CN1091479A - A kind of processing method of clarifying lead electrolytic solution - Google Patents
A kind of processing method of clarifying lead electrolytic solution Download PDFInfo
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Abstract
The present invention relates to the purifying method of lead electrolytic solution, its technology is that 40-350 lead electrolytic solutions gram/liter silicofluoric acid and that contain bismuth that contain to be clean are contacted with the chelating Zeo-karb, behind the absorption bismuth ion, with the aqueous solution that contains 1-10 gram/liter sodium hydroxide, 1-60 gram/liter EDTA is desorbed solution, and wash-out is removed the bismuth on the resin.This processing method does not produce acid mist, and is free from environmental pollution, and the EDTA in the solution after the parsing can be recycled, and cost is low, and lead electrolytic solution to be clean must directly not purify through any processing, does not change the component of electrolytic solution again.
Description
The present invention relates to the purifying method of lead electrolytic solution, contain the method for purification of the lead electrolytic solution of silicofluoric acid more precisely.
When adopting Bei Cifa to carry out the electrorefining of lead bullion, electrolytic solution is made up of materials such as PbSiF6 and H2SiF6.During the lead bullion anode electrolysis, reductibility originally should not enter electrolytic solution than plumbous strong metal as elements such as gold and silver, copper, bismuth, antimony, arsenic, stays on the anode anode scrap and should form spongy metal, and enters in the anode sludge.But in actual production, always have a small amount of above-mentioned metal to enter in the electrolytic solution, particularly bismuth under electrophoretic action, is separated out the major impurity that forms in the electrolytic lead at negative electrode.
For reclaiming plumbous and silicofluoric acid (H2SiF6), the anode sludge washes with water, and formed anode sludge wash water generally all returns in the lead electrolytic solution, and in the anode sludge wash water, the content of bismuth and antimony is often very high, thereby has further polluted lead electrolytic solution.
Normally carry out quality with negative electrode lead for what guarantee plumbous electrolytic process, must from lead electrolytic solution, remove detrimental impurity such as bismuth periodically (or constantly).
In order to purify lead electrolytic solution, remove detrimental impurity such as bismuth in the lead electrolytic solution, can adopt different purifying methods, for example the whole bag of tricks such as chemical method, active carbon adsorption, extraction process.
The extraction process technical process is long, and energy consumption is big, and the organic solvent contaminate environment is hindered health of operators.The advantage of active carbon adsorption is simple to operate, does not need other auxiliary reagents, and some mineral ions are had certain adsorption, and its shortcoming is that rate of adsorption is slower; The clarification filtration difficulty, particularly the fine particulate activated carbon is difficult to separate from solution, and the gac of load is resolved difficulty, general is used once, and has increased the cost of purification process widely.
Recently, the Japanese documentation spy opens clear 62-9193 and has reported the technical process of using the ion-exchange purification lead electrolytic solution.This technology is to contain the lead of 40-80 gram/liter, 40-120 gram/liter silicofluoric acid contacts with the chelating Zeo-karb with the electrolytic solution to be clean of detrimental impurity such as bismuth metal, adsorb deleterious foreign ion such as bismuth in the lead electrolytic solution to be clean, the aqueous solution of hydrochloric acid of using the silicofluoric acid of 2-6N or 2-8N then is as detrimental impurity ionic desorbed solutions such as bismuths, wash-out is adsorbed on the detrimental impurity ions such as bismuth on the chelating Zeo-karb, and lead electrolytic solution is purified.The advantage of this processing method is directly to handle lead electrolytic solution, and do not change the component of electrolytic solution, and not causing secondary pollution, the lead electrolytic solution after the processing can directly return in the electrolyzer, do not need numerous and diverse processing of giving, the chelating Zeo-karb can recycle simultaneously.This method technology and equipment are simple, easy to operate, the purification efficiency height, and the purification expense is cheap; It is changeable also to have scale, but the handiness of periodical operation continuously.The shortcoming of this technical process is that detrimental impurity ionic desorbed solutions such as employed bismuth are the silicofluoric acid aqueous solution of 2-6N or the aqueous hydrochloric acid of 2-8N.With the desorbed solution of 2-6N silicofluoric acid as detrimental impurity such as bismuths, detrimental impurity ionic resolution factors such as bismuth are too low, and adopt the hydrochloric acid of 2-8N respond well as detrimental impurity ionic desorbed solutions such as bismuths.But the corrodibility of hydrochloric acid is big, produces acid mist and waste water, and contaminate environment endangers health of operators, and can not recycle again as the hydrochloric acid of desorbed solution.
