CN102424983A - Combined electrolysis technology for high-impurity Sn-Pb alloy - Google Patents
Combined electrolysis technology for high-impurity Sn-Pb alloy Download PDFInfo
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Abstract
The invention discloses a combined electrolysis technology for high-impurity Sn-Pb alloy. The combined electrolysis technology comprises the following working procedures of melting, pouring, electrolyzing Sn slag frame material, electrolyzing an anode plate and recovering and self-supplementing anode mud Sn. The combined electrolysis technology comprises the following specific steps: smelting the high-impurity Sn-Pb alloy in a Sn melting pot at the temperature of 500-650DEG C, taking out the Sn slag is taken out and carrying out anode pouring; preparing the Sn slag which is taken out into particles of which the granularity is 5-30mm, placing the particles into a frame, adding frame material electrolyte, and carrying out diaphragm electrolysis, wherein the voltage of an electrolytic bath is 0.3-3.5V, and the current density is 30-80A/m<2>; pouring the alloy into the anode plate and carrying out plate material electrolysis; and recovering the anode mud Sn for supplementing the electrolyte by self. According to the combined electrolysis technology disclosed by the invention, the high-impurity Sn-Pb alloy is firstly divided into particle material and plate material, and the particle material and the plate material are respectively subjected to frame material electrolysis and plate material electrolysis; the Sn in the anode mud is recovered and supplemented by self to improve the ion concentration of the electrolyte; a series of problems that anode is passivated in the electrolysis process, ion concentration is lowered, bath voltage is too high, current efficiency is low and the like can be solved; and the electrolysis process can be successfully carried out, the current efficiency and the direct yield of the product are improved, and the comprehensive direct yield is 98%.
Description
Technical field
The invention belongs to the non-ferrous metal metallurgy technical field, be specifically related to a kind of process stabilizing, easy and simple to handle, energy-saving and cost-reducing, effectively reduce production costs, be suitable for the combination electrolysis process of high assorted terne metal.
Background technology
Thick tinsel tradition is carried out the bi-metal electrolysis method and is produced astute and able tin with the casting positive plate in silicofluoric acid electrolytic solution.The stanniferous flue dust that tin industry is given up admittedly and when fuming is handled, produced, and the difficult ore dressing of the many metals of slicker solder, the slag of the plumbous refining process of tin; The alloy that when retailoring, produces mostly contains a large amount of antimony (Sb>2%), arsenic (As>2%), copper (Cu>1%), iron (Fe>0.5%), bismuth (Bi>0.2%), uses electrorefining; Then when anode casting, produce a large amount of slicker solder slags, reduced the electrolysis direct yield, during positive plate electrolysis simultaneously because the existence of hard point phase (is the sosoloid of base with compound S nSb); Can form tight zone and produce passivation, cause the electrolytic solution concentration of metal ions to descend, bath voltage raises; Current efficiency reduces, even electrolytic process can't carry out.Existing for this reason people develops and use membrane electrolysis, and thick tinsel is refilled the frame electrolysis after with shrend corning, and this method exists production efficiency low, the reduction of electrolytic solution concentration of metal ions, problems such as additional difficulty.The inventor has developed a kind of combination electrolysis process that is suitable for high assorted terne metal through research for many years, has overcome the deficiency of prior art well, and evidence is respond well.
Summary of the invention
The present invention provides a kind of process stabilizing, and is easy and simple to handle, energy-saving and cost-reducing, effectively reduces production costs, and is suitable for the combination electrolysis process of high assorted terne metal.
