CN102230185A - Device and method for absorbing chlorine acid mist in electrodeposited cobalt production process - Google Patents
Device and method for absorbing chlorine acid mist in electrodeposited cobalt production process Download PDFInfo
- Publication number
- CN102230185A CN102230185A CN2011101653478A CN201110165347A CN102230185A CN 102230185 A CN102230185 A CN 102230185A CN 2011101653478 A CN2011101653478 A CN 2011101653478A CN 201110165347 A CN201110165347 A CN 201110165347A CN 102230185 A CN102230185 A CN 102230185A
- Authority
- CN
- China
- Prior art keywords
- absorption
- chlorine
- jetting type
- absorption unit
- acid mist
- 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.)
- Pending
Links
Images
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention discloses a device for absorbing chlorine acid mist in the electrodeposited cobalt production process. The device is characterized by comprising an electrodeposition cell, an anode gas collecting tank, a dilute cobalt chloride recycling tank, a jet type absorbing device I, a jet type absorbing device II, an absorbing tower I, an absorbing tower II, an absorbing liquid cooler and a draught fan, wherein a cathode and an anode are placed on the electrodeposition cell; and the absorbing tower I and the absorbing tower II are connected with each other in series. The invention also discloses a method for absorbing the chlorine acid mist. The method is characterized by comprising the steps of absorbing the chlorine acid mist in the anode gas collecting tank and the dilute cobalt chloride recycling tank through the jet type absorbing device to chemically react with alkali liquor so as to generate sodium hypochlorite bleaching liquor; reabsorbing the incompletely absorbed chlorine acid mist or the chlorine which is partially desorbed after being absorbed through a series of absorbing towers; and discharging out tail gas via the draught fan so that the absorbing rate of the chlorine can finally reach more than 99.5%. The device and the method disclosed by the invention have the advantages of simple equipment, easiness in maintenance, good absorbing effect, effective protection for the production environment, low cost and obvious economic benefit.
Description
Technical field
The present invention relates to the absorption unit of chlorine acid mist in a kind of electrodeposited cobalt production process, and utilize above-mentioned absorption unit to absorb the absorption process of chlorine acid mist, belong to the hydrometallurgy field.
Background technology
Cobalt is a kind of application metal more widely, can be used for alloying, permanent magnet, Precise Alloy, accumulate material etc.Produce by electrodeposition in the production process of cobalt with cobalt chloride solution, on anode, Cl
-1Take place to generate chlorine after oxidizing reaction loses electronics, and discharge the chlorine acid mist from anode.As untimely the chlorine acid mist is removed, can be caused murder by poisoning and corrosion environment and operator.Because the corrodibility of chlorine acid mist is extremely strong, the vacuum pump of suction chlorine acid mist often uses titanium material, the costing an arm and a leg and the maintenance cost height of equipment; In the treatment process of old in addition chlorine acid mist, often vacuum pump system is located at the outlet on absorption tower, make the operation of tower be in operation under the vacuum condition like this, be unfavorable for the absorption of chlorine acid mist, therefore the specific absorption of chlorine acid mist is only about 90%, and the chlorine bleach liquor after the absorption contains available chlorine only about 3%-5%, can only enter in the sewage lagoon as waste liquid, waste resource, polluted environment.Therefore, should provide a kind of new technical scheme to address the above problem.
Summary of the invention
The objective of the invention is: at above-mentioned deficiency, provide the absorption unit of chlorine acid mist in a kind of electrodeposited cobalt production process, another object of the present invention is that the using method of above-mentioned absorption unit is provided.