Purpose of the present invention just is to work out a kind of processing method of new purification lead electrolytic solution, finds out a kind of new detrimental impurity ionic desorbed solutions such as wash-out bismuth, avoids the corrodibility of hydrochloric acid, resolution factor is high again, do not produce acid mist, do not have environmental pollution again, do not endanger health of operators; And the EDTA in the chelating Zeo-karb, desorbed solution can be recycled again, kept the various advantages of above-mentioned prior art intermediate ion exchange process simultaneously again.
The processing method of a kind of clarifying lead electrolytic solution of the present invention, to contain lead electrolytic solution to be clean silicofluoric acid 40-350 gram/liter and that contain detrimental impurity such as bismuth contacts with the chelating Zeo-karb, adsorb the detrimental impurity ions such as bismuth in the lead electrolytic solution to be clean, with containing 1-10 gram/liter alkali metal hydroxide, 1-60 gram/liter disodium EDTA (EDTA, C10H14N208Na2.2H2O) the aqueous solution is detrimental impurity ionic desorbed solutions such as bismuth, wash-out is removed the detrimental impurity ions such as bismuth that are adsorbed on the chelating Zeo-karb, and lead electrolytic solution is purified.
Consisting of of the lead electrolytic solution to be clean that the present invention is used: contain 10-130 gram/liter lead (plumbous for good) to contain 50-100 gram/liter, 40-350 gram/liter silicofluoric acid (to contain 100-120 gram/liter silicofluoric acid for well), 0.001-3.5 gram/liter bismuth (contain＜1.0 gram/liter bismuths are good), 0.01-4.0 gram/liter antimony (with contain＜2.0 gram/liter antimony are for well), 0.1-5 gram/liter iron (with contain＜3 gram/liter iron are good).Said lead electrolytic solution also comprises plumbous electrolysis anode sludge washing lotion.The Controllable Temperature of lead electrolytic solution to be clean is built in 5 °-55 ℃ (to be controlled at 15 °-45 ℃ for good).The used chelating Zeo-karb of the present invention does not adsorb basically to plumbous and silicofluoric acid, so lead and the change in concentration of silicofluoric acid in solution are to not influence of detrimental impurity ionic such as bismuth absorption.Because the impurity in the electrolytic lead mainly is bismuth, it accounts for 50% in total impurities, therefore in the purification of lead electrolytic solution, most importantly purifies bismuth.
Used chelating Zeo-karb is aminoalkyl group phosphate chelating Zeo-karb (for example D411,2#), pyridyl chelating Zeo-karb (for example 1#, 4#, 5#, D280); aminocarboxylic acidic group chelating Zeo-karb (3#, 6#); wherein a kind of such as polyamides base chelating Zeo-karb, but be good with aminoalkyl group phosphate chelating Zeo-karb, pyridyl chelating Zeo-karb.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.Aminoalkyl group phosphate chelating Zeo-karb (D411) is to be raw material with primary amine resin, phosphorous acid, formaldehyde, and by Mannicn reaction synthetic, its functional group is: R-CH2NHCH2PO(OH) 2 chelating Zeo-karb.Aminoalkyl group phosphate chelating Zeo-karb is 0.01-2.0 milligramequivalent/gram dried resin to the loading capacity of bismuth, is preferably 0.03-1.2 milligramequivalent/gram dried resin.