The objective of the invention is to realize like this, comprise that smelting and pouring, the electrolysis of scruff frame material, positive plate electrolysis, anode sludge tin reclaim the self-adding operation, specifically comprise following operation:
A, smelting and pouring: the assorted terne metal of height is put into 500 ~ 650C ° solder pot fusing, pull scruff out, carry out anode casting;
B, the electrolysis of scruff frame material: the scruff of pulling out is processed the particle that granularity is 5 ~ 30mm; Frame up then; Put into frame material electrolytic solution; Carry out diaphragm electrolysis; Bath voltage 0.3 ~ 3.5V, current density 30 ~ 80A/
;
C, positive plate electrolysis: alloy pours into positive plate, puts into plate electrolytic solution, carries out board-like electrolysis;
D, anode sludge tin reclaim self-adding: the anode sludge that described plate and the electrolysis of frame material produce is put into acid-resistant reacting kettle with 100 ~ 350g/l hydrochloric acid after washing, and liquid-solid ratio 5:1 ~ 8:1, stirs 3 ~ 5 hours to leach tin, arsenic, antimony, copper, bismuth by temperature 80 ~ 95C °; Leached mud solution is with steam-heated cal(l)andria to 40 ~ 65C °, through iron powder replacement 4 ~ 6 hours, removes impurity such as antimony in the solution, bismuth, copper, arsenic; Solution after the displacement removal of impurities is heated to 50 ~ 80 C °; Be neutralized to PH0.5 ~ 1 degree of depth with calcium hydroxide again and take off antimony; Continue to be neutralized to PH4.5 ~ 5 and make the stannic hydroxide hydrolytic precipitation, stannic hydroxide with hot water clean to the chlorine root below 0.5 ~ 1%, the stannic hydroxide that obtains; Recycle silicon fluorate electrolytic solution normal temperature leaches, and leach liquor returns the consumption of electrolytic solution tin ion in electrolytic system complementary block material electrolyzer and the plate electrolyzer.
The present invention makes up electrolysis process the assorted terne metal of height is divided into pellet and plate earlier, carries out electrolysis of frame material and plate electrolysis respectively; A series of problems such as the tin and the self-sufficiency of reclaiming in the anode sludge cover to improve electrolyte ion concentration, have solved the anode passivation that occurs in the electrolytic process, and ionic concn descends, and groove is pressed too high, and current efficiency is low.Electrolytic process is carried out smoothly, and improved current efficiency and product direct yield, comprehensive direct yield 98%.
Description of drawings
Accompanying drawing is a process flow diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing the present invention is further described, but never in any form the present invention is limited, any change or improvement based on training centre of the present invention is done all belong to protection scope of the present invention.
Shown in accompanying drawing, the present invention includes smelting and pouring, the electrolysis of scruff frame material, positive plate electrolysis, anode sludge tin recovery self-adding operation, specifically comprise following operation:
Described smelting and pouring is the assorted terne metal of height to be put into 500 ~ 650C ° solder pot fusing, pulls scruff out, carries out anode casting;
The electrolysis of described scruff frame material is that the scruff of pulling out is processed the particle that granularity is 5 ~ 30mm, frames up then, puts into frame material electrolytic solution, carries out diaphragm electrolysis, bath voltage 0.3 ~ 3.5V, current density 30 ~ 80A/m
2
Described positive plate electrolysis is that the tin alloy fused solution is poured into positive plate, puts into plate electrolytic solution, carries out board-like electrolysis;
Described anode sludge tin reclaim self-adding be the anode sludge that plate and the electrolysis of frame material are produced after washing, put into acid-resistant reacting kettle with 100 ~ 3500g/l hydrochloric acid, liquid-solid ratio 5:1 ~ 8:1, stirs 3 ~ 5 hours with leaching tin, arsenic, antimony, copper, bismuth by temperature 80 ~ 95C °; Leached mud solution to 40-65C °, through iron powder replacement 4 ~ 6 hours, is removed impurity such as antimony in the solution, bismuth, copper, arsenic with steam-heated cal(l)andria; 50 ~ 80 C ° of solution heating after the displacement removal of impurities; Be neutralized to PH0.5 ~ 1 degree of depth with calcium hydroxide again and take off antimony; Continue to be neutralized to PH4.5 ~ 5 and make the stannic hydroxide hydrolytic precipitation, stannic hydroxide with hot water clean to the chlorine root below 0.5 ~ 1%, the stannic hydroxide that obtains; Recycle silicon fluorate electrolytic solution normal temperature leaches, and leach liquor returns the consumption of electrolytic solution tin ion in electrolytic system complementary block material electrolyzer and the plate electrolyzer.
The described diaphragm electrolysis that frames up is that the slicker solder slag that cast produces is packed in plastics and other the acidproof bag; Put into conducting plates in the bag by the cast of homogeneity alloy; Bag is put into acidproof frame of plastic form anode; Negative electrode is formed by tin alloy homogeneity of the product alloy casting, and anode, negative electrode are packed in the frame material electrolyzer, and put into silicofluoride salt electrolytic solution and carry out electrolysis.
The total acid H of described frame material silicofluoride salt electrolytic solution
2SiF
6Be 50 ~ 120g/l, free acid H
2SiF
6Be 40 ~ 90g/l, Sn
AlwaysBe 10 ~ 80g/l.
The total acid H of described frame material silicofluoride salt electrolytic solution
2SiF
6Be 60 ~ 100g/l, free acid H
2SiF
6Be 50 ~ 80g/l, Sn
AlwaysBe 17 ~ 70g/l.
The total acid H of described frame material silicofluoride salt electrolytic solution
2SiF
6Be 70 ~ 90g/l, free acid H
2SiF
6Be 65 ~ 75g/l, Sn
AlwaysBe 25 ~ 50g/l.
Described alloy liquid then is cast into alloy anode, puts into normal plate silicofluoride salt electrolytic solution and carries out electrolysis, bath voltage 0.1 ~ 0.3V during electrolysis, current density 60 ~ 120A/m
2
The total acid H of described plate silicofluoride salt electrolytic solution
2SiF
6Be 60 ~ 210g/l, free acid H
2SiF
6Be 45 ~ 160g/l, Sn
AlwaysBe 8 ~ 80g/l.
The total acid H of described plate silicofluoride salt electrolytic solution
2SiF
6Be 80 ~ 190g/l, free acid H
2SiF
6Be 65 ~ 140g/l, Sn
AlwaysBe 12 ~ 60g/l.
The total acid H of described plate silicofluoride salt electrolytic solution
2SiF
6Be 100 ~ 170g/l, free acid H
2SiF
6Be 85 ~ 120g/l, Sn
AlwaysBe 25 ~ 45g/l.
The total acid H of the leaching electrolytic solution of described D operation
2SiF
6Be 80 ~ 210g/l, free acid H
2SiF
6Be 40 ~ 160g/l, Sn 3 ~ 20g/l, Pb3 ~ 20g/l.
Embodiment 1
Melt through 500 ~ 650C ° of solder pot with the high assorted terne metal of raw material (composition stanniferous 45%, lead 35%, arsenic 2%, antimony 5%, copper 1%, bismuth 0.5%, iron 1%); Pulling 20% (wherein stanniferous 40%, plumbous 34%, arsenic 5%, antimony 8%, copper 1.2%, bismuth 0.7%, iron 1.5%) that scruff accounts for total alloy out, to process granularity be 5 ~ 30mm particle; The frame material electrolyzer of packing into is put into total acid H
2SiF
6Be 50g/l, free acid H
2SiF
6Be 40g/l, Sn
AlwaysFrame material silicofluoride salt electrolytic solution for 10g/l carries out electrolysis, bath voltage 0.3 ~ 3.5V, current density 30A/m
2, alloy product composition stanniferous 38.3%, lead 61.2%, arsenic 0.005%, antimony 0.012%, copper 0.0025%, bismuth 0.003%, iron 0.0023%, electrolysis direct yield 40%.
