ELECTROLYTIC TIN PLATING PROCESS WITH REDUCED SLUDGE PRODUCTION

Abstract: Continuous electrolytic tin plating is accomplished in a bath containing 90-160 g/L sulfuric acid, 40-70 g/L tin ion and a grain refiner, at a speed of 900-1600 feet per minute and a current density as much as 1500 amperes per square foot or more.

Description: Electrolytic Tin Plating Process with Reduced Sludge Production Technical Field This invention relates to continuous electrolytic tin plating. The process includes a novel set of conditions resulting in the production of significantly less sludge than previous processes. The process is environmentally friendly also in its reduced consumption of power and drastic reduction of waste products containing phenolic groups. Its economic efficiency is realized partly through a significant reduction in capital equipment. Background of the Invention Conventional electrolytic tin plating processes for many years have used phenol sulfonic acid (PSA) as the major acidifying constituent of the electrolyte. Being organic and based on phenol, this compound has come under criticism in recent years because of the waste disposal problems it creates. The organic sludge it generates, to a great extent in combination with tin compounds, is complex and contains a high concentration of phenolic compounds generally considered to be undesirable. In addition, PSA is difficult to analyze in the electrolytic plating line, is toxic, requires a large volume of solution for the plating process, and consumes excessive amounts of power because of its relatively low conductivity. An acceptable substitute for PSA which eliminates or minimizes the above recited shortcomings would be beneficial to the industry both economically ' and environmentally. Electrolytic tin plating requires a source of tin ion and a conductive bath to promote the process of tin deposition. The conductivity of an acid electrolyte for tin plating generally improves with its acidity; tin is conventionally introduced in the form of tin sulfate . An electrolyte comprising tin sulfate and sulfuric acid in the range of 100-140 g/1 has been used for depositing tin on copper wires, foils and other electronic parts to make them solderable, and is described in Metal Finishing guide Book and Directory Issue, v. 94, No. 1A, 1996 p 224-297; see Table VIII. A non-continuous process for depositing bright tin on unspecified substrates apparently for use in the electronics industry is described by Commander and Paneccasio in US Patent 5,061,351 wherein the novel pyridinyl brightening agents are said to be useful through wide ranges of current densities, sulfuric acid concentrations, and metal ion concentrations. In US Patent 3,860,502, Johnson introduced the use of ethoxylated naphthol sulfonic acid (ENSA) as a brightening agent providing reduced foam and sludge in plating solutions containing 6-30 g/1 of free acid (calculated as H 2 S0 4 ) , which may be added as sulfuric acid - see column 4, lines 27-29. See also JP 6346273, which also uses ENSA and a sludge suppressor such as hydroquinone or resorcinol in a continuous electrolytic tin process, with H 2 S0 4 concentrations of 5-50 g/1. The authors observe that higher concentrations of sulfuric acid will lead to less sludge formation, but that high sulfuric acid concentrations will calise evolution of hydrogen gas and low tin deposition efficiency due to redissolving of the tin after it is deposited. Accordingly, much of the disclosure of JP 6346273 is devoted to the efficacy of various sludge suppressants used in conjunction with lower concentrations of sulfuric acid, i.e. in the range of 5-50 g/1. In Japanese Patent Application (Kokai) Hei JP 6- 346272, Itatsu and Oyagi disclose a high current density tin plating process which uses a bath containing, as a major component, 5-50 g/L of sulfuric acid, 40-100 g/L of tin (II) , brightening agent, and sludge suppressing agent. The deposition is conducted at a current density of 50 A/dm 2 "or higher." The authors say that if the concentration of sulfuric acid is higher than 50 g/L, "the dissolution of the steel strip will become serious, so that the iron concentration in the bath will increase." The presence of