METHOD FOR PICKLING STEEL PRODUCTS

Abstract: Method for pickling products made of steel, characterised in that within the pickling bath Fe<3+> is present, directly added in a controlled concentration, or produced in the pickling bath itself by adding an oxidising agent such as hydrogen peroxide, ozone, permanganates, persulphates and oxygen.

Description: METHOD FOR PICKLING STEEL PRODUCTS DESCRIPTION The present invention relates to a method for pickling steels and, more specifically , carbon steels, magnetic steels (containing Si) and stainless steels with a chrome content lesser or equal to 15% (i.e. AISI 409), wherein the Fe 3+ ion is used as an additive in the bath to increase the reaction kinetics. In order to realise an efficient pickling process of the carbon steels, class whereto also magnetic steels containing Si belong, hydrochloric (HC1) or sulphuric (H 2 S0 4 ) acid is normally used, or mixtures thereof, at a temperature that generally varies between 60 and 75 °C. For stainless steels with a low chrome level, e.g. AISI 409 of the ferric class, analogous baths can be adopted as well. The main reaction of pickling, to allow the removal of the scale of thermal oxide, is the dissolution (through oxidation) of the iron base according to the anodic half-reaction: (1) Fe → Fe 2+ + 2e. The corresponding cathodic half-reaction in acid environment is the ion H + reduction that develops hydrogen: (2) 2rT +2e → H 2 Therefore, the resulting total reaction is: (3) Fe + 2H + → Fe 2+ + H 2 As is known from the study of electro-chemical reactions, the kinetics thereof is strongly influenced by the values of the electrode potential. According to the present invention, an additive of oxidising species is added to the pickling bath, enabling to obtain a more noble electrode potential of the steel to be pickled, thereby allowing higher reaction kinetics. The species preferred as oxidant is the Fe 3+ ion. The possibility of obtaining a more noble potential of the steel to be pickled derives from the fact that the added ferric ions Fe 3+ behave as oxidant (being reduced to Fe 2+ ions) with respect of the steel (Fe) that is to be pickled according to reaction (1) (that derives from the reversible electro-chemical potential scale: E rev = - 447 mV SHE for the Fe 2+ /Fe couple; E rev = +771 mV SHE for the Fe 3 V Fe 2+ couple) . Therefore, the Fe 3+ ion is capable of being reduced to Fe 2+ ion during the pickling process, according to the cathodic half-reaction below: (4) Fe 3+ → Fe 2+ + e Also the cathodic half-reaction (4) occurs at the same time of the anodic half-reaction (1) . The resulting reaction (1) + (4) therefore is: (5) Fe + 2Fe 3+ → 3Fe 2+ According to the present invention, when the Fe 3+ ion is present as an additive the reactions (3) and (5) occur at the same time, with an increase of the global iron (Fe) dissolution kinetics. The working electrode potential Ew results, in this case by effect of the addition of the oxidising species (Fe 3+ ) in the bath, more noble than the potential in absence of additions. The amount of Fe 3+ ion that has to be added must balance the amount of Fe 3+ ion consumed in the cathodic reaction (4 ) . A good stirring of the bath further improves the pickling kinetics, allowing the depolarisation of the total cathodic reaction resulting from the sum of the reactions (2) and (4) that would tend, without stirring, towards diffusion control conditions. According to the present invention, the Fe 3+ ion can after all be added directly, e.g. as ferric chloride or ferric sulphate. However, it can be obtained in the bath by the addition of other oxidants, particularly H 2 0 2 (hydrogen peroxide), ozone or permanganates. In fact, once added to the pickling bath those oxidants come to contact with a solution already rich in Fe 2+ (due to the - j - primary pickling reaction (1) the bath is always rich m Fe 2+ ions) and induce the oxidation of Fe 2+ to Fe 3+ . Even oxygen alone, added in conditions of stirring by air bubbling, or admixed n an external reactor with the pickling solution, works as an oxidising agent capable of producing Fe 3+ . A preferred embodiment of the method described here according to the invention is that of obtaining Fe 3+ electro-chemically, sending the pickling solution as anolyte m an electrolytic cell, and carrying out an anodic oxidation of the Fe 2+ ion that, as aforestated, is always present in the bath, according to the reaction: (6) Fe 2+ → Fe 3+ + e. Therefore, it is an object of the present invention to provide a method for pickling steel products characterised n that in the pickling bath Fe 3+ is present m a concentration comprised in the range 6-60 g/1, directly added