DE102009013164A1 - Method for partial galvanization of elongated products in electrolytes of electrolytic cell, which is associated to a bath current source, comprises placing the product for the treatment in the electrolytic cell between anode and cathode - Google Patents

Abstract

The method for partial galvanization of elongated products (1) in electrolytes (12) of electrolytic cell (4), which is associated to a bath current source, comprises placing the product for the treatment in the electrolytic cell that consists of a cathode (6) and an anode (5), between the anode and the cathode in electrical contact-less manner and rotating in bath current source with a revolution around its longitudinal axis. The anode, the cathode and/or the product arranged plane parallel to each other are moved for electrolyte exchange and/or for gas dissolution from the surface. The method for partial galvanization of elongated products (1) in electrolytes (12) of electrolytic cell (4), which is associated to a bath current source, comprises placing the product for the treatment in the electrolytic cell that consists of a cathode (6) and an anode (5), between the anode and the cathode in electrical contact-less manner and rotating in bath current source with a revolution around its longitudinal axis. The anode, the cathode and/or the product arranged plane parallel to each other are moved for electrolyte exchange and/or for gas dissolution from the surface in cyclic- or vibration-like manner. The galvanization of the product is carried out in electrolyte in which metal electrochemically deposited on the product is constant. The surface area of the product is cathodically and anodically or reversibly treated in a revolution. A metallization of the cathode of the electrolytic cell is prevented through placing the product near to the cathode during galvanization. The metallization of the cathode is prevented through electric conductive metal layer on the surface of the cathode that is not metallizable. Low cathodic current density emerges through an active surface of the cathode that is larger than the momentary active anodic surface of the product. A metal deposition on the cathode is prevented through cooling the cathode at a surface temperature below the process temperature of the electrolyte. The metallization of the surface of the cathode is prevented through the use of electrolytes in the area of the cathode that consists of metalion that is separated from the cathode. For preventing the metal deposition on the cathode through an ion selective and fluid tight membrane, the electrolyte in the area of the cathode as catolyte that consists of metalions is separated from process electrolyte that consists of metalions and exists in the product and the anode. The requirement of energy for cooling the cathode through an ion-permeable and heat-insulation layer as heat insulator is prevented against the electrolyte present at process temperature. The electrolytic cell is operated with the bath current source as direct current source, unipolar pulse current source, bipolar pulse current source or with technical alternating current. The electrolytic cell is electrochemically treated and/or galvanized through shielding the areas of the product against the anode. The partial electrochemical surface of the product to be treated is pre-selected and admitted by adjustable shielding. The product is partially galvanized by limited protection lacquer or safety caps. The product is promoted on supports by the electrolytic cell in a plane that lies plane-parallel to the plane and parallel electrodes. The product is pressed by a rotating band or a pendulum device in the area of the cathode against the support and is transported by spacer through the electrolytic cell. The guiding of the gas emerging during the treatment is accelerated through an oblique position transverse to transport direction of the plane of the electrode and the plane of the product. Gas emerging through a vibration-like or cyclic movement of the electrodes and/or the product in any direction is supported by the surface. During loading and unloading the product in and from the electrolytic cell, an electrode is sectionally engaged and/or disengaged corresponding to filling the electrolytic cell, where the flow of the bath current source is adapted to energy storage at the surface of the goods to be treated. The orifice plates shield the area of the electrodes. The required size of the bath current is diminished in given throughput through a series control of two electrolytic cells. The metallization limit is influenced through blending or partial blending. The single drives promote each product through the electrolytic cell. The product positioned in a dip bath between the electrodes is rotatably moved around the longitudinal axis. The radially changed product is promoted in axial direction through the electrolytic cell. The product to be metalized is dissolved in the used electrolyte. During galvanization, the metallization of the cathode is prevented through placing the product near the cathode. An independent claim is included for a device for partial galvanization of elongated products in electrolytes of electrolytic cell.

Description

The Invention relates to electroplating and other electrochemical Treatments of good, especially etching, electropolishing, Pickling and cleaning. The process finds application in continuous flow systems and dipping facilities. The estate is z. B. to rod-shaped Parts. These are z. B. elongated cylinders as engine valves or piston rods of vehicle shock absorbers or cylinders for actuators. To increase the wear resistance becomes such metallic good at least partially on the surface electrolytically provided with a particularly abrasion-resistant layer, z. B. with hard chrome or with a dispersion material. This coating As a rule, it is very much at the deposition thickness in the relevant area of the material evenly. In a partial galvanization Furthermore, the transition from the deposition area to the area with very little or no metal deposition almost stepped.

The electrochemical cleaning, in particular descaling, pickling and degreasing done cathodically and anodically, with requirements to a partial treatment usually does not exist. The same applies to the electrochemical anodic etching from good. Because these methods according to the invention technically are easier to implement, the invention will be predominantly on Example of technically demanding electroplating described. However, the invention is also fully applicable to Electrochemical etching, electropolishing, heating and Cleaning applicable. These latter methods are described in the Succession, the description of the invention summarized as Referred to pretreatments.

The publication DE 1 103 103 describes a device for the galvanic chrome plating of the outer surfaces of elongated material, in particular of poppet valve shafts. For this purpose, tubular open-form anodes are used, in which the material to be treated is placed centrically. The cathodic power connection takes place via a graduated metal core. An insulating body limits the non-electroplated surface of the material and the metal core. A disadvantage is the required fastening of the goods to the metal core and the insulating body and the centric introduction into the tubular anode. In a partial chrome plating of both ends of the goods, a protective lacquer is additionally applied and then removed again. Such tubular anodes require for uniformly thick deposition of the metal at the periphery of the statically arranged in the anode material on the one hand over its entire axial length precise centric positioning in the anode and on the other hand, a gleichaktiv aktiva surface of the entire insoluble anode. These two conditions are achievable especially with a long rod-shaped Good only with a great deal of technical effort.

In order to avoid an uneven, ie oval, metallisation of cylindrical material having a circular cross section when the cathodically contacted material is not exactly centrally positioned in the tubular anode, or when a planar anode is located on only one side of the material or two planar anodes on two sides of the material Good facing are arranged, the good must rotate about its longitudinal axis. Such Galvanisiergesteil describes the invention according to the document DE 25 24 315 , On a frame, the material to be plated is rotatably mounted about its longitudinal axis and rotated by a drive device. By means of power supply devices and one brush each as a high-current rotary contact the cathodic current is transmitted to each rotating Good. Such high-current rotary contacts represent a great technical challenge for trouble-free operation in the atmosphere laden with aerosols of a galvanizing device and in particular in a chromium plating bath with a chromic acid electrolyte. In addition, in this invention the technical complexity for the mechanics of the rotary drive for each good. The disadvantage of the individual high-current rotary contacts and the individual drives for each good to be treated, as well as the cost of loading and emptying the Galvanisiergestelles avoids the in the document DE 196 32 132 C1 described invention. Rod-shaped good, z. B. shock absorber cylinders are to be treated electrochemically to improve the wear and corrosion properties. The material is to be galvanized on the operationally stressed surfaces with hard chrome. The other surface areas should remain uncoated or preferably provided with a very thin electrodeposited chromium layer in comparison to the layer thickness on the claimed surface. This thin layer serves as a protective layer during the electrochemical treatment of the material and / or in subsequent process steps. Before electroplating, the material is cleaned in another electrolyte and optionally electrochemically etched in order to improve the adhesion of the chromium layer.

The electrochemical treatment is carried out according to the document DE 196 32 132 C1 using pliers-like grippers, which are located on a goods carrier. There are several goods, z. B. 25 pieces, at the same time gripped and sunk in a vertical orientation in stationary tubular electrodes or anodes. The material must be positioned exactly centric to avoid oval metallization. The grippers also serve as a high-current contact means for supplying the treatment current to each the estate. This current is in the preferred and economic reasons necessary application of a high current density of z. B. 100 A / dm ² according to the surface of the material to be plated very large, z. B. 250 A per good. Often the available gripping surface on the estate is very small or there is only one threaded connector for gripping and contacting available. This can lead to an inadmissible heating of the gripper and the goods. Furthermore, the gripping of the goods despite a possible wear during continuous use must be such that it is always exactly vertical and remains in this position during treatment. Overall, this requires a special technical effort to the execution of the current-carrying gripper and its contact material with correspondingly high costs and to the device for precise gripping a group of goods to a goods carrier.

each Good or each rod to be treated requires in this invention an individual electrolytic cell consisting of the tubular Electrode and the good. When electroplating this electrode the anode and the surface of the material the cathode. to Compensation u. a. of small geometrical tolerances is one certain anode / cathode spacing required, z. B. 60 mm. At a Bar diameter of z. B. 30 mm then has such a round electrolytic Cell has a diameter of about 150 mm. The center distance of a Group of electrolytic cells must then be for a group of goods in x and y direction be the same size. At only 5x5 cells, the entire electrochemical bath is then at least 0.75 m × 0.75 m in size, plus the space for the required supports and busbars. Overall, this results in a large bathroom, in which a large and very heavy goods carriers of correspondingly strong dimensioned means of transport is to be stored.

All these 25 goods of a goods carrier are electric connected in parallel. At the current of 250 A described above each cell must have a total current of 6250 A in the goods carrier be initiated by further electrical contacts, which u. a. correspondingly large cross sections of the electrical conductors on the product carrier requires a uniform To achieve power distribution to each asset of the group. same for for the electrical connections of the stationary Anodes in the bathroom. in total, this method requires electroplating rod-shaped good big and very heavy mechanical Construction elements of the corresponding electroplating device.

through upper and lower axially adjustable masks, which are elastic Sealants are located in the tubular anodes only the surfaces of the goods released, the intense to be galvanized. Overall, this effort is in accordance with the above invention especially for large good profitable.

