EP0845549B1 - Verfahren zur Entfernung von Eisen-II-Ionen aus sauren Verzinnung-Elektrolyten und Vorrichtung dafür - Google Patents

Verfahren zur Entfernung von Eisen-II-Ionen aus sauren Verzinnung-Elektrolyten und Vorrichtung dafür Download PDF

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Publication number
EP0845549B1
EP0845549B1 EP19970119907 EP97119907A EP0845549B1 EP 0845549 B1 EP0845549 B1 EP 0845549B1 EP 19970119907 EP19970119907 EP 19970119907 EP 97119907 A EP97119907 A EP 97119907A EP 0845549 B1 EP0845549 B1 EP 0845549B1
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EP
European Patent Office
Prior art keywords
electrolyte
methanesulfonic acid
acid
iron
tinning
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
EP19970119907
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English (en)
French (fr)
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EP0845549A1 (de
Inventor
Dieter Hahn
Uwe Dreissigacker
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.)
Rohm and Haas Electronic Materials Deutschland GmbH
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LeaRonal GmbH
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Publication date
Priority claimed from EP96119294A external-priority patent/EP0863229A1/de
Application filed by LeaRonal GmbH filed Critical LeaRonal GmbH
Priority to EP19970119907 priority Critical patent/EP0845549B1/de
Publication of EP0845549A1 publication Critical patent/EP0845549A1/de
Application granted granted Critical
Publication of EP0845549B1 publication Critical patent/EP0845549B1/de
Priority to GR20010400671T priority patent/GR3035823T3/el
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Expired - Lifetime legal-status Critical Current