Alloy liquid then is cast into alloy anode (stanniferous 51%, lead 40%, arsenic 1%, antimony 2.5%, copper 0.3%, bismuth 0.1%, iron 0.7%), puts into total acid H
2SiF
6Be 60g/l, free acid H
2SiF
6Be 45g/l, Sn
AlwaysCarry out electrolysis, bath voltage 0.2V, current density 60A/m in the plate silicofluoride salt electrolytic solution for 8g/l
2, alloy product stanniferous 50.8%, lead 49.1%, arsenic 0.003%, antimony 0.007%, copper 0.0016%, bismuth 0.001%, iron 0.002%, direct yield 85%.
The anode sludge (stanniferous 30 ~ 45%, lead 5 ~ 20%, arsenic 2 ~ 8%, antimony 8 ~ 30%, copper 2 ~ 8%, bismuth 1 ~ 8%, iron 2 ~ 10%) by plate and the electrolysis of frame material produce after washing, is put into acid-resistant reacting kettle and is used 250g/l hydrochloric acid, liquid-solid ratio 5:1; Temperature 80C ° of churning time leached tin, arsenic, antimony, copper, bismuth in 5 hours; Leaching yield>94%, leached mud is used for extracting precious metals such as silver, gold, palladium, solution with steam-heated cal(l)andria to 40C °; Through iron powder replacement 6 hours; Remove impurity such as antimony in the solution, bismuth, copper, arsenic, rate of displacement>85%, replacement slag is further separated arsenic, antimony, copper, bismuth.Displaced liquid heats 60 C ° and is neutralized to the PH0.5 degree of depth with calcium hydroxide and takes off antimony; Continue to be neutralized to PH4.5; Make the stannic hydroxide hydrolytic precipitation; Stannic hydroxide with hot water clean to the chlorine root below 1%, the stannic hydroxide that obtains (stanniferous 60.78%, plumbous 1.94%, arsenic 0.144%, antimony 0.1559%, copper 0.238%, calcium 6.07%, iron 0.776%, cl ions 0.67%) is with electrolytic solution (total acid H
2SiF
6Be 80g/l, free acid H
2SiF
6Be 40g/l; Tin 3g/l, plumbous 3g/l, iron 0.1g/l, cl ions 0.1g/l) the normal temperature leaching; Leach solid-to-liquid ratio 1:5, (stanniferous 37.5g/l, plumbous 10.8g/l, arsenic 0.01 ~ 0.02%, antimony 0.01 ~ 0.03g/l, copper 0.02 ~ 0.08g/l, bismuth 0.01 ~ 0.08g/l, iron 0.1 ~ 2g/l, cl ions 0.1 ~ 3g/l) return frame material and plate electrolytic system respectively to leach liquor.
Embodiment 2
Melt through 500 ~ 650C ° of solder pot with the high assorted terne metal of raw material (composition stanniferous 45%, lead 35%, arsenic 2%, antimony 5%, copper 1%, bismuth 0.5%, iron 1%); Pulling 20% (wherein stanniferous 40%, plumbous 34%, arsenic 5%, antimony 8%, copper 1.2%, bismuth 0.7%, iron 1.5%) that scruff accounts for total alloy out, to process granularity be 5 ~ 30mm particle; The frame material electrolyzer of packing into is put into total acid H
2SiF
6Be 120g/l, free acid H
2SiF
6Be 90g/l, Sn
AlwaysFrame material silicofluoride salt electrolytic solution for 80g/l carries out electrolysis, bath voltage 0.3-3V, current density 80A/m
2, alloy product composition stanniferous 41.5%, lead 58.0%, arsenic 0.004%, antimony 0.017%, copper 0.0023%, bismuth 0.003%, iron 0.0023%, electrolysis direct yield 50%.
Alloy liquid then is cast into alloy anode (stanniferous 48%, lead 43%, arsenic 1.4%, antimony 2.8%, copper 0.5%, bismuth 0.4%, iron 0.9%), puts into total acid H
2SiF
6Be 210g/l, free acid H
2SiF
6Be 160g/l, Sn
AlwaysCarry out electrolysis, bath voltage 0.3V, current density 120A/m in the plate silicofluoride salt electrolytic solution for 50g/l
2, alloy product stanniferous 51.6%, lead 48.5%, arsenic 0.002%, antimony 0.006%, copper 0.0016%, bismuth 0.001%, iron 0.002%, direct yield 86%.
