CN103086559A - Device and method for zinc sulfate wastewater crystal separation treatment - Google Patents
Device and method for zinc sulfate wastewater crystal separation treatment Download PDFInfo
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- CN103086559A CN103086559A CN 201310059454 CN201310059454A CN103086559A CN 103086559 A CN103086559 A CN 103086559A CN 201310059454 CN201310059454 CN 201310059454 CN 201310059454 A CN201310059454 A CN 201310059454A CN 103086559 A CN103086559 A CN 103086559A
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Abstract
The invention discloses a device and a method for zinc sulfate wastewater crystal separation treatment. The method comprises the following steps of: preheating raw material, treating the liquid through flash concentration crystallization to separate out the potassium chloride, preheating the crystallized liquid, and concentrating and crystallizing the preheated liquid, separating out sodium chloride, circulating repeatedly, until separating out all the potassium chloride and sodium chloride. The method is simple in process, reliable in operation and very suitable for treatment of wastewater of zinc sulfate factory.
Description
Technical field
The present invention relates to a kind of technology for treating industrial waste water field, particularly the device and method processed of a kind of zinc sulfate waste water Crystallization Separation.
Background technology
Fast development along with China's industry, zinc sulfate production is accompanied by a large amount of trade effluents and produces, how to adopt advanced technology that trade effluent is processed, turn waste into wealth, realizing cleaner production and developing a circular economy is to put a difficult problem in front in zinc sulfate manufacturing enterprise, and the treatment process of enterprises waste water should be briefly reliable with technique simultaneously, but convenient behavior major objective, the most complex structure of zinc sulfate waste water reclaiming device that produces after the sour zinc of present existing electrolysis stream, energy consumption is high.
Summary of the invention
The device and method that the objective of the invention is to overcome the above-mentioned deficiency of prior art and provide a kind of zinc sulfate waste water Crystallization Separation to process.The method technical process is brief, and operation is convenient, is fit to the processing of zinc sulfate waste water, adopts circulation crystallization, and product extracts fully, and the process operation energy consumption is low.
technical scheme of the present invention is: a kind of method that zinc sulfate waste water Crystallization Separation is processed, raw material reclaims condensed water heat by plate-type heat exchanger and carries out preheating, feed liquid after intensification is discharged into three series connection forced circulation evaporation tanks and carries out the shwoot condensing crystal, control simultaneously feed temperature at 20～50 degree, isolate Repone K by whizzer, end effect secondary steam is formed vacuum by the vacuum system condensation simultaneously, after feed liquid after crystallization absorbs the secondary steam intensification by plate type preheater, again be discharged into another forced circulation evaporation tank and carry out condensing crystal, control simultaneously feed temperature at 90～120 degree, isolate sodium-chlor by whizzer, move in circles with this, until the whole Crystallization Separation of sodium-chlor and Repone K.
At different temperature, separate out at different temperature province intercrystallines respectively and obtain highly purified Repone K and sodium-chlor by the principle of different solubility by sodium-chlor and Repone K for the method.
the device that a kind of zinc sulfate waste water Crystallization Separation is processed, it comprises the first plate-type heat exchanger, head tank, the first forced circulation evaporation tank, the second forced circulation evaporation tank, the 3rd forces circulation evaporator, top four's circulation evaporator processed, the second plate-type heat exchanger, the first separating centrifuge, the Repone K tank, vacuum system, the second separating centrifuge, the sodium-chlor tank, steam system, head tank connects the second plate-type heat exchanger by pipeline, the second plate-type heat exchanger connects the second forced circulation evaporation tank by pipeline, the second forced circulation evaporation tank connects the 3rd by pipeline forces circulation evaporator, the 3rd forces circulation evaporator to connect top four's circulation evaporator processed by pipeline, one end of top four's circulation evaporator processed is connected with vacuum system by pipeline, top four's circulation evaporator processed connects the first separating centrifuge by pipeline, the first separating centrifuge connects the Repone K tank, the first separating centrifuge connects the first plate-type heat exchanger by pipeline, the first separating centrifuge connects the first forced circulation evaporation tank by pipeline, the first separating centrifuge connects steam system by pipeline, the first separating centrifuge connects the second separating centrifuge by pipeline, the second separating centrifuge connects top four's circulation evaporator processed by pipeline, the second separating centrifuge connects the sodium-chlor tank.
The present invention compared with prior art has following features: present device is simple, and technique is brief, by circulation technology, can obtain highly purified sodium-chlor and Repone K simultaneously, and the zinc sulfate waste water energy is effectively addressed, and realizes cleaner production
Below in conjunction with the drawings and specific embodiments, detailed construction of the present invention is further described.
Description of drawings
Accompanying drawing 1 is structural representation of the present invention;
Embodiment
shown in accompanying drawing: the device that a kind of zinc sulfate waste water Crystallization Separation is processed, it comprises the first plate-type heat exchanger 1, head tank 2, the first forced circulation evaporation tank 301, the second forced circulation evaporation tank 302, the 3rd forces circulation evaporator 303, top four's circulation evaporator 304 processed, the second plate-type heat exchanger 4, the first separating centrifuge 5, Repone K tank 6, vacuum system 7, the second separating centrifuge 8, sodium-chlor tank 9, steam system 10, head tank 2 connects the second plate-type heat exchanger 4 by pipeline, the second plate-type heat exchanger 4 connects the second forced circulation evaporation tank 302 by pipeline, the second forced circulation evaporation tank 302 connects the 3rd by pipeline forces circulation evaporator 303, the 3rd forces circulation evaporator 303 to connect top four's circulation evaporator 304 processed by pipeline, one end of top four's circulation evaporator 304 processed is connected with vacuum system 7 by pipeline, top four's circulation evaporator 304 processed connects the first separating centrifuge 5 by pipeline, the first separating centrifuge 5 connects Repone K tank 6, the first separating centrifuge 5 connects the first plate-type heat exchanger 1 by pipeline, the first separating centrifuge 5 connects the first forced circulation evaporation tank 301 by pipeline, the first separating centrifuge 5 connects steam system 10 by pipeline, the first separating centrifuge 5 connects the second separating centrifuge 8 by pipeline, the second separating centrifuge 8 connects top four's circulation evaporator 304 processed by pipeline, the second separating centrifuge 8 connects sodium-chlor tank 9.
Shown in accompanying drawing 1: a kind of method that zinc sulfate waste water Crystallization Separation is processed, the trade effluent that contains sodium-chlor and Repone K process flow sheet of Crystallization Separation sodium-chlor and Repone K respectively in the differing temps zone, realize by quadruple effect evaporation energy-saving Technology and equipment, the energy-efficient equipment of quadruple effect comprises the compositions such as plate type preheater, pump feed evaporator, whizzer, vacuum cooling system, realizes continuous production requirement.
embodiment 1: pretreated zinc sulfate waste water carries out by plate-type heat exchanger and water of condensation the heat that water of condensation is reclaimed in heat exchange, improve the temperature of advancing tank raw material waste water, effectively reduce the consumption of steam, raw material waste water after intensification joins the second forced circulation evaporation tank 302, control feed temperature at 90 degree, be discharged to the 3rd after evaporation concentration and force circulation evaporator 303, control feed temperature at 70 degree, be discharged to top four's circulation evaporator 304 processed after evaporation concentration, control feed temperature at 50 degree, this moment, Repone K was along with the reduction of temperature is separated out, the mother liquor of separating out Repone K is discharged to the first forced circulation evaporation tank 301, control feed temperature at 120 degree by steam heating, the evaporating, concentrating and crystallizing precipitated sodium chloride, the mother liquor of precipitated sodium chloride is discharged the first forced circulation evaporation tank 301 to top four's circulation evaporator 304 concentrated Repone K of separating out of shwoot cooling processed, move in circles with this and realize the Crystallizing process of sodium-chlor and Repone K, obtain highly purified sodium-chlor and Repone K.
embodiment 2: pretreated zinc sulfate waste water carries out by plate-type heat exchanger and water of condensation the heat that water of condensation is reclaimed in heat exchange, improve the temperature of advancing tank raw material waste water, effectively reduce the consumption of steam, raw material waste water after intensification joins the second forced circulation evaporation tank 302, control feed temperature at 60 degree, be discharged to the 3rd after evaporation concentration and force circulation evaporator 303, control feed temperature at 40 degree, be discharged to top four's circulation evaporator 304 processed after evaporation concentration, control feed temperature at 20 degree, this moment, Repone K was along with the reduction of temperature is separated out, the mother liquor of separating out Repone K is discharged to the first forced circulation evaporation tank 301, control feed temperature at 90 degree by steam heating, the evaporating, concentrating and crystallizing precipitated sodium chloride, the mother liquor of precipitated sodium chloride is discharged the first forced circulation evaporation tank 301 to top four's circulation evaporator 304 concentrated Repone K of separating out of shwoot cooling processed, move in circles with this and realize the Crystallizing process of sodium-chlor and Repone K, obtain highly purified sodium-chlor and Repone K.
Principle of work of the present invention and using method are: the curve that sodium-chlor and Klorvess Liquid solubility with temperature change, increase sodium-chlor solubleness decline along with temperature, the increase of Repone K solubleness is larger, and along with the decline of temperature, sodium-chlor solubleness increases, Repone K solubleness descends larger, according to this characteristic, when raw materials evaporate is concentrated to Repone K and reaches 24.4%, this moment the sodium-chlor crystallization, then discharge mother liquor shwoot cooling when being concentrated to sodium-chlor and reaching 18.68%, this moment, Repone K was separated out.Discharge Recycling Mother Solution and carry out the condensing crystal precipitated sodium chloride to high temperature section, Repone K solubleness reaches new saturated discharge shwoot cooling condensing crystal and separates out Repone K, moves in circles and completes the Crystallization Separation of Repone K and sodium-chlor.
Claims (5)
1. the method processed of a zinc sulfate waste water Crystallization Separation is characterized in that: comprise following steps,
(1) raw material carries out the step of preheating;
(2) feed liquid is carried out the step that the shwoot condensing crystal is isolated Repone K;
(3) carry out the step that condensing crystal is isolated sodium-chlor after the feed liquid preheating after crystallization;
Repeat (2)-(3), until the whole Crystallization Separation of Repone K and sodium-chlor.
2. the method processed of a kind of zinc sulfate waste water Crystallization Separation according to claim 1 is characterized in that: the step that described condensing crystal is isolated sodium-chlor is to complete in feed temperature is the scopes of 90～120 degree.
3. the method for a kind of zinc sulfate waste water Crystallization Separation processing according to claim 1 and 2, is characterized in that, the step that described shwoot condensing crystal is isolated Repone K is to complete in feed temperature is 20～50 scopes of spending.
4. the corresponding device of method processed of a zinc sulfate waste water Crystallization Separation, it is characterized in that: it comprises, feed liquid after raw material or crystallization is carried out the plate-type heat exchanger of pre-recovery of heat heat, isolate the separating centrifuge of Repone K or sodium-chlor, feed liquid is carried out three series connection forced circulation evaporation tanks that the shwoot condensing crystal is isolated the continuous process of Repone K, feed liquid after crystallization is carried out the plate-type heat exchanger of preheating, and the feed liquid after crystallization is carried out the vacuum system that condensing crystal is isolated another forced circulation evaporation tank of sodium-chlor and the end effect secondary steam condensation formed vacuum.
5. the corresponding device of method processed of a kind of zinc sulfate waste water Crystallization Separation according to claim 4, it is characterized in that: it comprises, the first plate-type heat exchanger, head tank, the first forced circulation evaporation tank, the second forced circulation evaporation tank, the 3rd forces circulation evaporator, top four's circulation evaporator processed, the second plate-type heat exchanger, the first separating centrifuge, the Repone K tank, vacuum system, the second separating centrifuge, the sodium-chlor tank, steam system, head tank connects the second plate-type heat exchanger by pipeline, the second plate-type heat exchanger connects the second forced circulation evaporation tank by pipeline, the second forced circulation evaporation tank connects the 3rd by pipeline forces circulation evaporator, the 3rd forces circulation evaporator to connect top four's circulation evaporator processed by pipeline, one end of top four's circulation evaporator processed is connected with vacuum system by pipeline, top four's circulation evaporator processed connects the first separating centrifuge by pipeline, the first separating centrifuge connects the Repone K tank, the first separating centrifuge connects the first plate-type heat exchanger by pipeline, the first separating centrifuge connects the first forced circulation evaporation tank by pipeline, the first separating centrifuge connects steam system by pipeline, the first separating centrifuge connects the second separating centrifuge by pipeline, the second separating centrifuge connects top four's circulation evaporator processed by pipeline, the second separating centrifuge connects the sodium-chlor tank.
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| CN 201310059454 CN103086559A (en) | 2013-02-26 | 2013-02-26 | Device and method for zinc sulfate wastewater crystal separation treatment |
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| CN 201310059454 CN103086559A (en) | 2013-02-26 | 2013-02-26 | Device and method for zinc sulfate wastewater crystal separation treatment |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103601331A (en) * | 2013-11-27 | 2014-02-26 | 京博农化科技股份有限公司 | Treatment process of agrochemical high-concentration salt-containing wastewater |
| CN107381598A (en) * | 2017-06-09 | 2017-11-24 | 石家庄新奥环保科技有限公司 | A kind of retracting device and method |
| CN107416865A (en) * | 2017-08-25 | 2017-12-01 | 衡阳旭光锌锗科技有限公司 | Sewage treatment potassium, sodium device |
| CN109179540A (en) * | 2018-10-25 | 2019-01-11 | 中国轻工业长沙工程有限公司 | Brine waste MVR salt potassium sub-prime crystallization processes |
| CN110182831A (en) * | 2019-05-28 | 2019-08-30 | 昌鑫生态科技(陕西)有限公司 | The technology of salt lake extraction lithium carbonate |
| CN111908533A (en) * | 2020-06-26 | 2020-11-10 | 中国轻工业长沙工程有限公司 | Treatment process of high-concentration high-salt mother liquor in zero discharge of wastewater |
-
2013
- 2013-02-26 CN CN 201310059454 patent/CN103086559A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103601331A (en) * | 2013-11-27 | 2014-02-26 | 京博农化科技股份有限公司 | Treatment process of agrochemical high-concentration salt-containing wastewater |
| CN103601331B (en) * | 2013-11-27 | 2014-08-20 | 京博农化科技股份有限公司 | Treatment process of agrochemical high-concentration salt-containing wastewater |
| CN107381598A (en) * | 2017-06-09 | 2017-11-24 | 石家庄新奥环保科技有限公司 | A kind of retracting device and method |
| CN107381598B (en) * | 2017-06-09 | 2023-08-08 | 石家庄新奥环保科技有限公司 | Recovery device and recovery method |
| CN107416865A (en) * | 2017-08-25 | 2017-12-01 | 衡阳旭光锌锗科技有限公司 | Sewage treatment potassium, sodium device |
| CN109179540A (en) * | 2018-10-25 | 2019-01-11 | 中国轻工业长沙工程有限公司 | Brine waste MVR salt potassium sub-prime crystallization processes |
| CN110182831A (en) * | 2019-05-28 | 2019-08-30 | 昌鑫生态科技(陕西)有限公司 | The technology of salt lake extraction lithium carbonate |
| CN111908533A (en) * | 2020-06-26 | 2020-11-10 | 中国轻工业长沙工程有限公司 | Treatment process of high-concentration high-salt mother liquor in zero discharge of wastewater |
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Application publication date: 20130508 |