CN102676835B - Method for recovery of Ir from platinum group-containing solution - Google Patents
Method for recovery of Ir from platinum group-containing solution Download PDFInfo
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- CN102676835B CN102676835B CN201210026237.8A CN201210026237A CN102676835B CN 102676835 B CN102676835 B CN 102676835B CN 201210026237 A CN201210026237 A CN 201210026237A CN 102676835 B CN102676835 B CN 102676835B
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- acidic solution
- platinum group
- gac
- ionic strength
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D15/00—Separating processes involving the treatment of liquids with solid sorbents; Apparatus therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/02—Settling tanks with single outlets for the separated liquid
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/30—Active carbon
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G55/00—Compounds of ruthenium, rhodium, palladium, osmium, iridium, or platinum
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Water Treatment By Sorption (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The invention provides a method for recovery of Ir from a platinum group-containing solution. The method raises an adsorption rate of activated carbon by Ir and can recover Ir more effectively. The process of recovering Ir from platinum a group-containing solution comprises the following steps of: a neutralization process: adding a neutralizer for depositing vitriol in an acid solution including Ir to deposit and separate sulphate ions in the acid solution and to make free acid concentration of the acid solution be 0.03 mol/L-1.2 mol/L and to reduce ion strength in the acid solution; a vulcanization process: adding a vulcanizer to remove at least one impurity selected from the group of As, Cu, Fe, Ni, Zn, Bi, Pb, Te, Sn and Sb included in the acid solution including Ir; and an activated carbon adsorption process: passing the neutralized acid solution including Ir in activated carbon to make Ir absorb the activated carbon.
Description
Technical field
The present invention relates to a kind of recovery method reclaiming Ir from platinum group solution, particularly relate to a kind of acidic solution from containing Ir and such as Cu electrodeposit is carried out de-Cu leaching, potassium cloride, Au extraction, SO
2the method of Ir is effectively reclaimed in industrial water drainage after reduction.
Background technology
As the method reclaiming the platinum metals such as Ir from solution, there will be a known the method using and have ion exchange resin or solvent extraction agent.But these methods exist following shortcoming: the price comparison of ion exchange resin or solvent extraction agent is high, wash-out, the mixing due to base metal or coexisting ion exists and has weakening of performance.
Inherit such school, widely use the absorption to gac.Such as, following method is had: add vulcanizing agent in containing the acidic solution of Ir and remove impurity in Japanese Unexamined Patent Publication 2010-174336 publication (patent documentation 1), make filtrate passing through be filled into the gac of chromatographic column, make Ir be adsorbed onto gac thus and the method reclaimed from solution.
Conventional art document
Patent documentation
Patent documentation 1: Japanese Unexamined Patent Publication 2010-174336 publication
Summary of the invention
But even if use the method for patent documentation 1, also sometimes according to the difference of the condition of the acidic solution containing Ir, can not obtain the adsorption rate of Ir to gac fully, need research further.
Therefore, the invention provides a kind of method reclaiming Ir from platinum group solution, described method can improve the adsorption rate of Ir to gac, more effectively can reclaim Ir.
The present inventor etc. concentrate on studies to solve above-mentioned problem, and result is learnt containing the absorption of the ionic strength affect Ir in the acidic solution of Ir to gac.That is, learn: when too high containing the ionic strength in the acidic solution of Ir, there will be Ir and the adsorption rate of gac is reduced, the tendency of the desired Ir rate of recovery can not be obtained.Therefore, the discoveries such as the present inventor, the neutralizing treatment composition of impact being brought to remove to the ionic strength in solution is in advance implemented before activated carbon treatment, index as ionic strength decline evaluates the free acid concentration in acidic solution, as a result, the adsorption rate of Ir to gac can be improved significantly.