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Classifications

    • 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

Definitions

  • the present invention relates to a method for removing ferrous ions from acidic tin baths such as tinning electrolytes which are commonly used in the tinplating industry, and a tinning electrolyte recovery plant wherein this method is employed. More particularly, the present invention relates to a method by which ferrous ions are separated from acidic tinning electrolytes in the form of insoluble ferrous methanesulfonate or ferrous phenolsulfonate in the cold.
  • the Fe content can be kept constant in processes operating with hydrogen halide by adding soluble sodium ferrocyanide to form a ferrocyanide of iron.
  • a different approach has to be taken for tinplating baths operating with a polysulfonic acid, an acidic fluoroborate or MSA electrolyte. In such baths, a lowering of the Fe content has been attempted by diluting the bath with fresh electrolyte and discarding part of the old one, or by plating out tin with tungsten electrodes, and then by re-dissolving it.
  • Such processes are very expensive.
  • a process of precipitating iron with organic or inorganic acids has not been successful because the high proton concentration of the electrolyte causes a precipitation of the acids as such or contributes to redissolving the formed iron compound.
  • a chemical separation of iron by means of a pH change has also proven to be unsatisfactory.
  • divalent tin hydroxide Sn(OH) 2 precipitates, while iron only precipitates at pH values of around 3. Even in the best case, only mixtures of Sn(OH) 2 and an iron salt such as ferrous oxalate were obtained.
  • US-A-5 057 290 discloses processes and apparatus for the closed-loop regeneration of spent hydrochloric acid pickle liquors by recovering ferrous chloride from the spent pickle liquors at very low temperatures.
  • this patent does not relate to the recovery of tinning electrolytes and is not concerned with the particular necessity of separating stannous and ferrous ions in such an electrolyte.
  • the present invention wishes to avoid the above-mentioned problems involved with prior art methods for removing Fe ions from tin electrolytes, particularly from electrolytes used as tinplating baths. Moreover, the present invention aims at providing such a separation method which is reliable, inexpensive, provides a good separation performance and can be operated by personnel without specific education. Furthermore, the method should be suitable for the treatment of large amounts of electrolyte, particularly MSA-containing electrolyte. It would be especially advantageous if the method was also suitable for electrolytes containing a mixture of MSA and sulfuric acid.
  • a further object underlying the present invention is to provide a recovery plant for tinning electrolytes which allows the separation of ferrous ions from iron-containing tin electrolytes on the basis of MSA and, optionally, sulfuric acid.
  • the present invention provides:
  • a method for separating ferrous ions from an iron-containing tinning electrolyte on the basis of methanesulfonic acid or phenolsulfonic acid comprising the following steps:
  • the method according to the present invention further comprises the steps of:
  • a step (f) may be provided which comprises recycling of the recovered concentrated electrolyte from step (c) into the original tinning electrolyte or a tin dissolving station.
  • subject-matter of the present invention is:
  • a recovery plant for tinning electrolytes on the basis of methanesulfonic acid which comprises:
  • the above recovery plant further comprises a device for recovering methanesulfonic acid or phenolsulfonic acid from said iron-containing precipitate such as an ion exchanger and/or a device for washing the obtained precipitate with a cold mixture of water and methanesulfonic acid or phenolsulfonic acid.
  • a device for recovering methanesulfonic acid or phenolsulfonic acid from said iron-containing precipitate such as an ion exchanger and/or a device for washing the obtained precipitate with a cold mixture of water and methanesulfonic acid or phenolsulfonic acid.