The anode sludge that is produced by plate and the electrolysis of frame material is put into acid-resistant reacting kettle and is used 350g/l hydrochloric acid, liquid-solid ratio 5:1 after washing; Temperature 95C ° of churning time leached tin, arsenic, antimony, copper, bismuth, leaching yield in 3 hours>95%, leached mud is used for extracting precious metals such as silver, gold, palladium; Solution to 65C °, through iron powder replacement 4 hours, is removed impurity such as antimony in the solution, bismuth, copper, arsenic with steam-heated cal(l)andria; Rate of displacement>85%, replacement slag is further separated arsenic, antimony, copper, bismuth.Displaced liquid is heated to 80 C ° and is neutralized to PH0.5 with calcium hydroxide and purifies and to take off assortedly, continues to be neutralized to PH4.5, make the tin hydrolytic precipitation get stannic hydroxide with hot water clean to the chlorine root below 1%, obtain stannic hydroxide (stanniferous 39.0%), with electrolytic solution (total acid H
2SiF
6Be 210g/l, free acid H
2SiF
6Be 160g/l, tin 20g/l, plumbous 20g/l) the normal temperature leaching, leach solid-to-liquid ratio 1:8, leach liquor (stanniferous 40.5g/l, plumbous 8.8g/l) returns frame material and plate electrolytic system respectively.
Embodiment 3
Melt through 500 ~ 650C ° of solder pot with the high assorted terne metal of raw material (composition stanniferous 42%, lead 38%, arsenic 1.5%, antimony 4%, copper 1.5%, bismuth 0.7%, iron 0.8%); Pulling 16% (wherein stanniferous 36%, plumbous 37%, arsenic 6%, antimony 7%, copper 2.2%, bismuth 0.9%, iron 1.3%) that scruff accounts for total alloy out, to process granularity be 5 ~ 30mm particle; The frame material electrolyzer of packing into is put into total acid H
2SiF
6Be 100g/l, free acid H
2SiF
6Be 80g/l, Sn
AlwaysFrame material silicofluoride salt electrolytic solution for 60g/l carries out electrolysis, bath voltage 0.35 ~ 3V, current density 50A/m
2, alloy product composition stanniferous 43.5%, lead 55.0%, arsenic 0.004%, antimony 0.017%, copper 0.0023%, bismuth 0.003%, iron 0.0023%, electrolysis direct yield 52%.
Alloy liquid then is cast into alloy anode (stanniferous 49%, lead 41%, arsenic 1.5%, antimony 3.2%, copper 0.6%, bismuth 0.5%, iron 0.8%), puts into total acid H
2SiF
6Be 100g/l, free acid H
2SiF
6Be 140g/l, Sn
AlwaysCarry out electrolysis, bath voltage 0.3V, current density 120A/m in the plate silicofluoride salt electrolytic solution for 30g/l
2, alloy product stanniferous 50.6%, lead 48.0%, arsenic 0.002%, antimony 0.006%, copper 0.0016%, bismuth 0.001%, iron 0.002%, direct yield 84%.
