CN1028658C - Technology of purifying copper electrolyte - Google Patents
Technology of purifying copper electrolyte Download PDFInfo
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- CN1028658C CN1028658C CN92113237A CN92113237A CN1028658C CN 1028658 C CN1028658 C CN 1028658C CN 92113237 A CN92113237 A CN 92113237A CN 92113237 A CN92113237 A CN 92113237A CN 1028658 C CN1028658 C CN 1028658C
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Abstract
The present invention relates to a method for purifying a copper electrolyte. The method of the present invention has the technology that a copper electrolyte containing 50 to 250 g/l of sulphuric acid to be purified is in contact with chelate cation exchange resin; after antimony and bismuth are adsorbed, 2 to 60 g/l of EDTA water solution containing 1 to 10 g/l alkali metal hydroxide serves as analysis liquid, and antimony and bismuth on resin are removed by elution. The technology has the advantages of no generation of acid mist, no pollution to the environment, circulation use of EDTA in the analyzed solution and low cost. The copper electrolyte to be purified is taken out from a copper electrolytic tank, and is directly purified without any processing; the components of the electrolyte are not changed.
Description
The present invention relates to the Purification of Copper Electrolyte method, more precisely sulfuric acid Purification of Copper Electrolyte method.
When blister copper soluble-anode electrolysis refining, because the redox potential and the copper of antimony, bismuth are approaching, when these impurity run up to finite concentration in electrolytic solution, just may on negative electrode, separate out deposition together with copper, thereby pollute the cathode copper product, reduce the quality of electrolytic copper, and, these impurity such as antimony, bismuth not only influence the quality of electrolytic copper, current efficiency in the copper electrolytic process is descended, and is one of measure that guarantees electrolytic copper quality so remove detrimental impurity such as antimony, bismuth from copper electrolyte.
The Purification of Copper Electrolyte method is a lot, and various processing methodes such as extraction process, the precipitator method, active carbon adsorption are arranged.
Extraction process technology is to extract copper electrolyte out heating from electrolyzer to concentrate back electrolysis decopper(ing), used for electrolyte organic solvent behind the decopper(ing) extracts, remove impurity, the shortcoming of extraction process is that technical process is long, and energy consumption is big, the organic solvent contaminate environment, hinder health of operators, moreover the part detrimental impurity enters again in the blister copper when decopper(ing), and detrimental impurity antimony, bismuth are got back in the electrolytic solution again during blister refining.
The precipitator method are to add precipitation agent under certain operational condition, make detrimental impurity antimony, bismuth etc. generate precipitation, and precipitation is carried out filtering separation after generating, and the precipitator method that have also will be carried out the processing of electrolysis decopper(ing), and technical process is long, and equipment is many, and investment is big.
Active carbon adsorption is that gac is contacted with copper electrolyte to be clean, and the detrimental impurity in the solution is adsorbed on the gac.The shortcoming of this method is that active carbon adsorption can only be removed bismuth absorption from copper electrolyte, and the rate of removing of bismuth is lower, has only about 35.5-65.6%.In addition, the regeneration of activated carbon difficulty of load, solid-liquid separation also exists certain difficulty.
Recently the Japanese documentation spy opens clear 60-50192 and has reported the processing method of using the ion-exchange purification copper electrolyte, with sulfuric acid concentration is that the copper electrolyte to be clean that contains antimony, bismuth more than the 50 gram/liters contacts with aminomethylene phosphate positively charged ion resin, adsorb detrimental impurity such as antimony, bismuth ion in this copper electrolyte, aqueous hydrochloric acid with 5.5-6.5N is the desorbed solution of antimony, bismuth then, wash-out is adsorbed on antimony, the bismuth plasma on the resin, and copper electrolyte is purified, the advantage of this processing method is directly to handle copper electrolyte.And don't change the copper electrolyte component, and not causing secondary pollution, the copper electrolyte after the processing can directly return in the electrolyzer, does not need numerous and diverse pre-treatment, and resin can recycle simultaneously.Technology and equipment are simple, and is easy to operate, the purification efficiency height, and the purification expense is cheap; But also has changeable, the handiness of periodical operation continuously of scale.The shortcoming of this technical process is the concentrated hydrochloric acid aqueous solution of the desorbed solution of former antimony, bismuth as 5.5-6.5N that use, and corrodibility is big, produces acid mist and waste water, contaminate environment, and the harm health of operators, the hydrochloric acid in the desorbed solution can not recycle again.
