Electrogalvanization

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Electrogalvanization is a galvanization process in which a layer of zinc is bonded to steel in order to protect against corrosion. The process involves electroplating, running a current of electricity through a saline/zinc solution with a zinc anode and steel conductor. Zinc electroplating maintains a dominant position among other electroplating process options, based upon electroplated tonnage per annum. According to the International Zinc Association, more than 5 million tons are used yearly for both Hot Dip Galvanizing and Electroplating.[1] The Plating of Zinc was developed at the beginning of the 20th century. At that time, the electrolyte was cyanide based. A significant innovation occurred in the 60’s, with the introduction of the first acid chloride based electrolyte.[2] The 80’s saw a return to alkaline electrolytes, only this time, without the use of cyanide. Compared to hot dip galvanizing, electroplated zinc offers these significant advantages:

  • Lower thickness deposits to achieve comparable performance
  • Broader conversion coating availability for increased performance and color options
  • Brighter, more aesthetically appealing, deposits

History[edit]

Zinc plating was developed and continues to evolve, to meet the most challenging corrosion protection, temperature and wear resistance requirements. Electroplating of zinc was invented in 1800 but the first bright deposits were not obtained until the early 1930s with the alkaline cyanide electrolyte. Much later, in 1966, the use of acid chloride baths improved the brightness even greater. The latest modern development occurred in the 80’s, with the new generation of alkaline, cyanide-free zinc. Recent European Union directives (ELV/RoHS/WEEE)[3] prohibit automotive, other original equipment manufacturers (OEM) and electrical and electronic equipment manufacturers from using hexavalent chromium (CrVI). These directives combined with increased performance requirements by the OEM, has led to an increase in the use of alkaline zinc, zinc alloys and high performance trivalent passivate conversion coatings.

Processes[edit]

The corrosion protection afforded by the electrodeposited zinc layer is primarily due to the anodic potential dissolution of zinc versus iron (the substrate in most cases). Zinc acts as a sacrificial anode for protecting the iron (steel). While steel is close to ESCE= -400 mV (the potential refers to the standard Saturated calomel electrode (SCE), depending on the alloy composition, electroplated zinc is much more anodic with ESCE= -980 mV. Steel is preserved from corrosion by cathodic protection. Conversion coatings (hexavalent chromium (CrVI) or trivalent chromium (CrIII) depending upon OEM requirements) are applied to drastically enhance the corrosion protection by building an additional inhibiting layer of Chromium and Zinc hydroxides. These oxide films range in thickness from 10 nm for the thinnest blue/clear passivates to 4 µm for the thickest black chromates.

Additionally, electroplated zinc articles may receive a topcoat to further enhance corrosion protection and friction performance.[4]

The modern electrolytes are both alkaline and acidic:

Alkaline electrolytes[edit]

Cyanide electrolytes[edit]

Contain sodium cyanide (NaCN) and sodium hydroxide (NaOH). All of them utilize proprietary brightening agents. Zinc is soluble as a cyanide complex Na2Zn(CN)4 and as a zincate Na2Zn(OH)4. Quality control of such electrolytes requires the regular analysis of Zn, NaOH and NaCN. The ratio of NaCN : Zn can vary between 2 to 3 depending upon the bath temperature and desired deposit brightness level.The following chart illustrates the typical cyanide electrolyte options used to plate at room temperature:

Cyanide bath composition
Zinc Sodium hydroxide Sodium cyanide
Low cyanide 6-10 g/L (0.8-1.3 oz/gal) 75-90 g/L (10-12 oz/gal) 10-20 g/L 1.3-2.7 oz/gal)
Mid cyanide 15-20 g/L (2.0-2.7 oz/gal) 75-90 g/L (10-12 oz/gal) 25-45 g/L (3.4-6.0 oz/gal)
High cyanide 25-35 g/L (3.4-4.7 oz/gal) 75-90 g/L (10-12 oz/gal) 80-100 g/L (10.70- 13.4 oz/gal)

Alkaline non-cyanide electrolytes[edit]

Contain zinc and sodium hydroxide. Most of them are brightened by proprietary addition agents similar to those used in cyanide baths. The addition of quaternary amine additives contribute to the improved metal distribution between high and low current density areas. Depending upon the desired performance, the electroplater can select the highest zinc content for increased productivity or lower zinc content for a better throwing power (into low current density areas). For ideal metal distribution, Zn metal evolutes between 6-14 g/L (0.8-1.9 oz/gal) and NaOH at 120 g/L (16 oz/gal). But for the highest productivity, Zn metal is between 14-25 g/L (1.9-3.4 oz/gal)and NaOH remains at 120 g/L (16 oz/gal). Alkaline Non Cyanide Zinc Process containg lower concentration zinc metal concentration 6-14 g/L (0.8-1.9 oz/gal) or higher zinc metal concentration 14-25 g/L (1.9-3.4 oz/gal)provides superior plate distribution from high current density to low current density or throwing power when compared to any acidic baths such as choride based (Low ammonium chloride, Potassium chloride /Ammonium Chloride) - or (non-ammonium chloride, potassium chloride/Boric acid) or sulfate baths

Acidic electrolytes[edit]

High speed electrolytes[edit]

Dedicated to plating at high speed in plants where the shortest plating time is critical (i.e. steel coil or pipe that runs at up to 200 m/min (ft/min). The baths contain zinc sulfate and chloride to the maximum solubility level. Boric acid may be used as a pH buffer and to reduce the burning effect at high current densities. These baths contain very few grain refiners. If one is utilized, it may be sodium saccharine.

Traditional electrolytes[edit]

Initially based on ammonium chloride, options today include ammonium, potassium or mixed ammonium/potassium electrolytes. The chosen content of zinc depends on the required productivity and part configuration. High zinc improves the bath’s efficiency (plating speed), while lower levels improve the bath’s ability to throw into low current densities. Typically, the Zn metal level varies between 20 and 50 g/L (2.7-6.7 oz/gal). The pH varies between 4.8 and 5.8 units. The following chart illustrates a typical all potassium chloride bath composition:

Traditional acid bath composition
Parameters Value in g/L (oz/gal)
Zinc 40 g/l (5.4 oz/gal)
Total chloride 125 g/l (16.8 oz/gal)
Anhydrous zinc chloride 80 g/l (10.7 oz/gal)
Potassium chloride 180 g/l (24.1 oz/gal)
Boric acid 25 g/l (3.4 oz/gal)

Typical grain refiners include low soluble ketones and aldehydes. These brightening agents must be dissolved in alcohol or in hydrotrope. The resultant molecules are co-deposited with the zinc to produce a slightly leveled, very bright deposit. The bright deposit has also been shown to decrease chromate/passivate receptivity, however. The result is a reduction in the corrosion protection afforded.

References[edit]

  • JJ. Duprat (Coventya), Mike Kelly (Coventya), « Dedicated processes for electroplating on fasteners », Fasteners Technology International, August 2010, p. 56-60
  • L. Thiery, F. Raulin : « Advances in trivalent passivates on zinc and zinc alloy », Galvanotechnik 98(4) (2007) 862-869
  • Modern Electroplating, 5th Edition
  • H. Geduld, « Zinc Plating », Finishing Publications, 1988
  • El Hajjami, M.P. Gigandet, M. De Petris-Wery, J.C. Catonné, J.J. Duprat, L. Thiery, N. Pommier, F. Raulin, B. Starck, P. Remy : « Characterization of thin Zn-Ni alloy coatings electrodeposited on low carbon steel », Applied Surface Sciences, 254, (2007) 480-489
  • N. Pommier, L. Thiery, M.P. Gigandet, M. Tachez : « Electrochemical study of the degradation of an organomineral coating: polarization resistance and electrochemical impedance spectroscopy measurements », Ann. Chim. Sci. Mat, 1998, 23, 397-400
  • K. Wojczykowski, «New Developments in Corrosion Testing: Theory, Methods and Standards», Surfin proceedings 2010, Grand Rapids, MI, session 7
  • A. Jimenez, «Membrane Technology for electroplating processes», Surfin proceedings 2010, Grand Rapids, MI, session 4