The anode sludge that is produced by plate and the electrolysis of frame material is put into acid-resistant reacting kettle and is used 250g/l hydrochloric acid, liquid-solid ratio 8:1 after washing; Temperature 95C ° of churning time leached tin, arsenic, antimony, copper, bismuth, leaching yield in 4 hours>95%, leached mud is used for extracting precious metals such as silver, gold, palladium; Solution to 60C °, through iron powder replacement 5 hours, is removed impurity such as antimony in the solution, bismuth, copper, arsenic with steam-heated cal(l)andria; Rate of displacement>85%, replacement slag is further separated arsenic, antimony, copper, bismuth.Displaced liquid is heated to 70 C °; Be neutralized to the PH0.5 degree of depth with calcium hydroxide and take off antimony, continue to be neutralized to PH4.5, make the stannic hydroxide hydrolytic precipitation get stannic hydroxide with hot water clean to the chlorine root below 0.6%; Obtain stannic hydroxide (stanniferous 39.0%), with electrolytic solution (total acid H
2SiF
6Be 180g/l, free acid H
2SiF
6Be 120g/l, tin 15g/l, plumbous 10g/l) the normal temperature leaching, leach solid-to-liquid ratio 1:8, leach liquor (stanniferous 42.5g/l, plumbous 8.6g/l) returns frame material and plate electrolytic system respectively.
Embodiment 4
Melt through 500 ~ 650C ° of solder pot with the high assorted terne metal of raw material (composition stanniferous 37%, lead 36%, arsenic 1.4%, antimony 3.8%, copper 1.6%, bismuth 0.7%, iron 1.2%); Pulling 24% (wherein stanniferous 43%, plumbous 38%, arsenic 6.5%, antimony 6.8%, copper 2.2%, bismuth 0.9%, iron 1.5%) that scruff accounts for total alloy out, to process granularity be 5 ~ 30mm particle; The frame material electrolyzer of packing into is put into total acid H
2SiF
6Be 70g/l, free acid H
2SiF
6Be 65g/l, Sn
AlwaysFrame material silicofluoride salt electrolytic solution for 40g/l carries out electrolysis, bath voltage 0.25 ~ 2.5V, current density 40A/m
2, alloy product composition stanniferous 41.5%, lead 56.0%, arsenic 0.004%, antimony 0.017%, copper 0.0023%, bismuth 0.003%, iron 0.0023%, electrolysis direct yield 58%.
Alloy liquid then is cast into alloy anode (stanniferous 48%, lead 42%, arsenic 1.2%, antimony 2.5%, copper 0.7%, bismuth 0.4%, iron 0.9%), puts into total acid H
2SiF
6Be 170g/l, free acid H
2SiF
6Be 130g/l, Sn
AlwaysCarry out electrolysis, bath voltage 0.3V, current density 100A/m in the plate silicofluoride salt electrolytic solution for 80g/l
2, alloy product stanniferous 47.6%, lead 48.0%, arsenic 0.002%, antimony 0.006%, copper 0.0016%, bismuth 0.001%, iron 0.002%, direct yield 82%.
The anode sludge that is produced by plate and the electrolysis of frame material is put into acid-resistant reacting kettle and is used 100g/l hydrochloric acid, liquid-solid ratio 7:1 after washing; Temperature 85C ° of churning time leached tin, arsenic, antimony, copper, bismuth, leaching yield in 5 hours>95%, leached mud is used for extracting precious metals such as silver, gold, palladium; Solution to 50C °, through iron powder replacement 5 hours, is removed impurity such as antimony in the solution, bismuth, copper, arsenic with steam-heated cal(l)andria; Rate of displacement>85%, replacement slag is further separated arsenic, antimony, copper, bismuth.Displaced liquid is heated to 80 C ° and is neutralized to the PH0.5 degree of depth with calcium hydroxide and takes off antimony, continues to be neutralized to PH4.5, make the tin hydrolytic precipitation get stannic hydroxide with hot water clean to the chlorine root below 0.5%, obtain stannic hydroxide (stanniferous 39.0%), with electrolytic solution (total acid H
2SiF
6Be 160g/l, free acid H
2SiF
6Be 110g/l, tin 13g/l, plumbous 11g/l) the normal temperature leaching, leach solid-to-liquid ratio 1:7, leach liquor (stanniferous 41.6g/l, plumbous 7.6g/l) returns frame material and plate electrolytic system respectively.
