CN203754786U - System for recycling antimony and bismuth in copper electrolyte - Google Patents
System for recycling antimony and bismuth in copper electrolyte Download PDFInfo
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- CN203754786U CN203754786U CN201420139058.XU CN201420139058U CN203754786U CN 203754786 U CN203754786 U CN 203754786U CN 201420139058 U CN201420139058 U CN 201420139058U CN 203754786 U CN203754786 U CN 203754786U
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- antimony
- bismuth
- copper electrolyte
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Abstract
The utility model discloses a system for recycling antimony and bismuth in a copper electrolyte. The system comprises an extraction tank, a back-extraction tank, a neutralization and precipitation tank and a filter which are arranged in sequence, wherein the input end of the back-extraction tank is connected with an antimony and bismuth ionic recovery liquid outlet of the extraction tank; an antimony and bismuth ionic returning liquid outlet of the back-extraction tank is connected with the input end of the neutralization and precipitation tank; the output end of the neutralization and precipitation tank is connected with the input end of the filter. When antimony and bismuth ions in the copper electrolyte reach a certain concentration, the antimony and bismuth ions in the copper electrolyte can be recycled for resale by adopting the technical scheme, so that the production quality of electrolytic copper can be effectively ensured, and the pollution to environment can be reduced; the system is simple and convenient in operation, low in production cost and low in energy consumption. The system disclosed by the utility model mainly adopts a three-step method, namely organic phase extraction liquid extraction, stripping liquid complexing back-extraction and alkali liquor neutralization precipitation reaction to ensure that the antimony and bismuth ions in the recovery liquid containing the antimony and bismuth ions are precipitated to obtain an antimony and bismuth ion concentrate, thus realizing the purification of the copper electrolyte.
Description
Technical field
The utility model relates to chemical production field, is specifically related to the recovery system of antimony and bismuth in a kind of copper electrolyte.
Background technology
In prior art, the blister copper of exploitation is adopted electro deposition fine copper by copper mine enterprise, concrete steps are: first blister copper is made to slab as anode, pure copper flakiness is made negative electrode, using the mixed liquid of sulfuric acid and copper sulfate as electrolytic solution, like this after energising, the blister copper of anode loses cupric ion that electronics obtains to movable cathode, the cupric ion that arrives negative electrode obtains electronics and can separate out electrolytic copper (also claiming fine copper or cathode copper), but in actual production, antimony in blister copper, the impurity such as bismuth can be followed copper that electrolysis synchronously occurs and generate antimony ion and bismuth ion, antimony ion and bismuth ion can form the flocculent substance that solubleness is very little and adhere to the surface of negative electrode fine copper and electrolytic copper in copper electrolyte, not only affect the performance of negative electrode fine copper, and reduce widely the quality of the electrolytic copper generating.For addressing the above problem; enterprise adopts electrodeposition method (also referred to as revulsion) that impurity antimony and bismuth are enriched in electrodeposition product black copper powder more at present; thereby realize deviating from of antimony and bismuth; but in order to improve the yield of copper; the black copper powder that is rich in antimony and bismuth can return to refinement copper conventionally; will cause so constantly accumulating in impurity antimony and bismuth circulating production system; finally cause the foreign matter content in copper electrolyte too high, long-time continuous is produced the quality of production that equally also can have influence on electrolytic copper.
Summary of the invention
The purpose of this utility model is to provide the recovery system of antimony and bismuth in a kind of copper electrolyte, and the rate of recovery of this recovery system is high, and running cost is low.
For achieving the above object, the technical solution adopted in the utility model is: the recovery system of antimony and bismuth in a kind of copper electrolyte, it is characterized in that: comprise extraction tank, reextraction groove, neutralization precipitation groove and the strainer arranged successively, the input terminus of described reextraction groove reclaims liquid outlet with the antimony of extraction tank, bismuth ion and is connected, the antimony of reextraction groove, the anti-fluid outlet of bismuth ion are connected with the input terminus of neutralization precipitation groove, and the output terminal of described neutralization precipitation groove is connected with the input terminus of strainer.
The beneficial effect that adopts technique scheme to produce is: in the technique of electrorefining fine copper, in the time that the antimony in copper electrolyte, bismuth ion reach finite concentration, adopt technique scheme antimony wherein, bismuth ion can be reclaimed and sell, so not only effectively ensure the quality of production of electrolytic copper, and the pollution of reduction to environment, easy and simple to handle, production cost is low, and energy consumption is little.The utility model is mainly to utilize the extraction of organic extractant phase liquid, strip liquor complexing back extraction, this three-step approach of alkali lye neutralization-precipitation reaction to make to separate out and obtain antimony, bismuth ion enriched substance containing antimony, bismuth ion in the recovery liquid of antimony, bismuth ion, thereby realizes the purifying of copper electrolyte.