iron ions in the bath can be a significant problem, because, in addition to the corrosion of the strip, their generation implies a dissipation of current density to bring about the corrosion of the strip, thus making the process less efficient. High current density has a clear positive correlation to process efficiency. The presence of Fe t3 ions in the bath also tends to contribute to the generation of sludge by promoting the oxidation of stannous ions to stannic ions, which form the insoluble hydroxide; the Fe ** ions formed in the reaction can easily be oxidized again to Fe°, which again is available for the undesired conversion of the stannous ions to stannic. Summary of the Invention My invention is a high speed, high current density process for plating steel strip which utilizes an electrolyte bath of a particular composition under conditions which suppress the generation of sludge. My invention is a method of continuously tin plating steel strip comprising continuously passing said steel strip through an electrolyte bath. The bath may be contained in one, two, three or more vessels, but the economic benefit of the process is best achieved in one or two vessels. The bath comprises, in an aqueous medium, 90-160 g/L sulfuric acid, 40-70 g/L Sn ** and a grain refiner. The strip moves at a speed of 900-1600 feet/min while an electric current an electric current is imposed on the bath at a current density of up to 1500 or even as high as 2000 or more amperes per square foot of steel strip passing through the bath. In another form, my invention is a method of continuously tin plating steel strip while suppressing the generation of sludge having tin hydroxides as a major component comprising continuously passing the steel strip through an aqueous electrolytic bath at a speed of 900-1600 ft/min while imposing on the aqueous electrolytic bath an electric current at a current density of 200-1500 amperes per square foot of steel strip; the bath comprises 90-160 g/L sulfuric acid and 40-70 g/L Sn ++ from a source including less than 1 % hydroxides of tin. During the process, the pH of the bath is maintained no higher than 0.5 and its temperature between 90-130°F. The strip may then be passed to a rinsing tank. The process is highly efficient in the suppression of sludge formation, the production rate, the consumption of current, and the minimization of capital equipment. Unlike many contemporary electrolytic processes, my process does not use phenol sulfonic acid (PSA) , as the main component of the electrolyte. Rather, it uses sulfuric acid. While sulfuric acid itself is not new as a component of electrolytic tin plating processes, its use is new in my process conditions for tinplate manufacturing and in the concentrations I use, together with the other components of the bath which I employ. The particular balance of sulfuric acid concentration, pH, Sn ++ concentration, Fe ++ ions and temperature in the bath with current density imposed on the bath enables a high speed line to operate continuously with minimal generation of sludge, as will be demonstrated in the descriptions below. Brief Description of the Drawings Figure 1A is a graph of plating voltage as a function of H 2 S0 4 concentration, taken at a concentration of Sn ++ of 30 g/L; measurements were made at 300 and 1000 Amp/ft 2 and 110 °F. 5 a Figure IB is a graph of plating voltage as a function of H 2 S0 concentration, taken at a concentration of Sn ++ of 80 g/L; measurements were made at 300 and 1000 Amp/ft 2 and 110 °F. Figure 2 shows sludge generation as a function of H 2 S0 4 concentration, with 60 g/L Sn ++ and 110 °F. Figure 3 shows sludge generation as a function of Sn ++ concentration at 126 g/L H 2 S0 4 and 110°F. Figure 4 graphically compares sludge generation for PSA and sulfuric acid (SA) electrolyte with and without ENSA grain refiner, as a function of temperature. Figure 5 compares sludge collection by filtration from PSA and SA electrolyte under a variety of conditions. Figure 6 is a graph of the effect of ferric ion on sludge generation in my sulfuric acid electrolyte and the conventional PSA electrolyte, both with ENSA grain refiner. Detailed Description of the Invention My invention is based on the results of various experiments which will be explained below. Sulfuric acid was selected as the basic acid for the electrolyte because (a) it is a simple inorganic, adding no phenolic or other organic radicals to the bath, (b) its effect on pH is highly efficient, realizing a low sludge formation rate, and (c) its effect on conductivity is highly beneficial to the process . The optimum range of concentration of sulfuric acid was chosen taking into account the conductivity of the solution and the overall sludge production of the solution. 