Purpose of the present invention just is to work out a kind of processing method of new purifying copper electrolyte, finds out a kind of new wash-out antimony, the desorbed solution of bismuth, avoids the corrodibility of hydrochloric acid, does not produce acid mist and waste water, does not have environmental pollution, does not endanger health of operators; EDTA in ion exchange resin, the desorbed solution can be recycled again, has kept the various advantages of the ion exchange method in the above-mentioned prior art simultaneously again.
The processing method of a kind of cleaning copper electrolyte of the present invention, copper electrolyte to be clean sulfur acid 50-250 gram/liter and that contain antimony, bismuth is contacted with the chelating Zeo-karb, adsorb antimony, bismuth harmful ion in this copper electrolyte, with containing 1-10 gram/liter alkali metal hydroxide 2-60 gram/liter disodium EDTA (EDTA, C10H14N208Na2, aqueous solution 2H2O) is the desorbed solution of antimony, bismuth, wash-out is removed antimony, the bismuth ion that is adsorbed on the chelating Zeo-karb, and copper electrolyte is purified.
The consisting of of used copper electrolyte to be clean among the present invention: contain 28-65 gram/liter copper, 50-250 gram/liter sulfuric acid, 0.1-10 gram/liter iron, 0.1-10 gram/liter arsenic, 0.1-3.5 gram/liter antimony, 0.1-3.5 gram/liter bismuth, the Controllable Temperature of copper electrolyte to be clean is built in 15 °-60 ℃.Content with iron in copper electrolyte to be clean is good below 5 gram/liters, because the chelating Zeo-karb does not adsorb basically to copper, so the variation of the concentration of copper in solution is to the not influence of absorption of antimony and bismuth.
Used chelating Zeo-karb has aminoalkyl group phosphate chelating ion exchange resin, (D411 for example, 2#), pyridyl chelating ion exchange resin (for example 1#, 4#, 5#, D280), hydroxy amino ion exchange resin (3#, 6#), wherein a kind of such as polyamide-based ion exchange resin, but be good with aminoalkyl group phosphate chelating ion exchange resin, pyridyl chelating ion exchange resin.The fundamental mode of all resins can be H
+, type Na
+Type, Li
+Type, K
+Alkali metal ion types such as type are especially with H
+Type, Na
+Type is good, and aminoalkyl group phosphate chelating ion exchange resin (D411) is to be raw material with primary amine resin, phosphorous acid and formaldehyde, and by the Mannich reaction, the synthetic functional group is: R-CH2NHCH2PO(OH)
2The chelating Zeo-karb, aminoalkyl group phosphate chelating ion exchange resin, pyridyl chelating ion exchange resin are 0.1-2.0 milligramequivalent/gram dried resin to the loading capacity of antimony and bismuth, are preferably 0.3-1.2 milligram quantities/gram dried resin.
Copper electrolyte is all worked at a certain temperature in real work, so be necessary to find out the influence of temperature to adsorption rate, test shows that D411 chelating Zeo-karb does not adsorb copper in 15 °-60 ℃ temperature range.D411 chelating Zeo-karb does not change basically to the adsorption rate of antimony, bismuth in this temperature range, that is to say that temperature is little to the adsorption rate influence on D411 chelating Zeo-karb of antimony, bismuth in this temperature range, for example the adsorption rate to antimony is 86.73% in the time of 28 ℃, and the adsorption rate to antimony also only is 88.16% in the time of 60 ℃; Adsorption rate to bismuth in the time of 28 ℃ is 82.26%, and the adsorption rate to antimony also only is 83.66% 60 ℃ the time, usually the normal temperature range of copper electrolyte is about 50 °-55 ℃, directly exchange so can directly from electrolyzer, take out copper electrolyte to be purified, remove detrimental impurity such as antimony, bismuth.