Used desorbed solution is the EDTA aqueous solution that contains 1-10 gram/liter alkali metal hydroxide, 1-60 gram/liter.Said metal hydroxides 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 dissolving rapidly in water of EDTA sodium salt, and keep its stability, makes the aqueous solution of EDTA be alkalescence.The change in concentration of alkali metal hydroxides such as sodium hydroxide in desorbed solution has no significant effect detrimental impurity ionic resolution factors such as bismuths in the concentration range of above-mentioned oxyhydroxide.Containing concentration sodium hydroxide in the aqueous solution that contains 1-60 gram/liter EDTA is that 2-5 gram/liter is than suitable.Along with the increase of EDTA concentration in the desorbed solution, detrimental impurity ionic resolution factors such as bismuth significantly rise.But when the concentration of EDTA was greater than 12 gram/liters in desorbed solution, detrimental impurity ionic resolution factors such as bismuth changed little.Therefore, the aqueous solution with the 2-25 gram/liter EDTA that contains 2-5 gram/liter sodium hydroxide is good in the desorbed solution.The aqueous solution of citric acid, trisodium citrate salt also can be used as detrimental impurity ionic desorbed solutions such as bismuth, and effect is inexcellent.
The way of contact that contains detrimental impurity ionic such as bismuth lead electrolytic solution to be clean and chelating Zeo-karb has two kinds of static mode and dynamical fashions, is good with dynamical fashion.Dynamical fashion is easy to operate, is easy to operate continuously.
Said static mode is that the ratio with the volume (milliliter) of the lead electrolytic solution of dried chelating Zeo-karb (gram)/to be clean is under the condition of 5/100-40/100, with wet chelating Zeo-karb and lead electrolytic solution to be clean pack into (for example in the Erlenmeyer flask) in the container, at 5 °-55 ℃, shake and mix 5-100 minute (mixing 10-50 minute for good) to shake.Isolate the lead electrolytic solution after the purification, water (ion exchanged water or distilled water) with the chelating Zeo-karb of load wash to the PH of washing water be 3-5, ratio with chelating Zeo-karb (the gram)/desorbed solution (milliliter) of load is under the condition of 2/100-40/100, with the chelating Zeo-karb of load with contain 1-10 gram/liter sodium hydroxide as desorbed solution, the EDTA aqueous solution of 1-60 gram/liter, shake and mix 5-80 minute (mixing 30-50 minute for good) to shake, isolate desorbed solution, water (ion exchanged water or distilled water) is washed till washing water near neutral with the chelating Zeo-karb of load.
In the adsorption process of static mode (be the chelating Zeo-karb with the contacting of lead electrolytic solution to be clean in), along with the increase of the ratio of the volume (milliliter) of the lead electrolytic solution of chelating Zeo-karb (gram)/to be clean, the adsorption rate of detrimental impurity ions such as bismuth on the chelating Zeo-karb increases; Under the situation that other experiment conditions remain unchanged, along with the increase of the ratio of the volume (milliliter) of the lead electrolytic solution of chelating Zeo-karb (gram)/to be clean, the adsorption rate of detrimental impurity ions such as bismuth on the chelating Zeo-karb increases; Under the situation that other experiment conditions remain unchanged, along with the prolongation that chelating Zeo-karb and lead electrolytic solution to be clean shake and do time together, detrimental impurity ions such as bismuth adsorption rate on the chelating Zeo-karb obviously increases.In the resolving of static mode (be detrimental impurity ionic chelating Zeo-karbs such as load bismuth with the contacting of desorbed solution in), along with the prolongation that the chelating Zeo-karb and the desorbed solution of load shakes and do time, detrimental impurity ionic resolution factors such as bismuth increase.