For achieving the above object, the technical solution used in the present invention is:
The absorption unit of chlorine acid mist in a kind of electrodeposited cobalt production process, comprise and be placed with negative electrode and anodic Winning cell, the anode plenum chamber, rare cobalt chloride withdrawing can, jetting type absorption unit I, jetting type absorption unit II, absorption tower I and absorption tower II that string is connected, absorption liquid water cooler and induced draft fan, the top of described rare cobalt chloride withdrawing can is connected by the mixing section inlet mouth of pipeline with jetting type absorption unit II, the mixing section liquid-inlet of described jetting type absorption unit II is connected with centrifugal infusion pump by the absorption liquid water cooler, the pneumatic outlet of described anode plenum chamber is connected by the mixing section inlet mouth of dechlorination post with jetting type absorption unit I, the mixing section liquid-inlet of described jetting type absorption unit I is connected with centrifugal infusion pump by the absorption liquid water cooler, and described induced draft fan is arranged at the rear of absorption tower II.
The absorption process of chlorine acid mist comprises the steps: in a kind of electrodeposited cobalt production process
(1) the early-stage preparations stage
Input duct is connected with cobalt chloride material-compound tank, centrifugal infusion pump, cobalt chloride solution well heater, forms the production equipment of electrodeposited cobalt;
(2) cathode and anode is placed in the Winning cell, interpole gap is 80mm, and cobalt chloride solution by after the cobalt chloride solution heater heats to 55 ℃, is sent into Winning cell;
(3) start jetting type absorption unit, induced draft fan and each centrifugal infusion pump, treat that processing parameter is stable after, feed electric current, regulating voltage is to 2.8V-3.0V, and current density 220A/m2, cobalt chloride solution cobalt ion on negative electrode obtains electronics and is reduced, generated cobalt metal, Cl on the anode
-1Lose electronics, oxidizing reaction takes place generate chlorine, the chlorine acid mist of generation with the form of the bubble liquid level of constantly overflowing, and is collected in the anode plenum chamber around anodic;
(4) pneumatic outlet in the anode plenum chamber is connected with jetting type absorption unit I by the dechlorination post, the alkali lye that absorption tower I and II bottom alkali lye is indoor is cooled to after temperature is lower than 40 ℃ by the absorption liquid water cooler, be transported to the liquid-inlet of jetting type absorption unit I again with centrifugal infusion pump, when the laval nozzle of alkaline stream in jetting type absorption unit I, alkali lye produces at a high speed, form negative pressure in the mixing section of jetting type absorption unit I, at this moment the chlorine acid mist gas in the anode plenum chamber is under the effect of negative pressure, flow in the dechlorination post, after the liquid separation of carrying secretly, the chlorine acid mist then is drawn in the mixing section from jetting type absorption unit I mixing section inlet mouth, and the vacuum tightness of control jet formula absorption unit I mixing section inlet mouth reach-more than the 0.090MPa, chlorine mixes the generation chemical reaction with alkali lye, the clorox bleaching liquor that generates is back to the alkali lye chamber on absorption tower, go round and begin again like this, after the alkaline reaction of bottom, absorption tower is exhausted, bleaching liquor is pumped in the bleaching liquor basin the new alkali lye of restock in absorption tower I and the II;
(5) flow out continuously through the reacted rare cobalt chloride solution of electrodeposition, flow into rare cobalt chloride withdrawing can, owing to there is part chlorine to be dissolved in the cobalt chloride solution, the top of rare cobalt chloride withdrawing can is connected with the mixing section inlet mouth of pipeline with jetting type absorption unit II, the alkali lye that absorption tower I and II bottom alkali lye is indoor is cooled to after temperature is lower than 40 ℃ by the absorption liquid water cooler, be transported to the liquid-inlet of jetting type absorption unit II again with centrifugal infusion pump, when the laval nozzle of alkaline stream in jetting type absorption unit II, alkali lye produces at a high speed, form negative pressure in the mixing section of jetting type absorption unit II, at this moment the chlorine acid mist gas in rare cobalt chloride is under the effect of negative pressure, flow in the dechlorination post, after the liquid separation of carrying secretly, the chlorine acid mist then mixing section inlet mouth in the jetting type absorption unit II sucks in the mixing section, and the vacuum tightness of control jet formula absorption unit II mixing section inlet mouth reach-more than the 0.090MPa, chlorine mixes the generation chemical reaction with alkali lye, the clorox bleaching liquor that generates is back to the alkali lye chamber on absorption tower, go round and begin again like this, after the alkaline reaction of bottom, absorption tower is exhausted, bleaching liquor is pumped in the bleaching liquor basin, the new alkali lye of restock in absorption tower I and the II, through jetting type absorption unit I and II, the specific absorption of chlorine is greater than 95%, absorbed once more through placed in-line absorption tower I and II again by the chlorine of part desorb again after remaining chlorine acid mist that does not have absorption or the absorption, tail gas is discharged by induced draft fan, and final chlorine specific absorption can reach more than 99.5%.
The absorption unit of chlorine acid mist in the electrodeposited cobalt production process of the present invention has improved the specific absorption of chlorine acid mist, has guaranteed that production environment is not contaminated.Abandon expensive titanium material vacuum pump simultaneously, further reduced production cost.
The absorption process of chlorine acid mist in the electrodeposited cobalt production process of the present invention, entering the preceding alkali lye of jetting type absorption unit is 30m through an area
2-50 m
2The absorption liquid water cooler be cooled to 40
0Below the C, purpose is for the reaction effect in the mixing section that is increased in the jet absorption unit.The big I of the suction of jetting type absorption unit is determined by the flow velocity of alkali lye, adopt absorption process of the present invention that the chlorine acid mist is absorbed, behind the ejector air intake device, the specific absorption of chlorine is greater than 95%, absorbed once more through a placed in-line absorption tower again by the chlorine of part desorb again after remaining chlorine acid mist that does not have absorption or the absorption, tail gas is discharged by induced draft fan, and final chlorine specific absorption can reach more than 99.5%.But produce one ton of electrodeposited cobalt also by-product available chlorine obtain tangible economic benefit greater than about 12 tons of 10% chlorine bleach liquores.
Advantage of the present invention is: equipment is simple, easy-maintaining, and good absorbing effect has effectively been protected production environment, and cost is low, has tangible economic benefit.
Description of drawings
Below in conjunction with the drawings and specific embodiments the present invention is described in further detail.
Fig. 1 is an absorption unit structural representation of the present invention.
Wherein: 1, negative electrode, 2, anode, 3, Winning cell, 4, anode plenum chamber, 5, rare cobalt chloride withdrawing can, 6, jetting type absorption unit I, 7, jetting type absorption unit II, 8, absorption tower I, 9, the absorption tower II, 10, absorption liquid water cooler, 11, induced draft fan, 12, pipeline, 13, centrifugal infusion pump, 14, dechlorination post, 15, the cobalt chloride material-compound tank, 16, the cobalt chloride solution well heater.
Embodiment
As shown in Figure 1, the absorption unit of chlorine acid mist in a kind of electrodeposited cobalt production process of the present invention, comprise the Winning cell 3 that is placed with negative electrode 1 and anode 2, anode plenum chamber 4, rare cobalt chloride withdrawing can 5, jetting type absorption unit I6, jetting type absorption unit II 7, absorption tower I8 and absorption tower II 9 that string is connected, absorption liquid water cooler 10 and induced draft fan 11, the top of described rare cobalt chloride withdrawing can 5 is connected by the mixing section inlet mouth of pipeline 12 with jetting type absorption unit II 7, the mixing section liquid-inlet of described jetting type absorption unit II 7 is connected with centrifugal infusion pump 13 by absorption liquid water cooler 10, the pneumatic outlet of described anode plenum chamber 4 is connected by the mixing section inlet mouth of dechlorination post 14 with jetting type absorption unit I6, the mixing section liquid-inlet of described jetting type absorption unit I6 is connected with centrifugal infusion pump 13 by absorption liquid water cooler 10, and described induced draft fan 11 is arranged at the rear of absorption tower II 9.
The absorption process of chlorine acid mist comprises the steps: in a kind of electrodeposited cobalt production process of the present invention
(1) the early-stage preparations stage
Input duct is connected with cobalt chloride material-compound tank 15, centrifugal infusion pump 13, cobalt chloride solution well heater 16, forms the production equipment of electrodeposited cobalt;
(2) cathode and anode 1 and 2 is placed in the Winning cell 3, interpole gap is 80mm, cobalt chloride solution is heated to 55 ℃ by cobalt chloride solution well heater 16 after, send in the Winning cell 3;
(3) start jetting type absorption unit 6 and 7, induced draft fan 11 and each centrifugal infusion pump 13, after treating that processing parameter is stable, feed electric current, regulating voltage is to 2.8V-3.0V, current density 220A/m2, cobalt chloride solution cobalt ion on negative electrode obtains electronics and is reduced, and has generated cobalt metal, Cl on the anode
-1Lose electronics, oxidizing reaction takes place generate chlorine, the chlorine acid mist of generation with the form of the bubble liquid level of constantly overflowing, and is collected in the anode plenum chamber 4 around anodic;
(4) pneumatic outlet with anode plenum chamber 4 is connected with jetting type absorption unit I6 by dechlorination post 14, the alkali lye that absorption tower I8 and absorption tower II 9 bottom alkali lye are indoor is cooled to after temperature is lower than 40 ℃ by absorption liquid water cooler 10, be transported to the liquid-inlet of jetting type absorption unit I6 again with centrifugal infusion pump 13, when the laval nozzle of alkaline stream in jetting type absorption unit I6, alkali lye produces at a high speed, form negative pressure in the mixing section of jetting type absorption unit I6, at this moment the chlorine acid mist gas in the anode plenum chamber 4 is under the effect of negative pressure, flow in the dechlorination post 14, after the liquid separation of carrying secretly, the chlorine acid mist then is drawn in the mixing section from jetting type absorption unit I6 mixing section inlet mouth, and the vacuum tightness of control jet formula absorption unit I6 mixing section inlet mouth reach-more than the 0.090MPa, chlorine mixes the generation chemical reaction with alkali lye, the clorox bleaching liquor that generates is back to the alkali lye chamber on absorption tower, go round and begin again like this, after the alkaline reaction of bottom, absorption tower is exhausted, bleaching liquor is pumped in the bleaching liquor basin the new alkali lye of restock in absorption tower I8 and the absorption tower II 9;
(5) flow out continuously through the reacted rare cobalt chloride solution of electrodeposition, flow into rare cobalt chloride withdrawing can 5, owing to there is part chlorine to be dissolved in the cobalt chloride solution, the top of rare cobalt chloride withdrawing can 5 is connected with the mixing section inlet mouth of pipeline 12 with jetting type absorption unit II 7, the alkali lye that absorption tower I8 and absorption tower II 9 bottom alkali lye are indoor is cooled to after temperature is lower than 40 ℃ by absorption liquid water cooler 10, be transported to the liquid-inlet of jetting type absorption unit II 7 again with centrifugal infusion pump 13, when the laval nozzle of alkaline stream in jetting type absorption unit II 7, alkali lye produces at a high speed, form negative pressure in the mixing section of jetting type absorption unit II 7, at this moment the chlorine acid mist gas in rare cobalt chloride is under the effect of negative pressure, flow in the dechlorination post 14, after the liquid separation of carrying secretly, the chlorine acid mist then sucks in the mixing section from jetting type absorption unit II 7 interior mixing section inlet mouths, and the vacuum tightness of control jet formula absorption unit II 7 mixing section inlet mouths reach-more than the 0.090MPa, chlorine mixes the generation chemical reaction with alkali lye, the clorox bleaching liquor that generates is back to the alkali lye chamber on absorption tower, go round and begin again like this, after the alkaline reaction of bottom, absorption tower is exhausted, bleaching liquor is pumped in the bleaching liquor basin, the new alkali lye of restock in absorption tower I8 and the absorption tower II 9, through jetting type absorption unit I6 and jetting type absorption unit II 7, the specific absorption of chlorine is greater than 95%, absorbed once more through a placed in-line absorption tower I8 and absorption tower II 9 again by the chlorine of part desorb again after remaining chlorine acid mist that does not have absorption or the absorption, tail gas is discharged by induced draft fan 11, and final chlorine specific absorption can reach more than 99.5%.
Claims (2)
1. the absorption unit of chlorine acid mist in the electrodeposited cobalt production process, it is characterized in that: comprise being placed with negative electrode and anodic Winning cell, the anode plenum chamber, rare cobalt chloride withdrawing can, jetting type absorption unit I, jetting type absorption unit II, absorption tower I and absorption tower II that string is connected, absorption liquid water cooler and induced draft fan, the top of described rare cobalt chloride withdrawing can is connected by the mixing section inlet mouth of pipeline with jetting type absorption unit II, the mixing section liquid-inlet of described jetting type absorption unit II is connected with centrifugal infusion pump by the absorption liquid water cooler, the pneumatic outlet of described anode plenum chamber is connected by the mixing section inlet mouth of dechlorination post with jetting type absorption unit I, the mixing section liquid-inlet of described jetting type absorption unit I is connected with centrifugal infusion pump by the absorption liquid water cooler, and described induced draft fan is arranged at the rear of absorption tower II.
2. the absorption process of chlorine acid mist in the electrodeposited cobalt production process is characterized in that: comprise the steps:
(1) the early-stage preparations stage
Input duct is connected with cobalt chloride material-compound tank, centrifugal infusion pump, cobalt chloride solution well heater, forms the production equipment of electrodeposited cobalt;
(2) cathode and anode is placed in the Winning cell, interpole gap is 80mm, and cobalt chloride solution by after the cobalt chloride solution heater heats to 55 ℃, is sent into Winning cell;
(3) start jetting type absorption unit, induced draft fan and each centrifugal infusion pump, treat that processing parameter is stable after, feed electric current, regulating voltage is to 2.8V-3.0V, and current density 220A/m2, cobalt chloride solution cobalt ion on negative electrode obtains electronics and is reduced, generated cobalt metal, Cl on the anode
-1Lose electronics, oxidizing reaction takes place generate chlorine, the chlorine acid mist of generation with the form of the bubble liquid level of constantly overflowing, and is collected in the anode plenum chamber around anodic;
(4) pneumatic outlet in the anode plenum chamber is connected with jetting type absorption unit I by the dechlorination post, the alkali lye that absorption tower I and II bottom alkali lye is indoor is cooled to after temperature is lower than 40 ℃ by the absorption liquid water cooler, be transported to the liquid-inlet of jetting type absorption unit I again with centrifugal infusion pump, when the laval nozzle of alkaline stream in jetting type absorption unit I, alkali lye produces at a high speed, form negative pressure in the mixing section of jetting type absorption unit I, at this moment the chlorine acid mist gas in the anode plenum chamber is under the effect of negative pressure, flow in the dechlorination post, after the liquid separation of carrying secretly, the chlorine acid mist then is drawn in the mixing section from jetting type absorption unit I mixing section inlet mouth, and the vacuum tightness of control jet formula absorption unit I mixing section inlet mouth reach-more than the 0.090MPa, chlorine mixes the generation chemical reaction with alkali lye, the clorox bleaching liquor that generates is back to the alkali lye chamber on absorption tower, go round and begin again like this, after the alkaline reaction of bottom, absorption tower is exhausted, bleaching liquor is pumped in the bleaching liquor basin the new alkali lye of restock in absorption tower I and the II;
(5) flow out continuously through the reacted rare cobalt chloride solution of electrodeposition, flow into rare cobalt chloride withdrawing can, owing to there is part chlorine to be dissolved in the cobalt chloride solution, the top of rare cobalt chloride withdrawing can is connected with the mixing section inlet mouth of pipeline with jetting type absorption unit II, the alkali lye that absorption tower I and II bottom alkali lye is indoor is cooled to after temperature is lower than 40 ℃ by the absorption liquid water cooler, be transported to the liquid-inlet of jetting type absorption unit II again with centrifugal infusion pump, when the laval nozzle of alkaline stream in jetting type absorption unit II, alkali lye produces at a high speed, form negative pressure in the mixing section of jetting type absorption unit II, at this moment the chlorine acid mist gas in rare cobalt chloride is under the effect of negative pressure, flow in the dechlorination post, after the liquid separation of carrying secretly, the chlorine acid mist then mixing section inlet mouth in the jetting type absorption unit II is drawn in the mixing section, and the vacuum tightness of control jet formula absorption unit II mixing section inlet mouth reach-more than the 0.090MPa, chlorine mixes the generation chemical reaction with alkali lye, the clorox bleaching liquor that generates is back to the alkali lye chamber on absorption tower, go round and begin again like this, after the alkaline reaction of bottom, absorption tower is exhausted, bleaching liquor is pumped in the bleaching liquor basin, the new alkali lye of restock in absorption tower I and the II, through jetting type absorption unit I and II, the specific absorption of chlorine is greater than 95%, absorbed once more through a placed in-line absorption tower I and II again by the chlorine of part desorb again after remaining chlorine acid mist that does not have absorption or the absorption, tail gas is discharged by induced draft fan, and final chlorine specific absorption can reach more than 99.5%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101653478A CN102230185A (en) | 2011-06-20 | 2011-06-20 | Device and method for absorbing chlorine acid mist in electrodeposited cobalt production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101653478A CN102230185A (en) | 2011-06-20 | 2011-06-20 | Device and method for absorbing chlorine acid mist in electrodeposited cobalt production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102230185A true CN102230185A (en) | 2011-11-02 |
Family
ID=44842784
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101653478A Pending CN102230185A (en) | 2011-06-20 | 2011-06-20 | Device and method for absorbing chlorine acid mist in electrodeposited cobalt production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102230185A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102505129A (en) * | 2011-12-26 | 2012-06-20 | 烟台凯实工业有限公司 | Tank face integral sealing device for electrodeposition production in sulfuric acid system |
| CN103361483A (en) * | 2013-07-26 | 2013-10-23 | 浙江钛合仪器有限公司 | Technology for removing cobalt by dynamic wave chlorine oxidation |
| CN103383064A (en) * | 2013-08-07 | 2013-11-06 | 内蒙古君正化工有限责任公司 | Leaked chlorine absorption device |
| CN103409771A (en) * | 2013-08-13 | 2013-11-27 | 四川省尼科国润新材料有限公司 | Environment-friendly process unit and process for continuous stable production of electrolytic nickel or electrolytic cobalt |
| CN106835194A (en) * | 2017-01-12 | 2017-06-13 | 江苏凯力克钴业股份有限公司 | A kind of cobalt chloride electrodeposition process |
| CN112795953A (en) * | 2020-12-28 | 2021-05-14 | 格林美（江苏）钴业股份有限公司 | Electric cobalt production method capable of recycling byproducts |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2339564Y (en) * | 1997-10-07 | 1999-09-22 | 宜兴环保科技工业园电力环保设备厂 | Jet-flow type chlorine-absorbing device |
| JP2004158730A (en) * | 2002-11-08 | 2004-06-03 | Canon Inc | Gas treatment method |
| CN2670329Y (en) * | 2003-11-04 | 2005-01-12 | 李凤山 | Chlorinedioxide gas absorbing tower |
| CN201482410U (en) * | 2009-07-30 | 2010-05-26 | 浙江华友钴业股份有限公司 | Copper electrodeposition acid mist absorbing device |
-
2011
- 2011-06-20 CN CN2011101653478A patent/CN102230185A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2339564Y (en) * | 1997-10-07 | 1999-09-22 | 宜兴环保科技工业园电力环保设备厂 | Jet-flow type chlorine-absorbing device |
| JP2004158730A (en) * | 2002-11-08 | 2004-06-03 | Canon Inc | Gas treatment method |
| CN2670329Y (en) * | 2003-11-04 | 2005-01-12 | 李凤山 | Chlorinedioxide gas absorbing tower |
| CN201482410U (en) * | 2009-07-30 | 2010-05-26 | 浙江华友钴业股份有限公司 | Copper electrodeposition acid mist absorbing device |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102505129A (en) * | 2011-12-26 | 2012-06-20 | 烟台凯实工业有限公司 | Tank face integral sealing device for electrodeposition production in sulfuric acid system |
| CN102505129B (en) * | 2011-12-26 | 2014-01-15 | 烟台凯实工业有限公司 | Tank face integral sealing device for electrodeposition production in sulfuric acid system |
| CN103361483A (en) * | 2013-07-26 | 2013-10-23 | 浙江钛合仪器有限公司 | Technology for removing cobalt by dynamic wave chlorine oxidation |
| CN103361483B (en) * | 2013-07-26 | 2015-04-08 | 浙江钛合仪器有限公司 | Technology for removing cobalt by dynamic wave chlorine oxidation |
| CN103383064A (en) * | 2013-08-07 | 2013-11-06 | 内蒙古君正化工有限责任公司 | Leaked chlorine absorption device |
| CN103409771A (en) * | 2013-08-13 | 2013-11-27 | 四川省尼科国润新材料有限公司 | Environment-friendly process unit and process for continuous stable production of electrolytic nickel or electrolytic cobalt |
| CN103409771B (en) * | 2013-08-13 | 2017-07-21 | 四川省尼科国润新材料有限公司 | A kind of environment-friendly type electrolytic nickel continuous and stable production technique |
| CN106835194A (en) * | 2017-01-12 | 2017-06-13 | 江苏凯力克钴业股份有限公司 | A kind of cobalt chloride electrodeposition process |
| CN112795953A (en) * | 2020-12-28 | 2021-05-14 | 格林美（江苏）钴业股份有限公司 | Electric cobalt production method capable of recycling byproducts |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102230185A (en) | Device and method for absorbing chlorine acid mist in electrodeposited cobalt production process | |
| CN207551970U (en) | A kind of device of iron-carbon micro-electrolysis processing industrial wastewater | |
| CN109252168A (en) | A kind of devices and methods therefor of efficient activated acid etching solution | |
| CN107162281A (en) | The processing method and Waste Water Treatment of heavy metal ion in a kind of removal smelting wastewater | |
| CN203440472U (en) | Acid mist recovery system device | |
| CN112458463A (en) | Acid etching solution recycling system and method | |
| WO2013079802A1 (en) | An apparatus for treating off-gas including acid mist originating from a source that forms acid mist | |
| CN211445922U (en) | Dechlorination system for ionic membrane caustic soda | |
| CN105126514A (en) | Graphite purification tail gas treatment apparatus and graphite purification tail gas treatment process | |
| CN108160737A (en) | Extruding die for aluminum shaped material alkali-washing waste liquid recovery processing technique | |
| CN104445569A (en) | Method and system for seawater foam control | |
| CN207928979U (en) | The processing system of the nitric acid exhaust gas generated in oxidation process | |
| CN101428191A (en) | Method for improving washing efficiency for tail gas from wet-process phosphoric acid manufacture | |
| CN212309310U (en) | Device for batch treatment of acidic tail gas | |
| CN209242855U (en) | De- drift sewage treatment process system | |
| CN208500478U (en) | A kind of device of acidic etching waste liquid processing | |
| CN208637544U (en) | A kind of alkaline electrolyte recyclable device | |
| CN113981449B (en) | Method for recovering and treating waste etching solution | |
| CN206676196U (en) | One kind is used for electrolysis and prepares NF3The safe purifier of anode gas | |
| CN106086896A (en) | Based on the wiring board acidity etching liquid recycling system in heavy metal containing wastewater treatment | |
| CN207738495U (en) | A kind of electric flocculation air-floating apparatus | |
| CN115487669B (en) | Absorption washing tower for lithium hexafluorophosphate tail gas | |
| CN104906874A (en) | Automatic gas-liquid separation device and method for chlorine dioxide generator under high negative pressure environment | |
| CN209576214U (en) | A kind of waste gas and liquids treatment device producing delustering agent generation | |
| CN201424389Y (en) | Reverse osmosis vacuum degassing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20111102 |