CN204529926U - The ion-exchange dechlorination system of solution of zinc sulfate in wet method zinc abstraction - Google Patents
The ion-exchange dechlorination system of solution of zinc sulfate in wet method zinc abstraction Download PDFInfo
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- CN204529926U CN204529926U CN201520230540.9U CN201520230540U CN204529926U CN 204529926 U CN204529926 U CN 204529926U CN 201520230540 U CN201520230540 U CN 201520230540U CN 204529926 U CN204529926 U CN 204529926U
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- ion
- zinc
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
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Abstract
The ion-exchange dechlorination system of solution of zinc sulfate in a kind of wet method zinc abstraction, it is characterized in that, the zinc sulfate storage pond storing solution of zinc sulfate connects ion exchange column by first pump, strippant storage pond is also connected with ion exchange column by pipeline, ion exchange column connects transfer pond further by pipeline, transfer pond is connected to electrolysis cycle pond and neutralizing well via second pump, and neutralizing well is connected to pressure filter via the 3rd pump, and the filtrate outlet of pressure filter is connected to settling tank.
Description
Technical field
The utility model relates to the ion-exchange dechlorination system of solution of zinc sulfate in a kind of wet method zinc abstraction.
Background technology
In wet zinc-making system, as long as there is the existence of chlorine will seriously etching apparatus, cause electrolytic anode plate life cycle to shorten, plate be burnt in electrolysis, and production can not be normal, causes Business Economic Benefit directly to decline.The applicant unit, since establishment, has taken secondary zinc oxide as raw material, and adopt alkali cleaning fluorine and chlorine removal technique, there is volume abnormal expansion, in liquid, fluorine chlorine ion concentration exceeds standard always, pole plate severe attrition.In recent years, along with low-grade zinc oxide ore, the popularization of the direct smelting technology of secondary zinc oxide waste residue and the direct use of zinc powder, the leaching of impurity element chlorine and accumulation are just unavoidable.At present, the leaching of most of wet method zinc abstraction manufacturer Chlorine in Solution is at 100-3000mg/L, and the highest reaches 5000mg/L.Direct impact has: one is that pole plate life cycle shortens, and consumes and obviously increases, and two is separate out lead tolerance in zinc to increase, and quality product obviously declines; Three is that pole plate utilization ratio is low, production cost showed increased, and economic benefit reduces.
How to remove the chlorion existed in dezincify liquid, be a great problem that zinc hydrometallurgy industry faces.Existing technical scheme, most of zinc hydrometallurgy dechlorination mainly carries out alkali cleaning, makes chlorine enter alkaline wash, makes water-soluble zinc and alkali reaction: ZnCoH
2, ZnCl
2+ 2NaOH=ZnCoH
2+ 2NaCl.In employing alkaline cleaning procedure, because alkaline residue is block, during slag input, slag surface is that acid-base neutralisation reaction first occurs, and produces a large amount of reaction heat, part alkaline residue can be wrapped up on the contrary, form hard particles, hinder reaction.Its shortcoming has: one is that washing dechlorination does not wash clean clearly, and chlorion about 60% still exists in zinc liquid, causes electrolysis to burn plate; Two is need a large amount of water to clean, and the water yield increases, and causes production cost to increase; Three is that in water, chlorion does not eliminate totally, causes water body environment pollution serious.
The application of ion exchange resin is an emphasis research topic of recent domestic zinc metallurgy industry, is the modern important symbol of Zn Cr coating.Adopt the chlorion generation replacement(metathesis)reaction in the commutative group of resin and electric effusion, the chlorion in solution is adsorbed on resin, and the corresponding ion-exchange of resin enters in solution, reaction formula [R] SO
4+ 2Cl
-=[R] Cl
2+ SO
4 2-.
But, in this area, still demand is also existed for the improved system of the chlorine in solution of zinc sulfate in removing wet method smelting process.
Utility model content
Present inventor is through prolonged and repeated scientific experimentation and exploitation, work out the ion-exchange dechlorination system of a set of solution of zinc sulfate, to dechlorinate method with ion-exchange, chlorion in production process is significantly reduced, and pole block rate of utilization greatly improves, production cost reduces, economic benefit significantly improves, and meanwhile, realizes the comprehensive utilization of resource, repeatedly prove through practice, the qualifying liquid Cl after its process
-content can drop to 200mg/L from 18000mg/L, owing to not needing large water gaging in process, environmental benefit is obvious, and economic benefit significantly improves.
The technical solution of the utility model is as described below:
The ion-exchange dechlorination system of solution of zinc sulfate in a kind of wet method zinc abstraction, it is characterized in that, the zinc sulfate storage pond storing solution of zinc sulfate connects ion exchange column by first pump, strippant storage pond is also connected with ion exchange column by pipeline, ion exchange column connects transfer pond further by pipeline, transfer pond is connected to electrolysis cycle pond and neutralizing well via second pump, and neutralizing well is connected to pressure filter via the 3rd pump, and the filtrate outlet of pressure filter is connected to settling tank.
Further, neutralizing well is connected with neutralizing agent feeding device.
Further, the sludge outlet of pressure filter connects sludge sump.
In said system, the solution of zinc sulfate (new liquid) after leaching enters ion exchange column, Cl in solution by certain flow velocity 0.25-0.3 meter per second
-by the SO in resin
4 2-exchange and enter in resin, thus reaching the object of zinc liquid dechlorination, the solution of zinc sulfate after exchange enters electrolysis cycle pond, after electrolysis, return leaching process.Resin to reach capacity state through the absorption of for some time, and the resin that absorption is saturated, passes into strippant by certain flow rate 0.25-0.3 meter per second, and resin, after desorb after a while, makes the Cl of resin absorption
-ion is by SO
4 2-exchange, stripping liquid is containing Cl
-ionic concn is higher, enters wastewater treatment equipment, and the resin (ion exchange column) after desorption and regeneration enters the subsequent work cycle.
Ion-exchange adsorption process: solution of zinc sulfate control certain flow 10-15 cubic meter/hour enters ion exchange column and exchanges, and the solution after exchange enters Chu Chi.When carrying out ion-exchange, control the flow velocity of solution, as Cl in solution
-when concentration reaches Con trolling index, resin absorption process stops, and starts resin desorption process.
Ion-exchange desorption process: strippant is sulfuric acid (H
2sO
4) and water preparation solution, the Chu Chizhong that is formulated in of strippant carries out.Strippant in strippant storage pond is undertaken adsorbing in satisfied ion exchange column by certain flow 10-15 cubic meter/hour, measures the Cl in stripping liquid
-concentration is until resin desorption meets processing requirement, and stripping liquid enters wastewater treatment equipment.
Ion exchange waste water process: waste water flows in neutralizing well to stir and adds the adjust ph such as lime, sodium sulphite, when pH value reaches control overflow, through pressure filter press filtration, waste residue enters waste dump, filtrate direct current enters settling tank, makes heavy metal fully precipitate further, and supernatant liquor can qualified discharge.
1, the solution of zinc sulfate in zinc sulfate storage pond sends into ion exchange column by ceramic pump, Cl in solution of zinc sulfate
-by the SO in resin
4 2-exchange and enter in resin, thus reaching the object of zinc liquid dechlorination: resin to reach capacity state through the absorption of 8-10 hour, and the resin that absorption is saturated, the solution of zinc sulfate after exchange enters transfer pond by being pumped into electrolysis cycle pond.
2, the strippant that the resin that absorption is saturated is made by adding sulfuric acid and water, resin, after the desorb of 4-6 hours, makes the Cl of resin absorption
-ion is by SO
4 2-exchange, the resin (ion exchange column) after desorption and regeneration enters the subsequent work cycle.
3, stripping liquid is containing Cl
-ionic concn is higher, then enter be added with milk of lime, the neutralizing well of sodium-chlor neutralizes, then by being pumped into pressure filter press filtration, being press-filtered out a part is mud, and a part is that filtrate enters the qualified rear discharge of settling tank precipitation again.
Advantage of the present utility model:
1. can cancel alkaline process flow process, save steam, water and starting material in a large number, reduce production cost;
2. from feed operation mode, easier, what decrease into alkaline residue is cumbersome;
3. from input speed, more rapidly, thus can reaction heat be made full use of, reduce and supplement quantity of steam;
4. from the reaction mechanism of meutral innersion, reaction effect is better; In employing alkaline cleaning procedure, because alkaline residue is block, during slag input, slag surface is that acid-base neutralisation reaction first occurs, and produces a large amount of reaction heat, part alkaline residue can be wrapped up on the contrary, form hard particles, hinder reaction.
5. from neutral leach liquor qualitatively, liquid phase is to pure.Owing to accompanying a large amount of alkali lye in alkaline residue, when leaching, can sodium sulfate be generated, increasing the viscosity of liquid, leaching operation in impact.
6. from system balancing, be more prone to control volumetric balance.Both can reduce the impact of alkaline residue band water, adjustable more slag washing water again, slag washing water is conducive to reclaiming the zinc in heavy alum slag and plumbous mud more, reduces and occurs that system bulk expands.
7. environmental protection and energy-saving benefit obvious.In ion exchange process, the feature of waste water is that foreign matter content is few, in acid.The Zn of water-soluble impurity mainly resin clip
2+, the Cl desorbed
-, SO
4 2-and F, wastewater treatment adopts lime flocculation neutralizing treatment technology, and the heavy metal precipitation in waste water is got off, and waste liquid is limpid, colourless, and each objectionable impurities all reduces, discharged wastewater met the national standard, realizes environmental protection and energy-conservation bumper harvests.
Accompanying drawing explanation
Fig. 1 is the ion-exchange dechlorination system of solution of zinc sulfate in wet method zinc abstraction of the present utility model.
Embodiment
The utility model is illustrated below by way of accompanying drawing.
As shown in Figure 1, disclose the ion-exchange dechlorination system of solution of zinc sulfate in a kind of wet method zinc abstraction, wherein, the zinc sulfate storage pond 1 storing solution of zinc sulfate connects ion exchange column 3 by first pump 2, strippant storage pond 4 is also connected with ion exchange column 3 by pipeline, ion exchange column 3 connects transfer pond 5 further by pipeline, transfer pond 5 is connected to electrolysis cycle pond 7 and neutralizing well 8 via second pump 6, neutralizing well 8 is connected to pressure filter 10 via the 3rd pump 9, and the filtrate outlet of pressure filter 10 is connected to settling tank 11.
Solution of zinc sulfate (new liquid) after leaching enters ion exchange column 3 by first pump 2 (ceramic pump) by 0.25-0.3 meter per second flow velocity, Cl in solution from zinc sulfate storage pond 1
-by the SO in resin
4 2-exchange and enter in resin, thus reaching the object of zinc liquid dechlorination, the solution of zinc sulfate after exchange enters transfer pond 5, sends into electrolysis cycle pond 7 by second pump 6, after electrolysis, return leaching process.Resin to reach capacity state through the absorption of 8-10 hours, and the resin that absorption is saturated, pass into strippant by 0.25-0.3 meter per second flow velocity from strippant storage pond 4, resin, after the desorb of 4-6 hours, makes the Cl of resin absorption
-ion is by SO
4 2-exchange, stripping liquid is containing Cl
-ionic concn is higher, enter transfer pond 5, neutralizing well 8 is sent into by second pump 6, neutralizing agent is added in neutralizing well 8, send in pressure filter 10 by the 3rd pump 9 after neutralization, the sludge outlet of pressure filter 10 connects sludge sump (not shown), and the filtrate outlet of pressure filter 10 connects settling tank 11, and in settling tank 11, after precipitation, waste water can qualified discharge.Resin (ion exchange column) after desorption and regeneration enters the subsequent work cycle.
Claims (3)
1. the ion-exchange dechlorination system of solution of zinc sulfate in a wet method zinc abstraction, it is characterized in that, the zinc sulfate storage pond storing solution of zinc sulfate connects ion exchange column by first pump, strippant storage pond is also connected with ion exchange column by pipeline, ion exchange column connects transfer pond further by pipeline, transfer pond is connected to electrolysis cycle pond and neutralizing well via second pump, and neutralizing well is connected to pressure filter via the 3rd pump, and the filtrate outlet of pressure filter is connected to settling tank.
2. ion-exchange dechlorination system according to claim 1, is characterized in that, neutralizing well is connected with neutralizing agent feeding device.
3. ion-exchange dechlorination system according to claim 1 and 2, is characterized in that, the sludge outlet of pressure filter connects sludge sump.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520230540.9U CN204529926U (en) | 2015-04-16 | 2015-04-16 | The ion-exchange dechlorination system of solution of zinc sulfate in wet method zinc abstraction |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520230540.9U CN204529926U (en) | 2015-04-16 | 2015-04-16 | The ion-exchange dechlorination system of solution of zinc sulfate in wet method zinc abstraction |
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|---|---|
| CN204529926U true CN204529926U (en) | 2015-08-05 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106191440A (en) * | 2016-08-22 | 2016-12-07 | 吉首大学 | A kind of remove the method for fluorion in solution of zinc sulfate |
| CN106381397A (en) * | 2016-09-27 | 2017-02-08 | 吉首市金湘资源科技开发有限公司 | Method for dechlorinating through zinc ash material ammonia-leaching ion exchange combined process |
| CN106399715A (en) * | 2016-09-27 | 2017-02-15 | 吉首市金湘资源科技开发有限公司 | Method for producing electrolytic zinc through high-chloride zinc ash material ammonia leaching ion exchange combined process |
-
2015
- 2015-04-16 CN CN201520230540.9U patent/CN204529926U/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106191440A (en) * | 2016-08-22 | 2016-12-07 | 吉首大学 | A kind of remove the method for fluorion in solution of zinc sulfate |
| CN106381397A (en) * | 2016-09-27 | 2017-02-08 | 吉首市金湘资源科技开发有限公司 | Method for dechlorinating through zinc ash material ammonia-leaching ion exchange combined process |
| CN106399715A (en) * | 2016-09-27 | 2017-02-15 | 吉首市金湘资源科技开发有限公司 | Method for producing electrolytic zinc through high-chloride zinc ash material ammonia leaching ion exchange combined process |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150805 Termination date: 20200416 |