Said dynamical fashion is that lead electrolytic solution to be clean is injected in the exchange column that the chelating Zeo-karb is housed, control flow velocity that lead electrolytic solution to be clean flows out exchange column and be the 25-150 milliliter/hour, be preferably the 40-120 milliliter/hour, be that lead electrolytic solution to be clean is when flowing out exchange column, control SV=0.5-2.5, be preferably 0.8-2.0, be 5-100 minute duration of contact that makes lead electrolytic solution to be clean and chelating Zeo-karb, be preferably 10-50 minute, after lead electrolytic solution to be clean flows out exchange column fully, the chelating Zeo-karb of water (ion exchanged water or distilled water) wash load to the PH of washing water be 4-5, with containing 1-10 gram/liter sodium hydroxide, the aqueous solution of 1-60 gram/liter EDTA is 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 the 40-80 milliliter/hour, control SV=0.5-2.5 when being desorbed solution outflow exchange column, be preferably 0.8-2, be 5-80 minute duration of contact that makes the chelating Zeo-karb of desorbed solution and load, be preferably 30-50 minute, after liquid to be resolved all flowed out exchange column, it was near neutral that water (ion exchanged water or distilled water) washs to effluent liquid.
In the adsorption process and resolving of dynamical fashion (being the lead electrolytic solution to be clean and the contact process of chelating Zeo-karb and the contact process of detrimental impurity ionic chelating Zeo-karbs such as desorbed solution and load bismuth), be the ratio that amount (milliliter) and the lead electrolytic solution to be clean or the desorbed solution of chelating Zeo-karb flows out the flow velocity (ml/min) of exchange column said duration of contact.
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 is packed stand-by resin in the post in the mode of wet type, and 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 height of ion exchange column is through than being 5: 1-70: 1, be preferably 8: 1-50: 1.Used chelating Zeo-karb is sodium type or Hydrogen, and the chelating Zeo-karb of sodium type, Hydrogen does not have marked difference to detrimental impurity ionic absorption properties such as bismuths.As desorbed solution, adopt sodium salt better with the aqueous solution of the EDTA that contains sodium hydroxide, need not make the transition and just can adsorb again; If use H
+Type need be handled with aqueous hydrochloric acid.The exhausted desorbed solution promptly contains the aqueous solution of the EDTA of sodium hydroxide, and the method for all knowing with the those of ordinary skill under this area makes EDTA obtain reclaiming repeated use.
The advantage of processing method of the present invention just is to have found out a kind of new detrimental impurity ionic desorbed solutions such as bismuth and replaces concentrated hydrochloric acid, does not produce acid mist, does not produce environmental pollution, is of value to health of operators.The exhausted desorbed solution after treatment, EDTA can recycle, and has reduced cost.The various advantages that kept simultaneously above-mentioned prior art intermediate ion exchange process again.And processing method of the present invention can reach 99% to the adsorption rate of bismuth, and the resolution factor of bismuth can reach more than 90%.Processing method of the present invention can be taken out lead electrolytic solution to be clean and directly be purified without any processing from plumbous electrolyzer, easy to operate, equipment is simple, does not also change the component of lead electrolytic solution.Processing method of the present invention can also be removed impurity iron and part organism objectionable impuritiess such as (for example sulfonic acid calcium salts) in the lead electrolytic solution to be clean simultaneously.
With following indefiniteness embodiment processing method of the present invention is further described, will helps understanding the present invention and advantage thereof, and not as the qualification to protection domain of the present invention.Protection scope of the present invention is decided by claim.
Embodiment 1
It consists of (gram/liter) to used lead electrolytic solution to be clean as raw material:
Plumbous silicofluoric acid bismuth
93.51 130.0 0.0095
Used ion exchange column is made by glass, and its height is through than being 50: 1.Used chelating Zeo-karb is aminoalkyl group phosphate chelating Zeo-karb (D411, Tianjin Chemical Plant of Nankai Univ. produces, in following embodiment, all abbreviate the D411 resin as), be 0.028 milligramequivalent/gram dried resin to the loading capacity of bismuth.Temperature is 25 ℃, in adsorption process stock liquid is injected in the exchange column, and the flow velocity that the control stock liquid flows out exchange column is 60 milliliters/hour, and making its stock liquid and D411 resin duration of contact is 40 minutes.The consumption of stock liquid is 2.6 liters.The composition (gram/liter) of the stock liquid after the D411 resin absorption purifies is:
Plumbous silicofluoric acid bismuth
93.0 130.0 0.0018
After being about 4 with the D411 resin of ion exchanged water wash load to the PH of washing water, carry out resolving.With the aqueous solution that contains 4 gram/liter sodium hydroxide, 15 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, making the duration of contact of detrimental impurity ionic D411 resins such as desorbed solution and load bismuth is 42 minutes, and the desorbed solution consumption is 0.95 liter.The resolution factor of bismuth is 94.4%.The content of various components is respectively in the aqueous solution after the parsing: plumbous 2 gram/liters, silicon chloric acid＜0.5 gram/liter, bismuth are 0.021 gram/liter.
