Patent Application
20140158528
The present invention relates to an installation for continuously electroplating a plurality of elongated metal elements with another metal.
Installations for continuously electroplating a plurality of elongated metal elements with another metal are widely known and used in the art.
For example, EP-A1-0 297 178 of applicant, discloses an installation for electroplating a plurality of steel wires. The steel wires function as cathode and a soluble anode provides the metal to be coated on the steel wires.
As a matter of another example, U.S. Pat. No. 5,478,457 discloses an apparatus for the continuous electrolytic plating of wire-shaped objects. The wires follow a zigzag path of travel past a succession of anodes and cathodes. There is sliding contact between the cathodes and the wires. The anodes may have channel-shaped recesses through which the wires are running. Holes are made in the bottom of the anodes to allow flow of the electrolyte.
GB-A-2 067 223 and US-Al -2002/0011419 disclose an electro-deposition apparatus for electroplating a film on a single planar substrate.
There is a general trend in the art to increase the number of elongated metal elements to be plated from twenty to thirty-six, forty, and even more. This large-scale mass production allows to reduce the investment and maintenance cost per elongated element.
However, there are also drawbacks associated with the increased number of metal elements. Indeed, it has become a real challenge to obtain an equal and homogeneous coating on all the elongated elements. An equal coating means that all the elongated elements have the same average thickness of coating or the same weight of the other metal. A homogeneous coating means that there is no thickness variation in the coating over the circumference of the elongated elements.
The problem is complex and complexity increases with increasing number of elongated elements. Various parameters are supposed to play a role.
There is the type of anode: soluble or inert anode. The form and dimensions can play a part. If soluble, also the amount of anodes can play a part.
There is the type of electrolyte and the concentration of the electrolyte.
There is the flow of the electrolyte through the bath: homogeneous, laminar, presence or absence of turbulences, . . .
There is the current density.
There is the position of the pumps circulating the electrolyte. Indeed, the position of the pumps at one side of the installation is not symmetric and is expected to negatively influence the eventual coating weight on the elongated elements. An elongated element running close to the pump experiences another electrolyte flow than an elongated element running most remote from the pump.
As the elongated elements function as cathodes, the voltage level on the elongated elements, or better, the absence of differences thereof, may influence the eventual coating weight on the elongated elements.
It is an object of the invention to avoid the drawbacks of the prior art.
It is another object of the invention to reduce the differences in coating weight over the plurality of elongated metal elements.
It is also an object of the invention to avoid displacing the pumps for circulating the electrolyte.
According to the invention, there is provided an installation for continuously electroplating a plurality of elongated metal elements with another metal. The installation comprises a plurality of elongated metal elements to be plated. The elongated metal elements function as cathodes. The installation further comprises a bath of an electrolyte wherein the elongated metal elements are immersed and are travelling, one adjacent and parallel to another one, along a rectilinear path. The bath comprises a collector space positioned under the elongated metal elements for receiving the electrolyte. The bath further comprises an anode and a distribution plate between the collector space and the elongated metal elements. The distribution plate has a multiplicity of openings for allowing flow of an electrolyte. The installation has a pump for circulating the electrolyte in the bath in a direction from the collector space through the distribution plate to the elongated metal elements.
The collector space causes first flow losses to the flow of the electrolyte. The distribution plate has a multiplicity of openings for allowing the flow of the electrolyte. These openings in the distribution plate cause second flow losses to the flow of the electrolyte. Each of the second flow losses through the distributor plate are at least five times, preferably more than ten times, most preferably more than hundred times, greater than the first flow losses in the collector space.
One way to determine the degree and amount of flow losses is to control the velocity or speed of the electrolyte, amongst others by the cross-section. Indeed according to Darcy's law, the flow losses are proportional to the square value of the average speed of the liquid. According to the same law, the flow losses are inversely proportional to the hydraulic diameter of the medium. With a given value of the pump height, the speed of the liquid is higher for a small cross-section than for a big cross-section.
The collector space has a first cross-section for allowing the flow of the electrolyte and the distribution plate has a multiplicity of openings allowing the flow of the electrolyte from the collector space towards the elongated elements.
The openings in the distribution plate have a second cross-section which is at least three times, and preferably at least ten times, and most preferably much more times, smaller than the first cross-section.
The functioning of the invention will be further explained with reference to the drawings, particularly with reference to
The elongated metal elements may be steel wires, steel cords, steel strands, steel strips or steel ropes.
The other metal to be coated on the elongated metal elements may be zinc, tin, nickel, copper, or alloys thereof. Noble metals such as gold, silver, platinum are not excluded either.
The elongated metal elements function as cathode, the electrical charge is transmitted to the elongated metal elements through driving or guiding rolls or wheels which are negatively charged.
The number of elongated metal elements running in parallel to each other and to be coated simultaneously can vary from twenty to forty and more.