Be not centric retraction of the goods in the anodes and / or obliquely oriented Good on the goods carrier there is a risk of destruction of the masks or not completely enclosing the goods. In both cases, it may lead to an impermissible change in the metallization of the good. To avoid this disadvantage in the document DE 198 37 973 C1 proposed radially movable shielding membranes. They are installed in a cage in which they act self-centering. This improves the shield while avoiding destruction of the membranes with inaccurately positioned Good, especially when it is long, z. B. 0.6 m.

task The invention is to provide methods and apparatus for electrochemical Treatment of elongated, broad or even good to describe the disadvantages of the prior art described do not have, in particular, are technically complex High current contacts or high current rotary contacts for electrical contacting of the goods as well as large compared to the dimensions of the goods and heavy goods carriers may not be required. additionally should be in rotationally symmetrical goods one very uniform layer thickness distribution would be reached at the periphery.

Solved The object is achieved by the methods according to the claims 1 and 56 and by the devices according to the claims 28, 76 and 99. The subclaims describe advantageous embodiments the invention.

The Solving these technically demanding tasks according to the invention on the one hand by a momentary only partial treatment of every good and on the other hand by rotation of the rotationally symmetric good during the treatment. Very advantageous for the rotation of the goods no high-current rotary contacts needed. Overall, this results in a very economical electrochemical plant also for small goods, which meets the high technical demands.

The invention provides an electrolytic cell, consisting of preferably planar and stationary electrodes as insoluble anode and as cathode, which in turn are preferably arranged plane-parallel and spaced apart in the electrolyte of the electroplating or electrochemical plant. The long-awkward goods are conveyed with their longitudinal axes lying in a plane through the electrolytic cell, wherein this plane is preferably plane-parallel to the electrodes. The promotion of the rotationally symmetrical good by the electrolytic cell is rotating about its longitudinal axis. Because this is electrically contactless in particular during electroplating, the high-current contacts or high-current rotary contacts required according to the prior art are not required. The good that is between the electrodes acts as an intermediate conductor. This conductor has a much greater electrical conductivity than the first class conductor as the conductor of the second class. The estate concentrates the electric field lines that pass from the anode to the cathode. The side of the rotating material currently facing the anode is currently being treated cathodically. The opposite side of the material, which faces the cathode, is treated anodically at the same time. These alternating polarities are very well suited for the pretreatments. A galvanized material is always metallized on one side only. At the same time the anodic treatment takes place on the other side. This may be electrolytic demetallization or anodic etching, pickling and cleaning. When galvanizing the material anodic current etching or demetalling must be avoided in order to achieve a metallization of the goods in the sum. This is z. B. always the case when the cathodically deposited metal used in the electrolyte is anodically non-releasable. Examples include electrolytes for the deposition of nickel, chromium, hard chrome and precious metals or their alloys. In such electrolytes, the electrically non-contacted material is cathodically metallized on the side facing the anode. On the side of the good, which faces the cathode, anodic gas is formed, for. B. oxygen. By the rotation of the material is a very uniform treatment and deposition on the surface of the entire circumference.

Because always only a part of the rotating material is galvanized results this compared to the prior art with a tubular anode a longer treatment time for each individual good. However, this is not a disadvantage in terms of throughput of goods a plant according to the invention. The throughput is even significantly increased, because in confined spaces many z. B. rod-shaped goods in the electrolytic Cell can be located and treated at the same time. They can be arranged close together or at a distance which makes them practically a wall as an intermediate conductor. By at least one revolution about the longitudinal axis a complete electrochemical treatment throughout Scope of the goods. The rotation also has the big one Advantage that a very even treatment over the entire extent of the goods takes place. Every generatrix of the goods becomes during one revolution the ointment treatment conditions exposed. The same applies to preferably several revolutions of the product in the electrolytic cell and through it.

at Partial galvanization of the goods will become part of the process should not be metallized and currently or constantly the cathode faces anodically treated. This means that one Electrolyte must be used, in which the base metal of the Good or its metallic protective layer does not dissolve anodically. Otherwise, the non-metallizing areas would have to be electrically isolated by means of z. As caps, paints or other Insulators. In most cases, the deposited metal is also suitable as metallic protective layer, e.g. As nickel or chromium.

• • Kühlung der Kathode auf eine Temperatur, die wesentlich unterhalb der zur elektrolytischen Abscheidung von Metall erforderlichen Arbeitstemperatur des Elektrolyten Liegt. Als Beispiel sei ein Elektrolyt zur Abscheidung von Hartchrom genannt. Die Arbeitstemperatur des Chromsäurebades beträgt ca. 65°C. In diesem Bad wird bei einer Oberflächentemperatur der Kathode von etwa 20°C und damit auch des Elektrolyten in der Grenzschicht kein Chrom abgeschieden. Die elektrolytische Gegenreaktion ist allein eine Gasbildung, d. h. es wird Wasserstoff gebildet. Auch eine Betriebsart nach dem Stand der Technik verursacht eine erhebliche Gasbildung infolge der geringen Stromausbeute derartiger Metallisierungsbäder. Auch bei einem kathodischen Gut, das sich auf der hohen Arbeitstemperatur des Elektrolyten befindet, kann nur etwa 30% des eingesetzten Stromas zur Metallabscheidung genutzt werden. Die Kühlung der Kathode der elektrolytischen Zelle kann z. B. mittels Kühlwasser mit einer Vorlauftemperatur von z. B. 8°C oder elektrisch mit Peltierelementen erfolgen. Des Kühlwasser kann durch die als Hohlkörper ausgebildete Kathode der elektrolytischen Zelle geleitet werden. Zur Trennung bzw. zur Isolation gegen den auf hoher Temperatur befindlichen Elektrolyten kann die Kathode mit einem Wärmeisolator an oder nahe ihrer Oberfläche versehen sein. Dies kann z. B. ein ionendurchlässiges und gasdurchlässiges Tuch oder dergleichen sein. Ein derartiger poröser Isolator sorgt dafür, dass nur eine sehr kleine Menge von Elektrolyt nahe der Kathode zu kühlen ist.
• • Verwendung eines Elektrolyten im Bereich der Kathode der elektrolytischen Zelle, der keine Metallionen enthält, die auf der Oberfläche der Kathode abgeschieden werden können. Zur Trennung dient hierzu eine ionenselektive und flüssigkeitsdichte Membrane, die den Arbeitselektrolyten der übrigen elektrolytischen Zelle vom Elektrolyten im Bereich der Kathode trennt. Derartige semipermeable Membranen sind für die verbreiteten Elektrolyte verfügbar.
• • Das Metallisieren der Kathode kann auch durch eine Oberfläche derselben vermieden werden, die im Elektrolyten kathodisch beständig ist und auf der das Metall des Elektrolyten nicht abscheidbar ist. Bei einem Hartchrombad ist dies z. B. eine Kathode mit einer Zinnbeschichtung. Auch in diesem Falle wird kathodisch nur Gas als Gegenreaktion gebildet.
• • Verwendung einer aktiven Oberfläche der Kathode, die wesentlich größer ist als die momentan wirksame anodische Oberfläche des Gutes. Zum Beispiel wird eine dreifach größere Kathodenfläche realisiert. Dies hat eine kathodische Stromdichte zur Folge, die nur ein Drittel der Stromdichte am Gut aufweist. Zur elektrolytischen Metallabscheidung ist stets eine bestimmte Mindeststromdichte erforderlich. Ansonsten wird an der Kathode Gas als Gegenreaktion gebildet. Die aktive Oberfläche der Kathode kann so groß gewählt werden, dass die kathodische Mindeststromdichte nicht erreicht wird.

In practice, without inventive measures, metal would also be deposited on the actual cathode of the electrolytic cell, which is electrically connected to the negative terminal of the bath current source, if it is a galvanizing process. This would not only mean a loss of metal to be deposited, but in a short time lead to the uselessness of the electrolytic cell. To avoid metallization of the cathode, the following alternative or combinable measures are provided according to the invention:

• Cooling the cathode to a temperature substantially below the working temperature of the electrolyte required for the electrolytic deposition of metal. An example of this is an electrolyte for the deposition of hard chrome. The working temperature of the chromic acid bath is about 65 ° C. In this bath, no chromium is deposited at a surface temperature of the cathode of about 20 ° C and thus also of the electrolyte in the boundary layer. The electrolytic counter-reaction alone is a gas formation, ie hydrogen is formed. Also, a prior art mode causes significant gas formation due to the low current efficiency of such metallization baths. Even with a cathodic material, which is located on the high working temperature of the electrolyte, only about 30% of the stroma used can be used for metal deposition. The cooling of the cathode of the electrolytic cell may, for. B. by means of cooling water with a flow temperature of z. B. 8 ° C or done electrically with Peltier elements. The cooling water can be passed through the formed as a hollow body cathode of the electrolytic cell. For separation or isolation from the high temperature electrolyte, the cathode may be provided with a heat insulator at or near its surface. This can be z. As an ion-permeable and gas-permeable cloth or the like. Such a porous insulator ensures that only a very small amount to cool electrolyte near the cathode.
• Use of an electrolyte in the region of the cathode of the electrolytic cell, which contains no metal ions, which can be deposited on the surface of the cathode. For separation purposes, an ion-selective and liquid-tight membrane is used, which separates the working electrolyte of the remaining electrolytic cell from the electrolyte in the region of the cathode. Such semipermeable membranes are available for the common electrolytes.
• • The metallization of the cathode can also be avoided by a surface thereof, which is cathodically stable in the electrolyte and on which the metal of the electrolyte is not separable. In a Hartchrombad this z. B. a cathode with a tin coating. Also in this case, only gas is cathodically formed as a backlash.
• Use of an active surface of the cathode which is substantially larger than the currently effective anodic surface of the material. For example, a threefold larger cathode area is realized. This results in a cathodic current density, which has only one third of the current density at Gut. For electrolytic metal deposition always a certain minimum current density is required. Otherwise, gas is formed as a counterreaction at the cathode. The active surface of the cathode can be chosen so large that the cathodic minimum current density is not achieved.

In In practice, there is often the task, especially flat decorative To metallize goods only on the visible side in order to z. B. save precious metal where it is not seen in use or technically not needed. This is suitable not only the described measure for the placement of the goods very close to the cathode, but the invention in general. The one for this According to the invention required arrangement of the electric conductive and anodic resistant in the electrolyte used Good in the electrolytic cell is particularly easy because a rotation of the same is not required. That according to the state the technique usual consuming masking, painting or generally isolating the non-metallizing backside of the goods deleted. The side to be metallized has Direction of the anode. In this orientation that passes through Good the electrolytic cell or it remains there static for the Duration of required exposure time. At the back of the material is anodically formed gas and takes place at the cathode a cathodic gas formation. The gases are through appropriate Suction removed.

According to the invention preferably used planar electrodes. This allows in addition to insoluble Anodes advantageous also the use of soluble anodes as plate anodes or as bulk material in baskets, if non-rotating material is to be galvanized. soluble Anodes are often more cost effective and procedural easier, however, the back of the goods must be protected because the surface is there as well as the soluble one Anode could dissolve.

insoluble Anodes or form anodes, as required by the prior art are, require appropriate chemicals for metal supplementation, Salts or ion generators, but also for rotating Electroplating required according to this invention are. If soluble anodes are the deposited layer from the same metal that makes up the anodes. Consequently, would the metallization on the estate at the momentary anodic Resolve treatment as a result of rotation, d. H. be demetallised.

to Achieving special effects can be used to power the electrolytic cell the known Badstromversorgungsquellen be used.

This are z. B. current sources for direct current, unipolar pulse current or bipolar pulse current. This can z. B. the dispersion of the deposition to be influenced. For hard chrome, the formation of required Microcracks are controlled in the surface. For electrolytic degreasing or cleaning, the anodic and cathodic, the invention is basically for a material rotating in the electrolytic cell. It is alternately treated anodically and cathodically during rotation. In this rough, the electrolytic cell can also be used at a low cost operated alternating current. The change of the two Types of treatment anodic / cathodic z. B. with 50 Hz.

In a good that should be treated only partially, in particular, which should be partially galvanized, the remaining areas of the good by means of z. B. screened shields. For this purpose, it is sufficient that the shields are arranged only on the side of the good, which faces the anode of the electrolytic cell. This significantly simplifies the constructive measures for partial electroplating. The shields can be combined with the supports for rotating rod-shaped material. The non-electroplated surfaces of the material are anodically charged, if they are not shielded against the cathode of the electrolytic cell. Such shields may also be constructed and arranged as described for the region of the anode of the electrolytic cell. Without this shielding of the electric field emanating from the cathode of the electrolytic cell could the material is anodically dissolved at the points which are not to be galvanized, if the base material of the material is not anodically resistant in the electrolyte used. In this case, the material can be first galvanized on all sides for a short time to avoid the technical effort for these cathodic shields. This first thin galvanizing layer then protects the base material against anodic dissolution of the areas of the material which are not to be reinforced during the further galvanizing of the regions of the material which are to be reinforced. The all-round thin electroplating and the partial strengthening of the functional of the areas of the material takes place in the same working container with the same electrolyte. There is no additional process or operation required for this. In the working container, only the conditions for the goods in the initial area are open and run closed in the remaining area of the transport path. Details on all-round electroplating and partial electroplating follow below.

Should in the area of the metallization boundary the transition from the Metallization to the area of this good without metallization axially be very short, z. B. 2 mm, then as a blonde in addition an elastic material can be used. In these the rotating becomes or not rotating Well pressed, causing the Material largely applies to the circumference of the goods. The result is a very abrupt metallization limit.

For axially differently long good can the conditions and / or the diaphragms on the anode side carried out according to conceivable be. In special cases, the areas not to be treated can of the goods also with electrically insulating protective caps or protective varnish and the like.

In a preferred embodiment of the invention is the good, as described, on editions, in particular in a galvanizing process are electrically isolated. Only one-sided treatment or to electroplating good can be pushed through the electrolytic cell or pulled. Rod-shaped rotating and on the circumference very good to be galvanized Good on the electrically isolated pads rolling through the electrolytic Cell promoted. This can be done close to you or z. B. spaced for gas discharge. In the simplest case form the pads an inclined plane on which the round good close to rolls tight.

The Promotion of round good, which should rotate, too by means of at least one over the level of the goods circulating Bandes done. The band is not pressing at the moment balsa galvanizing top against this and bring it promoting in rotation. A similar transport of the goods can be achieved with at least one pendulum thruster become. At the top of the estate in the area of the cathode space the electrolytic cell pushes an elastic driver on the estate and pushes it rolling a short distance in the transport direction. Then the driver lifts off and drives back to where a new lowering and pushing takes place. At least two drivers can phase-shift the good evenly rotate through the electrolytic cell. there It is permanently against the conditions and if necessary against the pressed elastic diaphragm on the metallization. This promotion of the goods can be spaced again or done close to each other.

electrochemical Pretreatments take place in practice partially unipolar z. B. only anodic during etching or electropolishing. Also in the Device according to the invention, the property for this purpose electrically be contacted. Because in this case the contact means in contrast can not be metallized for electroplating, can these in the treatment liquid and against the electrical Field unprotected. According to the invention at least the pages of the editions or of the tracks on which the goods rolls in the working container, as electrically conductive Contact tracks formed. These are with the one pole of the rectifier electrically connected. The other pole is at least one in the Working container arranged electrode as a counter electrode electrically connected. For the pretreatment processes mentioned here the contact tracks are anodic and the counter electrode (s) are cathodic connected.

The Press the rotating belt or the pendulum push devices the rolling or pushed Good against the contact tracks, which An increase in the contact force is effected and a safer electrical contact is made to the good. Compared to that subsequent plating process in another working container or electrolytes, the current density to be used here is low, z. B. only one fifth to one tenth. Therefore, also the to be transmitted and electrically contacted streams small in the pretreatment processes. Special high current contacts for electrical contacting of the goods are therefore not required.

The electrochemical treatment of the elongated material can also be carried out in a horizontal or vertical orientation in an electrolytic cell according to the invention as an immersion bath. It is introduced into this and remains in place during the treatment. There, it remains static in a one-sided treatment or galvanization on the entire circumference, it is placed in place by means of a drive in rotation. Also in this rotary embodiment of the invention will be advantageous No high-current rotary contacts needed.

Well, which is statically arranged in the electrolytic cell is galvanized only on the side facing the anode. The not to be treated side, usually one not in use The bare back is also without electrical insulation not metallized.

at a substantially horizontal alignment of the electrodes and of the goods, the entire device or only the good slightly be inclined transversely to the transport direction to the derivative to assist the gases produced during the electrochemical process.

at In all embodiments of the invention, the electrodes and / or the goods vibrationally or cyclically by means of a movement of goods to be moved. This reduces the diffusion layer on the surfaces and it promotes the detachment of gas bubbles from the surfaces. The electrochemically required electrolyte exchange in the electrolytic cell is opened by the plane-parallel Arrangement of the electrodes and the goods much easier. Of the Electrolyte, the electrolytic cell z. B. in the transport direction flow through unhindered. In contrast, there is an electrolyte exchange in the prior art in tubular anodes, the individually enclose each good, much more complex to realize.

at longer flow systems can be at least one of the two Electrodes, preferably the anode, in the transport direction in electrical be separated from each other separated electrode sections. Corresponding filling with goods when entering and when Extend these Elektrodonabschnitte by means of electrical Switch switched on or off the bath power source. This will be an unnecessary gas formation with the use of electrical Energy avoided. The size of the bath stream will be controlled according to the current need. For undivided electrodes can when entering the first goods and at Extending the last goods from the electrolytic cell also electrically conductive or non-conductive dummies ahead or conveyed to the goods by the conveyor system become. Even so, can the correct electrochemical treatment all goods are controlled. The same applies to Apertures, the unnecessary areas of the electrodes shield.

to Influence of the metallization limit can in this Area individually sized apertures or partial apertures, so-called Soft screens, be arranged. This allows the axial Length from the area of the metallization to the non-metallized one or thin metallized area of the goods very accurately. The partial screens or soft covers allow a gentle, in this case longer way of transition from one treatment condition to another.

The length of a continuous system depends on the procedural parameters according to the required throughput of goods per unit of time. The same applies to the number of electrolytic cells in Tauchbadanlagen. A long pass plant according to the invention may be divided into a plurality of electrolytic cells and arranged in separate and electrically insulated working vessels. in each of the z. B. three working containers can be done a complete treatment of the goods. The throughput is then one third in each area due to the slower transport speed. However, very advantageously, these three electrolytic cells can be electrically connected in series and supplied with treatment current by only a single bath current source. Jade of the three electrolytic cells in this example flows through the same current. This is in contrast to a single correspondingly longer electrolytic cell only one third of the required power. This advantageous series circuit requires a threefold greater output voltage of the bath current source. Overall, the required power remains the same. The smaller power is technically much easier to realize. All electrical conductors have smaller cross sections and the Badstromquelle with larger output voltage and smaller current is cheaper to produce. This advantageous series connection is particularly well suited for the realization of the present invention, because even with an empty part cell, a current flow takes place with formation of gas. On the other hand, according to the state of the art for current flow, there should always be a good in the electrolytic cell in order not to interrupt the serial current flow, which can not be the case at least when moving in and out of goods. For example, for hard chrome plating, it is always necessary to galvanize with large currents for economic reasons. A reduction of the current to z. As a date is therefore very advantageous. This shows the following sizing. According to the prior art are for a typical electrolytic plant z. B. 4000 A at 12 V required. According to the invention, however, can be galvanized at the same large system throughput with only 1000 A and 48 V when the continuous system is divided into four subsystems or sub-cells. The higher voltage is technically problem-free and designing a system for only 1000 A is considerably more cost-effective than a system for 4000 A. Electrical switch contacts can bridge currently unfilled units for energy savings. When entering goods in an empty continuous flow system, ie when continuously filling currently not required system areas, preferably the anode compartment also be shielded by means of controlled apertures or partial apertures in order to avoid a still unnecessary current flow to the cathode. The bath power source is controlled according to the size of its current.

In The electrolytic cell usually contains many goods. These can, as described, by the electrolytic Cell promoted and at the same time be set in rotation, if complete treatment is needed on the perimeter becomes. Especially with immersion baths or vertical flow systems Each good could also be set in rotation by means of a single drive. For horizontal throughput systems, the promotion can These also through individual transport means or individual drives respectively.

The Metallization limit, d. H. the transition from the area of Metallization to the non-metallizing area, is in the Shelf specified very precisely. Especially with a very steep boundary course may be additional treatment limiters to the in the work container located panels and supports required be. These are in the anode space at the respective Metallisierungsgrenze arranged. They are preferably made of an elastic material, who applies to the good and this embraces when it against the Treatment limiter is pressed. This will become the galvanizing side facing the anode, further protected and shielded. The metallization border on the estate can also through individual panels, caps, sleeves and the like or by electrically insulating coatings in front of or on top of Well influenced. Wagon of this required additional operations will be these measures only used in exceptional cases.

The Invention is not only suitable for radially uniform rod-shaped good, but u. a. also for radial pronounced profiled good such. B. mushroom-shaped Well. This can be arranged alternately in the axial direction The electrolytic cell should be promoted to one as possible close to a tight arrangement. This will change the plant length optimally used for throughput.

The Conditions can limit the anode space at the same time, though the estate should be treated partially. For this they reach z. B. to the bottom of the working container. In an all-round electrochemical treatment of the goods, the pads should the anode compartment do not limit. They serve only as carriers on which the Well promoted by the continuous flow system. The carriers exist z. B. profiled rails. A profile is preferred used, which at the generatrix to the good a small contact surface having. The remaining area of the anode compartment is open, so that the electric field lines emanating from the anode all Achieve areas for all-round electrochemical treatment can. To this treatment can the conditions in the transport direction preferably also obliquely, to avoid blind spots on the rotating material. So look in In this case all surface areas of the material the electrodes with the same exposure time.

The invention is described below with reference to the schematic and not to scale 1 to 9 described in detail.

1a shows in section A-B a working container according to the invention a continuous system with rod-shaped Good z. B. has a round cross-section, for the electrochemical treatment of the central rod area.

1b shows the same work container in plan view.

1c likewise shows the working container of 1a on average C-D.

2a shows in section A-B a working container according to the invention a continuous system with rod-shaped Good z. B. has a round cross-section, for complete electrochemical treatment of the goods.

2 B shows the same work container in plan view.

2c likewise shows the working container of 2a on average C-D.

3 shows a continuous system in section for partial galvanization of the goods with axially adjustable supports for adapting the continuous system to different lengths of goods.

4 shows measures in the cathode compartment to avoid metallization of the cathode in a galvanizing process.

5a shows a possible active transport of the goods through the working container of a continuous system by means of at least one circulating belt.

5b shows a further possible active transport of the goods through the working container of a continuous system by means of at least one pendulum thruster.

6 shows an electrolytic cell according to the invention with an electrode which can be switched on and off in sections to the bath power source.

7 shows a continuous system which is arranged in three separate working container, wherein the portions are connected to reduce the total treatment current electrically in series.

8th shows a possible arrangement of mushroom-shaped material for optimal use of the length of the continuous system.

9 shows on average a dip system with vertical arrangement of the goods or a vertical continuous system.

The 1a shows in section A-B a work container 2 a continuous system for a rod-shaped good 1 with a circular cross-section. This good 1 is conveyed in this figure perpendicular to the plane of the drawing. It rolls on editions 3 lying down. The rotation of the goods 1 can by an arrangement of the pads 3 be achieved as a sloping inclined plane in the transport direction. Also transport as active drives for rotation and / or transport of the goods 1 through the continuous flow system are applicable. Examples of this are described below. The on the pads 3 lying goods 1 form a plane. Preferably, plane-parallel to this plane are two electrodes of an electrolytic cell 4 namely an anode 5 and a cathode 6 , The goods 1 are in the electrolytic cell 4 in their plane between the electrodes 5 . 6 , The area between the anode 5 and the estate 1 or its surface is the anode compartment 7 , where the distance of the goods 1 from the anode 5 as anode distance 8th referred to as. The area between the cathode 6 and the estate 1 is the cathode compartment 9 , where the distance of the goods 1 , or its surface, which faces the cathode, from the cathode 6 as cathode distance 10 referred to as. The anode 5 is over an electrical conductor 11 connected to the positive pole of a Badstromquelle not shown, and the cathode 6 corresponding to the negative pole of the same. The good 1 is not contacted electrically. Therefore, according to the invention, no high-current contacts or high-current rotary contacts are required, which would be technically very complicated and which would also have to be demetallised continuously. The good 1 is contactless in the electrolyte 12 the electrolytic cell 4 , The level 26 of the electrolyte 12 is enough in the work container 2 through the top electrode, preferably the cathode 6 the electrolytic cell 4 is. The electrochemical treatment of the goods 1 takes place in this electrolytic cell 4 on the surface, that of the anode 5 facing, ie in the anode compartment 7 cathodic and at the same time on the surface of the estate 1 that the cathode 6 facing, ie in the cathode compartment 9 anodic. Because of the rotation of the goods 1 the surface is alternately treated cathodically and anodically at each revolution. This. is for pretreatment z. B. for electrochemical cleaning in a corresponding electrolyte 12 very suitable. The galvanizing of good 1 in a device according to the invention, however, requires that an electrolyte 12 is used, in which the deposited metal does not dissolve anodically when the good 1 in the electrolytic cell 4 rotates, so if each surface area is treated alternately cathodic metallizing and anodic. Such electrolytes are z. B. for hard chrome plating, for nickel plating and generally for precious metal deposition known. In the anode room 7 is with such an electrolyte 12 the one surface area of the rotating material 1 currently galvanized. At the same time the other opposite surface area of the goods 1 in the cathode compartment 9 treated anodically. Because by the treatment stream passing through the estate 1 flows, the deposited metal can not be anodically dissolved, there is gas, z. B. oxygen formed as a backlash. As a result of the rotation, the material is thus galvanized uniformly over the entire circumference. The required suction devices for the gas are in the 1a to 1c not shown.

So that the cathode 6 the electrolytic cell 4 is not galvanized, special measures are required, which are still on hand 5 be described in detail.

When galvanizing rod-shaped material 1 Often there is the task of only partially metallizing it in the axial direction. So z. B. cylinder for shock absorbers to improve the Abriebeigenschaften only in the middle range with hard chrome or with a Hartchromdispersionwerkstoff to metallize. The outer areas of the property 1 For other reasons, they must remain free or largely free of hard chrome. Again, the invention is very well suited. The terms 3 be in the work container 2 positioned so that the good 1 with its metallization limit on these requirements 3 rests. These requirements 3 be like in the 1a represented, so with the container bottom 14 connected, that a closed to the side anode space 7 is formed. This is the outer areas of the goods 1 which are not to be metallized, outside the electric field, that of the anode 5 towards the bottom of the estate 1 emanates. Although these outer areas of the goods 1 in the work container 2 in the electrolyte 12 Therefore, they are not metallized. They do not extend into the anode compartment 7 into it. This results in a very accurately positioned metallization boundary at the two ends of the material 1 reached. The dimension of the cathode 6 in the axial direction of the goods 1 has only a small influence on the metallization limit. Therefore, the cathode compartment 9 in relation to the axial dimensions of the goods 1 be unlimited, as it is in the 1a shown on the right is. The cathode 6 is longer than the metallization area of the material at this point 1 ,

The cathode compartment 9 can also be limited if necessary in the axial direction, z. B. if the base metal could be dissolved anodically in the electrolyte. in this case the cathode is 6 maximum as long as the center area of the material to be plated 1 , For limiting the cathode space 9 then serves on each side of the good ever an upper insulating wall 13 as they are in the 1a is exemplified on the left side. These insulating walls arranged on both sides 13 cause the axially outwardly facing areas of the property 1 Anodisch not be charged or only very slightly. Therefore, there is no anodic dissolution of the unprotected base metal, warm this otherwise anodic in the electrolyte used 12 would be resolvable. In a plating process, the axial length of the cathode 6 and the insulating walls arranged laterally therefrom 13 shorter than the area of the material to be electroplated 1 to the fashionable penetration of the cathode 6 to completely prevent the ends of the goods.

Electroplating turns into an insoluble anode 5 , z. B. lead or platinum titanium used. The required metal supplement in the electrolyte 12 as well as the circulation promotion of the electrolyte 12 through the electrolytic cell 4 are state of the art and therefore not shown in the figures.