Embodiment 2
Its working method and equipment are with embodiment 1.
Stock liquid is formed (gram/liter):
Plumbous silicofluoric acid bismuth
58.52 200.0 0.0281
The aspect ratio of exchange column is 40: 1.The D411 resin is 0.0521 milligramequivalent/gram dried resin to the loading capacity of bismuth.29 ℃ of temperature.The flow velocity of stock liquid outflow exchange column is 100 milliliters/hour in adsorption process, and be 21 minutes duration of contact.Stock liquid consumption 1.8 liters.The composition (gram/liter) of the stock liquid after the D411 resin absorption purifies is:
Plumbous silicofluoric acid bismuth
58.21 200.0 0.0078
Using the aqueous solution of the 10 gram/liter EDTA that contain 4 gram/liter sodium hydroxide in resolving is desorbed solution, and the flow velocity that desorbed solution flows out exchange column is 50 milliliters/hour, 42 minutes duration of contact, desorbed solution consumption 0.4 liter.The resolution factor of bismuth is 90%.The content of various components is respectively in the aqueous solution after the parsing: lead＜1 gram/liter, silicofluoric acid＜0.5 gram/liter, bismuth 0.083 gram/liter.
Embodiment 3
Its working method and equipment are with embodiment 1.
Stock liquid is formed (gram/liter):
Plumbous silicofluoric acid bismuth
66.38 316.8 0.0415
Exchange column aspect ratio 50: 1.The D411 resin is 0.09346 a milligram/gram dried resin to the loading capacity of bismuth.25 ℃ of temperature.The flow velocity of stock liquid outflow exchange column is 60 milliliters/hour in adsorption process, and be 35 minutes duration of contact.Stock liquid is plumbous electrolysis anode sludge washing lotion, and its consumption is 1.5 liters.The composition (gram/liter) of the stock liquid after the D411 resin absorption purifies is:
Plumbous silicofluoric acid bismuth
66.17 314.53 0.00064
Using the aqueous solution of 8 gram/liter EDTA of the sodium hydroxide that contains 4 gram/liters in resolving is desorbed solution.The flow velocity that desorbed solution flows out exchange column is 50 milliliters/hour, 42 minutes duration of contact.Desorbed solution consumption 0.66 liter.The resolution factor of bismuth is 70%.The content of various components is in the aqueous solution after the parsing: lead＜1.0 gram/liters, silicofluoric acid＜0.5 gram/liter, bismuth 0.063 gram/liter.
Embodiment 4
Its working method and equipment are with embodiment 1.
Stock liquid is formed (gram/liter):
Plumbous silicofluoric acid bismuth
57.13 200.55 0.08
The aspect ratio of exchange column is 50: 1.The D411 resin is 0.1103 milligramequivalent/gram dried resin to the loading capacity of bismuth.27 ℃ of temperature.The flow velocity of stock liquid outflow exchange column is 60 milliliters/hour in adsorption process.35 minutes duration of contact.Stock liquid is plumbous electrolysis anode sludge washing lotion, and its consumption is 1.0 liters.The composition (gram/liter) of the stock liquid after the D411 resin absorption purifies is:
Plumbous silicofluoric acid bismuth
56.10 200.20 0.00064
Using the aqueous solution that contains 4 gram/liter sodium hydroxide, 12 gram/liter EDTA in resolving is desorbed solution.The flow velocity that desorbed solution flows out exchange column is 50 a milliliters/liter.42 minutes duration of contact.Desorbed solution consumption 0.9 liter.The resolution factor of bismuth is 98%.The content of various components is respectively in the aqueous solution after the parsing: lead＜1.0 gram/liters, silicofluoric acid＜0.5 gram/liter, bismuth 0.086 gram/liter.