  • a method for separating ferrous ions from an iron-containing tinning electrolyte on the basis of methanesulfonic acid (or phenolsulfonic acid, the same applies hereinafter) is provided.
  • the tinning electrolyte can be any solution suitable for the electrodeposition (plating) of tin on other metals, particularly iron or iron alloys. Such electrolytes are commonly used in the tinplating industry.
  • the tinning electrolyte in the present invention should be on the basis of methanesulfonic acid, i.e. it should contain an aqueous acidic solution mainly consisting of methanesulfonic acid.
  • one or more further acids may be present as well.
  • a particularly suitable tinning electrolyte for use in the present invention is Ronastan® TP containing about 20 g/l Sn, 25 to 100 g/l MSA, 20 g/l H 2 SO 4 and 7% w/v of additives (organic compounds, e.g. antioxidants).
  • the pH value of this electrolyte is around 0.8 at room temperature.
  • tinning and tinplating electrolytes are either operated with soluble or insoluble anodes.
  • Soluble anodes are made of metallic tin, while insoluble anodes consist of e.g. iridium or another inert metal.
  • the latter case usually requires an additional tin dissolving station to bring metallic tin into the dissolved state.
  • the thus obtained solution containing stannous ions is then transferred into the tinplating bath.
  • the expression "tinning electrolyte” should be understood here as including both a tinning or tinplating electrolyte with soluble and insoluble anodes. In the latter case it is, however, more advantageous to recirculate the recovered electrolyte into the tin dissolving station rather than into the tinning electrolyte itself.
  • the MSA dissolves part of the iron out of the steel ribbon or sheet, which accumulates in the tinning electrolyte.
  • Typical iron content values in a tinning electrolyte after some time in use are 10 - 25 g/l Fe.
  • MSA is bound in the electrolyte. If part of the electrolyte is removed and replaced with fresh electrolyte, as was the industrial practice in the state of the art, relatively large amounts of expensive MSA must be supplemented to maintain the acid content of the electrolyte. This is disadvantageous both from an economical and ecological point of view.
  • One of the objects of the invention therefore is to find a convenient method for recovering the methanesulfonic acid from its ferrous salt so that it may be reused in a tinning electrolyte.
  • the invention comprises a multi-step method which is essentially based on the different solubilities of tin methanesulfonate and ferrous methanesulfonate in the cold, which were heretofore unknown.
  • a concentrated tin and iron-containing electrolyte containing 0.75 mols/l (corresponding to approx. 75 g/l) or more methanesulfonic acid, more preferably 150 g/l or more is provided.
  • concentration tin and iron-containing electrolyte means any electrolyte wherein the concentration of methanesulfonic acid and, preferably, also of tin and iron is higher than in a normal electrolyte used for tinning or tinplating.
  • Such a concentrated electrolyte can be prepared by concentrating a normal tinning electrolyte to about 50% of its original volume or less, more preferably 40% or less, most preferably about 1/3.
  • This concentration can be carried out by conventional means, e.g. by applying a vacuum, by distillation or by a combination thereof. Particularly preferable is a cautious heating of the electrolyte to about 40°C under a pressure of about 2130 Pa (16 Torr).
  • Increasing the concentration, particularly the MSA concentration serves to lower the freezing point of the electrolyte.
  • Conventional electrolytes for tin plating processes have an MSA concentration of about 2.5 - 10% by weight.
  • the freezing point of e.g. a solution containing about 20 g tin methanesulfonate, 12 g iron as methanesulfonate and 7% w/v Ronastan® additives would be around -1 to -5°C in static conditions. If the concentration of free MSA in the electrolyte is increased to 15 - 18%, the freezing point is lowered even more. Agitating the solution lowers the freezing point still further.
  • the concentrated electrolyte used in step (a) can also be provided just by adding methanesulfonic acid to a regular tinning electrolyte, without a concentration process.