The 1b shows the top view of the working container 2 , the Indian 1a in section A-B is shown. in this plan view is a very short horizontal flow system or electrolytic cell 4 with rotating rolling material 1 shown. The transport arrow 15 shows the transport direction of the goods 1 , The handling equipment for loading and unloading the continuous system are not shown. They are also state of the art. For better illustration, the upper electrode, here the cathode 6 only as cathode outline 16 located. These 1b shows the very simple structure of the electrolytic cell 4 and thus the continuous flow system. The good 1 can be slightly dense or slightly spaced for faster gas discharge, as shown, are conveyed in the transport direction. For spacing z. B. at the two metallization on the estate electrically insulating disks or O-rings are arranged, wherein the outer diameter corresponding to the spacing is greater than the outer diameter of the goods.

It can also be seen that a rod-shaped material has very little space in the electrolytic cell compared to the prior art in tubular anodes according to the prior art 4 takes up. Therefore, the only currently electroplating surface of the material 1 more than balanced with regard to the throughput of a galvanizing plant. Because in the electrolytic cell according to the invention 4 with a certain length in the direction of transport at the same time many to many goods 1 the required exposure time is always achieved even with a short cycle time, ie fast feed cycles.

The 1c shows the work container 2 of the 1a and 1b on average C-D. The good 1 rolls on the illustrated inclined plane of the pads 3 through the electrolytic cell 4 , which is also shown very briefly here in the transport direction. The length depends in practice, inter alia, on the required throughput of the goods 1 as well as the required size of the treatment stream. Even if no rotating electrical contacts for the good 1 are required, currents of several thousand ampere always require particularly large and heavy constructions of the busbars and the electrodes, which are to be avoided. The invention makes it possible to realize cost-effective small-scale systems in place of a large-scale system customary according to the state of the art. The known facilities for loading and emptying the continuous system are in the 1c not shown.

The 2a to 2c show a working container according to the invention 2 for the all-round treatment of rolling stock 1 , For the placement of the goods 1 serve in the 2a illustrated electrically insulating laying as rails 17 , These form an open anode space 7 , The good 1 rolls on the generatrices of the two rails 17 from. Because of the openness of the Anodenrau mes 7 and because of the z. B. round profile of the rails 17 becomes almost the entire surface of the rotating material 1 from the electric field of the electrolytic cell 4 reached and treated electrochemically. For all-round plating of the rolling stock 1 can the electrodes 5 . 6 be adapted to the axial length of the goods as it is the 2a and 2 B demonstrate. With the in the 2 B shown inclined position of the rails 17 becomes a permanent shading of the electric field at one or two points of the goods 1 avoided. The momentary minor shadowing is distributed in the axial direction over a larger area of the goods 1 , Overall, the whole estate is thereby treated uniformly electrochemically.

The 2c shows the work container 2 for the all-round treatment of the goods in the side view. The cross section of the rails 17 is dimensioned so that on the one hand the good 1 can be worn and on the other hand, the anode compartment 7 is limited.

Should be a good 1 first with a thin protective layer metallized on all sides, so there can not be dissolved anodically after a corresponding base material, so is a juxtaposition of the electrolytic cells 4 according to the 2a to 2c with the following embodiment according to the 1a to 1c , In terms of design, this is very easy to realize because in both cases the same electrolyte 12 is usable. Thus, only a single work container 2 needed. The open rails 17 at the entrance of the working container are short in the transport direction corresponding to the required all-round first thin metallization. The rest of the transport path with closed supports 3 is much longer to the required layer thickness in the functional useful range of the goods 1 to reach. The electrodes 5 . 6 may extend over both areas, requiring only a single source of bath power. When divided in the direction of transport electrodes 5 . 6 in the two areas the use of two bath power sources is possible. These can be set independently of each other in their output current.

The continuous systems of 1 and 2 show a good with a circular cross section, rotating through the working container 2 is promoted to achieve a uniform electrochemical treatment at the periphery. Such systems and continuous systems are generally suitable for one-sided treatment of non-rotating Good, especially for one-sided electroplating of z. B. decorative good. So z. B. galvanized in a flat good as a cover usually only the visible side. In this all of the electrically non-contacted Good is not rotating in the electrolytic cell according to the invention 4 arranged and / or pushed through. The side of the estate, located in the anode room 7 is metallized and on the opposite side, located in the cathode compartment 9 Anodic gas is formed. The base material or an electrically conductive protective coating or the electrolyte must be chosen so that the good 1 in the cathode compartment 9 anodically not dissolved. If necessary, in order to avoid the anodic dissolution, a protective metallization of the material may be required 1 respectively. A partial insulating layer, as required by the prior art to avoid metallization of the back, is not required.

The 3 shows a work container 2 a continuous system for partial plating of the central region of rod-shaped Good 1 , where the editions 3 in the axial direction of the goods 1 are adjustable. Thus, the continuous flow system for the treatment of differently long good 1 be changed or adapted. At least one of the two editions 3 must be axially adjustable. The other edition 3 can, as in the 1 shown stuck in the work container 2 be arranged and the anode compartment 7 limit on this page.

The 3 shows an example of two options for the axial adjustment of the conditions 3 , On the left side is the pads 3 on a preferably horizontal cover plate 18 attached. The cover plate 18 protrudes slidably and approximately liquid-tight through the side wall of the working container 2 therethrough. The move can z. B. by means of at least one spindle, not shown. The anode 5 is transverse to the transport direction of the goods 1 seen for galvanizing the longest good 1 dimensioned. For shorter good, just like the 3 shows, the electrically insulating cover plate acts 18 as a dense aperture, the anode space 7 axially limited as it is for partial plating of the goods 1 is required. The work container 2 is in an overflow container 19 , Overflowing and out of the slot 20 of the working container 2 leaking electrolyte 12 enters the overflow tank 19 , From there, it is recirculated through the working container 2 pumped.

As a further embodiment for adjusting the conditions 3 is on the right side of the 3 an electrically insulating bellows 21 shown. This again covers the unneeded area of the anode 5 from, resulting in the not to be galvanized end of the goods 1 outside the electric field of the anode 5 located. This end area is not galvanized. Because of the elastic bellows 21 becomes the associated edition 3 z. B. supported by the spindles for axial adjustment or other construction elements, not shown.

Depending on the electrolyte used 12 and its scattering properties, it may be necessary to influence the metallization boundary to take additional isolation measures. The 3 shows next to the pads 3 one elastic diaphragm each 22 , This can, for. B. consist of an electrically non-conductive foam or sponge rubber, over the top edge of the pads 3 protrudes. The good 1 is represented by transport means shown schematically 23 with pressing construction elements as a driver on the pads 3 pressed. This encloses the elastic panel 22 the material largely, whereby the transition from the metallization region to the non-metallized region is achieved on a very short axial length, z. Within 2 mm.

One-sided or two-sided flat profiles as axial limiters 24 can fix the axial position of the goods and thus the metallization very close to the good 1 position. A suction 25 above the work container 2 ensures the removal of the gases and aerosols generated during the processes.

The 4 shows several individually applicable measures to avoid metallization of the cathode 3 in a plating process in the electrolytic cell 4 , If necessary, these measures can also be combined with each other. They are not shown in all other figures, but partially required. The cathode 6 is designed as a metallic hollow body, which is a cooling medium 27 is flowed through. This is z. B. the cooling water available in production. The flow temperature is z. B. 8 ° C. Almost the same temperature takes up the surface of the cathode 6 and the electrolyte 12 in the boundary layer to the cathode 6 at. Because a much higher temperature is required for metal deposition usually, despite the current flow to the cathode 6 on this no metal deposited but gas formed, usually hydrogen.

To speed up the processes in the electrolytic cell 4 is preferably a turbulent flow of the electrolyte 12 applied. This also causes an increased heat transfer to the cooled cathode 6 with an increased cooling capacity requirement. For thermal insulation of the surface of the cathode 6 can this with a heat insulator 28 be surrounded. This consists z. B. from a porous tissue that must be ion permeable and gas permeable. Suitable is z. As a cloth made of polypropylene or the like.

Another measure to avoid the metallization of the cathode 6 is the separation of the cathode space 9 in front of the remaining area of the electrolytic cell 4 by means of an ion-selective and liquid-tight membrane 29 , in the room, the cathode 6 surrounds, a separate electrolyte than catholyte 30 used. This contains no metal ions on the cathode 6 at current flow through the semipermeable membrane 29 to the cathode 6 could be separated. As a backlash is at the cathode 6 gas is formed again.

Also by the choice of the material on the surface of the cathode 6 it is possible to influence the metallization of the same or non-metallization. Depending on the electrolyte used 12 and metal to be deposited at the front there are materials which can not be metallized electrochemically. An example of this is a cathodically poled surface of tin in a hard chrome bath.

One good 1 that is in the electrolytic cell 4 between the anode 5 and the cathode 6 is located in the anode room 7 a first cell voltage to the anode 5 and a second cell voltage to the cathode 6 , These cell voltages correspond in their sum to the cell voltage U _Z of the anode 5 to the Kothode 6 , The size of the first and the second cell voltage is determined by the anode distance 8th and from the cathode gap 10 certainly. The closer the good 1 on one of the two electrodes 5 . 6 is, the smaller is the associated first or second cell voltage. Accordingly, the cell voltage becomes larger over the larger distance. Thus, exist in the electrolytic cell 4 two electrolytic sub-cells with the same or different cell voltages U _Z. These subcells are electrically switched in view. They are traversed by the same stream. On the estate to be deposited with this stream of metal, for which a certain minimum current density is required. On the cathode 6 Should no metal be deposited at the same current, for which purpose this minimum current density must be undercut. Because the treatment current is the same in both cases, these current densities were adjusted by means of the size of the areas. The cathode 6 must have a larger area compared to the current anodic surface of the property 1 exhibit. This can be z. B. by a multi-layer expanded metal arrangement with a very large surface area as a cathode 6 be reached, which is formed on it due to the small current density through the current only gas as an electrochemical backlash.