or produced m the pickling bath itself by the addition of an oxidising agent selected from the group comprising: hydrogen peroxide, ozone, permanganates, persulphates, and oxygen. Advantageously, the obtained increase of the pickling kinetics is a function of the added Fe 3+ concentration that is maintained m the pickling bath itself, thereby improving also the productivity of the industrial lines. A further advantage, according to the invention, lies m the fact that the maintenance and/or the control of the Fe 3+ ions concentration m the pickling bath allows a strict control of the most critical parameter of the process (that is the potential redox value of the system) with further advantages on the final quality of the product as well. According to the present invention, continuous pickling lines of carbon and/or magnetic steels can be employed advantageously also for the pickling of stainless steels with a < 15% Cr content. This result was ,„„^, 27162 - 4 - made possible by the fact that, according to the present invention, the Fe 3+ /Fe 2+ ratio is employed as a control parameter of the reaction kinetics, jointly with tne acid concentration control. In fact, when it is desired to use the same carbon and magnetic steels production line for tne stainless steels, e.g. of the AISI 409 type, the presence and the maintenance of appropriate Fe 3+ concentration values allows in any case to widely control the pickling kinetics, for the carbon steels as well as for the stainless ones, thereby making possible the combined utilisation of these production lines. Advantageously, the method according to the invention proves to be compatible with the possible presence of corrosion inhibitors, normally employed to avoid drawbacks of carbon steels over-picklmg . Furthermore, always according to the present invention, it is possible to pickle these abovementioned steel types without resorting to mechanical processes of descaling such for instance as peenmg. A further object of the present invention is to provide different embodiments, as hereinafter specified, of the method for the direct production of the oxidant Fe 3+ within the pickling bath: (l) direct addition of Fe 3+ as reactant (for instance: ferric chloride or sulphate) ; (n) addition of oxidants for the production Fe 3+ by oxidation of the Fe 2+ ion present in the bath to Fe 3+ ; (m) oxidation of the Fe 2+ ion n an electrolytic cell present in the bath itself to Fe 3+ . According to the third embodiment, the same pickling solution itself (composed of aqueous solution of hydrochloric acid and/or sulphuric and, optionally of phosphoric acid) constitutes the cell anolyte, the oxidising agent to be added as additive being the ferric ion produced at the anode by oxidation of tne ferrous ion present within the bath. The catholyte is preferably composed of an aqueous solution of hydrochloric and/or sulphuric acid. Also the catholyte is preferably sent out continuously nto the pickling solution, to reintegrate the HC1 or the H 2 S0 4 that is consumed during the pickling reaction. According to the method of the invention, an electro-chemical cell of the memorane type is preferably employed. The use of a cell to generate the oxidising species Fe 3+ , according to the third embodiment, is more advantageous in respect of a method wherein oxidants are directly added. A remarkable saving in operation cost is obtained, on account of the higher cost of the oxidising reactants themselves . Furthermore, some reactants entail stability problems within . the bath, or may cause, if not opportunely measured, the development of chlorine from the hydrochloric acid bath. The pickling bath according to the present invention has a temperature preferably comprised in the range 45-85 °C. The pickling solution is an aqueous solution of hydrochloric and/or sulphuric acid and optionally of pnosphoric acid, with the composition hereinafter expressed as percent by weight: - free HC1 from 0 to 250 g/1 (>100 g/1 if alone) ; - free H 2 S0 4 from 0 to 250 g/1 (>100 g/1 if alone) ; - free H 3 P0 4 from 0 to 100 g/1; - Fe tot = ( Fe 2+ + Fe 3+ ) > 50 g / 1 ; - Fe 3+ (additive) from 5 to 60 g/1; Furthermore, . products containing iron (steels) whereto the method of the present invention can be applied are selected from the group comprising: - carbon steels, rolled or anyhow hot or cold worked, particularly low carbon steels and carbon steels with a low, medium or high content of alloying elements; - magnetic steels (containing Si or Si and Al); - stainless steels with a low (<15%) Cr content, as, particularly, AISI 409. The present invention will be more clearly illustrated in the following detailed description