Used desorbed solution is the EDTA aqueous solution that contains 1-10 gram/liter alkali metal hydroxide 2-60 gram/liter, and said alkali metal hydroxide is lithium hydroxide, sodium hydroxide, potassium hydroxide, rubidium hydroxide, cesium hydroxide.But with sodium hydroxide is good, because its low price, the existence of alkali metal hydroxide (for example sodium hydroxide) can make the EDTA sodium salt dissolve in water rapidly, and keep its stability, in the EDTA aqueous solution, add an amount of oxyhydroxide, make the aqueous solution of EDTA be alkalescence.But the change in concentration of alkali metal hydroxides such as sodium hydroxide, to antimony, the resolution factor influence of bismuth is little, only make antimony, the resolution factor of bismuth slightly improves, containing and containing concentration sodium hydroxide in the EDTA aqueous solution of 2-60 gram/liter is that 3-5 gram/liter suits, increase antimony along with EDTA concentration in the desorbed solution, the resolution factor of bismuth significantly rises, when but the concentration of EDTA is greater than 25 gram/liters in the desorbed solution, antimony, the resolution factor of bismuth changes little, therefore the aqueous solution with the 10-25 gram/liter EDTA of the sodium hydroxide that contains 3-5 gram/liter is good in the desorbed solution, citric acid, the aqueous solution of trisodium citrate also can be used as antimony, the desorbed solution of bismuth, but effect is inexcellent.
The way of contact that contains the copper electrolyte to be clean of antimony, bismuth and chelating Zeo-karb has two kinds of static mode and dynamical fashions, but is good with dynamical fashion, and dynamical fashion is easy to operate, is easy to operate continuously.
Said static mode is that the ratio with the volume (milliliter) of the cupric electrolysis of dried chelating Zeo-karb (gram)/to be clean is under the condition of 1/25-8/25, chelating Zeo-karb and copper electrolyte to be clean pack in the container into (for example in the Erlenmeyer flask) at 15 °-60 ℃, shake and mix the copper electrolyte of isolating in 5-120 minute after the purification, water (ion exchanged water or distilled water), the chelating Zeo-karb of load is washed to the color of not having cupric ion, ratio with chelating Zeo-karb (the gram)/desorbed solution (milliliter) of load is under the condition of 1/25-8/25, with the chelating Zeo-karb of load and the EDTA aqueous solution as the 2-60 gram/liter that contains 1-10 gram/liter sodium hydroxide of desorbed solution, shake and mixed 5-120 minute, isolate desorbed solution, water (ion exchanged water or distilled water) is washed till nearly neutrality with the chelating Zeo-karb of load.
In the adsorption process of static mode (be the chelating Zeo-karb with the contacting of copper electrolyte to be clean in), along with increase antimony, the adsorption rate of bismuth on the chelating Zeo-karb of the ratio of the volume (milliliter) of the copper electrolyte of chelating Zeo-karb (gram)/to be clean enlarges markedly; Under the situation that other experiment conditions remain unchanged, along with the shake prolongation of mixed time of chelating Zeo-karb and copper electrolyte to be clean together, antimony, the adsorption rate of bismuth on the chelating Zeo-karb obviously increase, the prolongation that (being in the contacting of chelating Zeo-karb and desorbed solution of load antimony, bismuth) shaken and done time along with the chelating Zeo-karb and the desorbed solution of load in the resolving of static mode, the resolution factor of antimony, bismuth increases.
Said dynamical fashion is exactly that copper electrolyte to be clean is injected in the exchange column that the chelating Zeo-karb is housed, control flow velocity that copper electrolyte to be clean flows out exchange column and be the 20-100 milliliter/hour, be preferably the 35-60 milliliter/hour, (SV=0.5-2.5, be preferably SV=0.8-1.25), be 5-120 minute duration of contact that makes copper electrolyte to be clean and chelating Zeo-karb, be preferably 15-60 minute, after copper electrolyte to be clean flows out exchange column fully, the chelating Zeo-karb of water (ion exchanged water or distilled water) wash load is to the color of not having cupric ion, with the aqueous solution that contains 1-10 gram/liter sodium hydroxide 2-60 gram/liter EDTA as desorbed solution, be injected in the exchange column, the flow velocity that the control desorbed solution flows out exchange column be the 20-100 milliliter/hour, be preferably 40-80 milliliter/hour (SV=0.5-2.5, best SV=0.8-1.25), be 5-60 minute duration of contact that makes desorbed solution and chelating Zeo-karb, be preferably 15-45 minute, after liquid to be resolved all flows out exchange column, water (ion exchanged water or distilled water), scrub stream fluid are near neutral.
Be the ratio that amount (milliliter) and the copper electrolyte to be clean or the desorbed solution of chelating Zeo-karb flows out the flow velocity (ml/min) of exchange column (being the chelating Zeo-karb contact process of the contact process of copper electrolyte to be clean and chelating Zeo-karb and desorbed solution and load antimony, bismuth) said duration of contact in the adsorption process and resolving of dynamical fashion.
The exchange column that used exchange column can be made with synthetic glass or glass, the exchange column that also can adopt 50 milliliters alkaline drop-burette to make, in the mode of wet type stand-by resin is packed in the post, this is the method that those skilled in the art all know, regulate the duration of contact of electrolytic solution to be clean or desorbed solution and chelating Zeo-karb with the flow velocity of control outflow exchange column, the aspect ratio of ion exchange column is 5: 1-70: 1, be preferably 10: 1-50: 1.If used chelating Zeo-karb is sodium type and Hydrogen, the chelating Zeo-karb of sodium type and Hydrogen does not have marked difference to the absorption property of antimony and bismuth, with the aqueous solution of the EDTA that contains sodium hydroxide as desorbed solution, adopt the sodium type better, need not make the transition and just can adsorb again; If use H
+Type need be handled with aqueous hydrochloric acid, and the exhausted desorbed solution promptly contains method that the aqueous solution of the EDTA of sodium hydroxide all knows with the those of ordinary skill under this area to be made EDTA obtain reclaiming to reuse.
The advantage of processing method of the present invention just is to find out a kind of new antimony, the desorbed solution of bismuth replaces concentrated hydrochloric acid, do not produce acid mist, do not produce environmental pollution, the healthy of easy handling personnel arranged, and desorbed solution EDTA after treatment can be recycled, and has reduced cost, and processing method of the present invention can be taken out copper electrolyte to be clean and directly purified without any processing from copper electrolysis cells, easy to operate, equipment is simple, does not also change the component of copper electrolyte.
With following indefiniteness embodiment processing method of the present invention is further described, will helps understanding, and not as the qualification to protection domain of the present invention, protection scope of the present invention is decided by claims the present invention and advantage thereof.
Embodiment 1
It consists of (gram/liter) to used copper electrolyte to be clean as raw material
Cu H
2SO
4Fe As Sb Bi
42.74 202.86 2.59 3.86 0.41 1.30
Used ion exchange column is made by glass, its height is through than being 50: 1, used chelating Zeo-karb is an aminoalkyl group phosphate chelating Zeo-karb (D411), (Chemical Plant of Nankai Univ.'s product), in following embodiment, all be called for short the D411 resin, adsorptive capacity to antimony and bismuth is 0.5508 milligramequivalent/gram thousand resins, temperature is 33 ℃, in adsorption process, stock liquid is injected in the exchange column, the flow velocity that the control stock liquid flows out exchange column is 50 milliliters/hour, making its stock liquid and D411 resin duration of contact is 38 minutes, the consumption of stock liquid is 1.01 liters, and the composition (gram/liter) of the stock liquid after the D411 resin absorption purifies is:
Cu H
2SO
4Fe As Sb Bi
42.18 202.47 - - ＜0.002 0.006
The adsorption rate of antimony, bismuth is more than 99%, with the D411 resin of ion exchanged water wash load to the color of not having cupric ion, carry out resolving, with the aqueous solution that contains 4 gram/liter sodium hydroxide, 25 gram/liter EDTA is desorbed solution, be injected in the exchange column, the flow velocity that the control desorbed solution flows out exchange column is 50 milliliters/hour, and making the duration of contact of desorbed solution and load antimony, bismuth D411 resin is 42 minutes, and the desorbed solution consumption is 0.88 liter.The resolution factor of antimony is 70%, and the resolution factor of bismuth is 95%.Antimony 0.4 gram/liter in the aqueous solution after the parsing, bismuth is 1.74/ liter.
Embodiment 2
Its working method and equipment are with embodiment 1.