Claims (10)
1. one kind high assorted terne metal combination electrolysis process comprises smelting and pouring, the electrolysis of scruff frame material, positive plate electrolysis, anode sludge tin recovery self-adding operation, specifically comprises following operation:
A, smelting and pouring: the assorted terne metal of height is put into 500 ~ 650C ° solder pot fusing, pull scruff out, carry out anode casting;
B, the electrolysis of scruff frame material: the scruff of pulling out is processed the particle that granularity is 5 ~ 30mm; Frame up then; Put into frame material electrolytic solution; Carry out diaphragm electrolysis; Bath voltage 0.3 ~ 3.5V, current density 30 ~ 80A/
;
C, positive plate electrolysis: alloy pours into positive plate, puts into plate electrolytic solution, carries out the plate electrolysis;
D, anode sludge tin reclaim self-adding: the anode sludge that described plate and the electrolysis of frame material produce is after washing; Put into acid-resistant reacting kettle with 100 ~ 350 0g/l hydrochloric acid; Liquid-solid ratio 5:1 ~ 8:1, stirs 3 ~ 5 hours to leach tin, arsenic, antimony, copper, bismuth by temperature 80 ~ 95C °; Infusion solution is with steam-heated cal(l)andria to 40 ~ 65C °, through iron powder replacement 4 ~ 6 hours, removes impurity such as antimony in the solution, bismuth, copper, arsenic; The solution of displacement after the removal of impurities is heated to 50 ~ 80 C ° and is neutralized to PH0.5 ~ 1 degree of depth with calcium hydroxide again and takes off antimony; Continued is neutralized to PH4.5 ~ 5 and makes the stannic hydroxide hydrolytic precipitation; Stannic hydroxide with hot water clean to the chlorine root below 0.5 ~ 1%; The stannic hydroxide that obtains, recycle silicon fluorate electrolytic solution normal temperature leaches, and leach liquor returns the consumption of tin ion in the electrolytic solution in electrolytic system complementary block material electrolyzer and the plate electrolyzer.
2. the assorted terne metal combination of height according to claim 1 electrolysis process; It is characterized in that: the described diaphragm electrolysis that frames up is that the slicker solder slag that cast produces is packed in plastics and other the acidproof bag; Put into conducting plates in the bag, bag is put into acidproof frame of plastic form anode by the cast of homogeneity alloy; Negative electrode is formed by the casting of tin alloy homogeneity of the product alloy; Anode, negative electrode are packed in the frame material electrolyzer, and put into silicofluoride salt electrolytic solution and carry out electrolysis.
3. the assorted terne metal combination of height according to claim 1 electrolysis process is characterized in that: the total acid H of said frame material silicofluoride salt electrolytic solution
2SiF
6Be 50 ~ 120g/l, free acid H
2SiF
6Be 40 ~ 90g/l, Sn
AlwaysBe 10 ~ 80g/l.
4. according to claim 1 or the assorted terne metal combination of 3 described height electrolysis process, it is characterized in that: the total acid H of said frame material silicofluoride salt electrolytic solution
2SiF
6 For60 ~ 100g/l, free acid H
2SiF
6Be 50 ~ 80g/l, Sn
AlwaysBe 17 ~ 70g/l.
5. according to claim 1 or the assorted terne metal combination of 3 described height electrolysis process, the total acid H of said frame material silicofluoride salt electrolytic solution
2SiF
6 For70 ~ 90g/l, free acid H
2SiF
6Be 65 ~ 75g/l, Sn
AlwaysBe 25 ~ 50g/l.
6. the assorted terne metal combination of height according to claim 1 electrolysis process; It is characterized in that: described alloy liquid then is cast into alloy anode, puts into normal plate electrolyzer, carries out electrolysis with plate silicofluoride salt electrolytic solution; Bath voltage 0.1 ~ 0.3 V during electrolysis, current density 60 ~ 120A/m
2
7. according to claim 1 or the assorted terne metal combination of 6 described height electrolysis process, it is characterized in that: the total acid H of said plate silicofluoride salt electrolytic solution
2SiF
6Be 60 ~ 210g/l, free acid H
2SiF
6Be 45 ~ 160g/l, Sn
AlwaysBe 8 ~ 80g/l.
8. according to claim 1 or the assorted terne metal combination of 6 described height electrolysis process, it is characterized in that: the total acid H of said plate silicofluoride salt electrolytic solution
2SiF
6Be 80 ~ 190g/l, free acid H
2SiF
6Be 65 ~ 140g/l, Sn
AlwaysBe 12 ~ 60g/l.
9. according to claim 1 or the assorted terne metal combination of 6 described height electrolysis process, it is characterized in that: the total acid H of described plate silicofluoride salt electrolytic solution
2SiF
6Be 100 ~ 170g/l, free acid H
2SiF
6Be 85 ~ 120g/l, Sn
AlwaysBe 25 ~ 45g/l.
10. the assorted terne metal combination of height according to claim 1 electrolysis process is characterized in that: the total acid H of the leaching electrolytic solution of described D operation
2SiF
6Be 80 ~ 210g/l, free acid H
2SiF
6Be 40 ~ 160g/l, Sn 3 ~ 20g/l, Pb3 ~ 20g/l.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104018188A (en) * | 2014-05-06 | 2014-09-03 | 马光甲 | Process for reclaiming copper, steel and soldering tin from waste pins of electronic components |
| CN104141152A (en) * | 2014-07-28 | 2014-11-12 | 蒙自矿冶有限责任公司 | Method for recycling tin from lead bullion |
| CN104805294A (en) * | 2015-04-21 | 2015-07-29 | 梧州市海邦科技有限公司 | Method for recovering silver from scrap copper anode slime |
| CN107475752A (en) * | 2017-08-31 | 2017-12-15 | 中南大学 | Clean metallurgy method and device for low-temperature molten salt electrolysis of tin dross |
| CN109536982A (en) * | 2018-12-27 | 2019-03-29 | 广东先导稀材股份有限公司 | Preparation method of nano tin dioxide |
| CN110219019A (en) * | 2019-07-22 | 2019-09-10 | 广东汉合有色金属有限公司 | A kind of diaphragm electrolysis technique of tin copper ashes |
| CN110484744A (en) * | 2019-08-26 | 2019-11-22 | 珠海格力电器股份有限公司 | A method of recycling noble metal from waste and old patch capacitor |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104018188A (en) * | 2014-05-06 | 2014-09-03 | 马光甲 | Process for reclaiming copper, steel and soldering tin from waste pins of electronic components |
| CN104141152A (en) * | 2014-07-28 | 2014-11-12 | 蒙自矿冶有限责任公司 | Method for recycling tin from lead bullion |
| CN104805294A (en) * | 2015-04-21 | 2015-07-29 | 梧州市海邦科技有限公司 | Method for recovering silver from scrap copper anode slime |
| CN107475752A (en) * | 2017-08-31 | 2017-12-15 | 中南大学 | Clean metallurgy method and device for low-temperature molten salt electrolysis of tin dross |
| CN109536982A (en) * | 2018-12-27 | 2019-03-29 | 广东先导稀材股份有限公司 | Preparation method of nano tin dioxide |
| CN109536982B (en) * | 2018-12-27 | 2021-04-13 | 广东先导稀材股份有限公司 | Preparation method of nano tin dioxide |
| CN110219019A (en) * | 2019-07-22 | 2019-09-10 | 广东汉合有色金属有限公司 | A kind of diaphragm electrolysis technique of tin copper ashes |
| CN110484744A (en) * | 2019-08-26 | 2019-11-22 | 珠海格力电器股份有限公司 | A method of recycling noble metal from waste and old patch capacitor |
| CN110484744B (en) * | 2019-08-26 | 2020-07-24 | 珠海格力电器股份有限公司 | Method for recovering precious metal from waste chip capacitor |
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