of a preferred embodiment thereof, given as a non limiting example, with reference to the annexed figure. The addition of the Fe 3+ ion as oxidant if performed according to the methods as per the embodiments (1) and (n) is carried out by the introduction of the reagent into the bath m stechiometrically calculated amounts and considering the yields, both automatically and manually. According to the invention, in the method of the embodiment (m), an electro-chemical cell is employed. According to this method an electro-chemical treatment of the solution is carried out, whereby it is directly obtained n situ formation and the control at the appropriate concentration levels of the oxidising species Fe 3+ , originated by the Fe 2+ species anyhow contained within the bath. The control of the Fe 3+ ions concentration within the pickling bath and/or of the Fe 3+ /Fe 2_r ratio is obtained in an easy way by the setting and the regulations of the operative parameters of the cell. Hereinafter, the principles and criteria for the construction of a Fe 3+ producing electro-chemical cell are defined. a) Anolyte: The pickling solution itself is employed, continuously circulated (but a discontinuous treatment as well can be foreseen) from the bath by pumping; b) Anodic reaction: The anodic half-reaction which occurs in the cell (6) Fe 2+ → Fe 3+ + e. Regulating the cell flow the reaction (6) kinetics is controlled, and it becomes therefore possible to keep steady at the desired level the concentration of the oxidising additive Fe 3+ in the pickling solution. c) Catholyte: It was found that the most convenient way consists m utilising as catholyte a hydrochloric and/or sulphuric acid solution, that is sent to the bath according to the fact that the specific pickling process foresees the m- oath utilisation of hydrochloric or sulphuric acid or mixtures thereof. In principle, however, any catholyte wnatsoever may be utilised, or even directly the pickling solution, if the catholyte in this case is sorted out as exhausted. d) Cathodic reaction The cathodic reaction, for ease of description referred only to the hydrochloric acid, is: 2) 2H + + 2 e — H 2 ; (cathodic half-reaction) e) Anodic control: Regarding the control of the anodic current flow inside the electrolytic cell two alternatives are effective : e.l) Potenziostatic cell control. Operating with an electrode potential (> 771 mV SHE) that allows the oxidation reaction (6); regarding the maximum value it is advisable to choose a maximum value that does not allow (or anyhow limits to values that are not excessive) oxygen development, according to the following reaction: (7) 0 2 + 4H + + 4e - 2H 2 0 (E rev = +1229 mV SHE) Theoretically, the preselected potential E finally lies within the range 771 - 1229 mV SHE. In practice it can prove useful to set it at values even relatively nigher than 1229 mV (e.g. 1600), exploiting the fact that the oxygen development reaction occurs at a certain overvoltage and the kinetics involved may be negligible. e.2) Galvanostatic control This control is simpler (more cost-effective) to realise in a plant, but the abovementioned advantages right be lost. f) Membranes Different commercial membranes may be used , that differ in efficiency, employ temperature, duration, dimension. The electro-chemical cell considered, tested in a pilot plant, gave the following performances, that are reported hereinafter, merely by way of exemplification: - current efficiency: > 95% - cell potential (ΔV at terminals) = 2V - specific power ≡ 5W/dm 2 - anodic current density = 5A/dm 2 - consumption per mole of Fe 3+ produced < 0.1 k h Subsequently, preliminary lab tests were carried out, demonstrating that higher than standard weight losses are obtained by employing Fe 3+ additioned solutions. Finally, experimental results were verified in industrial processes. Further, the method of the invention is applicable for pickling products made of titanium and alloys thereof . EXAMPLES Hereinafter, examples of pickling of an hot-rolled AISI 409 steel carried out in lab and m industrial line and of two hot-rolled magnetic steels containing Si (the first magnetic steel being a Fe28 with an unoriented gram, 2.8%Sι, 0.4%A1; the second being an oriented gram G32, 3.2%Sι, 0.18%Cu) . 