CN110194545A - Nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process in a kind of waste water - Google Patents
Nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process in a kind of waste water Download PDFInfo
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- CN110194545A CN110194545A CN201910557814.8A CN201910557814A CN110194545A CN 110194545 A CN110194545 A CN 110194545A CN 201910557814 A CN201910557814 A CN 201910557814A CN 110194545 A CN110194545 A CN 110194545A
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/20—Heavy metals or heavy metal compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
Abstract
The present invention relates to a kind of nickel-containing wastewater, cobalt heavy metals to separate with magnesium, is enriched with and recovery process, belongs to wastewater treatment and technical field of wet metallurgy.Nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process in a kind of waste water of the present invention, specific step is as follows: (1) oxidizer in P507 raffinate, feed liquid that treated stores spare after filtering and oil removing, to feed liquid COD < 200mg/l, SS < 200mg/l, oil are less than 50mg/l；(2) feed liquid obtained by step (1) is subjected to ion exchange, 3 ion exchange resin columns one are for dual-purpose；(3) step (2) obtain waste water after ion exchange exchanges and feed liquid (4) saturated resin that step (3) obtains is subjected to parsing parsing with the acid of 5 ~ 10% and 12-16% respectively after ion exchange resin using 4-8% lye, enter step (2) after being washed till PH=6 ~ 9.
Description
Technical field
The present invention relates to a kind of nickel-containing wastewater, cobalt heavy metals to separate with magnesium, is enriched with and recovery process, belongs to wastewater treatment and wet
Method metallurgical technology field.
Background technique
When producing cobalt salt (cobaltous sulfate, cobalt chloride) as raw material using product among cobalt concentrate and cobalt, the impurity such as cobalt and nickel, magnesium are used
P507 extraction and separation mainly contain the valuable gold such as nickel (500-2000mg/l) and a small amount of cobalt (1 ~ 50mg/l) in raffinate waste water
Belong to；Sodium content 50000-60000 mg/l, content of magnesium 2000-8000mg/l belong to high-salt wastewater；Contain a small amount of oil simultaneously.It passes
Technique of uniting uses fractional precipitation, and treated, and over-standard phenomenon still occurs in heavy metals ion, has been unable to meet increasingly serious
Environmental Protection Situation, and precipitate and generate nickel and cobalt containing magnesium slag as hazardous waste, processing cost is high.
In order to recycle valuable element in waste water, discharged wastewater met the national standard and reduce solid waste discharge, U.S. Tulsion uses CH-
90 be a chelating large hole cation exchanger resin, can be widely used in chlor-alkali industry solution purification, Call Provision in PTA industry
Magnesium, removes in plating, plating wastewater and rinse water or recycling heavy metal, heavy metal-containing wastewater treatment, or even from EDTA
The heavy metals such as cobalt ambrose alloy are removed in chelating agent, heavy metal precision can be accomplished 0.1mg/L hereinafter, reaching wastewater discharge standard, but
The import ion exchange resin price, investment cost are high.
Shanghai Sean Science and Technology Co., Ltd. is used using CN-27 styrene positive chelating resin resin, Su Qing group
SQD-412 resin is all the cation exchange resin that can adsorb the valuable metals such as nickel, copper, cobalt, makes nickel in waste water, cobalt, copper etc.
Heavy metal is separated with calcium, magnesium, and resin is in the Na after the pretreatment of persalt and NaOH, on resin+It can be with the metal in waste water
Ion swaps, and valuable metal ions are adsorbed on resin, backwash is carried out using hydrochloric acid, by metal ion backwash to salt
In acid, achieve the purpose that discharged wastewater met the national standard, valuable metal enriching and recovering.The resin adsorption amount is low, changes to import resin
Good, operating cost is high.
Summary of the invention
Technical problem to be solved by the invention is to provide a kind of nickel-containing wastewater, cobalt heavy metals to separate, be enriched with and recycle with magnesium
Technique, concrete scheme are as follows:
Nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process in a kind of waste water, the specific steps are as follows:
(1) oxidizer (reduce its COD) in P507 raffinate, feed liquid that treated store standby after filtering and oil removing
With until feed liquid COD < 200mg/l, SS < 200mg/l, oil is less than 50mg/l；
(2) 3 ion exchange resin columns one pass through weak acid ion-exchange resin, discharge liquor PH=8.5 for dual-purpose, with NaOH solution
Tap water top is added to wash, the enterprising lower row of tap water, waste water drains into soda storage tank, it is spare to be washed till PH=7.4；
(3) feed liquid obtained by step (1) is subjected to ion exchange exchange using the weak acid ion-exchange resin after step (2) transition
Afterwards, waste water and feed liquid are obtained；Waste water is the solution of high magnesium, and waste water processing station to content of beary metal is sent to reach discharge standard heel row
It puts；After ion exchange resin saturation, solution Ni > 0.1 mg/L, Co > 0.1mg/L, switching feed liquid to its spare amberlite
Rouge column continues to exchange, and obtains saturated resin；
(4) saturated resin that step (3) obtains is parsed with the acid of 5 ~ 10% and 12-16% respectively；The nickel salt of parsing drains into
Discharge liquor is drained into dilute nickel salt storage tank, and stop parsing, the ion exchange after parsing when discharge liquor PH is less than 4 by dense nickel salt case
Resin uses 4-8% lye, enters step (2) after being washed till PH=6 ~ 9.
Oxidant in the step (1) is one of sodium hypochlorite, sodium chlorate or hydrogen peroxide or multiple combinations, described
The additional amount of oxidant is 5-9 times of P507 raffinate COD mass.
Oxidant in the step (1) is sodium chlorate, and the additional amount of the oxidant is P507 raffinate COD mass
7 times, by treated COD < 200mg/L, feed liquid PH is 4-6 after filtering.
Equipment used by filtering in the step (1) is the combination of self-cleaning filter and ZGC107 resin.
Weak acid ion-exchange resin in the step (2) is one of D851, D852 or D860 or multiple combinations.
7 ~ 8% hydrochloric acid solutions or 13-14% sulfuric acid are parsed in the step (4), stop solution as discharge liquor PH < 3.5
Analysis；Resolution temperature is 25-30 DEG C.
Product among cobalt concentrate and cobalt are that raw material produces the raffinate waste water oxygenation of cobalt salt to reduce its COD by the present invention,
Feed liquid is through self-cleaning filtering and resin adsorption oil removing after oxidation, the feed liquid after oil removing again D851, D852 or D860 through sodium from
Sub-exchange resin, so that the heavy metal adsorptions such as nickel, cobalt separate on resin with magnesium, the resin of adsorption saturation is through sulfuric acid or salt acidolysis
Nickel sulfate or nickel chloride solution can be obtained in analysis, and regenerating after resin parsing can be recycled, which effectively recycles valuable in waste water
Metallic element the advantages that no waste sludge discharge, belongs to process for cleanly preparing, has very significant warp so that discharged wastewater met the national standard
Benefit of helping and the value of environmental protection.
Detailed description of the invention
Nickel, cobalt heavy metal are separated with magnesium, are enriched with and the process flow of recovery process is illustrated in a kind of waste water of Fig. 1 present invention
Figure.
Specific embodiment
Embodiment 1
(1) P507 raffinate (ingredient Ni:624mg/L, Co:18mg/L, Mg:5271 mg/L, COD:896 mg/L, SS:
1579mg/L, oil: 142mg/L), the sodium chlorate of 7.5 times of P507 raffinate COD mass ratio is added, temperature 50 C stirs 2h,
COD is reduced to 126 mg/L, and processing feed liquid stores after self-cleaning filtering and ZGC107 resin adsorption spare again.
(2) 3 D851 weak acid ion-exchange resin columns one are for dual-purpose, with the 4%NaOH solution of 2BV with the flow velocity of 1.6BV/h
By resin layer, discharge liquor PH=8.2 plus tap water top are washed, and the enterprising lower row of tap water, waste water drains into soda storage tank, be washed till PH=
7.5 spare.
(3) feed liquid obtained by step (1) is passed through with 25m3/ h is handed over by the D851 ion exchange resin after step (2) transition
Solution after changing is the solution of high magnesium, and content of beary metal reaches discharge standard, waste water processing station is sent to discharge.Ion exchange resin is full
With rear, solution Ni > 0.1 mg/L, Co > 0.1mg/L, switches feed liquid to its spare ion exchange resin column and continue to exchange.
(4) step (3) saturated resin is parsed with 8% and 13% sulfuric acid respectively.The nickel salt of parsing drains into dense nickel salt case,
When discharge liquor PH is less than 4, discharge liquor is drained into dilute nickel salt storage tank, and stop parsing, the ion exchange resin after parsing enters
Step (2).
Experimental result:
Embodiment 2
(1) P507 raffinate (ingredient Ni:985mg/L, Co:29mg/L, Mg:6245 mg/L, COD:768 mg/L, SS:
1786mg/L, oil: 179mg/L), the sodium chlorate of 8 times of P507 raffinate COD mass ratio is added, temperature 50 C stirs 2h, COD
It is reduced to 108mg/L, processing feed liquid stores after self-cleaning filtering and Archon filter spare again.
(2) 3 D860 weak acid ion-exchange resin columns one are for dual-purpose, with the 3%NaOH solution of 2BV with the flow velocity of 1.8BV/h
By resin layer, discharge liquor PH=8.5 plus tap water top are washed, and the enterprising lower row of tap water, waste water drains into soda storage tank, be washed till PH=
7.4 spare.
(3) feed liquid obtained by step (1) is passed through with 18m3/ h is handed over by the D860 ion exchange resin after step (2) transition
Solution after changing is the solution of high magnesium, and content of beary metal reaches discharge standard, waste water processing station is sent to discharge.Ion exchange resin is full
With rear, solution Ni > 0.1 mg/L, Co > 0.1mg/L, switches feed liquid to its spare ion exchange resin column and continue to exchange.
(4) step (3) saturated resin is parsed with 8% and 14% sulfuric acid respectively.The nickel salt of parsing drains into dense nickel salt case,
When discharge liquor PH is less than 4, discharge liquor is drained into dilute nickel salt storage tank, and stop parsing, the ion exchange resin after parsing enters
Step (2).
Experimental result:
Embodiment 3
(1) P507 raffinate (ingredient Ni:124mg/L, Co:12mg/L, Mg:3234 mg/L, COD:568 mg/L, SS:
954mg/L, oil: 123mg/L), the sodium chlorate of 7 times of P507 raffinate COD mass ratio is added, temperature 50 C stirs 2h, COD
126 mg/L are reduced to, processing feed liquid stores after self-cleaning filtering and ZGC107 resin adsorption spare again.
(2) 3 D851 weak acid ion-exchange resin columns one are for dual-purpose, with the 4%NaOH solution of 2BV with the flow velocity of 1.7BV/h
By resin layer, discharge liquor PH=8.4 plus tap water top are washed, and the enterprising lower row of tap water, waste water drains into soda storage tank, be washed till PH=
7.5 spare.
(3) feed liquid obtained by step (1) is passed through with 45m3/ h is handed over by the D851 ion exchange resin after step (2) transition
Solution after changing is the solution of high magnesium, and content of beary metal reaches discharge standard, waste water processing station is sent to discharge.Ion exchange resin is full
With rear, solution Ni > 0.1 mg/L, Co > 0.1mg/L, switches feed liquid to its spare ion exchange resin column and continue to exchange.
(4) step (3) saturated resin is parsed with 8% and 13% hydrochloric acid respectively.The nickel salt of parsing drains into dense nickel salt case,
When discharge liquor PH is less than 4, discharge liquor is drained into dilute nickel salt storage tank, and stop parsing, the ion exchange resin after parsing enters
Step (2).