Stock liquid is formed (gram/liter):
Cu H
2SO
4Fe As Sb Bi
42.74 202.86 2.59 3.86 0.41 1.30
The exchange column aspect ratio is 50: the 1.D411 resin is 0.5345 milligramequivalent/gram dried resin to the adsorptive capacity of antimony and bismuth, 31 ℃ of temperature.The flow velocity of stock liquid outflow exchange column is 50 milliliters/hour in adsorption process, 38 minutes duration of contact, and stock liquid consumption 0.98 liter, the composition (gram/liter) of the stock liquid after the D411 resin absorption purifies is:
Cu H
2SO
4Fe As Sb Bi
42.32 202.51 - - ＜0.002 0.006
Antimony, bismuth adsorption rate are more than 99%, using the aqueous solution of the 20 gram/liter EDTA that contain 4 gram/liter sodium hydroxide in resolving is desorbed solution, the flow velocity that desorbed solution flows out exchange column is 40 milliliters/hour, 34 minutes duration of contact, desorbed solution consumption 0.76 liter, the resolution factor of antimony are 71%, the resolution factor 95% of bismuth, contain antimony 0.38 gram/liter in the aqueous solution after the parsing, bismuth is 1.6 gram/liters.
Embodiment 3
Its working method and equipment are with embodiment 1.
Stock liquid is formed (gram/liter):
Cu H
2SO
4Fe As Sb Bi
42.7 236 - - 0.41 0.83
Exchange column aspect ratio 40: 1, every gram D411 dried resin adsorptive capacity, antimony is 14.84 milligrams, 15.29 milligrams of bismuths, 30 ℃ of temperature.The flow velocity of stock liquid outflow exchange column is 50 milliliters/hour in adsorption process, 31 minutes duration of contact.Is desorbed solution in resolving with the aqueous solution that contains 4 gram/liter sodium hydroxide, 15 gram/liter EDTA, 80 milliliters/hour of the flow velocitys of desorbed solution outflow exchange column, 21 minutes duration of contact, desorbed solution consumption 0.7 liter.The resolution factor of antimony is 70%.The resolution factor 95.6% of bismuth.Contain antimony 0.61 gram/liter in the solution after the parsing, bismuth-containing is 0.81 gram/liter.
Embodiment 4
Its working method and equipment are with embodiment 1.
Stock liquid is formed (gram/liter):
Cu H
2SO
4Fe As Sb Bi
42.7 236 - - 0.41 0.83
Exchange column aspect ratio 40: 1, every gram D411 dried resin adsorptive capacity, antimony is 14.86 milligrams, 16.74 milligrams of bismuths, 29 ℃ of temperature.The flow velocity of stock liquid outflow exchange column is 50 milliliters/hour in adsorption process, 31 minutes duration of contact.Using the aqueous solution that contains 4 gram/liter sodium hydroxide, 10 gram/liter EDTA in resolving is desorbed solution, and the flow velocity that desorbed solution flows out exchange column is 50 milliliters/hour.31 minutes duration of contact, desorbed solution consumption 0.6 liter, the resolution factor of antimony are 70%, and the resolution factor 95% of bismuth contains antimony 0.48 gram/liter in the solution after the parsing, and bismuth-containing is 0.75 gram/liter.
Embodiment 5
The composition (gram/liter) of stock liquid (copper electrolyte to be clean):
Cu H
2SO
4Fe As Sb Bi
31.3 233 2.21 - 0.655 0.61
12 gram D411 " are done " resin and 50 milliliters of stock liquids pack in the Erlenmeyer flask, shook under room temperature (about 25 ℃) mixed 30 minutes, obtain the resin and the adsorbed solution of load after the separation, the composition in the adsorbed solution (gram/liter) is as follows:
Cu H
2SO
4Fe As Sb Bi
31.2 232.5 - - 0.054 0.056
Load has the resin of antimony and bismuth to resolve as desorbed solution for 80 milliliters with the aqueous solution that contains 3 gram/liter sodium hydroxide, 15 gram/liter EDTA, shake and do time 25 minutes, the content of antimony and bismuth is respectively in the solution after obtaining after the separation resolving: antimony 0.27 gram/liter, bismuth 0.33 gram/liter.
Embodiment 6
The composition (gram/liter) of stock liquid (copper electrolyte to be clean):
Cu H
2SO
4Fe As Sb Bi
28.2 223 - - 0.49 0.93
10 gram D411 " are done " resin and 50 milliliters of stock liquids pack in the Erlenmeyer flask, shook mixed 40 minutes in 45 ℃, obtain the resin and the adsorbed solution of load after the separation, the composition of adsorbed solution (gram/liter) is as follows:
Cu H
2SO
4Fe As Sb Bi
28.2 222.8 1 1 0.059 0.082
Load has the resin of antimony and bismuth to resolve as desorbed solution for 80 milliliters with the aqueous solution that contains the former 18 gram/liter EDTA of 5 gram/liter sodium hydroxide.Shake and do time 30 minutes, the content of antimony and bismuth is respectively in the solution after obtaining after the separation resolving: antimony 0.18 gram/liter, bismuth 0.42 gram/liter.
Claims (10)
1, a kind of processing method of cleaning copper electrolyte, copper electrolyte to be clean sulfur acid 50-250 gram/liter and that contain antimony, bismuth is contacted with the chelating Zeo-karb, adsorb antimony, bismuth harmful ion in this copper electrolyte, it is characterized in that, with the aqueous solution that contains 1-10 gram/liter alkali metal hydroxide 2-60 gram/liter disodium EDTA (EDTA) is the desorbed solution of antimony, bismuth, and wash-out is removed antimony, the bismuth that is adsorbed on the chelating Zeo-karb.
According to the processing method of a kind of cleaning copper electrolyte of claim 1, it is characterized in that 2, the chelating Zeo-karb is a kind of in aminoalkyl group phosphate chelating ion exchange resin, the pyridyl chelating ion exchange resin.
3, according to the processing method of a kind of cleaning copper electrolyte of claim 1, it is characterized in that said alkali metal hydroxide is a sodium hydroxide.
4, according to the processing method of a kind of cleaning copper electrolyte of claim 1 or 3, it is characterized in that, is desorbed solution with the aqueous solution that contains 3-5 gram/liter sodium hydroxide 10-25 gram/liter EDTA.
According to the processing method of a kind of cleaning copper electrolyte of claim 1, it is characterized in that 5, the way of contact that contains the copper electrolyte to be clean of antimony, bismuth and chelating Zeo-karb is a kind of in static mode, the dynamical fashion.
6, processing method according to a kind of cleaning copper electrolyte of claim 5, it is characterized in that, said static mode is, ratio with the volume (milliliter) of the copper electrolyte of the copper electrolyte of dried chelating Zeo-karb (gram)/to be clean is under the condition of 1/25-8/25, mixed 5-120 minute shaking in chelating Zeo-karb and the dried container of copper electrolyte to be clean, wash the chelating Zeo-karb of load after the separation with water, ratio with chelating Zeo-karb (the gram)/desorbed solution (milliliter) of load is the condition of 1/25-8/25, the chelating Zeo-karb and the EDTA aqueous solution that contains 1-10 gram/liter hydrogen-oxygen sodium 2-60 gram/liter with load, shake and mixed 5-120 minute, isolate desorbed solution.
7, processing method according to a kind of cleaning copper electrolyte of claim 5, it is characterized in that, said dynamical fashion is that the copper electrolyte that will purify is injected in the exchange column that the chelating Zeo-karb is housed, control flow velocity that copper electrolyte to be clean flows out exchange column and be the 20-100 milliliter/hour, be 5-120 minute the duration of contact of copper electrolyte to be clean and chelating Zeo-karb, after copper electrolyte to be clean flows out exchange column fully, wash the chelating Zeo-karb of load with water, the aqueous solution with the 2-60 gram/liter EDTA that contains 1-10 gram/liter sodium hydroxide is desorbed solution, be injected in the exchange column, the flow velocity of outflow exchange column of control desorbed solution be the 20-100 milliliter/hour, be 5-60 minute duration of contact that makes desorbed solution and chelating Zeo-karb.
8, according to the processing method of a kind of cleaning copper electrolyte of claim 7, it is characterized in that, the flow velocity that copper electrolyte to be clean flows out exchange column be the 35-60 milliliter/hour, 15-60 minute duration of contact.
9, according to the processing method of a kind of cleaning copper electrolyte of claim 7, it is characterized in that, the flow velocity that desorbed solution flows out exchange column be the 40-80 milliliter/hour, 15-45 minute duration of contact.
10, according to the processing method of a kind of cleaning copper electrolyte of claim 7, it is characterized in that the aspect ratio of ion exchange column is 5: 1-70: 1.
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|---|---|---|---|
| CN92113237A CN1028658C (en) | 1992-12-02 | 1992-12-02 | Technology of purifying copper electrolyte |
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|---|---|---|---|
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| Publication number | Priority date | Publication date | Assignee | Title |
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| TWI487660B (en) * | 2010-07-09 | 2015-06-11 | Nippon Chemical Ind | Preparing method of high purity phosphorus and high purity phosphoric acid |
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