Embodiment 5
Stock liquid (is stock liquid with plumbous electrolysis anode sludge washing lotion) is formed (gram/liter):
Plumbous silicofluoric acid bismuth
57.13 200.55 0.061
(be processed into wet during use 4 gram D411 dried resins, treatment process is known for those skilled in the art) and 50 milliliters stock liquid pack in the Erlenmeyer flask, under room temperature (about 25 ℃), shake and mixed 40 minutes, obtain the resin and the adsorbed solution of load after the separation, the composition in the adsorbed solution (gram/liter) is:
Plumbous silicofluoric acid bismuth
57.01 200.32 0.00756
Load has the D411 resin of detrimental impurity such as bismuth, resolves as desorbed solution for 150 milliliters with the aqueous solution of the 7.5 gram/liter EDTA that contain 3 gram/liter sodium hydroxide.Shake and mixed 45 minutes, the content of the each component in the solution after the parsing that separation obtains is respectively: lead＜1.0 gram/liters, silicofluoric acid＜0.5 gram/liter, bismuth 0.030/ liter.The resolution factor 75.5% of bismuth.
Embodiment 6
Stock liquid (is stock liquid with lead electrolytic solution to be clean) is formed (gram/liter):
Plumbous silicofluoric acid bismuth
75.74 107.66 0.059
(be processed into wet during use 5 gram D411 dried resins, treatment process is known for those skilled in the art) and 50 milliliters stock liquid pack in the Erlenmeyer flask, under room temperature (about 29 ℃), shake and mixed 30 minutes, obtain the resin and the adsorbed solution of load after the separation, the composition in the adsorbed solution (gram/liter) is:
Plumbous silicofluoric acid bismuth
75.63 107.59 <0.001
Load has the D411 resin of detrimental impurity such as bismuth, resolves as desorbed solution for 120 milliliters with the aqueous solution of the 15 gram/liter EDTA that contain 2 gram/liter sodium hydroxide.Shake and mixed 30 minutes, the content of the each component in the solution after the parsing that separation obtains is respectively: lead＜1.0 gram/liters, silicofluoric acid＜0.5 gram/liter, bismuth 0.041/ liter.The resolution factor 81.14% of bismuth.
Claims (10)
1, a kind of processing method of clarifying lead electrolytic solution, to contain lead electrolytic solution to be clean silicofluoric acid 40-350 gram/liter and that contain detrimental impurity such as bismuth contacts with the chelating Zeo-karb, adsorb the detrimental impurity ions such as bismuth in the lead electrolytic solution to be clean, it is characterized in that, with the aqueous solution that contains 1-10 grams per liter alkali metal hydroxide, 1-60 gram/liter disodium EDTA (EDTA) is detrimental impurity ionic desorbed solutions such as bismuth, and wash-out is removed the detrimental impurity ions such as bismuth that are adsorbed on the chelating Zeo-karb.
According to the processing method of a kind of clarifying lead electrolytic solution of claim 1, it is characterized in that 2, the chelating Zeo-karb is wherein a kind of of aminoalkyl group phosphate chelating Zeo-karb, pyridyl chelating Zeo-karb.
3, according to the processing method of a kind of clarifying lead electrolytic solution 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 clarifying lead electrolytic solution of claim 1, it is characterized in that, is desorbed solution with the aqueous solution that contains 2-5 gram/liter sodium hydroxide, 2-25/ liter EDTA.
According to the processing method of a kind of clarifying lead electrolytic solution of claim 1, it is characterized in that 5, the way of contact that contains detrimental impurity ionic such as bismuth lead electrolytic solution to be clean and chelating Zeo-karb is wherein a kind of of static mode, dynamical fashion.
6, processing method according to a kind of clarifying lead electrolytic solution of claim 5, it is characterized in that, said static mode is, ratio with the volume (milliliter) of the lead electrolytic solution of dried chelating Zeo-karb (gram)/to be clean is under the condition of 5/100-40/100, wet chelating Zeo-karb and lead electrolytic solution to be clean are packed in the container, shake and mixed 5-100 minute, isolate the lead electrolytic solution after the purification, wash the chelating Zeo-karb of load with water, ratio with chelating Zeo-karb (the gram)/desorbed solution (milliliter) of load is under the condition of 2/100-40/100, with the chelating Zeo-karb of load with contain 1-10 gram/liter sodium hydroxide, the EDTA aqueous solution of 1-60 gram/liter, shake and mixed 5-80 minute, isolate desorbed solution.
7, processing method according to a kind of clarifying lead electrolytic solution of claim 5, it is characterized in that, said dynamical fashion is that lead electrolytic solution to be clean is injected in the exchange column that the chelating Zeo-karb is housed, when lead electrolytic solution to be clean flows out exchange column, control SV=0.5-2.5, be 5-100 minute duration of contact that makes lead electrolytic solution to be clean and chelating Zeo-karb, after lead electrolytic solution to be clean flows out exchange column fully, wash the chelating Zeo-karb of load with water, with containing 1-10 gram/liter sodium hydroxide, the aqueous solution of 1-60 gram/liter EDTA is desorbed solution, be injected in the exchange column, when desorbed solution flows out exchange column, control SV=0.5-2.5, be 5-80 minute duration of contact that makes the chelating Zeo-karb of desorbed solution and load.
8, according to the processing method of a kind of clarifying lead electrolytic solution of claim 7, it is characterized in that, when lead electrolytic solution to be clean flows out exchange column, control SV=0.8-2.0, be 10-50 minute duration of contact that makes lead electrolytic solution to be clean and chelating Zeo-karb.
9, according to the processing method of a kind of clarifying lead electrolytic solution of claim 7, it is characterized in that, when desorbed solution flows out exchange column, control SV=0.8-2.0, making the duration of contact of the chelating Zeo-karb of desorbed solution and load is 30-50 minute.
10, according to the processing method of a kind of clarifying lead electrolytic solution of claim 7, it is characterized in that the aspect ratio of ion exchange column is 5: 1-70: 1.
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1993
- 1993-02-25 CN CN 93101688 patent/CN1028659C/en not_active Expired - Fee Related
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102206750A (en) * | 2011-05-04 | 2011-10-05 | 中南大学 | Method for recovering lead from lead-containing material by matching leaching-electrowinning method |
| CN103374728A (en) * | 2012-04-12 | 2013-10-30 | 梁达保 | Method for preparing lead electrolyte by utilizing industrial waste liquids |
| CN103374728B (en) * | 2012-04-12 | 2016-08-03 | 梁达保 | Utilize the method that industrial wastes produces lead electrolytic solution |
| CN104131317A (en) * | 2014-08-01 | 2014-11-05 | 昆明理工大学 | Method for preparation of fine lead powder by electrodeposition |
| CN104131317B (en) * | 2014-08-01 | 2016-08-24 | 昆明理工大学 | The method of thin lead powder is prepared in a kind of electro-deposition |
| CN110219020A (en) * | 2019-07-08 | 2019-09-10 | 云南驰宏资源综合利用有限公司 | A method of improving lead electrolytic solution electric conductivity |
| CN110219020B (en) * | 2019-07-08 | 2021-03-16 | 云南驰宏资源综合利用有限公司 | Method for improving conductivity of lead electrolyte |
| CN111519214A (en) * | 2020-06-09 | 2020-08-11 | 内蒙古兴安银铅冶炼有限公司 | Lead electrolyte purification process |
| CN112403028A (en) * | 2020-08-13 | 2021-02-26 | 郴州雄风环保科技有限公司 | Method for purifying lead electrolyte by using columnar activated carbon |
| CN113061941A (en) * | 2021-03-22 | 2021-07-02 | 刘罗平 | Bismuth removing method in high bismuth crude lead electrolysis process |
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