In a first aspect of the present invention completed based on above opinion, for a kind of recovery method reclaiming Ir from platinum group solution, it comprises following operation: in and operation, make the neutralizing agent of sulfuric acid precipitation by interpolation in the acidic solution containing Ir and sulfuric acid and make the sulfate ion in acidic solution precipitate and be separated, make the free acid concentration in acidic solution be 0.03mol/L ~ 1.2mol/L, the ionic strength in acidic solution is reduced; Charcoal absorption operation, by the logical liquid in gac of the acidic solution containing Ir after neutralization, makes Ir be adsorbed in gac.
One embodiment of the recovery method from platinum group solution recovery Ir of the present invention, neutralizing agent comprises Ca (OH)
2, CaO, CaCO
3, Sr (OH)
2, SrO, SrCO
3in any one.
Of the present inventionly reclaim the recovery method of Ir in another embodiment from platinum group solution, in and the operation mode that comprises making the ionic strength in acidic solution reach less than 2 add the step of neutralizing agent.
The another embodiment of the recovery method from platinum group solution recovery Ir of the present invention, vulcanization process comprises the oxidation reduction potential control of the acidic solution containing Ir after by neutralization at 70 ~ 90mV.
According to the present invention, a kind of recovery method reclaiming Ir from platinum group solution can be provided, even if the solution containing Ir that the content that described platinum group solution is Ir is trace, ionic strength is high, also can improve the adsorption rate of Ir to gac, and more effectively reclaim Ir.
Accompanying drawing explanation
Fig. 1 represents a mode of the processing flow chart of the recovery method of the Ir described in embodiments of the present invention.
Fig. 2 represents the example of the relation of free acid concentration in neutralizing treatment and Ir liquid partition ratio.
Fig. 3 represents the example of the relation of the ionic strength of free acid concentration in neutralizing treatment and solution.
Fig. 4 represents the example of the ionic strength of liquid and the relation of Ir adsorption rate before the absorption in charcoal absorption process.
Embodiment
Below, embodiments of the present invention are described in detail.
Handling object thing of the present invention is the acidic solution of platinum group solution namely containing Ir, more specifically, for Cu electrodeposit being carried out de-Cu leaching, potassium cloride, Au extraction, SO
2industrial water drainage after reduction.Not only containing Ir in this handling object thing, and containing impurity such as As, Cu, Fe, Ni, Zn, Bi, Pb, Te, Sn, Sb, be the strongly acidic solution containing sulfuric acid concentration 1mol/L, concentration of hydrochloric acid 1mol/L.Containing in the acidic solution of Ir at this, is sulfuric acid to the composition that ionic strength affect is maximum, by removing sulfuric acid from containing in the acidic solution of Ir, the ionic strength of the acidic solution containing Ir can be made effectively to reduce.
As from containing the method removing sulfuric acid in the acidic solution of Ir, the neutralization method of adding neutralizing agent in the acidic solution containing Ir can be utilized.As neutralizing agent, preference is as Ca (OH)
2, CaO, CaCO
3deng Ca compound, Sr (OH)
2, SrO, SrCO
3deng the neutralizing agent for making sulfuric acid precipitation such as Sr compound.At use CaCO
3when, preferably use the calcium carbonate of slurry.Such as, in use Ca (OH)
2when as neutralizing agent, preferably according to (1) formula, make containing the sulfate ion in the acidic solution of Ir and sulfuric acid as gypsum (CaSO
42H
2o) precipitate, make the ionic strength of the acidic solution containing Ir and sulfuric acid be reduced to less than 2.
2H
++SO
4 2-+Ca(OH)
2→CaSO
4·2H
2O ...(1)
In and operation in, preferably the ionic strength of the acidic solution containing Ir and sulfuric acid is set as less than 2, is more preferably less than 1.2.Make ionic strength higher than 2 time, effectively can not reclaim Ir.The lower value of ionic strength is not particularly limited, and can be set as the ionic strength of such as Ir ion.It should be noted that, with regard to the ionic strength of the acidic solution containing Ir and sulfuric acid, the volumetric molar concentration of the ion of i kind contained in solution is set as ci, when charge number is set as zi, be (1/2) ∑ cizi
2, can be obtained by the volumetric molar concentration measuring the ion in solution.
In above-mentioned and in operation, the mode that the mode, the more preferably free acid concentration that are preferably 0.03mol/L ~ 1.2mol/L with the free acid concentration of the acidic solution containing Ir and sulfuric acid are 0.1mol/L ~ 1.2mol/L adds neutralizing agent.When free acid concentration is higher than 1.2mol/L, sulfate ion exists in large quantities in containing the acidic solution of Ir, and therefore, ionic strength raises, and the Ir adsorption rate in charcoal absorption operation described later reduces.On the other hand, when free acid concentration is lower than 0.03mol/L, containing the sulfate ion termination reaction in the acidic solution of Ir, the positively charged ion (such as using the situation of Ca compound to be Ca ion) etc. becoming superfluous neutralizing agent starts to dissolve, therefore, ionic strength raises again.And by neutralization, Ir precipitates, and therefore, when free acid concentration is lower than 0.03mol/L, Ir precipitates, Ir liquid partition ratio reduces, and it should be noted that, free acid concentration can utilize neutralization titration to measure.
Also can with in the acidic solution containing Ir and sulfuric acid pH control in and operation carry out situation.Now, the mode being pH=-0.08 ~ 1.5 with the pH in the acidic solution containing Ir and sulfuric acid adds neutralizing agent.
The CaSO of precipitation
42H
2o is separated by filtration, reclaims the acidic solution containing Ir.The impurity such as As, Cu, Fe, Ni, Zn, Bi, Pb, Te, Sn, Sb are comprised in the acidic solution (neutralization filtrate) containing Ir.Therefore, the vulcanization process of the impurity being removed As, Cu, Fe, Ni, Zn, Bi, Pb, Te, Sn, Sb more than at least a kind by the interpolation of vulcanizing agent is preferably implemented.
As vulcanizing agent, preferably use sodium sulfhydrate, sodium sulphite, hydrogen sulfide etc.For the concentration of vulcanizing agent when dropping into vulcanizing agent in the solution, the control of the redox potential of solution when considering increase or the sulfuration of amount of filtrate, preferably 20 ~ 30mass%.About the interpolation speed of vulcanizing agent, the control of the redox potential (ORP) of solution during consideration sulfuration, relative to the acidic solution 1L containing Ir, preferred below 3ml/min.Temperature when carrying out sulfuration and the speed of vulcanization reaction have relation, are not limited to specific temperature, even if at normal temperatures or under heating, also can effectively be separated.
With regard to the redox potential (ORP) of electrode based on the Ag/AgCl electrode of liquid after sulfuration, after redox potential when relation, the sulfuration of the partition ratio of redox potential during sulfuration and Ru, Ir and sulfuration, the relation of impurity (hindering impurity, such as As, Pb, Sn etc. of the absorption of Ir when the making charcoal absorption Ir) concentration of liquid is considered, preferably with the scope of 70 ~ 90mV for index.
To the solution after sulfidizing, filtering impurity by crossing, reclaiming the acidic solution (after sulfuration liquid) containing Ir.Thereafter, the acidic solution containing Ir after recovery is contacted with gac, makes Ir be adsorbed in gac.
About the contact method of gac and solution, preferably gac is filled in chromatographic column, in this chromatographic column, flows into the mode of the acidic solution containing Ir continuously.
The kind of gac is not particularly limited, and wherein, the adsorptive capacity of activated coco nut charcoal is maximum, and rate of adsorption is also fast, therefore preferably.In addition, preferably before absorption, deaeration process is carried out.About the logical liquid speed to gac, preferably control in the scope of SV (space velocity)=1 ~ 20.
[embodiment]
, embodiments of the invention are shown below, but the present invention is not limited to following embodiment.