1 st Example with an AISI 409 type steel The standard pickling solution for the AISI 409 steel is composed by: - free HC1 =200 g/1 - total Fe (Fe to t = Fe 2+ + Fe 3+ ) in solution up to 90 g/1. It is essentially Fe 2+ , but a certain amount of Fe 3+ up to about 5g/l is always present due to natural oxidation m air . - T = 75 °C The industrial plant considered foresees four baths, each of approximately 15m. The line speed for the AISI 27162 -9 409 utilised in the tests is 10 m/mm and the resulting total pickling time is 360s. The preliminary experimental tests were carried out performing two subsequent dippings into the solution, of 180s each, or by a single dipping of 360s. Below Table 1 reports the obtained results. Table 1 AISI 409 STEEL T=75°C; HC1 =200 g/1 SCE=Standard Calomel Electrode The increases in the pickling kinetics (measured by the total weight loss ΔPtot values) are self evident when the additive Fe 3+ is present. Equally, as evidence of the illustrated mechanisms relative to the effect of the ferric ion on the steel working potential and, therefore, on the reaction kinetics, the table shows how in presence of Fe 3+ an increase of the electrode potentials (expressed in relation to the standard Calomel Electrode = SCE) occurs. The possibility of increasing the rates, according to the experimental data, was then verified m line. Then, a hot-rolled unpeened coil was utilised in a first trial with a specific speed of 10 m/mm with the abovedescπbed standard solution to proαuce a reference coil . The reference solution was then enriched with Fe 3 + until the Fe 3+ > 30 g/1 value was obtained. The amount of Fe 3+ to be produced per bath tank is obtained by the following expression: 60 g/1 x 25000 1 = 750 kg where 25000 1 is the volume of a bath tank. In subsequent test trials, three different methods were adopted as described hereinafter: a) Addition of hydrogen peroxide in the amount stechiometrically needed to obtain Fe + in solution 60 g/1, considering a total yield of approximately 80%. b) Additions of FeCl 3 for a Fe 3+ amount equal to 750kg Fe 3+ per bath tank. c) Adoption of an electro-chemical cell of the membrane type as follows : Surface : 5 m 2 of surface (V) C ei l = 2.5V Current (I) = 2.5kA, supplied as long as needed to obtain the desired Fe 3+ concentration of 30g/l. The amount of electrical charge Q needed to produce the desired Fe 3+ amount (i.e. 750kg) from Fe 2+ is easily calculated with the Faraday constant (i.e., 96500 Coulomb per mole of Fe 3+ produced) . Then, it is obtained: Q = 96500x750xl0 3 /56 = 1.3xl0 9 Coulombs. Then, the temperature was adjusted at 75°C and the trial was carried out with the line speed increased by 20% (from 10 to 12 m/min) . The coil obtained at the end of the trial is perfectly pickled according to the specifications. This result is perfectly reproducible with no variations and independent from the method utilised to add within the bath the desired amount of Fe 3+ . 2 πd Example with magnetic steels With reference to the case of the magnetic steel the procedure was completely analogous to the abovementioned one for the AISI 409 steel example. Two different steels were employed, both for the lab and in line trial tests: - Fe28 unoriented grain, 2.8% Si, 0.4% Al - G32 oriented grain, 3.2% Si, 0.18% Cu . For the pickling of these magnetic steels a line was utilised having three baths, each of 15m length. For the test materials the results were as follows: 2. a) G32 magnetic steel Line speed = 36 m/min HC1 concentration variable from 120 to 200 g/1 Temperature = 75°C Total pickling time = 75s. 2.b) Fe28 magnetic steel Line speed = 30 m/min HC1 concentration = 120 g/1 Temperature = 75°C Total pickling time = 90s. Preliminary lab tests were carried out with a single dipping for a time equal to the total (standard) pickling time. The data so obtained are reported in Tables 2 and 3, showing that additioned solutions with Fe 3+ (by addition of ferric chloride) and pickling times being equal, higher weight losses were obtained. Table 2 G32 MAGNETIC STEEL T=75°C SCE= Standard Calomel Electrode (*) Undetected potential T.able 3 Fe28 MAGNETIC STEEL T=75°C SCE= Standard Calomel Electrode (*) Undetected potential For the testing on the in line production, and with reference to a G32 coil having a thickness of 2.8mm, a line speed of 36 m/min was utilised with the standard solution to produce a reference coil. The reference solution was then enriched with Fe 3+ until obtaining a. concentration > 45 g/1 as an optimal value, by means of the described above two different methods for the AISI 409 steel example. Then, the temperature was adjusted at 75°C and the pickling started with a 20% increase of the line speed (43 m/min). Therefore, a coil perfectly pickled was obtained according to the specifications. Completely analogous results were obtained with the Fe28 steel, thus increasing of 20% the line speed (from 30 to 36 m/min) . The present invention is not limited to the embodiment examples, but includes any variation in the embodiments comprised within the scope of the following claims .