19542 Effect of Sulfuric Acid Concentration on Conductivity Plating power consumption is the product of volts and amperes and is affected by the conductivity of the electrolyte. When the .conductivity is increased, the voltage decreases for a given applied amperage, and consequently the power consumption decreases. Experiments measuring the plating voltage as a function of sulfuric acid concentration at two different concentrations of Sn ++ are summarized in Figure 1. The data were gathered at 110°F. The results show that the sulfuric acid electrolyte containing stannous ion provides excellent conductivity in the range 90-160 g/L. Above 180g/L there is a significant risk of increased power consumption due to the passivation of tin anodes, and higher viscosity of the electrolyte, which lowers the mobility of ions responsible for transferring the current in the solution. Effect of Sulfuric Acid Bath on Sludge Generation All of the conventional commercially used tin plating processes generate sludge. The sludge is classified as a hazardous waste, particularly if it contains phenol, as is the case with sludge generated by PSA- based electrolytes, or cyanide, as in the case of the halogen systems. Disposal is difficult and costly. In addition, sludge can produce scratches, nodules, "pick-up", and stains on the product, and can block nozzles, pumps and other circulation equipment. Using an electrolyte containing 60 g/L Sn* + and 3 g/L ENSA at 110°F, solutions were prepared containing 0, 8 18, 36, 54, 72, 90, 108, 126, 144, 162, 216 and 234 g/L of H 2 S0 4 and maintained in vessels in a water bath at 110°F for 24 hours. Solutions were then filtered through filter paper, the filter paper was rinsed on the outside to remove absorbed sulfuric acid, and upon drying the filter paper was re-weighed to determine the dry weight of the sludge. Results in Figure 2 show that the generation of sludge declines steadily as a function of sulfuric acid concentration, reaching a minimum at about 90 g/L and increasing rapidly beginning about 162 g/L; solubility of the sludge products appears to decrease as the concentration of free sulfuric acid increases. The results shown in Figure 2 were confirmed by similar experiments using solutions of sulfuric acid at different concentrations. The upper limit of sulfuric acid concentration, based on these experiments, was determined to be 160 g/L; the optimum was determined to be 130 g/L ±10 g/L. Relation of Sn" Concentration to Current Density A relatively high concentration of tin ions in an operation conducted at high current density will enable good production rates in an economically efficient plant. Operation at high current density is desirable for reducing the amount of solution, plating tanks, rolls, other equipment, and for maintenance of the plating line. Conventionally as many as 12 tanks may be used, and many commercial tinning lines use from 5 to 12 tanks of electrolyte. The use of relatively high concentrations of tin ions allows for better diffusion of the ions to the surface of the fast-traveling strip, and enables the economically efficient high current density to produce consistently good product . Effect of Sn Concentration on Sludge Generation To evaluate the effect of tin concentration on sludge generation, an experiment was conducted in six 500 ml sulfuric acid solutions containing 130 g/L of H 2 S0 4 . Tin sulfate was then added to the solutions to give concentrations of Sn tt of 30, 40, 50, 60, 70, and 80 g/L. The solutions (in vessels) were then placed in a water bath at 110°F and allowed to stand for 24 hours. They were then filtered through weighed filter paper and the filter