  • MSA is commercially available as a 70% aqueous solution having a freezing point of about -60°C. However, in view of the high costs of methanesulfonic acid, this is a less preferred embodiment of the invention.
  • the most favorable way to prepare a concentrated tin and iron-containing electrolyte containing 0.75 mols/l or more methanesulfonic acid is to concentrate a commercial tinning electrolyte.
  • the addition of further methanesulfonic acid can optionally be performed before or during the cooling (step (b)).
  • the freezing point of the concentrated electrolyte can be decreased.
  • the electrolyte is stirred during the cooling process by conventional means.
  • a 0.75 mols/l or higher concentration of methanesulfonic acid in the electrolyte preferably about 1 mol/l or more, is favorable in view of the desirable lowering of the freezing point on the one hand and overall costs on the other.
  • the MSA contributes to a better crystallization of the ferrous methanesulfonate.
  • the concentrated tin and iron-containing electrolyte as provided in step (a) is an electrolyte on the basis of methanesulfonic acid or phenolsulfonic acid and may, optionally, contain further acids such as sulfuric acid, and additives.
  • This concentrated electrolyte is cooled in step (b) to temperatures at which an insoluble Fe-salt precipitates. These temperatures depend on the exact state and composition of the electrolyte. Typically, the electrolyte is cooled to temperatures of about 0°C or less.
  • an insoluble iron salt precipitates which essentially consists of ferrous methanesulfonate or phenolsulfonate and, optionally, other ferrous salts such as ferrous sulfate.
  • concentration of tin methanesulfonate in the precipitate is fairly small, about 2% by weight or less, and may, in a preferable embodiment of the invention, be further reduced by washing the ferrous methanesulfonate crystals with a cold mixture of water and MSA (about 25% by volume), step (d).
  • step (c) the iron-containing precipitate is separated from the concentrated electrolyte by conventional means, preferably by centrifugation or filtration techniques. Most preferable is centrifugation.
  • the concentrate still contains approx. 7% of the original Fe concentration, whereby account has been taken for the volume change.
  • step (e) which is a further preferred embodiment of the present invention, the methanesulfonic acid is recovered from said iron-containing precipitate, e.g. by means of ion exchange.
  • the recovered methanesulfonic acid may be reused to provide the electrolyte used in step (a) or for other purposes, e.g. to be supplemented into a tinning electrolyte.
  • a step (f) may be additionally provided which comprises the recycling of the concentrated electrolyte into the original tinning electrolyte or a tin dissolving station.
  • the present invention allows a complete method for recovering a Fe-containing tinning electrolyte by removing the undesirable iron component and recycling the valuable tin and MSA component.
  • the present invention provides a recovery plant for tinning electrolytes on the basis of methanesulfonic acid, which is suitable for conducting the above process.
  • This plant may comprise:
  • the above apparatus according to the present invention further comprises a device for washing the obtained precipitate with a cold mixture of water and methanesulfonic acid or phenolsulfonic acid.
  • Ronastan® TP-Sn-electrolyte (Fa. Rasselstein) were concentrated to 1200 ml by cautious distillation under vacuum.
  • the concentrated electrolyte was poured into a glass reactor and put into a methanol bath.
  • the methanol bath was gradually cooled by adding dry ice.
  • the original electrolyte had an acid content (MSA) of 55 g/l, a content of ferrous ions of 10 g/l and a content of stannous ions of 18-19 g/l.
  • MSA acid content
  • the respective values were 165 g/l acid, 33 g/l Fe and 55 g/l Sn.
  • the final liquid electrolyte had a concentration of 1.5 g/l Fe and 65 g/l Sn and an acid content of about 255 g/l. This concentrated recovered electrolyte was diluted to an Fe concentration of 0.5 g/l and then reused in the original tinning electrolyte.
  • the solid ferrous methanesulfonate crystals were dissolved in warm water and passed through an acidic ion exchanger to recover MSA in very good yields.