Claims: CLAIMS 1. A method for pickling steel products characterised in that in the pickling bath Fe 3+ is present in a concentration comprised in the range 6- 60g/l, directly added or produced in the pickling bath itself by means of the addition of an oxidising agent selected from the group comprising: hydrogen peroxide, ozone, permanganates, persulphates, and oxygen. 2. The method according to claim 1, wherein the presence of the oxidant ion Fe 3+ within the pickling bath is obtained by means of one of the following steps: direct addition of Fe 3+ as reactant deriving from ferric chloride or sulphate; - addition of oxidants apt to produce Fe 3+ by oxidation of the Fe 2+ ion present within the bath; and - oxidation of ion Fe 2+ to Fe 3+ in an electrolytic cell. 3. The method according to claim 1 or 2, wherein the said pickling solution is the cell anolyte, and is composed of an aqueous solution of hydrochloric and/or sulphuric acid and, optionally, of phosphoric acid; the oxidising agent to be added as an additive being the ferric ion which is produced at the anode by oxidation of the ferrous ion present within the bath. 4. The method according to any of the preceding claims, wherein the pickling solution is an aqueous solution of hydrochloric and/or sulphuric acid and, optionally, of phosphoric acid, having a composition hereinafter expressed as percent by weight: - free HCl from 0 to 250 g/1 (>100 g/1 if alone) - free H 2 S0 4 from 0 to 250 g/1 (>100 g/1 if alone) - free H 3 P0 4 from 0 to 100 g/1 - Feto as (Fe 2+ + Fe 3+ ) > 50 g/1 - Fe 3+ (additive) from 5 to 60 g/1 - Fe 3+ / Fe 2+ > 0.1 5. The method according to claim 4, wherein said pickling solution is at a temperature comprised within the range 40-90 °C. 6. The method according to any of the preceding claims, wherein the catholyte is preferably constituted by an aqueous solution of hydrochloric and/or sulphuric acid. 7. The method according to any of the preceding claims, wherein the catholyte is introduced continuously into said pickling solution. 8. The method according to any of the preceding claims, wherein said electro-chemical cell is of the membrane type, and wherein the operation is carried out by controlling the anodic electrode potential or galvanostatically. 9. The method according to any of the preceding claims, wherein the working electro-chemical potential (Ew) of said anode is > 771 mV SHE. 10. The method according to any of the preceding claims, wherein oxygen is fed in an external reactor with respect to the pickling bath; said reactor being set at a temperature lower and/or at a pressure higher or equal to the pickling bath. 11. The method according to any of the preceding claims, wherein the steel products to be pickled are selected from the group comprising: - carbon steels, rolled or anyhow hot or cold worked, particularly low carbon steels and carbon steels with a low, medium or high content of alloying elements; - magnetic steels (containing Si or Si and Al) ; and - stainless steels with a low (<15%) Cr content. 12. A method for pickling metal alloy products containing iron and/or titanium and alloys thereof, as previously described, exemplified and claimed.

Inventors: FORTUNATI SANDRO, MANCIA FRANCO, MUSSO AUGUSTO, FORTUNATI, SANDRO, MANCIA, FRANCO, MUSSO, AUGUSTO
Applicants: ACCIAI SPECIALI TERNI SPA, FORTUNATI SANDRO, MANCIA FRANCO, MUSSO AUGUSTO, ACCIAI SPECIALI TERNI S.P.A., FORTUNATI, SANDRO, MANCIA, FRANCO, MUSSO, AUGUSTO
Application year: 1998
Main classification: C23G1
IPC codes: C23G1