The Applicant declares that the foregoing is merely a specific embodiment of the invention, but protection scope of the present invention not office
It is limited to this, it should be clear to those skilled in the art, any to belong to those skilled in the art and take off in the present invention
In the technical scope of dew, any changes or substitutions that can be easily thought of, and all of which fall within the scope of protection and disclosure of the present invention.
Experimental result:
The above content is combine the preferred embodiment of the invention to made by provided technical solution further specifically
It is bright, and it cannot be said that the invention specific implementation be confined to it is above-mentioned these explanation, for the invention technical field
Those of ordinary skill for, without departing from the concept of the premise of the invention, can also make it is several it is simple deduction or replace
It changes, all shall be regarded as belonging to the protection scope of the invention.
Claims (6)
1. nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process in a kind of waste water, which is characterized in that specific step is as follows:
(1) oxidizer in P507 raffinate, feed liquid that treated through filter and oil removing after store it is spare, until feed liquid COD <
200mg/l, SS < 200mg/l, oil are less than 50mg/l；
(2) 3 ion exchange resin columns one pass through weak acid ion-exchange resin, discharge liquor PH=8.5 for dual-purpose, with NaOH solution
Tap water top is added to wash, the enterprising lower row of tap water, waste water drains into soda storage tank, it is spare to be washed till PH=7.4；
(3) feed liquid obtained by step (1) is subjected to ion exchange exchange using the weak acid ion-exchange resin after step (2) transition
Afterwards, waste water and feed liquid are obtained；Waste water is the solution of high magnesium, and waste water processing station to content of beary metal is sent to reach discharge standard heel row
It puts；After ion exchange resin saturation, solution Ni > 0.1 mg/L, Co > 0.1mg/L, switching feed liquid to its spare amberlite
Rouge column continues to exchange, and obtains saturated resin；
(4) saturated resin that step (3) obtains is parsed with the acid of 5 ~ 10% and 12-16% respectively；The nickel salt of parsing drains into
Discharge liquor is drained into dilute nickel salt storage tank, and stop parsing, the ion exchange after parsing when discharge liquor PH is less than 4 by dense nickel salt case
Resin uses 4-8% lye, enters step (2) after being washed till PH=6 ~ 9.
2. nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process, feature exist in a kind of waste water as described in claim 1
In: the oxidant in the step (1) is one of sodium hypochlorite, sodium chlorate or hydrogen peroxide or multiple combinations, the oxidation
The additional amount of agent is 5-9 times of P507 raffinate COD mass.
3. nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process, feature exist in a kind of waste water as described in claim 1
In: the oxidant in the step (1) is sodium chlorate, and the additional amount of the oxidant is 7 times of P507 raffinate COD mass,
By treated COD < 200mg/L, feed liquid PH is 4-6 after filtering.
4. nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process, feature exist in a kind of waste water as described in claim 1
In: equipment used by filtering in the step (1) is the combination of self-cleaning filter and ZGC107 resin.
5. nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process, feature exist in a kind of waste water as described in claim 1
In: the weak acid ion-exchange resin in the step (2) is one of D851, D852 or D860 or multiple combinations.
6. nickel, cobalt heavy metal are separated with magnesium, are enriched with and recovery process, feature exist in a kind of waste water as described in claim 1
In: 7 ~ 8% hydrochloric acid solutions or 13-14% sulfuric acid are parsed in the step (4), stop parsing as discharge liquor PH < 3.5；Solution
Eutectoid temperature is 25-30 DEG C.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910557814.8A CN110194545B (en) | 2019-06-26 | 2019-06-26 | Process for separating, enriching and recovering nickel, cobalt and heavy metal from magnesium in wastewater |
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| CN201910557814.8A CN110194545B (en) | 2019-06-26 | 2019-06-26 | Process for separating, enriching and recovering nickel, cobalt and heavy metal from magnesium in wastewater |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111115903A (en) * | 2020-01-06 | 2020-05-08 | 湖南中伟新能源科技有限公司 | Method for removing cobalt in cobaltosic wastewater through two-stage ion exchange |
| CN113087211A (en) * | 2021-04-12 | 2021-07-09 | 浙江中金格派锂电产业股份有限公司 | Treatment method of waste water after cobalt salt preparation |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994002417A2 (en) * | 1992-07-21 | 1994-02-03 | Davy Mckee (Stockton) Limited | Process for the removal of sodium values from sodium contaminated solids |
| CN101415848A (en) * | 2006-02-02 | 2009-04-22 | 瓦利·德·利奥多斯公司 | Hybrid process using ion exchange resins in the selective recovery of nickel and cobalt from leaching effluents |
| CN103693711A (en) * | 2013-11-12 | 2014-04-02 | 郑州大学 | Method for treating nickel/copper-containing electroplating wastewater by using weak acid ion exchange fibers |
| CN105601020A (en) * | 2016-03-30 | 2016-05-25 | 北京赛科康仑环保科技有限公司 | Treatment technology of raffinate wastewater of nickel, cobalt and manganese |
| CN207726830U (en) * | 2017-08-31 | 2018-08-14 | 四川思达能环保科技有限公司 | The recovery system of hydrometallurgy raffinate |
| CN108529791A (en) * | 2018-05-02 | 2018-09-14 | 北京赛科康仑环保科技有限公司 | The processing method of deep removal COD in a kind of raffinate from nickel cobalt |
| CN109626662A (en) * | 2019-01-29 | 2019-04-16 | 浙江中金格派锂电产业股份有限公司 | Sodium chlorate-ion exchange resin treatment metallurgical waste water technique |
| CN109867400A (en) * | 2019-02-19 | 2019-06-11 | 北京中科康仑环境科技研究院有限公司 | A kind of method that the depth of nickel (cobalt) raffinate removes nickel, cobalt |
-
2019
- 2019-06-26 CN CN201910557814.8A patent/CN110194545B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994002417A2 (en) * | 1992-07-21 | 1994-02-03 | Davy Mckee (Stockton) Limited | Process for the removal of sodium values from sodium contaminated solids |
| CN101415848A (en) * | 2006-02-02 | 2009-04-22 | 瓦利·德·利奥多斯公司 | Hybrid process using ion exchange resins in the selective recovery of nickel and cobalt from leaching effluents |
| CN103693711A (en) * | 2013-11-12 | 2014-04-02 | 郑州大学 | Method for treating nickel/copper-containing electroplating wastewater by using weak acid ion exchange fibers |
| CN105601020A (en) * | 2016-03-30 | 2016-05-25 | 北京赛科康仑环保科技有限公司 | Treatment technology of raffinate wastewater of nickel, cobalt and manganese |
| CN207726830U (en) * | 2017-08-31 | 2018-08-14 | 四川思达能环保科技有限公司 | The recovery system of hydrometallurgy raffinate |
| CN108529791A (en) * | 2018-05-02 | 2018-09-14 | 北京赛科康仑环保科技有限公司 | The processing method of deep removal COD in a kind of raffinate from nickel cobalt |
| CN109626662A (en) * | 2019-01-29 | 2019-04-16 | 浙江中金格派锂电产业股份有限公司 | Sodium chlorate-ion exchange resin treatment metallurgical waste water technique |
| CN109867400A (en) * | 2019-02-19 | 2019-06-11 | 北京中科康仑环境科技研究院有限公司 | A kind of method that the depth of nickel (cobalt) raffinate removes nickel, cobalt |
Non-Patent Citations (1)
| Title |
|---|
| 赵志安: "树脂法回收技术在湿法冶金中的应用", 《安徽科技》 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111115903A (en) * | 2020-01-06 | 2020-05-08 | 湖南中伟新能源科技有限公司 | Method for removing cobalt in cobaltosic wastewater through two-stage ion exchange |
| CN113087211A (en) * | 2021-04-12 | 2021-07-09 | 浙江中金格派锂电产业股份有限公司 | Treatment method of waste water after cobalt salt preparation |
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| CN110194545B (en) | 2021-04-27 |
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