The distribution plate is different from the anode.
The distribution plate is preferably a flat plate and does not provide channel like structures for each separate elongated element.
Due to the functioning of the distribution plate, there is no need to relocate the pump, e.g. somewhat centrally under the bath. A central location under the bath will make repair and maintenance of the pump more cumbersome.
Steel wires 12 run parallel and rectilinear with respect to each other in an electrolyte bath 14. An anode 16, soluble or not, is installed under the wires 12. The steel wires function as cathode. Ions leave the anode 16 and travel through the electrolyte towards the negatively loaded steel wires 12.
A collector space 17 is arranged below the anode 16. A circulation pump 18 circulates electrolyte from the collector space 17 over or through the anode 16 towards the steel wires 12 and the surface of the electrolyte bath 14. An amount of electrolyte is overflowing the bath 14 at upstream and downstream side and is recuperated (not shown).
As the circulation pump 18 is located at one side of the installation, the flow of the electrolyte in the neighbourhood of the steel wires 12′ which are close to the pump 18 may be completely different than the flow of the electrolyte in the neighbourhood of the steel wires 12″ which are most remote from the pump 18. The inventors have noticed that these differences may negatively influence the homogeneity and equality of coating on the steel wires 12. After having discovered this, the challenge was to make as uniform as possible the flow of electrolyte around each and every steel wire 12, 12′,12″.
Steel wires 21 run parallel to each other in an electrolyte bath 22. An anode 23, soluble or not, is installed under the wires 21. The steel wires 21 function as cathode. Ions leave the anode 23 and travel through the electrolyte towards the negatively loaded steel wires 21.
A collector space 24 is arranged below the anode 23. A circulation pump 25 circulates electrolyte from the collector space 24 over or through the anode 23 towards the steel wires 21 and the surface of the electrolyte bath 22. An amount of electrolyte is overflowing the bath 22 at upstream and downstream side and is recuperated (not shown).
The main difference with the prior art installation 10 is the presence of a distribution plate 26, different from the anode 23, located between the collector space 24 and the anode 23. This distribution plate 26 has a plurality of small openings which present a high resistance to the electrolyte flowing through. The flow losses of the electrolyte through the openings of the distribution plate are so high in comparison with the flow losses of the electrolyte in the collector space 24 that the losses of the electrolyte in the collector space 24 can be neglected.
The main principle of this functioning is explained again in
The total electrical resistance going from the left side of electrical scheme 30 towards left upper point 36′ is almost the same as the total electrical resistance going from the left side of the electrical scheme 30 towards right upper point 36″. The reason is that the values of the electrical resistances Rc are to be neglected in comparison with values of the electrical resistances Rh.
Returning back to
As already mentioned low losses in the collector space 24 are realized by having a relatively great cross-section. Having a smooth inner surface may also contribute to reduce the losses. Smooth transitions from the pump to the collector space 24 may avoid turbulences and also reduce the amount of flow losses.
In comparison with the prior art, the total losses of the electrolyte flow from the pump to the elongated elements may be higher due to the presence of the distributor plate. As a result, a higher pump height may be necessary.
The distribution plate 26 may be made of any material chemically resistant against the used chemicals in the electrolyte.
The distribution plate may have a thickness varying from 1 mm to 30 mm, e.g. from 2 mm to 20 mm.
Any type of opening (square, rectangular, circular, hexagonal . . . ) can be used. If circular the openings in the distribution plate may have a diameter varying between 3 mm to 20 mm diameter.
The invention can be practiced for soluble and non-soluble anodes and for various types of metal and for electrolytes. In contrast with the distribution plate 26, the anode is made of an electrically conductive material such as stainless steel.
A distribution plate is applied to a copper plating installation of forty steel wires. The electrolyte can be copper-citrate, copper-amine, copper-tartrate, copper-sulfate, copper-pyrophosphate, copper fluoroborate or copper cyanide.
The anode is formed by a soluble copper anode lying on a supporting plate. The cathode current density varies between 1 and 20 A/dm2. The speed of the steel wires may vary between 10 m/min and 150 m/min.
Test Results
The variation of coating weight between wires, defined as
is typically reduced with 1%.
10 electroplating installation according to the prior art
12, 12′, 12″ steel wires
14 electrolyte bath
16 anode
17 collector space
18 circulation pump
20 electroplating installation according to the invention
21, 21′, 21″ steel wires
22 electrolyte bath
23 anode
24 collector space
25 circulation pump
26 distribution plate
30 electrical scheme
32 collector space resistance Rc
34 distribution plate hole resistance Rh
36′ left upper point
36″ right upper point
| Number | Date | Country | Kind |
|---|---|---|---|
| 11173037.0 | Jul 2011 | EP | regional |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/EP2012/058073 | 5/3/2012 | WO | 00 | 1/6/2014 |