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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)
  • Electrolytic Production Of Metals (AREA)
  • Manufacture And Refinement Of Metals (AREA)

Claims (11)

  1. Verfahren zur Abtrennung von Eisen(II)ionen aus einem eisenhaltigen Verzinnungselektrolyten auf Basis von Methansulfonsäure oder Phenolsulfonsäure, umfassend die folgenden Schritte:
    (a) Bereitstellen eines konzentrierten zinn- und eisenhaltigen Elektrolyten, der 0,75 mol/ℓ oder mehr Methansulfonsäure oder Phenolsulfonsäure enthält,
    (b) Rühren und Kühlen des konzentrierten Elektrolyten auf Temperaturen, bei denen ein unlösliches Fe-Salz ausfällt,
    (c) Abtrennen des unlöslichen Niederschlags, um einen Elektrolyten mit einer reduzierten Eisenkonzentration wiederzugewinnen.
  2. Verfahren gemäss Anspruch 1, das mindestens einen der folgenden Schritte zusätzlich umfasst:
    (d) Waschen des unlöslichen Niederschlags mit einer kalten Mischung aus Wasser und Methansulfonsäure oder Phenolsulfonsäure,
    (e) Wiedergewinnen der Methansulfonsäure oder Phenolsulfonsäure aus dem Niederschlag mittels Ionenaustausch.
  3. Verfahren gemäss Ansprüchen 1 oder 2, zusätzlich umfassend einen Schritt (f), der die Rückführung des wiedergewonnenen konzentrierten Elektrolyten aus Schritt (c) in den ursprünglichen Verzinnungselektrolyten oder eine Station zum Zinnauflösen umfasst.
  4. Verfahren gemäss einem der vorhergehenden Ansprüche, wobei der Elektrolyt Methansulfonsäure oder eine Mischung aus Methansulfonsäure und Schwefelsäure als ansäuerndes Mittel enthält.
  5. Verfahren gemäss einem der vorhergehenden Ansprüche, wobei der konzentrierte zinn- und eisenhaltige Elektrolyt, der in Schritt (a) verwendet wird, durch Aufkonzentrieren eines Verzinnungselektrolyten auf 1/3 seines ursprünglichen Volumens mittels Destillation im Vakuum und optional Zugabe von Methansulfonsäure oder Phenolsulfonsäure hergestellt wird.
  6. Verfahren gemäss einem der vorhergehenden Ansprüche, wobei in Schritt (b) der Elektrolyt auf Temperaturen von 5°C oder weniger gekühlt wird.
  7. Verfahren gemäss einem der vorhergehenden Ansprüche, wobei die Konzentration von Methansulfonsäure oder Phenolsulfonsäure im zinn- und eisenhaltigen Elektrolyten, der in Schritt (a) verwendet wird, 1 mol/ℓ oder mehr beträgt.
  8. Verfahren gemäss einem der vorhergehenden Ansprüche, wobei der Elektrolyt auf Methansulfonsäure basiert.
  9. Wiedergewinnungsanlage für Verzinnungselektrolyten auf Basis von Methansulfonsäure oder Phenolsulfonsäure, umfassend:
    eine Vorrichtung zum Aufkonzentrieren des Elektrolyten, um einen konzentrierten zinn- und eisenhaltigen Elektrolyten auf Basis von Methansulfonsäure oder Phenolsulfonsäure zu erhalten,
    eine Vorrichtung zum Kühlen und Rühren des konzentrierten Elektrolyten auf Temperaturen, bei denen ein unlösliches Fe-Salz ausfällt,
    optional ein Versorgungsmittel zur Zufuhr einer Lösung aus Methansulfonsäure oder Phenolsulfonsäure in den konzentrierten Elektrolyten,
    eine Vorrichtung zur Abtrennung des eisenhaltigen Niederschlags aus dem konzentrierten Elektrolyten,
    Leitungen zur Rückführung des gewonnenen konzentrierten Elektrolyten in den ursprünglichen Verzinnungselektrolyten oder eine Station zum Zinnauflösen.
  10. Wiedergewinnungsanlage gemäss Anspruch 9, die zusätzlich eine Vorrichtung zur Wiedergewinnung der Methansulfonsäure oder Phenolsulfonsäure aus dem eisenhaltigen Niederschlag umfasst.
  11. Wiedergewinnungsanlage gemäss Anspruch 9, die zusätzlich eine Vorrichtung zum Waschen des erhaltenen Niederschlags mit einer kalten Mischung aus Wasser und Methansulfonsäure oder Phenolsulfonsäure und einen Ionenaustauscher zur Wiedergewinnung der Methansulfonsäure oder Phenolsulfonsäure aus dem eisenhaltigen Niederschlag umfasst.
EP19970119907 1996-12-02 1997-11-13 Verfahren zur Entfernung von Eisen-II-Ionen aus sauren Verzinnung-Elektrolyten und Vorrichtung dafür Expired - Lifetime EP0845549B1 (de)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP19970119907 EP0845549B1 (de) 1996-12-02 1997-11-13 Verfahren zur Entfernung von Eisen-II-Ionen aus sauren Verzinnung-Elektrolyten und Vorrichtung dafür
GR20010400671T GR3035823T3 (en) 1996-12-02 2001-04-30 Method for removing ferrous ions from acidic tinning electrolytes and tinning electrolyte recovery plant using the same

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP96119294A EP0863229A1 (de) 1996-12-02 1996-12-02 Verfahren zur Entfernung von Eisen-II Ionen aus sauren Zinn-Elektrolyten und Vorrichtung zur Durchführung des Verfahrens
EP96119294 1996-12-02
EP19970119907 EP0845549B1 (de) 1996-12-02 1997-11-13 Verfahren zur Entfernung von Eisen-II-Ionen aus sauren Verzinnung-Elektrolyten und Vorrichtung dafür

Publications (2)

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EP0845549A1 EP0845549A1 (de) 1998-06-03
EP0845549B1 true EP0845549B1 (de) 2001-02-14

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EP19970119907 Expired - Lifetime EP0845549B1 (de) 1996-12-02 1997-11-13 Verfahren zur Entfernung von Eisen-II-Ionen aus sauren Verzinnung-Elektrolyten und Vorrichtung dafür

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Publication number Priority date Publication date Assignee Title
JPH06346299A (ja) * 1993-06-11 1994-12-20 Kawasaki Steel Corp 錫めっき液の回収再生方法

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EP0845549A1 (de) 1998-06-03

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