Brief description of the drawings
Fig. 1 is system construction drawing of the present utility model.
Embodiment
The recovery system of antimony and bismuth in a kind of copper electrolyte, as shown in Figure 1, it comprises the extraction tank 10 of arranging successively, reextraction groove 20, neutralization precipitation groove 30 and strainer 40, the antimony of the input terminus of described reextraction groove 20 and extraction tank 10, bismuth ion reclaims liquid outlet 11 and is connected, the antimony of reextraction groove 20, the anti-fluid outlet 21 of bismuth ion is connected with the input terminus of neutralization precipitation groove, the output terminal of described neutralization precipitation groove 30 is connected with the input terminus of strainer 40, like this in the technique of electrorefining fine copper, when the antimony in copper electrolyte, when bismuth ion reaches finite concentration, employing technique scheme can be by antimony wherein, bismuth ion reclaims and sells, so not only effectively ensure the quality of production of electrolytic copper, and the pollution of reduction to environment, easy and simple to handle, production cost is low, energy consumption is little.The utility model is mainly to utilize the extraction of organic extractant phase liquid, strip liquor complexing back extraction, this three-step approach of alkali lye neutralization-precipitation reaction to make to separate out and obtain antimony, bismuth ion enriched substance containing antimony, bismuth ion in the recovery liquid of antimony, bismuth ion, thereby realize the purifying of copper electrolyte, the rate of recovery that operates antimony, bismuth by substep is high, the concrete step that uses is as follows: 1) adopt the copper electrolyte of organic extractant phase liquid counter-current extraction containing antimony, bismuth ion, obtain the copper electrolyte of purifying and the recovery liquid containing antimony, bismuth ion; 2) adopt strip liquor to strip containing the recovery liquid of antimony, bismuth ion, obtain extracting phase and the anti-fluid containing antimony, bismuth ion; 3) be 7～8.5 to adding ammoniacal liquor modulation pH value in the anti-fluid containing antimony, bismuth ion, filter, the filter residue obtaining is antimony bismuth enriched substance, preferred, described strainer 40 is vacuum filtration machine, obtains the antimony bismuth enriched substance that remains in strainer 40 tops after vacuum filtration.As shown in Figure 1, two storage tanks that are positioned at extraction tank 10 tops are respectively used to hold organic phase extraction liquid and the copper electrolyte containing antimony, bismuth ion, the storage tank that is positioned at extraction tank 10 left sides is for collecting the copper electrolyte after storage purifying, being positioned at the storage tank of reextraction groove 20 tops for holding anti-stripping agent.
As further preferred version: described recovery system also comprises strip liquor Preparation tank 60, the filtrate outlet 41 of strainer 40 is connected with the import of strip liquor Preparation tank 60, as shown in Figure 1, so-called strip liquor Preparation tank 60 is namely for preparing the cell body of strip liquor, when actual use, can prepare the thiocarbamide of certain pH value and the mixture of sulfuric acid as strip liquor, owing to containing a large amount of strip liquors in the filtrate in strainer 40, therefore the filtrate in strainer 40 is incorporated into strip liquor Preparation tank 60 can through preparation after recycling, greatly improve the utilization ratio of resource, concrete, described recovery system also comprises the vaporizer 70 of arranging successively, cooling room 80 and whizzer 90, the input terminus of described vaporizer 70 is connected with the filtrate outlet 41 of strainer 40, the vapour outlet of vaporizer 70 is connected with the input terminus of cooling room 80, the input terminus of described whizzer 90 is connected with the output terminal of cooling room 80, the centrifugate outlet 91 of whizzer 90 is connected with the import of strip liquor Preparation tank 60, preferably, connecting pipeline between described strainer 40 and vaporizer 70 is furnished with surge tank 100.Because strip liquor is to recycle, and strip liquor and between the ammoniacal liquor of pH value, chemical reaction can occur and generate ammonium sulfate for modulating, this just causes long-time production can cause the excessive concentration of the ammonium sulfate in filtrate after neutralization precipitation until the value of reaching capacity, therefore in actual production process, the utility model adopt technique scheme by the filtrate in strainer 40 successively by vacuum-evaporation, crystallisation by cooling and centrifuging treatment, ammonium sulfate in filtrate can be separated, thereby guarantee that system is able to continual and steady operation, the concentration of the ammonium sulfate in concrete filtrate can regularly detect and learn, also can observe intuitively and in reextraction groove 20, whether contain crystal, in the time containing crystal, illustrate that the ammonium sulfate concentrations in circulation fluid is higher, need to carry out separating treatment.