The 5a shows an example of a means of transport 23 as an active drive to the rotating promotion of the goods 1 through the electrolytic cell 4 , This is z. B. in the cathode compartment 9 at least one electrically insulated circulating belt 31 , This rests with the bottom strand 32 on the round estate 1 and takes this around the longitudinal axis rotating in the transport direction. It rolls on the pads 3 in the transport direction, with the transport arrow 15 is marked. The good 1 can be conveyed slightly spaced from each other close to each other or for faster gas discharge. The distances are z. B. by means of spacers 33 or takers, the band 31 are attached, realized. This type of transport is suitable according to the invention for all electrochemical processes, in particular for electrical contacting of the goods on the conditions 3 and rails 17 in the pretreatments as described above. The same applies to the in the 5b illustrated transport as active drive of the rotating material 1 through the electrolytic cell 4 , The transport takes place by means of at least one pendulum thrust device 34 , At least one driver 35 , which extends along the entire transport path, the front active drive, ie from the pendulum thruster 34 against the estate 1 pressed. In this state, the one or more drivers moves 35 in the transport direction for a short distance, z. B. corresponding to the length of three diameters of the goods. The speed of this forward movement is the required peripheral speed of the goods 1 , After that, the driver lifts 35 from the estate 1 and moves quickly against the transport direction, which is followed by another lowering. There may also be several pendulum thrusters 34 and takers 35 be used to promote the good. These work advantageously out of phase with each other. This also results in a slow backward movement of the driver 35 a uniform rolling transport of goods 1 through the electrolytic cell 4 , To slip-free driving the goods, the drivers 35 on the side that touches the estate, be provided with an elastically adhesive material.

The 6 shows the electrodes 5 . 6 an electrolytic cell 4 wherein one electrode in electrode portions electrically insulated from each other 36 divided in the transport direction. These electrode sections 36 can by means of controlled electrical switch 37 to which a bath current source, not shown, are switched. When driving in and out of goods 1 in or out of the electrolytic cell 4 temporarily not the entire electrode is needed. In the empty areas of the electrolytic cell 4 Gas would be generated by the application of electricity. To save energy, therefore, only the areas of the electrode are turned on, with good 1 are loaded. For this purpose, the partial shutdown of an electrode is sufficient. This is preferably the anode 5 because the measures to avoid the metallization of the cathode 6 structurally complicate the formation of sections.

The 7 shows three electrolytic cells 4 , located in three electrically isolated work containers 2 or baths A, B and C are located. In the three working containers 2 with the three electrolytic cells connected in series 4 can be same or different goods 1 be treated electrochemically, wherein in all baths of the same large treatment _current I _ZA = I _ZB = I _ZC = I _GR must be required. This allows the illustrated very advantageous electrical series connection of the three electrolytic cells 4 , The rectifier current I _GR flows through all working vessels 2 , However, it is only one-third compared to a single long electrolytic cell 4 , Only the cell voltages U _ZA + U _ZB + U _{ZC are added} . Their sum U _GR is the rectifier output voltage. The required total electrical power remains as large as in a parallel connection of the three electrolytic cells 4 , However, smaller currents and higher voltages are technically feasible cheaper. Because a cell voltage U _Z in such electrochemical processes is rarely greater than 12 volts, the sum of the cell voltages U _Z and U _{GR also} remains so small that the busbars remain safe with respect to contact by persons. If one or two of the electrolytic cells connected in soda 4 are temporarily not charged with good, the electrodes can 5 . 6 by means of electrical switching contacts 38 be bridged to save energy. In this case, the rectifier output voltage U _GR is reduced accordingly.

The 8th shows a mushroom-shaped good 1 , z. As engine valves that are to be galvanized only on the shaft to improve the wear resistance, z. B. with hard chrome or with an alloy. For optimal use of the electrolytic cell 4 They are arranged as shown and through the electrolytic cell 4 promoted rotating. Even with these small parts no high-current rotary contacts are required. Therefore, the invention also proves to be very economical for the precise electrochemical treatment of comparatively small material.

The 9 shows a vertical arrangement of the goods 1 in an electrolytic cell 4 in which also the electrodes 5 . 6 are arranged vertically. In such a dipping the good 1 be introduced and remain static or rotating locally. The possibly required limitations of the anode compartment 7 and the cathode compartment 9 are in this 9 not shown. For rotation of the vertical good 1 around the longitudinal axis are not shown drives 23 required from the top or bottom of the estate 1 act. in this vertical position can the good 1 also continuously through the electrolytic cell 4 be encouraged. This is a so-called vertical continuous flow system. It is particularly advantageous when non-rotating material is to be treated electrochemically. It can be contactless and free hanging or standing in the plane of the drawing 9 be promoted into.

1

Well

2

working container

3

pads

4

electrolytic cell

5

Anode, electrode

6

Cathode, electrode

7

anode chamber

8th

anode distance

9

cathode space

10

cathode distance

11

electrical ladder

12

electrolyte

13

insulating wall

14

container bottom

15

transportation arrow

16

cathode outline

17

rail

18

cover plate

19

Overflow tank

20

slot

21

bellow

22

elastic blonde

23

Mode of Transport

24

Axialbegrenzer

25

suction

26

level

27

cooling medium

28

thermal insulator

29

membrane

30

catholyte

31

tape

32

lower Trum

33

Spacer takeaway

34

Pendulum pusher

35

takeaway

36

electrode section

37

electrical switch

38

electrical switching contact

A

bath A

B

bath B

C

bath C

QUOTES INCLUDE IN THE DESCRIPTION

This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Cited patent literature

• DE 1103103 [0003]
• - DE 2524315 [0004]
• - DE 19632132 C1 [0004, 0005]
• - DE 19837973 C1 [0009]

Claims (107)

Process for the electrochemical treatment of electrically conductive material ( 1 ), in particular for etching, pickling, cleaning and galvanizing or for partial treatment, in particular for partial electroplating of elongated material ( 1 ) in the electrolyte ( 12 ) at least one electrolytic cell ( 4 ), which is associated with at least one bath source, characterized in that at least one good ( 1 ) for treatment in the electrolytic cell ( 4 ) consisting of at least one anode ( 5 ) and at least one cathode ( 6 ), between the anode ( 5 ) and the cathode ( 6 ) is placed electrically contactless and rotates with switched on bath current source with at least one revolution about its longitudinal axis. Method according to claim 1, characterized in that the planar anodes (preferably arranged plane-parallel to each other) 5 ) and plane cathodes ( 6 ) and / or the good ( 1 ) for electrolyte exchange and / or for gas separation To be moved cyclically or vibrantly from the surfaces. Method according to claims 1 and 2, characterized in that the galvanizing of the material in an electrolyte ( 12 ), in which the goods are stored on the estate ( 1 ) electrochemically deposited metal is anodic resistant and does not redissolve. Process according to claims 1 to 3, characterized in that the surface areas of the goods ( 1 ) are treated alternately cathodically and anodically or vice versa in one revolution. Method according to one of the claims 1 to 4, characterized in that during plating a metallization of the cathode ( 6 ) of the electrolytic cell ( 4 ) by placing the goods ( 1 ) near the cathode ( 6 ) is avoided. Method according to one of the claims 1 to 5, characterized in that by an electrically conductive metal layer at least on the surface of the cathode ( 6 ) used in the electrolyte used ( 12 ) is chemically resistant, but not metallizable, a metallization of the cathode ( 6 ) is avoided. Method according to one of the claims 1 to 6, characterized in that by an active surface of the cathode ( 6 ), which is substantially larger than the instantaneous effective anodic surface of the material ( 1 ), a much smaller cathodic current density occurs, whereby a metallization of the cathode ( 6 ) is avoided. Method according to one of the claims 1 to 7, characterized in that by cooling the cathode ( 6 ) to a surface temperature below the working temperature of the electrolyte ( 12 ) a metal deposit on the cathode ( 6 ) is prevented. Method according to one of the claims 1 to 8, characterized in that a metallization of the surface of the cathode ( 6 ) is avoided by the use of an electrolyte ( 12 ) in the region of the cathode ( 6 ) containing no metal ions deposited on the cathode ( 6 ) can be deposited. Method according to claims 9, characterized in that in order to avoid metal deposition on the cathode ( 6 ) by an ion-selective and liquid-tight membrane of the electrolyte in the region of the cathode ( 6 ) as catholyte ( 30 ), which contains no metal ions, from the working electrolyte ( 12 ), which contains metal ions and in which the good ( 1 ) and the anode ( 5 ), is kept separate. Method according to one of the claims 1 to 10, characterized in that the demand for energy for cooling the cathode ( 6 ) by an ion-permeable and heat-insulating layer as a heat insulator ( 28 ) against the electrolyte at working temperature ( 12 ) is reduced. Method according to one of the claims 1 to 11, characterized in that the electrolytic cell ( 4 ) is operated with at least one bath power source as a DC power source, unipolar pulse power source, bipolar pulse power source or with technical alternating current. Method according to one of the claims 1 to 12, characterized in that by shielding areas of the goods ( 1 ) at least against the anode ( 5 ) of the electrolytic cell ( 4 ) this is only partially electrochemically treated or galvanized. Method according to one of the claims 1 to 13, characterized in that the partially electrochemically treated surface of the material by means of adjustable shields ( 18 . 21 ) is selected and acknowledged. Method according to one of the claims 1 to 14, characterized in that the material ( 1 ) is partially galvanized by limiting protective varnish or protective caps. Method according to one of the claims 1 to 15, characterized in that the good on pads ( 3 ) rolling through the electrolytic cell ( 4 ) is conveyed in a plane which is preferably plane-parallel to the plane and parallel electrodes ( 5 . 6 ) lies. Method according to one of the claims 1 to 16, characterized in that at least the pads ( 3 ) form an inclined plane on which the material automatically rolls close together. Method according to one of the claims 1 to 17, characterized in that the material of at least one circulating belt ( 31 ) or at least one Pendeischubeinrichtung ( 34 . 35 ), preferably in the region of the cathode ( 6 ), against the conditions ( 3 ) and thereby close to each other or by spacers spaced by the electrolytic cell ( 4 ) is transported. Method according to one of the claims 1 to 18, characterized in that by an oblique position transversely to the transport direction of the planes of the electrodes ( 5 . 6 ) and the level of the good ( 1 ) the discharge of the gases produced during the treatment is accelerated. Method according to one of the claims 1 to 19, characterized in that by a vibration-like or cyclic movement of the electrodes ( 5 . 6 ) and / or the goods ( 1 ) in any direction an electrolyte exchange and / or the replacement of emerging gases is supported by the surfaces. Method according to one of the claims 1 to 20, characterized in that during the extension and retraction of the goods in and out of the electrolytic cell ( 4 ) at least one electrode ( 5 . 6 ) is switched on and off in sections, according to the filling of the electrolytic cell ( 4 ), wherein at the same time the current of the bath power source is adapted to save energy to the currently to be treated surface of the goods. Method according to one of the claims 1 to 21, characterized in that during the extension and retraction of the goods in and out of the electrolytic cell ( 4 ) Hide the currently not required surfaces of the electrodes ( 5 . 6 ) shield. Method according to one of the claims 1 to 22, characterized in that the required size of the bath stream at a given system throughput by a series connection of at least two electrolytic cells ( 4 ) is reduced. Method according to one of the claims 1 to 23, characterized in that by apertures or partial apertures the course of the metallization limit is influenced. Method according to one of the claims 1 to 24, characterized in that individual drives of each good through the electrolytic cell ( 4 ) rotate. Method according to one of the claims 1 to 25, characterized in that in an immersion bath the between the electrodes ( 5 . 6 ) positioned Good is locally rotated about the longitudinal axis. Method according to one of the claims 1 to 26, characterized in that radially pronounced profiled material ( 1 ) in the axial direction alternately through the electrolytic cell ( 4 ). Device for the electrochemical treatment of electrically conductive material ( 1 ), in particular for etching, electropolishing, pickling, cleaning and electroplating or for partial treatment, in particular for partial electroplating of elongated material ( 1 ) in the electrolyte ( 12 ) at least one electrolytic cell ( 4 ), at least one Badstromquelle is assigned, for carrying out the method according to claim 1, characterized by at least one anode ( 5 ) and at least one cathode ( 6 ) between which the goods to be treated ( 1 ) is electrically contactless placeable and there rotatably mounted with at least one revolution about its longitudinal axis. Device according to claim 28, characterized by preferably flat anodes ( 5 ) and plane cathodes ( 6 ), which in the electrolyte ( 12 ) are arranged plane-parallel or nearly plane-parallel to each other and by a plane between the electrodes ( 5 . 6 ), in which the estate ( 1 ) which are plane-parallel to the planes of the electrodes ( 5 . 6 ) lies. Device according to claims 28 and 29, characterized by cyclic drives or vibrators for moving at least one electrode ( 5 . 6 ) and / or the goods ( 1 ). Device according to claims 28 to 30, characterized by a cathode ( 6 ) of the electrolytic cell ( 4 ), which is coolable by means of more cooling device. Device according to one of the claims 28 to 31, characterized by a cooling device as at least partially hollow cathode ( 6 ), which is traversed by a cooling medium or by electric cooling elements as Peltier elements for the cathode ( 6 ). Device according to one of the claims 28 to 32, characterized by a surface of the Cathode ( 6 ), on which no metal in the pre-electrolyte ( 12 ) is electrochemically separable. Device according to one of the claims 28 to 33, characterized by a surface of the cathode ( 6 ), which is substantially larger than the currently effective anodic surface of the material ( 1 ). Device according to one of the claims 28 to 34, characterized by an ion-selective membrane for the liquid-tight separation of the cathode space ( 9 ) and its electrolyte as catholyte ( 30 ) from the remaining area of the electrolytic cell ( 4 ) and its electrolyte ( 12 ). Device according to one of the claims 28 to 35, characterized by a thermal insulating layer which is ion-permeable, as a heat insulator ( 28 ) in front of a cooled cathode ( 6 ). Device according to one of the claims 28 to 36, characterized by at least one bath power source as DC power source, unipolar pulse power source, bipolar pulse power source or power source for technical alternating current. Device according to one of the claims 28 to 37, characterized by supports ( 3 ) or rails ( 17 ) for positioning the product in the electrolytic cell ( 4 ) and / or for the promotion of the same by the electrolytic cell ( 4 ). Device according to one of the claims 28 to 38, characterized by at least one shield or support 3 at least in the region of the anode space ( 7 ) in front of the estate ( 1 ) for partial electrochemical treatment thereof in the longitudinal direction. Device according to one of the claims 28 to 39, characterized by at least one adjustment device for the shield (s) and / or the supports ( 3 ) for adaptation to differently long goods to be treated ( 1 ). Device according to one of the claims 28 to 40, characterized by supports ( 3 ), which is an inclined plane for the estate ( 1 ), with the valley in the transport direction for the self-rolling promotion of the goods in the electrolytic cell ( 4 ). Device according to one of the claims 28 to 41, characterized by supports ( 3 ), which is a level for the estate ( 1 ) for the rolling horizontal transport of goods ( 1 ) through the electrolytic cell ( 4 ) in a plane which is preferably plane-parallel to the electrodes ( 5 . 6 ). Device according to one of the claims 28 to 42, characterized by at least one circulating belt ( 31 ) or at least one pendulum thrust device ( 34 . 35 ), preferably in the cathode compartment ( 9 ) as drive means for rotation of the product in the electrolytic cell ( 4 ) and as conveyance of the goods through the electrolytic cell ( 4 ). Device according to one of the claims 28 to 43, characterized by at least one suction device ( 25 ) for the extraction of the gases produced during the electrochemical treatment. Device according to one of the claims 28 to 44, characterized by a subdivision in the transposing direction of at least one electrode ( 5 . 6 ) in electrode sections ( 36 ) and by electrical switches ( 37 ) for the controlled connection of the electrode sections ( 36 ) with the or the bath power source (s). Device according to one of the claims 28 to 45, characterized by controlled diaphragms or partial diaphragms, which are preferably in the anode space ( 7 ) are located. Device according to one of the claims 28 to 46, characterized by individual drives for rotation of the product in the electrolytic cell ( 4 ) and / or for conveying the product through the electrolytic cell ( 4 ). Device according to one of the claims 28 to 47, characterized by vertically positioned good for treatment in a dip or in a vertical bath. Device according to one of the claims 28 to 48, characterized by drives for rotation of vertical positioned material in the electrolytic vertical cell. Device according to one of the claims 28 to 49, characterized by elastic diaphragms ( 22 ) as a treatment limiter, which are arranged on the metallization border to the extended concerns of the rolling Good. Device according to one of the claims 28 up to 50, characterized by individual panels, caps, sleeves or insulating coatings that are at the metallization boundary are arranged in front of or on the estate. Device according to one of the claims 28 to 51, characterized by at least two electrolytic cells ( 4 ), which are electrically connected in series, for powering only one Badstromquelle. Device according to claim 52, characterized by electrical contacts ( 38 ) to electrical bridging of currently unused in-line electrolytic cells ( 4 ). Device according to one of the claims 28 to 53, characterized by supports ( 3 ), which at the same time the anode space ( 7 ) limit. Device according to one of the claims 28 to 54, characterized by supports as rails ( 17 ), which run obliquely in the transport direction to each other and the anode space ( 7 ) do not limit. Process for the one-sided electrochemical treatment of electrically conductive material ( 1 ), in particular for etching, pickling, cleaning and electroplating or for unilaterally partial treatment, in particular for partial electroplating of expanded material ( 1 ) in the electrolyte ( 12 ) at least one electrolytic cell ( 4 ), which is associated with at least one base current source, characterized in that at least one good ( 1 ) for treatment in the electrolytic cell ( 4 ) consisting of at least one anode ( 5 ) and at least one cathode ( 6 ), between the anode ( 5 ) and the cathode ( 6 ) is placed without electrical contact and with the bath power source of the good on the side, the anode ( 5 ), is galvanized and on the other side, the cathode ( 6 ), at the same time anodically without dissolution of metal of the goods ( 1 ) is treated. A method according to claim 56, characterized in that the material to be metallized on one side in the electrolyte used ( 12 ) is not resolved anodically. Process according to claims 56 and 57, characterized in that, during electroplating, metallisation of the cathode ( 6 ) electrolytic cell ( 4 ) by placing the goods ( 1 ) near the cathode ( 6 ) is avoided. Process according to claims 56 to 58, characterized in that by an electrically conductive metal layer at least on the surface of the cathode ( 6 ) used in the electrolyte used ( 12 ) is cathodically stable and on the in this electrolyte ( 12 ) no metallization occurs, a metal deposition on the cathode ( 6 ) is prevented. Method according to one of the claims 56 to 59, characterized in that by cooling the cathode ( 6 ) to a surface temperature below the working temperature of the electrolyte ( 12 ) a metal deposit on the cathode ( 6 ) is prevented. Method according to one of the claims 56 to 50, characterized in that a metallization of the surface of the cathode ( 6 ) is avoided by the use of an electrolyte ( 12 ) in the region of the cathode ( 6 ) containing no metal ions deposited on the cathode ( 6 ) are separable. A method according to claim 61, characterized in that the electrolyte in the region of the cathode (2) by an ion-selective and liquid-tight membrane ( 6 ) as catholyte ( 30 ) from the working electrolyte ( 12 ), in which the estate ( 1 ) and the anode ( 5 ) is disconnected. Method according to one of the claims 56 to 62, characterized in that the demand for energy for cooling the cathode ( 6 ) by an ion-permeable and heat-insulating layer as a heat insulator ( 28 ) against the electrolyte at working temperature ( 12 ) is reduced. Method according to one of the claims 56 to 63, characterized in that the electrolytic cell ( 4 ) is operated with at least one bath power source as a DC power source, unipolar pulse power source, bipolar pulse power source or with a technical AC power. Method according to one of the claims 56 to 64, characterized in that by shielding areas of the material at least against the anode ( 5 ) of the electrolytic cell ( 4 ) this is only partially treated or galvanized. Method according to one of the claims 56 to 65, characterized in that the one-sided surface of the material to be treated partially electrochemically ( 1 ) by means of adjustable shields ( 18 . 21 ) is selected and set. Method according to one of the claims 56 to 66, characterized in that the good ( 1 ) is partially galvanized on one side by limiting protective lacquer or protective caps. Method according to one of the claims 56 to 67, characterized in that the good is subject to conditions ( 3 ) through the electrolytic cell ( 4 ) is conveyed in a plane pulling or sliding, which preferably plane-parallel to the plane and parallel electrodes ( 5 . 6 ) lies. Method according to one of the claims 56 to 68, characterized in that the material of at least one circulating belt ( 31 ) or at least one pendulum thrust device ( 34 . 35 ) preferably in the region of the cathode ( 6 ), against the conditions ( 3 ) and thereby close to each other or by spacers spaced by the electrolytic cell ( 4 ) is transported. Method according to one of the claims 56 to 69, characterized in that by an oblique position transversely to the transport direction of the planes of the electrodes ( 5 . 6 ) and the level of the good ( 1 ) the discharge of the gases produced during the treatment is accelerated. Method according to one of the claims 56 to 70, characterized in that by a vibration-like or cyclic movement of the electrodes ( 5 . 6 ) and / or the goods ( 1 ) in any direction an electrolyte exchange and or the replacement of emerging gases is supported by the surfaces. Method according to one of the claims 56 to 71, characterized in that during the extension and retraction of the goods into and out of the electrolytic cell ( 4 ) at least one electrode ( 5 . 6 ) is switched on or off in sections, according to the filling of the electrolytic cell ( 4 ), wherein at the same time the current of the bath power source is adapted to save energy to the currently to be treated surface of the goods. Method according to one of the claims 56 to 72, characterized in that the required size of the bath stream at a given system throughput by a series connection of at least two electrolytic cells ( 4 ) is reduced. Method according to one of the claims 56 to 73, characterized in that by apertures or partial apertures the course of the metallization limit is influenced. Method according to one of the claims 56 to 74, characterized in that during the extension and retraction of the goods in and out of the electrolytic cell ( 4 ) Hide the currently not required surfaces of the electrodes ( 5 . 6 ) shield. Device for one-sided electrochemical treatment of electrically conductive material ( 1 ), in particular for etching, pickling, cleaning and electroplating or for unilaterally partial treatment, in particular for partial electroplating of expanded material ( 1 ) in the electrolyte ( 12 ) at least one electrolytic cell ( 4 ), which is associated with at least one Badstromquelle, for performing the method according to patent claim 60, characterized by at least one anode ( 5 ) and at least one cathode ( 6 ) between which the goods to be treated ( 1 ) is electrically contactless placeable. Device according to claim 76, characterized by preferably flat anodes ( 5 ) and plane cathodes ( 6 ), which in the electrolyte ( 12 ) are arranged plane-parallel or nearly plane-parallel to each other and by a plane between the electrodes ( 5 . 6 ) in which the estate ( 1 ) which are plane-parallel to the planes of the electrodes ( 5 . 6 ) lies. Device according to claims 76 and 77, characterized by cyclic drives or vibrators for moving at least one electrode ( 5 . 6 ) and / or the goods ( 1 ). Device according to claims 76 to 78, characterized by a cathode ( 6 ) of the electrolytic cell ( 4 ), which is coolable by means of a cooling device. Device according to one of the claims 76 to 79, characterized by a cooling device as at least partially hollow cathode ( 6 ), which is traversed by a cooling medium or by electric cooling elements as Peltier elements for cooling the cathode ( 6 ). Device according to one of the claims 73 to 80, characterized by a surface of the cathode ( 6 ), on which no metal in the electrolyte used ( 12 ) is electrochemically separable. Device according to one of the claims 78 to 81, characterized by an ion-selective membrane for the liquid-tight separation of the cathode space ( 9 ) and its electrolyte as catholyte ( 30 ) from the remaining area of the electrolytic cell ( 4 ) and its electrolyte ( 12 ). Device according to one of the claims 76 to 82, characterized by a thermal insulating layer which is permeable to ions, as a heat insulator ( 28 ) in front of a cooled cathode ( 6 ). Device according to one of the claims 76 to 83, characterized by at least one bath power source as DC power source, unipolar pulse power source, bipolar pulse power source or power source for technical alternating current. Device according to one of the claims 76 to 84, characterized by supports ( 3 ) for positioning the product in the electrolytic cell ( 4 ) and / or for pulling or pushing the same through the electrolytic cell ( 4 ). Device according to one of the claims 76 to 85, characterized by at least one shielding at least in the region of the anode space ( 7 ) in front of the estate ( 1 ) for partial electrochemical treatment thereof in the longitudinal direction. Device according to one of the claims 76 to 86, characterized by at least one adjusting device for the shield (s) and / or the conditions ( 3 ) for adaptation to differently long goods to be treated ( 1 ). Device according to one of the claims 76 to 87, characterized by at least one circulating belt ( 31 ) or at least one pendulum thrust device ( 34 . 35 ), preferably in the cathode compartment ( 9 ) as a means of propelling the good ( 1 ) through the electrolytic cell ( 4 ). Device according to one of the claims 76 to 88, characterized by at least one suction device ( 25 ) for the extraction of the gases produced during the electrochemical treatment. Device according to one of the claims 76 to 89, characterized by a division in the transport direction as seen from at least one electrode ( 5 . 6 ) in electrode sections ( 36 ) and by electrical switches ( 37 ) for controlled connection to the bath power source (s). Device according to one of the patent claims 75 to 90, characterized by controlled diaphragms or partial diaphragms, which are preferably in the anode compartment ( 7 ) are located. Device according to one of the claims 75 to 91, characterized by vertically positioned good for treatment in a dip or in a vertical bath. Device according to one of the claims 76 to 92, characterized by elastic misery ( 22 ) as a treatment limiter, which are arranged on the metallization border for tight contact with the good. Device according to one of the claims 76 to 93, characterized by individual apertures, caps, sleeves or insulating coatings that are at the metallization boundary are arranged in front of or on the estate. Device according to one of the claims 76 to 94, characterized by at least two electrolytic cells ( 4 ), which are electrically connected in series, for powering only one Badstromquelle. Device according to one of the claims 76 to 95, characterized by electrical contacts ( 38 ) for the electrical bridging of currently unused in series electrolytic cells ( 4 ). Device according to one of the claims 76 to 96, characterized by supports ( 3 ), which at the same time the anode space ( 7 ) limit. Device according to one of the claims 76 to 97, characterized by supports as rails ( 17 ), which run obliquely in the transport direction to each other and the anode space ( 7 ) do not limit. Device for the electrochemical treatment of electrically conductive material ( 1 ), in particular for etching, electropolishing, pickling, and cleaning of elongated material ( 1 ) in the electrolyte ( 12 ) at least one electrochemical cell ( 4 ) associated with at least one source of bath power, characterized by the good ( 1 ) as the one electrode of the electrolytic cell ( 4 ) and at least one electrode ( 5 . 6 ) as counterelectrode (n) and by electrically conductive contact paths on the supports ( 3 ) or on the rails ( 17 ) for the electrical contacting of the rolling or sliding material moving thereon by the electrolytic cell ( 4 ). Device according to claim 99, characterized by at least one circulating belt ( 31 ) or at least one pendulum thrust device ( 34 . 35 ), as drive means for rotating the material in the electrolytic cell ( 4 ) and as conveyance of the goods through the electrolytic cell ( 4 ). Device according to claims 99 and 100, characterized by a circulating belt ( 31 ) or by a pendulum push device ( 34 ) than on the estate ( 1 ) pressing means of transport, at the same time as a means for increasing the contact force of the electrical contacting of the goods ( 1 ) serve to contact tracks. Device according to claims 99 to 101, characterized by cyclic drives or vibrators for moving at least one electrode ( 5 . 6 ). Device according to one of the claims 99 to 102, characterized by at least one bath current source as DC source, unipolar pulse current source, bipolar pulse current source or power source for technical alternating current. Device according to one of the claims 99 to 103, characterized by supports ( 3 ) or rails ( 17 ) with contact tracks for electrical contacting of the material in the electrolytic cell ( 4 ) and for the promotion of the same by the electrolytic cell ( 4 ). Device according to one of the claims 99 to 104, characterized by supports ( 3 ), which is an inclined plane for the estate ( 1 ), with the valley in the transport direction for the self-rolling promotion of the goods in the electrolytic cell ( 4 ). Device according to one of the claims 99 to 105, characterized by editions ( 3 ), which is a level for the estate ( 1 ) for the rolling horizontal transport of goods ( 1 ) through the electrolytic cell ( 4 ) in a plane which is preferably plane-parallel to the electrodes ( 5 . 6 ). Device according to one of the claims 99 to 106, characterized by supports as sheers ( 17 ), which run obliquely in the transport direction to each other and which do not limit the electrode space.