(embodiment 1)
In and operation in, add slurry calcium carbonate and stir, until relative to Cu electrodeposit is carried out de-Cu leaching, potassium cloride, Au leach, SO
2trade effluent 9.3m after reduction
3free acid concentration is 1.2mol/L, makes the ionic strength in solution be reduced to 1.2 from 3.2.
Table 1 form with the liquid of operation in representing, free acid concentration and to the partition ratio neutralizing afterwards liquid.By the interpolation of calcium carbonate, amount of liquid increases, and Ir strength of fluid reduces, but Ir content has almost no change, can using 96.1% of Ir as the rear liquids recovery of neutralization.
[table 1]
The removing of the impurity utilizing the vulcanization process of the rear liquid of neutralization is described.That reclaims with operation in utilization contains in Ir and rear liquid (before sulfuration liquid) 20m
3in, based on Ag/AgCl electrode, electrode adds 25 quality % sodium sulfhydrates to ORP=80mV.Table 2 represents the liquid composition of vulcanization process, the Liquid distribution rate in vulcanization process.Utilize vulcanization process the impurity such as Cu, Fe, Ni, Zn, Pb, Te, Sb, Sn, As, the Bi except Ir, Ru can be removed substantially, can Ir99.3%, Ru72.7% be reclaimed in liquid after curing.
[table 2]
The absorption of Ir to gac about the charcoal absorption operation of liquid after utilizing sulfuration is described.Reclaim utilizing vulcanization process containing liquid (absorption before liquid) 20m after the sulfuration of Ir
3logical liquid, in the adsorption tower being filled with gac, makes Ir be adsorbed in gac.Table 3 represents liquid composition, the adsorption rate of charcoal absorption operation.85.7% of Ir can be adsorbed in gac and reclaim.
[table 3]
(embodiment 2)
As Cu electrodeposit is carried out de-Cu leaching, potassium cloride, Au extract, SO
2ca (OH) is added in containing in the acidic solution 200ml of Ir of trade effluent after reduction
2, until free acid concentration is 0.1mol/L, makes the ionic strength in solution be reduced to 1.73 from 4.89, contained the acidic solution of Ir by filtered and recycled.Table 4 represents the liquid composition in neutralization, the partition ratio to liquid after neutralization.In and front liquid in, to SO
4 2-, the impact of ionic strength that produces of Cl, free acid concentration is large, after the neutralization in liquid, although Ir Liquid distribution rate is 75.4%, but, can SO be removed
4 2-, free acid concentration is declined, reduces ionic strength.
[table 4]
(embodiment 3)
Except by and time free acid concentration be set as except 1.0mol/L, utilize neutralizing treatment similarly to Example 1, sulfidizing ionic strength is adjusted to 1.14 containing in the acidic solution of Ir, the gac of deaeration has been carried out with the ratio input being 4g relative to solution 100mL, thereafter, stir 24 hours, make Ir be adsorbed in gac.Table 5 represents liquid composition, adsorption rate in charcoal absorption, by charcoal absorption, 84.1% of Ir can be made to adsorb and reclaim.
[table 5]
(embodiment 4)
The relation > of the free acid concentration in < neutralizing treatment and Ir Liquid distribution rate
The relation of the Ir Liquid distribution rate of the change to the free acid concentration (free acid concentration) in neutralizing treatment and the solution containing Ir to recovery is evaluated.Fig. 2 represents result.In fig. 2, about in and operation, under condition similarly to Example 2, change Ca (OH)
2addition and free acid concentration is changed.Learn: by neutralization, free acid concentration is step-down compared with about 1.2mol/L, accompanies with it, Ir Liquid distribution rate step-down.
(embodiment 5)
Free acid concentration in < neutralizing treatment and the relation > of solution ion strength
Fig. 3 represents the result evaluated the relation of free acid concentration when making free acid concentration (free acid concentration) change under condition similarly to Example 2 and solution ion strength.Ca (OH)
2before neutralization before interpolation, the ionic strength of liquid is up to 4.9, affects free acid, sulfate ion, chloride ion widely.By Ca (OH)
2interpolation, free acid concentration reduces, and sulfate ion becomes CaSO
42H
2o also precipitates, and therefore, the ionic strength of solution reduces.Learn: ionic strength when free acid concentration is 1.0mol/L is 1.4, when reducing free acid concentration further, sulfate ion reaction terminating, become superfluous Ca and dissolve, therefore, ionic strength raises.
(embodiment 6)
The relation > of < ionic strength and Ir charcoal absorption rate
About charcoal absorption, use liquid before the different absorption of ionic strength, after namely dropping into carried out the gac of deaeration with the ratio that is 4g relative to solution 100mL under condition similarly to Example 3, stir 24 hours, make Ir be adsorbed in gac.Fig. 4 represents result.Before absorption, the ionic strength of liquid and Ir adsorption rate see mutual relationship, the side that ionic strength is low, surely make Ir easily be adsorbed in gac.
(comparative example 1)
As Cu electrodeposit is carried out de-Cu leaching, potassium cloride, Au extract, SO
2trade effluent after reduction containing Ir acidic solution 200ml in, add Ca (OH)
2be 0.01mol/L to free acid concentration, by the acidic solution of filtered and recycled containing Ir.Table 6 represents liquid composition, Liquid distribution rate based on neutralization.When free acid concentration is 0.01mol/L, Ir concentration contained in liquid after neutralization is low, and 69.8% of Ir precipitates by neutralizing, and therefore, when containing the solution of Ir by filtered and recycled, Ir can only reclaim 30.2%.
[table 6]
(comparative example 2)
About charcoal absorption, under condition similarly to Example 3, use neutralizing treatment terminate after ionic strength be 3.17, free acid concentration is set as the absorption of 1.9mol/L before liquid carry out charcoal absorption.Table 7 represents result.Ir adsorption rate is 58.2%, can not reclaim Ir fully.Therefore, effectively can not reclaim Ir with liquid before the absorption that ionic strength is high, but sure reduce ionic strength by neutralizing, improve the adsorption rate of Ir thus.
[table 7]
Claims (4)
1. reclaim a recovery method of Ir from platinum group solution, it comprises following operation:
In and operation, make the neutralizing agent of sulfuric acid precipitation by interpolation in the acidic solution containing Ir and sulfuric acid and make the sulfate ion in acidic solution precipitate and be separated, make the free acid concentration in acidic solution be 0.03mol/L ~ 1.2mol/L, make the ionic strength in acidic solution reduce and reach less than 2; And
Charcoal absorption operation, leads to liquid in gac by the acidic solution containing Ir after neutralization, makes Ir be adsorbed in gac.
2. the recovery method reclaiming Ir from platinum group solution according to claim 1, wherein, described neutralizing agent comprises Ca (OH)
2, CaO, CaCO
3, Sr (OH)
2, SrO, SrCO
3in any one.
3. the recovery method reclaiming Ir from platinum group solution according to claim 1 and 2, wherein,
The described acidic solution containing Ir and sulfuric acid also containing the impurity of more than at least a kind that is selected from As, Cu, Fe, Ni, Zn, Bi, Pb, Te, Sn, Sb,
Also there is vulcanization process, described vulcanization process is before charcoal absorption operation, vulcanizing agent is added to the acidic solution containing Ir after described neutralization, thus the impurity of described more than at least a kind of being selected from As, Cu, Fe, Ni, Zn, Bi, Pb, Te, Sn, Sb is removed.
4. the recovery method reclaiming Ir from platinum group solution according to claim 3, described vulcanization process comprises the oxidation reduction potential control of the acidic solution containing Ir after by neutralization at 70 ~ 90mV.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2011-029892 | 2011-02-15 | ||
| JP2011029892A JP5220143B2 (en) | 2011-02-15 | 2011-02-15 | Method for recovering Ir from platinum group-containing solution |
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| Publication Number | Publication Date |
|---|---|
| CN102676835A CN102676835A (en) | 2012-09-19 |
| CN102676835B true CN102676835B (en) | 2015-06-10 |
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|---|---|
| JP (1) | JP5220143B2 (en) |
| KR (1) | KR101313474B1 (en) |
| CN (1) | CN102676835B (en) |
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| CN104451144A (en) * | 2014-12-07 | 2015-03-25 | 金川集团股份有限公司 | Method for reducing acidity of precursor feed liquid for extracting noble metals |
| JP6907791B2 (en) * | 2017-08-07 | 2021-07-21 | 住友金属鉱山株式会社 | How to recover iridium |
| CN107512813B (en) * | 2017-08-25 | 2020-11-03 | 金川集团股份有限公司 | Multi-way recycling method for acid-making wastewater of smelting flue gas |
| CN107445352B (en) * | 2017-09-28 | 2020-07-31 | 黄河三角洲京博化工研究院有限公司 | Innocent treatment process for acidic water of reforming device in petrochemical industry |
| CN108640390B (en) * | 2018-05-31 | 2021-10-22 | 阳谷祥光铜业有限公司 | Treatment method of antimony-containing wastewater |
| JP7183694B2 (en) * | 2018-10-25 | 2022-12-06 | 住友金属鉱山株式会社 | Ruthenium recovery method |
| CN110777259A (en) * | 2019-10-23 | 2020-02-11 | 金川集团股份有限公司 | Method for pre-treating platinum group metal refining tailings to enrich precious metals by fire method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2861370B2 (en) * | 1990-11-09 | 1999-02-24 | 三菱マテリアル株式会社 | Wastewater treatment method |
| JP2004190058A (en) * | 2002-12-09 | 2004-07-08 | Sumitomo Metal Mining Co Ltd | Method of separating and refining iridium |
| JP2010174336A (en) * | 2009-01-30 | 2010-08-12 | Nippon Mining & Metals Co Ltd | METHOD OF RECOVERING Ru AND/OR Ir FROM SOLUTION CONTAINING PLATINUM GROUP |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2941073B2 (en) * | 1991-02-01 | 1999-08-25 | 田中貴金属工業株式会社 | Method for separating platinum group metals |
| JPH11207365A (en) * | 1998-01-26 | 1999-08-03 | Ebara Corp | Treatment of selenium-containing waste water |
| JP2002194450A (en) * | 2000-12-27 | 2002-07-10 | Muromachi Chemical Kk | Selective adsorbent for platinum-group noble metal |
| JP4403259B2 (en) | 2004-03-23 | 2010-01-27 | Ｄｏｗａメタルマイン株式会社 | Method for recovering platinum group elements |
-
2011
- 2011-02-15 JP JP2011029892A patent/JP5220143B2/en not_active Expired - Fee Related
-
2012
- 2012-02-07 CN CN201210026237.8A patent/CN102676835B/en not_active Expired - Fee Related
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2861370B2 (en) * | 1990-11-09 | 1999-02-24 | 三菱マテリアル株式会社 | Wastewater treatment method |
| JP2004190058A (en) * | 2002-12-09 | 2004-07-08 | Sumitomo Metal Mining Co Ltd | Method of separating and refining iridium |
| JP2010174336A (en) * | 2009-01-30 | 2010-08-12 | Nippon Mining & Metals Co Ltd | METHOD OF RECOVERING Ru AND/OR Ir FROM SOLUTION CONTAINING PLATINUM GROUP |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102676835A (en) | 2012-09-19 |
| JP2012167334A (en) | 2012-09-06 |
| KR20120093792A (en) | 2012-08-23 |
| KR101313474B1 (en) | 2013-10-01 |
| JP5220143B2 (en) | 2013-06-26 |
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