CN203715400U - Low-concentration lead-containing wastewater treatment equipment - Google Patents
Low-concentration lead-containing wastewater treatment equipment Download PDFInfo
- Publication number
- CN203715400U CN203715400U CN201320540087.2U CN201320540087U CN203715400U CN 203715400 U CN203715400 U CN 203715400U CN 201320540087 U CN201320540087 U CN 201320540087U CN 203715400 U CN203715400 U CN 203715400U
- Authority
- CN
- China
- Prior art keywords
- ion exchange
- lead
- waste water
- regenerated liquid
- ion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
The utility model relates to low-concentration lead-containing wastewater treatment equipment for treating lead-containing wastewater with the lead concentration less than 10mg/L. The equipment comprises a first ion exchange device, a second ion exchange device and a first chemical depositing tank, wherein the lead-containing wastewater is input to the first ion exchange device, the ion exchange is performed on the lead-containing wastewater under the acidic condition that the pH value is less than 3 to enable the lead concentration of the lead-containing wastewater to be not more than 0.1mg/L, acid liquid is input to the first ion exchange device to regenerate saturated ion exchange resin to obtain regenerated liquid, and the ion exchange resin is strong acid styrene cation exchange resin; the regenerated liquid is input to the second ion exchange device, the ion exchange is performed on the regenerated liquid, and the ion exchange resin with the selective adsorption performance is filled in the second ion exchange device to selectively adsorb impurity metal ions except for lead in the regenerated liquid; the regenerated liquid is input to the first chemical depositing tank, and the pH value of the regenerated liquid is adjusted to enable lead in the regenerated liquid to be fully deposited to obtain pure lead-containing sludge.
Description
Technical field
The utility model relates to wastewater processing technology, especially relates to the treatment facility of lower concentration lead waste water.
Background technology
Lead is used extensively in modern industrial and agricultural production, in industries such as store battery, paint, printing, pigment, all needs to use lead element.Lead is again a kind of environmental pollutant wide, that have the property accumulated that distribute, and a large amount of discharges of lead waste water will directly cause the pollution of soil, atmosphere and water body.Along with the lifting of Chinese environmental protection standard and law enforcement dynamics, the lead concentration in lead waste water need to be reduced to the concentration of the 0.1mg/L of discharge permission.
Now widely used is that treatment process is that the precipitator method are removed the lead in water, and this can be divided into physical sedimentation and chemical precipitation again.Physical sedimentation is to dosing coagulant or heavy metal chelating agent in lead waste water, form with waste water in the colloid of the similar electric charge of gritty particle band, by gravity settling, give separation.Chemical precipitation has hydroxide precipitation method, sulphide precipitation and carbonate precipitation method, by adding lime, caustic soda, sulphide salt, soda ash and phosphoric acid salt etc., lead is precipitated, and wherein hydroxide precipitation method application is more.In theory, when lead waste water pH value is adjusted to 9.2-9.5, processes lead tolerance concentration in draining and can be reduced to 0.01-0.03mg/L.But due to complicated components in waste water, lead some organism often and in waste water forms complex compound, and chemical precipitation method cannot be reduced to Pb In Exhausted Water concentration below the 0.1mg/L of current national Specification effectively.And the process of plumbous precipitation is used a large amount of soda acids, waste water salinity raises, and is unfavorable for the water reuse after processing.In addition, chemical precipitation together precipitates the metal ion in water, and leaded chemical sludge belongs to dangerous solid waste, and unprocessed meeting causes secondary pollution to environment, and human body and animals and plants are caused to toxic action.But then, leaded mud the purify a large amount of ammoniacal liquor of plumbous process need or the vitriol oil, complex process, economic worth is not high.
Another kind of common method is absorption method, utilize specific surface area is large, micro content is abundant porous adsorbate as wilkinite, zeolite, gac even active sludge etc. waste water is carried out to adsorption treatment.The absorption utilization ratio of the method deleading efficiency and adsorbate is inversely proportional to, and good deleading efficiency can reduce the utilization ratio of adsorbate.Under good deleading efficiency, although waste water can be purified preferably, the adsorbate of Adsorption of Lead needs appropriate disposal, prevents the lead generation desorption of absorption, causes secondary pollution.On the whole, although absorption method is removed lead from waste water, can not make lead resource utilization, can not make the plumbous form that changes, be a kind of method that makes pollution transportation.
Ion exchange method be utilize ion-exchanger self entrained move freely ion and treatment soln intermediate ion exchanges to realize, the power that promotes ion-exchange is function base on interionic concentration difference and the exchanger affinity to ion.At present, by ion exchange method, remove plumbous Engineering Projects and scientific research is all rare, reason is that most of ion exchange resin only has good absorption property to the lead in certain concentration range, the lead concentration of the water outlet 0.1mg/L of regulation that all cannot be up to state standards when the higher and concentration of concentration is lower.Calcium ions and magnesium ions in waste water and other impurity metal ions also can be by resin absorption, affect resin and plumbous exchange capacity, and application is improperly difficult to make plumbously in water obtain good removal.In addition, the lead solution after exhausted resin regeneration still needs again to process, so the application of ion exchange resin has been subject to certain restriction.
Electrolytic process refers to the ultimate principle of application electrolysis, makes Pb In Exhausted Water ion oxidation and reduction reaction occur respectively on sun-cloudy the two poles of the earth and enrichment by electrolytic process.Electrolytic process is the method for wastewater treatment that redox, decomposition, precipitation combine.Plumbous electrolysis is most commonly used to refining of lead bullion lead bullion, method technical maturity, and occupation area of equipment is little, can reclaim pure metal.But plumbous electrolysis is low to the Faradaic current efficiency of lead waste water, and current consumption is large, and wastewater treatment capacity is little.
Electrodialytic technique is a traditional water technology, the desalting performance that electrodialysis appts is good is sloughed the most salinities in lead waste water, make can become and be back to use the pure water that complex acid technique is used after wastewater treatment, although the method can reach the object of processing lead waste water and water reuse, but technical process is complicated, complex steps, certainly will cause floor space large, the problems such as complex management.
Utility model content
Technical problem to be solved in the utility model is to provide a kind for the treatment of facility of lower concentration lead waste water, can, under lower cost and less floor space, realize plumbous recovery.
The utility model is to solve the problems of the technologies described above the treatment facility that the technical scheme adopting is a kind of lower concentration lead waste water of proposition, lead waste water for the treatment of lead concentration lower than 10mg/L, this equipment comprises: the first ion exchange unit, input this lead waste water, and in pH value, be less than under 3 acidic conditions this lead waste water is carried out to ion-exchange, make the lead concentration in this lead waste water be less than or equal to 0.1mg/L, and this first ion exchange unit input acid solution is regenerated to saturated ion exchange resin, obtain regenerated liquid, wherein this ion exchange resin is superacicd styrene cation exchange resin, the second ion exchange unit, inputs this regenerated liquid, and this regenerated liquid is carried out to ion-exchange, and in this second ion exchange unit, the ion exchange resin of the selective absorption property of filling agent is with the foreign metal ion beyond deleading in this regenerated liquid of selective adsorption, and the first chemical precipitation groove, input this regenerated liquid, regulate the pH value of this regenerated liquid to the lead in regenerated liquid is precipitated completely, obtain pure leaded mud.
In an embodiment of the present utility model, treatment facility also comprises pH regulator pond, before being connected to this first ion exchange unit, the pH value of this lead waste water is adjusted to 3 left and right.
In an embodiment of the present utility model, treatment facility also comprises reverse osmosis unit, after being connected to the first ion exchange unit, the lead waste water through ion-exchange is carried out to reverse-osmosis treated, obtains reuse water.
In an embodiment of the present utility model, this reverse osmosis unit also by the concentrate recirculation of reverse-osmosis treated to this first ion exchange unit, carry out ion-exchange together with this lead waste water.
In an embodiment of the present utility model, this first chemical precipitation groove is also back to this first ion exchange unit by the regenerated liquid of removing plumbous precipitation, carries out ion-exchange together with this lead waste water.
Compare with existing ion exchange technique, the utility model is optimized by the selection of resin, lead concentration in water outlet can be reduced to below 0.1mg/L.In addition, existing ion exchange technique often adopts slightly acidic to neutral water inlet, easily there is precipitation and deposition pollution resin in resin column in impurity, and regulate in pH value process and use a large amount of soda acids, be unfavorable for the recycling of waste water, the utility model is intake under acidic conditions, has avoided pH value to regulate, save the cost of soda acid medicament, avoided the pollution of resin simultaneously.
Accompanying drawing explanation
For above-mentioned purpose of the present utility model, feature and advantage can be become apparent, below in conjunction with accompanying drawing, embodiment of the present utility model is elaborated, wherein:
Fig. 1 illustrates the structure iron for the treatment of facility of the lead waste water of the utility model one embodiment.
Fig. 2 illustrates the processing flow chart of the lead waste water of the utility model one embodiment.
Embodiment
Embodiment of the present utility model will describe the treatment facility of lead waste water, and this technology is based on ion exchange method.Although exist, once investment is large, the difficult shortcoming of regenerating, and ion exchange method has been one of best approach of processing the various trade effluents that the water yield is large, concentration is low.Success of ion exchange method is for the treatment of various heavy metal-containing waste waters such as nickel-containing waste water, chromate waste waters.
Although ion exchange method also can be adsorbed for lead, the present situation of this technical study is shown, various types of ion exchange resin, for example strong acid, weak acid and resin only have good absorption property to the lead in certain concentration range.When the higher and concentration of concentration is lower, the water outlet lead concentration of ion exchange method all cannot reach the 0.1mg/L of GB regulation.By ion exchange method and other Combination of Methods, further to remove lead, the 0.1mg/L that makes its concentration reach GB regulation is no doubt feasible method, but this makes technique more complicated after all.
Embodiment expectation of the present utility model improves ion exchange method, makes it directly the lead content of lead waste water to be reduced to the 0.1mg/L of GB regulation.
Fig. 1 illustrates the structure iron of the lead waste water recovery system of the utility model one embodiment.Shown in figure 1, lead waste water recovery system 100 mainly comprises wastewater equalization pond 101, pH regulator pond 102, the sour storage tank 104 of the first ion exchange unit 103, first, the sour storage tank 106 of intermediate pool 105, second, back flushing pond 107, reverse osmosis unit 108, the second ion exchange unit 109, reuse water chemical precipitation groove 110 and lead waste water chemical precipitation groove 111.Wastewater equalization pond 101, pH regulator pond 102, the first ion exchange unit 103 are for connecting successively.The first sour storage tank 104 connects the input terminus of the first ion exchange unit 103 by the pipeline that contains pump 112.PH regulator pond 102 connects the input terminus of the first ion exchange unit 103 by the pipeline that contains pump 113.
The first ion exchange unit 103 comprises regenerated liquid output terminal and waste water output terminal.Waste water output terminal connects intermediate pool 105, the rear connection reverse osmosis unit 108 of intermediate pool 105.Regenerated liquid output terminal connects back flushing pond 107, rear connection the second ion exchange unit 109 in back flushing pond 107.Reverse osmosis unit 108 comprises dense water output terminal and reuse water output terminal, and wherein dense water output terminal connects the input terminus of the first ion exchange unit 103.The second sour storage tank 106 connects the input terminus of the second ion exchange unit 109 by the pipeline that contains pump 114.Back flushing pond 107 connects the input terminus of the second ion exchange unit 109 by the pipeline that contains pump 115.The second ion exchange unit 109 comprises regenerated liquid output terminal and waste water output terminal.Waste water output terminal connects lead waste water chemical precipitation groove 111, and regenerated liquid output terminal connects reuse water chemical precipitation groove 110.Lead waste water chemical precipitation groove 111 is connected the input terminus of wastewater equalization pond 101 with the output terminal of reuse water chemical precipitation groove 110.
Wastewater equalization pond 101 can store pending waste water, and flows to pH regulator pond 102.In pH regulator pond 102, can add acid for adjusting pH value to strongly-acid, to meet the required condition of ion-exchange.
The first ion exchange unit 103 can be inputted lead waste water, and under strong acidic condition, lead waste water is carried out to ion-exchange.
As previously mentioned, most of ion exchange resin only has good absorption property to the lead in certain concentration range, and when in concentration, higher and concentration is lower, the water outlet lead concentration of ion exchange method all cannot reach the 0.1mg/L of GB regulation.Yet the application's utility model people finds after various ion exchange resin is screened, for the lead waste water of lower concentration (lead concentration is lower than 10mg/L), under specific pH value condition, part ion exchange resin shows good absorption property, the lead concentration in lead waste water can be dropped to the degree that is less than or equal to 0.1mg/L.
For example, experimental results show that, when water inlet lead concentration 5.92mg/L, select strongly acidic styrene type cation exchange resin, and keep the strong acidic condition of pH value < 3, when resin volume is 25ml, filter after 10L, in water outlet, lead concentration is 0.05mg/L, is less than the national standard of 0.1mg/L.
Therefore in the present embodiment, the first ion exchange unit 103 is filled strongly acidic styrene type cation exchange resin, in pH value, be less than under 3 strong acidic condition, lead concentration is carried out to ion-exchange lower than the lead waste water of 10mg/L, make the lead concentration in lead waste water be less than or equal to 0.1mg/L.
The added advantage of carrying out ion-exchange under strong acidic condition is without adding alkali lye, to regulate waste water to neutral, so can reduce the saltiness in the aqueous solution.
After ion exchange resin is saturated, the first ion exchange unit 103 can be regenerated to saturated ion exchange resin from the first sour storage tank 104 input acid solutions by pump 112, obtains regenerated liquid.Regenerated liquid enters back flushing pond 107.Resin after regeneration can repeat to utilize after cleaning.
Wastewater collection after ion-exchange is in intermediate pool 105, and the lead concentration in these waste water has been less than or equal to 0.1mg/L, and therefore only need by existing purifying method, remove all the other impurity again gets final product reuse.For example, can use reverse osmosis unit 108 to be further processed, the specific conductivity of generation is less than the reuse water of 50 μ s/cm, and direct reuse is in production.Preferably, the dense water of reverse osmosis unit 108 can be back to the first ion exchange unit 103 and processes.
On the other hand, the regenerated liquid that enters back flushing pond 107 is generally the mixing solutions of impurity such as containing lead, iron, calcium, magnesium.Under both of these case, can use different flow processing.Conventionally, regenerated liquid carries out impurity separation by pump 115 injection the second ion exchange units 109.The second ion exchange unit 109 can the selective adsorbing ion exchange resin of filling agent, to adsorb the foreign metal ion beyond deleading.
For example, lead acid cell factory water of productive use is the pure water that after reverse-osmosis treated, specific conductivity is less than 10 μ S/cm, and calcium in waste water, magnesium ion content are lower, and principal pollutant are iron ion.Under hydrochloric acid system, the solution of iron content, lead is through having after the ion exchange resin of selective adsorption effect, and in water, iron concentration can be reduced to below 1mg/L.
Regenerated liquid (being the regenerated liquid of the first ion exchange unit 103) after ion-exchange purifies is lead waste water, and it flows into lead waste water chemical precipitation groove 111.In lead waste water chemical precipitation groove 111, can to regulate pH value complete to Pb In Exhausted Water precipitation, obtain pure leaded mud by adding such as alkali lye such as NaOH, can directly recycle.
Preferably, the supernatant liquor of lead waste water chemical precipitation groove 111 can be used as return of waste water to wastewater equalization pond 101 further to process.
After the absorption of ion exchange resin in the second ion exchange unit 109 is saturated, the acid solution that can draw in the second sour storage tanks 106 by pump 114 be regenerated, and reuse water is the solution that contains foreign metal ion, and it enters reuse water chemical precipitation groove 110.
At reuse water chemical precipitation groove 110, through overregulate pH and precipitation after, throw out is transported outward as waste, supernatant liquor can be used as return of waste water to wastewater equalization pond 101 further to process.
In some cases, the metal ion in regenerated liquid may only have lead, and does not comprise the foreign metal ions such as iron, calcium, magnesium.Now, can control by walking around pipeline and the valve of the second ion exchange unit 109, make regenerated liquid directly enter lead waste water chemical precipitation groove 111 and precipitate.Or the second ion exchange unit 109 can directly be omitted.
Fig. 2 illustrates the processing flow chart of the lead waste water of the utility model one embodiment.Shown in Fig. 2, to conclude, the treatment scheme of the lead waste water of the utility model one embodiment, comprises the following steps:
Step 201, is less than in pH value under 3 acidic conditions lead waste water is carried out to ion-exchange, makes the lead concentration in lead waste water be less than or equal to 0.1mg/L, and wherein ion exchange resin is superacicd styrene cation exchange resin;
Step 202, regenerates to ion exchange resin, obtains regenerated liquid;
Step 204, if contain the foreign metal ion beyond deleading in regenerated liquid, under pH value is less than 3 acidic conditions, regenerated liquid is carried out to ion-exchange, use the ion exchange resin selective adsorption foreign metal ion with selective adsorption performance, then enter step 205; If do not contain the foreign metal ion beyond deleading in regenerated liquid, directly enter step 205;
Step 205, regulates the pH value of regenerated liquid to the lead in regenerated liquid is precipitated completely, obtains pure leaded mud.
Before step 201, also can comprise optional step 200, the pH value of lead waste water is adjusted to 3 left and right.
After step 201, also can comprise optional step 203, the lead waste water after ion-exchange is carried out to reverse-osmosis treated, obtain pure water.
In step 203, can comprise the concentrate recirculation of reverse-osmosis treated, carry out ion-exchange together with lead waste water.
In step 205, can comprise the regenerated liquid of removing plumbous precipitation is refluxed, carry out ion-exchange together with lead waste water.
Compare with existing ion exchange technique, embodiment of the present utility model optimizes by the selection of resin, lead concentration in water outlet can be reduced to below 0.1mg/L.In addition, existing ion exchange technique often adopts slightly acidic to neutral water inlet, easily there is precipitation and deposition pollution resin in resin column in impurity, and regulate in pH value process and use a large amount of soda acids, be unfavorable for the recycling of waste water, embodiment of the present utility model is intake under acidic conditions, has avoided pH value to regulate, save the cost of soda acid medicament, avoided the pollution of resin simultaneously.
Compare with existing chemical precipitation method, embodiment of the present utility model can well precipitate without adding iron ion coagulating agent, and the plumbous mud of generation can directly be recycled, and omits sludge disposal link.And, by ion exchange resin, to plumbous inrichment, greatly reduce the water yield of settling step, dwindle the size of settling tank to 1/10th of original size, save floor space and one-time investment.
In addition, compare with existing absorption method, embodiment of the present utility model has the advantage that can directly recycle plumbous mud.Compare with existing electrolytic process, embodiment of the present utility model has the advantage that wastewater treatment capacity is large.Compare with existing electroosmose process, embodiment of the present utility model has the advantage that technique is simple, floor space is little.
Although the utility model is described with reference to current specific embodiment, but those of ordinary skill in the art will be appreciated that, above embodiment is only for the utility model is described, in the situation that not departing from the utility model spirit, also can make variation or the replacement of various equivalences, therefore, as long as the variation of above-described embodiment, modification all will be dropped in the application's the scope of claims within the scope of connotation of the present utility model.
Claims (5)
1. a treatment facility for lower concentration lead waste water, the lead waste water for the treatment of lead concentration lower than 10mg/L, is characterized in that this equipment comprises:
The first ion exchange unit, inputs this lead waste water and carries out ion-exchange, and inputs acid solution saturated ion exchange resin is regenerated, and wherein this ion exchange resin is superacicd styrene cation exchange resin;
The second ion exchange unit, inputs this regenerated liquid and carries out ion-exchange, the ion exchange resin of the selective adsorption performance of the foreign metal ion beyond deleading in this regenerated liquid of the selective absorption of filling agent in this second ion exchange unit; And
The first chemical precipitation groove, inputs this regenerated liquid and precipitates, and obtains pure leaded mud.
2. the treatment facility of lower concentration lead waste water as claimed in claim 1, is characterized in that, also comprises pH regulator pond, before being connected to this first ion exchange unit.
3. the treatment facility of lower concentration lead waste water as claimed in claim 1, is characterized in that, also comprises reverse osmosis unit, after being connected to the first ion exchange unit.
4. the treatment facility of lower concentration lead waste water as claimed in claim 3, is characterized in that, this reverse osmosis unit also by the concentrate recirculation of reverse-osmosis treated to this first ion exchange unit.
5. the treatment facility of lower concentration lead waste water as claimed in claim 1, is characterized in that, this first chemical precipitation groove is also back to this first ion exchange unit by the regenerated liquid of removing plumbous precipitation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320540087.2U CN203715400U (en) | 2013-08-30 | 2013-08-30 | Low-concentration lead-containing wastewater treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320540087.2U CN203715400U (en) | 2013-08-30 | 2013-08-30 | Low-concentration lead-containing wastewater treatment equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203715400U true CN203715400U (en) | 2014-07-16 |
Family
ID=51154568
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320540087.2U Expired - Fee Related CN203715400U (en) | 2013-08-30 | 2013-08-30 | Low-concentration lead-containing wastewater treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203715400U (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107651783A (en) * | 2017-11-07 | 2018-02-02 | 长沙埃比林环保科技有限公司 | A kind of method of ion-exchange treatment lead waste water |
| CN107754389A (en) * | 2016-08-22 | 2018-03-06 | 江苏三环实业股份有限公司 | A kind of new lead plaster recycle device |
| CN110372125A (en) * | 2019-07-24 | 2019-10-25 | 无锡市道格环保科技有限公司 | Difficult removal metal ion Integrated Processing Unit in a kind of waste water |
| CN111908652A (en) * | 2020-07-07 | 2020-11-10 | 上海盛通时代印刷有限公司 | Waste water treatment system in printing technology |
| CN112408633A (en) * | 2020-11-06 | 2021-02-26 | 江苏海普功能材料有限公司 | Method for recycling lead-containing waste acid by adsorption method |
-
2013
- 2013-08-30 CN CN201320540087.2U patent/CN203715400U/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107754389A (en) * | 2016-08-22 | 2018-03-06 | 江苏三环实业股份有限公司 | A kind of new lead plaster recycle device |
| CN107651783A (en) * | 2017-11-07 | 2018-02-02 | 长沙埃比林环保科技有限公司 | A kind of method of ion-exchange treatment lead waste water |
| CN110372125A (en) * | 2019-07-24 | 2019-10-25 | 无锡市道格环保科技有限公司 | Difficult removal metal ion Integrated Processing Unit in a kind of waste water |
| CN111908652A (en) * | 2020-07-07 | 2020-11-10 | 上海盛通时代印刷有限公司 | Waste water treatment system in printing technology |
| CN112408633A (en) * | 2020-11-06 | 2021-02-26 | 江苏海普功能材料有限公司 | Method for recycling lead-containing waste acid by adsorption method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102603097B (en) | Advanced treatment and recycling process for wastewater containing heavy metal ions | |
| CN203715400U (en) | Low-concentration lead-containing wastewater treatment equipment | |
| CN103553249B (en) | In electroplating effluent, acid is separated and heavy metal collection method | |
| CN104445095A (en) | Method for purifying smelting waste acid | |
| CN110282783B (en) | Ammonium phosphate chemical wastewater treatment system and method | |
| CN103011347B (en) | Method for carrying out electrolytic treatment on copper-containing electroplating wastewater and recycling copper | |
| CN101234827A (en) | Treatment and resource reclaiming method for chromium-containing wastewater containing high concentration sodium sulfate | |
| CN104129831A (en) | Method for simultaneous removal and recovery of heavy metal ions and organic acid by using chelating resin | |
| CN109626672A (en) | Based on nitrate nitrogen method in electrochemistry and resin combination technique advanced treatment of waste water | |
| CN105565533A (en) | Zero-discharge on-line treatment process for preparing deionized water from copper sulphate electroplating waste water | |
| CN107176726A (en) | Desulphurization for Coal-fired Power Plant waste water integrates defluorination method | |
| CN104817213A (en) | Heavy metal wastewater treatment process in electroplating and special device thereof | |
| CN103408102A (en) | Ion exchange resin regeneration method reducing desorbed liquid | |
| CN104291498B (en) | A kind for the treatment of process of chemical nickel plating waste solution containing nitric acid and the treatment system of correspondence | |
| CN103936189A (en) | Processing method for recovery processing of high ammonia nitrogen wastewater | |
| CN103449623A (en) | Method for preparing metal nanometer material by recovering from industrial waste water | |
| CN103274560B (en) | Heavy metal wastewater thereby technique of zero discharge | |
| CN104005050A (en) | Method for treating and recycling divalent manganese in electrolytic manganese wastewater | |
| CN103043834A (en) | Rear earth smelting wastewater treatment process | |
| CN104310659A (en) | Separating reclaiming technology for humic acid in garbage leachate MBR+NF concentrated liquid containing high concentration of SO42 | |
| CN104418446B (en) | The processing method of low concentration lead waste water and equipment | |
| CN203269712U (en) | Zero discharge treatment device for heavy metal wastewater | |
| CN215906017U (en) | Silver cyanide wastewater treatment system | |
| CN104973710A (en) | Method of treating high-concentration arsenic and cadmium in acidic waste water with granular titanium dioxide | |
| CN105565532A (en) | Zero-discharge on-line treatment process for preparing deionized water from copper sulphate electroplating wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140716 Termination date: 20160830 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |