 of the plant according to the invention, an anode in massive form (not shown on the Figures 3 to 5 ).
  • the electro-tinning installation represented on the figure 3 comprises, in addition to the coating tank 30 and the tin dissolution reactor 10, an oxygen degassing tank 210 and a hydrogen degassing tank 310.
  • the oxygen degassing tank 210 is part of a recirculation circuit 200 of the electrolyte connecting the coating tank 30 and the anode zone 1600 of the dissolution reactor 10, the degassing tank 210 being disposed upstream of the reactor of dissolution (10) in the recirculation direction of the electrolyte in the circuit 200.
  • the hydrogen degassing tank 310 is part of a recirculation circuit 300 of the electrolyte contained in the cathode zone 1200 of the dissolution reactor 10, in which the electrolyte is subjected to degassing of the hydrogen in a hydrogen degassing tank 310.
  • An electrolyte depleted of stannous ions is thus obtained, part of which is taken from the coating tank 30, and is then subjected to degassing of the oxygen gas in the degassing tank 210 before being introduced into the anode zone 1600 of the dissolution reactor 10.
  • the electrolytic dissolution of the tin granules 161 ensures the production of Sn 2+ stannous ions, which thanks to the selective permeability of the cationic membrane 140 remain mainly in the vicinity of the anode.
  • CMX-S cationic membrane
  • the cationic membrane 140 has a selective permeability that allows the transfer of ions H + to the cathode 120 and the maintenance of Sn 2+ ions near the anode 160.
  • the electrolyte of the anodic zone 1600 thus recharged with stannous ions can then be recovered and directed again towards the coating tank 30.
  • the H + ions present in the anodic zone 1600 cross the cationic membrane 140 because of the field
  • the H + ions recovered in the cathode zone 1200 of the reactor 10 are then recombined with the anions A - , in order to reform the acid AH.
  • a dissolution reactor 10 comprising a tank 130 filled with electrolyte, which may be of cylindrical shape and which is separated in two by a cationic electrodialysis membrane 140, which may also be cylindrical shape, thereby defining a central anode zone 1600 comprising the soluble anode 160, and an external cathode zone 1200 comprising the cathode 120.
  • the cylindrical shape of the reservoir 130 and the cationic membrane 140 is given here by way of example. But, the reservoir 130 and the cationic membrane 140 may also be of parallelepipedal shape.
  • the cathode 120 is connected to the negative pole of a source of electric current (represented by the symbol "-" on the figure 4 ) and the anode 160 is connected, in its upper part, to the positive pole (represented by the symbol “+” on the figure 4 ) from the same source of electrical power.
  • the lower 1621 and middle 1622 areas of the dissolution basket 162 of the anode 160 are both made of non-electrically conductive material.
  • an electrically nonconductive material usable according to the invention for producing the lower zones 1621 and median 1622 of the basket 162 of the soluble anode 160 plastics, and composites such as the polyester resins and the polyesters, are recommended. polymers coated steels.
  • the upper region 1623 for supplying tin granules 161 is made of an electrically conductive material.
  • an electrically conductive material that can be used according to the invention to produce the basket 162 of the soluble anode 160, mention may notably be made of stainless steel.
  • the lower zone 1621 immersed in the electrolyte comprises a mesh 163 comprising a plastic mesh net adapted to retain the tin granules, ie between 0.05 and 0.50 mm, and preferably between 0.1 and 0, 30 mm.
  • This net is supported by the envelope of the basket which has openings for contacting the electrolyte, which are at least 50 times wider than the mesh of the net openings (dashed on the figure 4 ) are formed in the casing of the basket 162.
  • the median zone 1622 includes a recovery trough 164 of the regenerated electrolyte, this trough being supplied via a trellis 165 (identical to that 163 of the lower zone 1621) and openings (in dashed lines on the trunk). figure 4 ) formed in the envelope of the basket 162 (identical to those of the lower zone 1621).
  • the median zone 1622 is wetted by the electrolytic solution of the tank 130 circulating in the circuit 200.
  • the upper zone 1623 comprises a filling hopper 166 in tin granules 161, which is connected to the positive pole of the power supply source and which transmits the electric dissolution current into the bed of tin pellets. via the contact surfaces between the tin granules and the electrically conductive material hopper.
  • the lower zone 1621 of the basket 162, which is immersed in the electrolyte, is surrounded by a cationic membrane 140 of circular shape.
  • This cationic membrane 140 is advantageously supported by at least one plastic net, which ensures the rigidity of the membrane 140.
  • the electrolyte to be treated is introduced into the lower zone 1621 of the basket by intake pipes 201 at a pressure sufficient to allow it to overflow into the recovery trough 164 of the median zone 1622.
  • the electric current ensures the dissolution of said granules 161 and the acid is charged with Sn ++ ions which remain close to the anode 160.
  • the electrolyte and reloaded tin is recovered at the level of the trough 164, before being returned to the coating tank 30 via the return lines 202.
  • dissolution reactor 10 which comprises a plurality of soluble anodes 160 each having a basket 162 filled with tin granules 161, each basket 162 being surrounded by a membrane cationic 140 circular.
  • a feed device 400 in granules 161 serves hoppers 166 of all baskets 162 of the dissolution reactor 10.
  • This device 400 may be a treadmill or vibrating, or non-electrically conductive pipes.
  • the device 400 operates intermittently according to a given signal by a granule level detection device in the hoppers 166, so as to maintain a constant level of granules 161 in the basket 162.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Electroplating Methods And Accessories (AREA)
  • Electrolytic Production Of Metals (AREA)

Claims (16)

  1. Vorrichtung (1) zur elektrolytischen Verzinnung eines kontinuierlich durchlaufenden Stahlbandes (2), wobei diese Anlage (1) Folgendes umfasst:
    • mindestens einen Behälter zur elektrolytischen Abscheidung (30), der mit einer Elektrolytlösung gefüllt wird, die eine Säure AH und Zinnionen Sn2+ in Form einer SnA2-Verbindung enthält, wobei A eine Säurefunktion bezeichnet, und der eine unlösliche Anode (60), die in die Elektrolytlösung des Behälters zur elektrolytischen Abscheidung (30) getaucht wird, und eine Kathode (20), die aus dem kontinuierlich in der Elektrolytlösung des Behälters zur elektrolytischen Abscheidung (30) durchlaufenden Band (2) besteht, umfasst, und
    • mindestens einen Reaktor zum Lösen des Zinns (10), der eine unlösliche Kathode (120) und mindestens eine lösliche Zinnanode (160) umfasst,
    dadurch gekennzeichnet, dass die Zinnanode (160) und die unlösliche Kathode (120) durch eine kationische Elektrodialyse- oder Elektrolysemembran (140) getrennt werden, die einen kathodischen Bereich (1200) begrenzt, der die Kathode (120) beinhaltet, und einen anodischen Bereich (1600), der die Zinnanode (160) beinhaltet, und weiterhin dadurch gekennzeichnet, dass diese Vorrichtung zur Verzinnung (1) zudem einen Kreislauf zur Rezirkulation (200) der Elektrolytlösung zwischen dem Behälter zur elektrolytischen Abscheidung (30) und dem anodischen Bereich (1600) des Zinnlösereaktors (10) umfasst.
  2. Vorrichtung (1) nach Anspruch 1, dadurch gekennzeichnet, dass der Kreislauf zur Rezirkulation (200) der Elektrolytlösung zwischen dem Behälter zur elektrolytischen Abscheidung (30) und dem anodischen Bereich (1600) des Zinnlösereaktors (10) einen Behälter zur Sauerstoffentgasung (210) umfasst, der in Fließrichtung des Elektrolyts in diesem Rezirkulationskreislauf (200) gesehen vor dem Lösereaktor (10) angeordnet ist.
  3. Vorrichtung (1) nach Anspruch 1 oder 2, dadurch gekennzeichnet, dass sie zudem einen Kreislauf (300) zur Entgasung der im kathodischen Bereich (1200) des Zinnlösereaktors (10) enthaltenen Elektrolytlösung umfasst, wobei der Entgasungskreislauf (300) einen Behälter zur Wasserstoffentgasung (310) beinhaltet.
  4. Vorrichtung (1) nach einem der vorangehenden Ansprüche, dadurch gekennzeichnet, dass die lösliche Zinnanode (160) in Form von Zinngranulat (161), das in einem Einsatz (162) enthalten ist, vorliegt.
  5. Vorrichtung (1) nach Anspruch 4, dadurch gekennzeichnet, dass der Einsatz (162) drei verschiedene übereinander liegende Teile umfasst:
    - einen unteren Bereich (1621), der in die im Gefäß (130) des Lösereaktors (10) enthaltene Elektrolytlösung eintaucht,
    - einen mittleren Bereich (1622) zur Rückführung des Elektrolyten, der an ihn angrenzend oberhalb des unteren Bereichs (1621) liegt und nicht in den im Gefäß (130) des Lösereaktors (10) enthaltenen Elektrolyten eintaucht, aber von der Elektrolytlösung befeuchtet wird, wenn sie in dem Kreislauf (200) in Zirkulation versetzt wird, und
    - einen oberen, trockenen Bereich (1623) zum Zuführen von Zinngranulat (161) und zum Übertragen des elektrischen Stroms zum Lösen, wobei dieser Bereich an ihn angrenzend über dem mittleren Bereich (1622) liegt.
  6. Vorrichtung (1) nach Anspruch 5, dadurch gekennzeichnet, dass der untere Bereich (1621) und der mittlere Bereich (1622) des Einsatzes (162) aus einem elektrisch nicht leitenden Material bestehen.
  7. Vorrichtung (1) nach Anspruch 6, dadurch gekennzeichnet, dass das elektrisch nicht leitende Material des unteren Bereichs (1621) und des mittleren Bereichs (1622) des Einsatzes (162) ein Kunststoff oder ein Verbundstoff ist, der aus der Gruppe der verstärkten Polyesterharze oder der polymerbeschichteten Stähle gewählt wird.
  8. Vorrichtung (1) nach einem der Ansprüche 5 bis 7, dadurch gekennzeichnet, dass der obere Bereich (1623) des Einsatzes (162) aus einem elektrisch leitenden Material ausgeführt ist.
  9. Vorrichtung (1) nach einem beliebigen der Ansprüche 5 bis 8, dadurch gekennzeichnet, dass der untere Bereich (1621) des Einsatzes (162) umfasst:
    - ein Gitter (163) mit einem Kunststoffnetz, dessen Maschenweite zwischen 0,05 mm und 0,5 mm beträgt, und
    - ein Gehäuse zum Tragen des Gitters (163), das eine oder mehrere Öffnungen zum Inkontaktbringen des Granulats (161) mit der Elektrolytlösung.
  10. Vorrichtung (1) nach einem beliebigen der Ansprüche 5 bis 9, dadurch gekennzeichnet, dass der mittlere Bereich (1622) des Einsatzes (162) umfasst:
    - ein Gitter (165) mit einem Kunststoffnetz, dessen Maschenweite zwischen 0,05 mm und 0,5 mm beträgt, und
    - eine Wanne zum Zurückführen (164) der Elektrolytlösung, wobei diese Wanne (164) über das Gitter (165) mit Elektrolytlösung gefüllt wird.
  11. Vorrichtung (1) nach einem beliebigen der vorangehenden Ansprüche, dadurch gekennzeichnet, dass der Lösereaktor (10) eine Vielzahl löslicher Anoden (160) umfasst, wobei jede dieser Anoden (160) einen Trichter (166) umfasst und von einer kationischen Elektrodialyse- oder Elektrolysemembran (140) umgeben ist.
  12. Vorrichtung (1) nach Anspruch 11, dadurch gekennzeichnet, dass sie eine Zuführvorrichtung (400) für das Granulat umfasst, die die Trichter (166) der Anoden (160) intermittierend beschickt.
  13. Vorrichtung (1) nach Anspruch 12, dadurch gekennzeichnet, dass die Zuführvorrichtung (400) für das Granulat (161) ein Rüttel- oder Förderband ist oder aus elektrisch nicht leitenden Rohrleitungen besteht.
  14. Verfahren zur elektrolytischen Verzinnung eines Stahlbandes (20), das kontinuierlich in mindestens einem Behälter zur elektrolytischen Abscheidung (30) durchläuft, der mit einer Elektrolytlösung gefüllt ist, die eine Säure AH und Zinnionen Sn2+ in Form einer SnA2-Verbindung enthält, wobei A eine Säurefunktion bezeichnet, wobei dieses Verzinnungsverfahren mindestens eine nicht lösliche Anode (60) einsetzt und das Metallband (20) eine Kathode darstellt, die beide in die Elektrolytlösung eintauchen und zwischen denen eine Potenzialdifferenz angelegt wird, und die SnA2-Verbindung aus einem Zinnlösereaktor (10) kommt, der eine unlösliche Kathode (120) und eine Zinnanode (1602) umfasst, zwischen denen eine Potenzialdifferenz angelegt wird,
    dadurch gekennzeichnet, dass die Konzentration der Säure AH in der Elektrolytlösung des Beschichtungsbehälters (30) konstant gehalten wird, indem die folgenden Schritte ausgeführt werden:
    a) im Zinnlösereaktor (10) wird zwischen der Zinnanode (160) und der unlöslichen Kathode (120) eine kationische Elektrodialysemembran (140) angeordnet, die so einen kathodischen Bereich (1200), der die unlösliche Kathode (120) beinhaltet, und einen anodischen Bereich (1600) begrenzt, und
    b) ein Teil der Elektrolytlösung wird zwischen dem Behälter zur elektrolytischen Abscheidung (30) und dem anodischen Bereich (1600) des Zinnlösereaktors (10) in Zirkulation versetzt.
  15. Verfahren nach Anspruch 14, dadurch gekennzeichnet, dass die im Beschichtungsbehälter (30) entnommene Elektrolytlösung einer Sauerstoffentgasung unterzogen wird, bevor sie in den anodischen Bereich (1600) des Reaktors eingeführt wird.
  16. Verfahren nach Anspruch 14 oder 15, dadurch gekennzeichnet, dass ein Teil der im kathodischen Bereich des Lösereaktors (10) enthaltenen Elektrolytlösung rezirkuliert wird und einer Wasserstoffentgasung unterzogen wird.
EP08826511A 2007-07-26 2008-06-09 Vorrichtung und verfahren zur elektrolytischen verzinnung von stahlstreifen mithilfe einer nichtlöslichen anode Not-in-force EP2173927B1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR0705487A FR2919311B1 (fr) 2007-07-26 2007-07-26 Installation et procede pour l'etamage electrolytique de bandes d'acier, mettant en oeuvre une anode insoluble.
PCT/FR2008/000789 WO2009013398A2 (fr) 2007-07-26 2008-06-09 Installation et procédé pour l'étamage électrolytique de bandes d'acier, mettant en oeuvre une anode insoluble

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EP2173927A2 EP2173927A2 (de) 2010-04-14
EP2173927B1 true EP2173927B1 (de) 2011-02-09

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EP (1) EP2173927B1 (de)
AT (1) ATE498025T1 (de)
DE (1) DE602008004917D1 (de)
ES (1) ES2360020T3 (de)
FR (1) FR2919311B1 (de)
WO (1) WO2009013398A2 (de)

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US9157160B2 (en) 2013-08-22 2015-10-13 Ashworth Bros., Inc. System and method for electropolishing or electroplating conveyor belts

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CN112111762A (zh) * 2020-09-26 2020-12-22 深圳市海里表面技术处理有限公司 高光洁度料带镀锡工艺及其制得的料带

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US4181580A (en) * 1973-11-28 1980-01-01 Nippon Steel Corporation Process for electro-tin plating
JP2559935B2 (ja) * 1991-12-20 1996-12-04 日本リーロナール株式会社 不溶性陽極を用いた錫又は錫ー鉛合金電気めっきの方法及び装置
US5312539A (en) * 1993-06-15 1994-05-17 Learonal Inc. Electrolytic tin plating method

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9157160B2 (en) 2013-08-22 2015-10-13 Ashworth Bros., Inc. System and method for electropolishing or electroplating conveyor belts

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DE602008004917D1 (de) 2011-03-24
FR2919311B1 (fr) 2009-10-09
WO2009013398A2 (fr) 2009-01-29
EP2173927A2 (de) 2010-04-14
FR2919311A1 (fr) 2009-01-30
WO2009013398A3 (fr) 2009-03-12
ATE498025T1 (de) 2011-02-15

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