paper was rinsed on the outside to remove absorbed sulfuric acid. Upon drying, the filter paper was re-weighed to determine the dry weight of the sludge. The results of the experiment are reported in Figure 3. Sludge generation increased only slightly between 30 and 70 g/L Sn ** , and then, above 70 g/L, a drastic increase was observed. It was speculated that the solutions above 70 g/L may not have been able to dissolve the tin sulfate. While concentrations of stannous ion in the range of 30-70 g/L are operable, I prefer to use 40-60 g/L, with a target of 50g/L. Comparison of Sludging due to Oxidation A series of experiments was devised to estimate the effect of atmospheric oxidation on the proposed H 2 S0 4 /Sn +* solution as compared to a conventional PSA electrolyte at temperatures ranging from 90 to 120°F. First, four solutions were made containing (a) 130 g/L sulfuric acid and 60 g/L Sn ++ with 3 g/L ENSA and (b) without ENSA, (c) 60 g/L PSA and 30 g/L Sn ++ with 3 g/L ENSA and (d) without ENSA. The four solutions, 10 500 mL each, were maintained at equal conditions for each run (temperatures held constant in a water bath at pressures of about 7 psi) and sparged with oxygen for four hours. After four hours of sparging, the sludge that had formed was collected by filtration through a weighed filte,r paper, and, upon drying the paper, the filter paper was re-weighed to determine the dry weight of the sludge produced by each of the four solutions. The results are shown in Figure 4, from which it may be seen that the sulfuric acid electrolyte produces less sludge with and without the ENSA additive. It may be seen also that sludging tends to increase above 110°F for all systems tested and accordingly, although my process is operable between 90 and 130°F, I prefer to conduct it at temperatures between 100 and 110°F. Note that ENSA' s beneficial effects in the sulfuric acid electrolyte are most noticeable when temperatures stray to levels above and below the preferred range. Antioxidants are known to be of benefit in electrolytic baths used for continuous tinplating, and many readily available antioxidants are useful in or at least compatible with my process. Antioxidants which may be used in effective amounts in my invention include tartaric acid, ammonium potassium tartrate, sodium tartrate, potassium sodium tartrate, hydroxylamine hydrochloride, resorcinal, p- nitrophensene, amino antipyrine, cerve ammonium nitrate, d-gluconic acid, N-propyl gallate, diphenyl amine sulfamic acid, hydroquinone , and pyrogallic acid. These and other antioxidants are effective in various amounts to various degrees to inhibit the oxidation of Sn +t to Sn +++< . 11 The Effect of pH on Sludge Formation Atmospheric oxidation is a major source of sludge generation under actual operating conditions. The reaction taking place due to the presence of dissolved oxygen is ^0 2 + 2H * + Sn +* -→ Sn 4+ + H 2 0 ΔG° = -49kcal (Eq. 1) Sn + * + 2H 2 0 -→ Sn(0H) 2 + 2H* K h = 2 x 10 "3 (Eq. 2) Sn 4 * + 2H 2 0 -→ Sn(OH) 4 + 2H + K h = 10 (Eq. 3) The negative free energy (ΔG°) value seen in equation 1 indicates that the reaction will go to the right in the presence of an oxidant, thus forming unstable Sn 4+ which further hydrolyzes and forms an insoluble Sn(OH) 4 . The insoluble hydroxides eventually precipitate out and are seen as sludge. The Sn ++ can also be hydrolyzed to produce the insoluble Sn(OH) 2 . However, the K h (hydrolysis constant) for stannic ions (10) is about 5000 times higher than that of stannous ions (2*10 ~3 ) , meaning the formation of Sn(OH) 4 is much more favorable than Sn(0H) 2 as seen in equations 1-3. It is believed that the difference in pH accounts for the difference in sludging results which may be seen in Figure 5. For this study, 500 ml solutions of PSA (with 30 g/L Sn t+ ) and sulfuric acid (with 60 g/L Sn ** ) and the sludge formed was collected through a series of five filtrations, with the filtrate from the previous filtration being used as the solution for the next. The first sludge filtration was performed after three hours of oxygen sparging in a 110°F water bath, the next three were performed after 24 hour intervals ΛΛ M Λ , „ PCT/US98/21150 99/19542 12 in a water bath at 110°F with no oxygen sparging, and the final filtration was performed after 48 hours at ambient temperature with no oxygen sparging. The sludges were collected by filtration through weighed filter paper and upon drying the dry weight of the sludge was determined. The PSA electrolyte consistently produced at least twice as much sludge as the sulfuric acid electrolyte. Furthermore, the PSA electrolyte continued to produce a significant amount of sludge after several filtrations, whereas the sludge produced by the sulfluric acid electrolyte dropped to approximately zero after three filtrations, with the majority seen in the figure for the last two filtrations due to H 2 S0 4 absorbed in the filter paper. Contribution of Ferric Ions to the Sludging Process Iron may enter the electrolyte in a commercial facility from dissolution of the strip in the plating solution and from drag-out from the pickling process. Equation 4 is the basis for the following discussion. 2Fe 3+ + Sn" -→ Sn + + 2Fe + * ΔG° = -28.5Kcal (Eq. 4) The reaction produces results similar to atmospheric oxidation, due to the same mechanism of transformation of more stable stannous ions to the less stable stannic state. Once the stannic ions are generated, the reaction that produces sludge is identical to the one described above for atmospheric sludge generation. To further complicate the problem, the Fe ++ ions generated may be oxidized in a second oxidation reaction by dissolved oxygen and/or anodically during 13 application of electrolysis conditions to become Fe 3t ions again. Therefore, this oxidation/reduction reaction becomes cyclic and consequently, significant amounts of sludge can be generated in this manner. Ferric ions can also be a problem because they tend to lower the current efficiency of the process by stealing the cathodic current and/or corroding the tinplate in the solution. Fe* ++ + e = Fe" (cathodic reduction) ΔG° = -35.5Kcal (Eq 5) 2Fe* *+ + Sn° (tinplate) = 2Fe* + + Sn + * (corrosion of tinplate); ΔG° = -41.9 Kcal (Eq 6) To investigate the effect of the presence of iron in the electrolyte, four solutions were prepared to compare the sulfuric acid electrolyte to a PSA electrolyte as in the previous experiment . Ferric ions (as ferric sulfate) were added to aliquats of the solutions in concentrations of 0.0, 0.2, 1.0, and 5.0 g/L Fe +++ for each of the two types of electrolytes . Once the solutions were prepared, they were maintained under equal conditions, and were sparged with oxygen for 4 hours to simulate the oxidation which might take place in a commercial facility. Throughout the experiments, the pressure was maintained at about 7 psi, and the temperature was held constant at 110°F in a water bath. After the four hour sparging, the sludge that had formed was collected by filtration through a weighed filter paper. Upon drying the filter paper, it was re-weighed to determine the dry weight of the sludge produced by each of the four types of solution. The results may be seen in Figure 6. Both types of solution demonstrated a tendency 14 toward increasing amounts of sludge with increasing iron content. However, the conventional PSA electrolyte showed a much greater increase in sludge generation as the ferric ions are added than the sulfuric acid electrolyte. These results are consistent with the discussion of the theory of tin hydrolysis above and its relation to the pH of the solution. They are also consistent with the other sludge generation results comparing PSA and sulfuric acid, in that the sulfuric acid solutions produced less sludge. Effect of the Condition of the Tin Source It is known that, because of internal redox reactions and a residue of acid moisture, commercial tin sulfate tends to discolor and degrade when held at around 60°C (140°F) . Such temperatures are not uncommon in steel mills and electrolytic tin plating mills. I have speculated that even at temperatures lower than 140°F, a slow degradation may take place in the solid state of the SnS0 4 over time under various types of storage conditions. Accordingly, an experiment was devised to test sludging with filtered and unfiltered tin sulfate solutions. The first test was conducted by first preparing three sulfuric acid electrolyte solutions differing only in the source of tin sulfate. The solutions, each containing 110 g/L SnS0 4 , were maintained under equal conditions and were sparged with oxygen for 4 hours to simulate oxidation. Throughout the experiments, the pressure was maintained at about 7 psi and the temperature was held constant at 110°in a water bath. After the four hour sparging, the sludge that had 15 formed was collected by filtration through a weighed filter paper, and upon drying the paper, the filter paper was re-weighed to determine the dry weight of the sludge produced by each of the four ((three??)) solutions. The results are seen in Table 1, which shows a definite relationship between the age of the tin sulfate and the amount of sludge formed. Table 1 Tin Sulfate Source Wt . Sludge (g/L) New Fisher SnS0 4 0.5 Atotech Commercial SnS0 4 1 Aged Fisher SnS0 4 46 In another test, a one liter solution of sulfuric acid and 110 g/L tin sulfate was split into two equal 500 ml portions. One of the portions was then filtered immediately and the other was left untouched. After the filtration was completed, both solutions were maintained under equal conditions and were sparged with oxygen for 4 hours to also simulate oxidation. Throughout the experiments the pressure was maintained at about 7 psi and the temperature was held constant at 110° in a water bath. After the four hour sparging, the sludge that had formed was collected by filtration through a weighed filter paper. Upon drying the paper, the filter paper was re-weighed to determine the dry weight of the sludge produced by each of the four solutions. As seen in Table 2, the results of this test are that the pre-filtered solution contained very little sludge compared to the one that was not filtered. 16 Table 2 Source t . Sludge (g/L) Old Atotech SnS0 4 (filtered) 0.18 Old Atotech SnS0 4 (not filtered) . 1.3 This shows, as was seen before, that the sludge, or a major portion of it, must have already been present in the tin sulfate before the solution was made. It should be understood that once the sludge is made or is present in the electrolyte, it cannot by present technology be conveniently re-dissolved. Also note that the PSA contains less tin sulfate than the sulfuric acid solution; therefore it should generate less sludge, meaning that the experiments above comparing PSA electrolyte with sulfuric acid electrolyte should be reviewed with the understanding that the sulfuric acid electrolyte may have begun the experiment with an absolute quantity of sludge present significant greater than the amount of sludge initially present in the PSA solutions. In any event, one aspect of my invention involves the filtration of the tin sulfate solution before adding it to the electrolyte. Grain Refiners It is known that the addition of surfactants to an electrolyte in an electrolytic deposition process can affect the nucleation process during electrocrystallization, and thereby affect the nature and appearance of the final coated surface. The mechanism of the interreaction of the surfactant is complex and there is not complete agreement in the art as to its specifics, but the prevailing view is that 17 the organic surfactant absorbs on the fast growing sides of the crystals, preventing or inhibiting dendritic powdery growth and promoting nucleation, leading to a more prolific nucleation and a final product which is smooth and compact. One absorbed organic molecule may affect many metal ions, and therefore the effects of even a small amount of surfactant are readily manifested. Generally any of the known grain refiners is compatible with my invention. I prefer to use nonionics; some of the more useful types are the ethoxylated nonionics such as ethylene oxide adducts of alkylated phenols (Triton X-114, Triton X-100, Tergitol NPX, Tergitol NP35, Tergitol NP-33, Tergitol TP-9, ENSA-6, Priminox T-25, Propomeen C/12, and bisphenol A. Aliphatic alcohols such as Surfonic TD- 90 and Surfonic TD-150 may also be used, as may alkylated mercaptans such as Tergitol 12-M-6, Tergitol 112-M-8.5, and Tergitol 12-M-10. I prefer to use as a grain refiner Tergitol TP-9 or Tergitol NP-33, in a concentration of 1-4 g/L.

Claims: 18 Claims 1. Method of continuously tin plating steel strip comprising continuously passing said steel strip through an electrolyte !bath comprising, in an aqueous medium, 90-160 g/L sulfuric acid, 40-70 g/L Sn ++ and a grain refiner, at a speed of 900-1600 feet/min while imposing on said bath an electric current at a current density of up to 2000 amperes per square foot of steel strip passing through said bath. 2. Method of claim 1 wherein said bath also includes an amount of antioxidant effective to inhibit the oxidation of Sn + * to Sn +4 . 3. Method of claim 1 wherein said grain refiner is Tergitol TP-9 or Tergitol NP-33 and is present in an amount of 1 to 4 g/L. 4. Method of claim 1 wherein said bath is present in one or two vessels. 5. Method of claim 1 wherein said bath has a pH no higher than 0.5. 6. Method of claim 1 wherein said bath generates no more than about lg/L sludge over a period of two weeks . 7. Method of claim 1 followed by passing said strip to a rinsing tank. 9. Method of claim 1 wherein said bath is maintained at temperatures between 90 and 130°F. 19 10. Method of claim 1 wherein the Sn** is introduced to the bath from a solution of tin sulfate which has been filtered. 11. Method of claim 1 wherein the current density is about 200 to about 15dθ amperes per square foot of steel strip passing through said vessels. 12. Method of continuously tin plating steel strip while suppressing the generation of sludge having tin* 4 hydroxides as a major component comprising continuously passing said steel strip through an aqueous electrolytic bath at a speed of 900-1600 ft/min while imposing on said aqueous electrolytic bath an electric current at a current density of 900- 1500 amperes per square foot of steel strip, said bath comprising 90-160 g/L sulfuric acid and 40-70 g/L SN * * from a source including less than 1 % hydroxides of tin, and while maintaining the pH of said bath no higher than 0.5 and its temperature between 90-130°F. 13. Method of claim 12 wherein no more than 1 gram of sludge is precipitated per liter of electrolyte. 14. Method of claim 12 wherein the Fe + * concentration in said electrolytic bath is between 1 and 20 grams per liter. 15. Method of claim 12 wherein the temperature of said bath is held between 100 and 110°F. AMENDED CLAIMS [received by the International Bureau on 25 January 1999 (25.01.99); original claim 8 cancelled; original claims 3, 11 and 14 replaced by amended claims 3, 10 and 13; original claims 9 - 15 renumbered 8 - 14; remaining claims unchanged (2 pages)] 1. Method of continuously tin plating steel strip comprising continuously passing said steel strip through an electrolyte bath comprising, in an 5 aqueous medium, 90-160 g/L sulfuric acid, 40-70 g/L Sn ** and a gram refiner, at a speed of 900-1S00 fee /mm while imposing on said bath an electric current at a current density of up to 2000 amperes per square foot of steel strip passing through said bath. 10 2. Method of claim 1 wherein said bath also includes an amount of antioxidant effective to inhibit the oxidation of Sn ** to Sn *4 . 3. Method of claim 1 wherein said gram refiner s a nomonic ethylene oxide adduct of an 15 alkylated phenol and is present in an amount of 1 to 4 g/L. 4. Method of claim 1 wherein said bath is present one or two vessels . 5. Method of claim 1 wherein said bath has 20 a pH no higher than 0.5. 6. Method of claim 1 wherein said bath generates no more than about lg/L sludge over a period of two weeks . 7. Method of claim 1 followed by passing 25 said strip to a rinsing tank. 8. Method of claim 1 wherein said bath is maintained at temperatures between 90 and 130°F. 9. Method of claim 1 wherein the Sn ** is introduced to the bath from a solution of tin sulfate 30 which has been filtered. 10. Method of claim 4 wherein the current density is about 200 to about 1500 amperes per square foot of steel strip passing through said vessels . 21 11. Method of continuously tin plating steel strip while suppressing the generation of sludge having tin* 4 hydroxides as a major component comprising continuously passing said steel strip through an aqueous electrolytic bath at a speed of 900-1600 ft/min while imposing on said aqueous electrolytic is bath an electric current at a current density of 900-1500 amperes per square foot of steel strip, said bath comprising 90-160 g/L sulfuric acid and 40-70 g/L SN ++ from a source including less than 1% hydroxides of tin, and while maintaining the pH of said bath no higher than 0.5 and its temperature between 90-130°F. 12. Method of claim 11 wherein no more than 1 gram of sludge is precipitated per liter of electrolyte. 13. Method of claim 11 wherein said electrolytic bath includes an Fe** concentration between 1 and 20 grams per liter. 14. Method of claim 11 wherein the temperature of said bath is held between 100 and 110°F.

Inventors: ILGAR ERSAN, ILGAR, ERSAN
Applicants: ILGAR ERSAN, USS ENG & CONSULT, ILGAR, ERSAN, USX ENGINEERS AND CONSULTANTS, INC.
Application year: 1998
Main classification: C25D3
IPC codes: C25D3