Further, described recovery system also comprises washing bath 50, the input terminus of washing bath 50 is connected with the organic phase outlet 22 of reextraction groove 20, the washing progression of washing bath 50 is level Four, adopt the organic phase of discharging after stripping in washing bath 50 level Four washings reextraction grooves 20 can efficient recovery organic extractant phase liquid, realize the recycle and reuse of raw material, make full use of resource, reduce the pollution to environment, as shown in Figure 1, the storage tank of described washing bath 50 tops is supply flume, the storage tank on washing bath 50 right sides is for collecting the organic extractant phase liquid of recovery, concrete, the counter-current extraction progression of described extraction tank 10 is three grades, the reextraction progression of reextraction groove 20 is Pyatyi, adopt three grades of extractions, Pyatyi is stripped can ensure Antimony in Waste Water, the rate of recovery of bismuth is higher, and cost recovery is low.
Claims (5)
1. the recovery system of antimony and bismuth in a copper electrolyte, it is characterized in that: comprise extraction tank (10), reextraction groove (20), neutralization precipitation groove (30) and the strainer (40) arranged successively, the input terminus of described reextraction groove (20) reclaims liquid outlet (11) with the antimony of extraction tank (10), bismuth ion and is connected, the anti-fluid outlet of antimony, bismuth ion (21) of reextraction groove (20) is connected with the input terminus of neutralization precipitation groove (30), and the output terminal of described neutralization precipitation groove (30) is connected with the input terminus of strainer (40).
2. the recovery system of antimony and bismuth in copper electrolyte according to claim 1, is characterized in that: described recovery system also comprises strip liquor Preparation tank (60), the filtrate outlet (41) of strainer (40) is connected with the import of strip liquor Preparation tank (60).
3. the recovery system of antimony and bismuth in copper electrolyte according to claim 1, is characterized in that: described recovery system also comprises washing bath (50), the input terminus of washing bath (50) is connected with the organic phase outlet (22) of reextraction groove (20).
4. the recovery system of antimony and bismuth in copper electrolyte according to claim 2, it is characterized in that: described recovery system also comprises the vaporizer (70) of arranging successively, cooling room (80) and whizzer (90), the input terminus of described vaporizer (70) is connected with the filtrate outlet (41) of strainer (40), the vapour outlet of vaporizer (70) is connected with the input terminus of cooling room (80), the input terminus of described whizzer (90) is connected with the output terminal of cooling room (80), the centrifugate outlet (91) of whizzer (90) is connected with the import of strip liquor Preparation tank (60).
5. the recovery system of antimony and bismuth in copper electrolyte according to claim 3, is characterized in that: the counter-current extraction progression of described extraction tank (10) is three grades, the reextraction progression of reextraction groove (20) is Pyatyi, and the washing progression of washing bath (50) is level Four.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420139058.XU CN203754786U (en) | 2014-03-25 | 2014-03-25 | System for recycling antimony and bismuth in copper electrolyte |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420139058.XU CN203754786U (en) | 2014-03-25 | 2014-03-25 | System for recycling antimony and bismuth in copper electrolyte |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203754786U true CN203754786U (en) | 2014-08-06 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420139058.XU Withdrawn - After Issue CN203754786U (en) | 2014-03-25 | 2014-03-25 | System for recycling antimony and bismuth in copper electrolyte |
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| CN (1) | CN203754786U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103849903A (en) * | 2014-03-25 | 2014-06-11 | 金隆铜业有限公司 | System for recovering antimony and bismuth in copper electrolyte |
-
2014
- 2014-03-25 CN CN201420139058.XU patent/CN203754786U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103849903A (en) * | 2014-03-25 | 2014-06-11 | 金隆铜业有限公司 | System for recovering antimony and bismuth in copper electrolyte |
| CN103849903B (en) * | 2014-03-25 | 2016-08-24 | 金隆铜业有限公司 | Antimony and the recovery system of bismuth in copper electrolyte |
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| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140806 Effective date of abandoning: 20160824 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |