WO2005040437A1 - Procede de traitement par voie humide de cendres volantes - Google Patents

Procede de traitement par voie humide de cendres volantes Download PDF

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Publication number
WO2005040437A1
WO2005040437A1 PCT/JP2004/016202 JP2004016202W WO2005040437A1 WO 2005040437 A1 WO2005040437 A1 WO 2005040437A1 JP 2004016202 W JP2004016202 W JP 2004016202W WO 2005040437 A1 WO2005040437 A1 WO 2005040437A1
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WO
WIPO (PCT)
Prior art keywords
filtrate
fly ash
residue
treatment
solid
Prior art date
Application number
PCT/JP2004/016202
Other languages
English (en)
Japanese (ja)
Inventor
Shuji Kuramochi
Taro Aichi
Hiroshi Asada
Hideki Yatsuduka
Kousuke Inoguchi
Tetsuo Dohi
Original Assignee
Dowa Mining Co., Ltd.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Dowa Mining Co., Ltd. filed Critical Dowa Mining Co., Ltd.
Publication of WO2005040437A1 publication Critical patent/WO2005040437A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/02—Working-up flue dust
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B19/00—Obtaining zinc or zinc oxide
    • C22B19/28—Obtaining zinc or zinc oxide from muffle furnace residues
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • C22B7/007—Wet processes by acid leaching
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J1/00—Removing ash, clinker, or slag from combustion chambers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE
    • B09B2101/00—Type of solid waste
    • B09B2101/30—Incineration ashes
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2900/00—Special arrangements for conducting or purifying combustion fumes; Treatment of fumes or ashes
    • F23J2900/01004—Separating water from ash
    • 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

Definitions

  • the present invention is a wet treatment for fly ash collected from combustion exhaust gas at the time of incineration of municipal waste etc., or fly ash collected from exhaust gas generated at the time of melting and processing ash and dust at the time of incineration More specifically, the present invention relates to a wet treatment method of separating and recovering heavy metals and gangue components contained in the fly ash in a form that can be effectively used.
  • Prior art
  • the heavy metal is leached out with mineral acid and then neutralized to form a neutralized sediment which is enriched with heavy metal, and this sediment is There is a method of separating and using it for non-ferrous kiln processes.
  • sulfuric acid or hydrochloric acid is generally used as the mineral acid from the viewpoint of processing cost.
  • the method using sulfuric acid is cheaper than the method using hydrochloric acid, but 13 and ⁇ a in the fly ash are not leached, so not only can the 13 The amount of residue will increase significantly. This is particularly problematic in fly ash with high Ca concentration. Although residues containing P b and gypsum can be used in the dry P b making process, there is also a problem that the treatment cost is increased due to the large amount of slag components (gypsum) and C a can not be used effectively. is there.
  • the present invention finds out a method of recovering Zn in fly ash in the most preferable form that can be used for the wet-Zn-making process. Was an issue.
  • the fly ash is subjected to acid leaching treatment using a hydrochloric acid solution of pH 3.5 or less, and a neutralizing agent is added to the treatment solution.
  • a neutralizing agent is added to the treatment solution.
  • the fly ash to be subjected to the acid leaching treatment is one that has been previously washed with washing water that does not exceed pH 10.
  • the filtrate L 3 is recycled for acid leaching treatment.
  • FIG. 1 is a view showing an example of the treatment flow of the wet treatment method of fly ash according to the present invention.
  • FIG. 2 is a diagram showing an example flow of the wet processing method of fly ash according to the present invention.
  • the fly ash to be treated in the present invention is collected from the exhaust gas from a combustion furnace, an incinerator, a melting furnace and the like, and is usually collected by a bag filter or an electric collector installed in the exhaust gas passage. Ru.
  • the present invention treats fly ash collected from exhaust gas from general waste incinerators and fly ash collected from exhaust gas when slag (including the above-mentioned fly ash) is slagged in an ash melting furnace. Exhaust gas dusts similar to this can be treated.
  • An example of the fly ash processing flow according to the present invention is shown in FIG.
  • the fly ash as described above is used as a starting material in the present invention, but as shown in FIG. 1, it is preferable to first wash it.
  • the leaching treatment of fly ash with a hydrochloric acid solution is carried out using a hydrochloric acid solution having a ⁇ 4 or less, preferably ⁇ 3 ⁇ , and more preferably ⁇ 3 or less.
  • a hydrochloric acid solution regenerated aqueous hydrochloric acid obtained in the final step of the present invention can be used. Although some of the heavy metal ions, Ca, etc. may be entrained in the regenerated hydrochloric acid solution, these are also recovered during the treatment process and hydrochloric acid will be recycled. It contributes to the improvement of the collection rate of metals and the cost reduction.
  • This acid leaching process is stirred in the leacher. It is preferable to carry out under stirring.
  • the temperature of the leaching treatment is from room temperature to 80 ° C., and the treatment time is suitably from 30 to 6 Q minutes.
  • the treated solution is subsequently sent to the neutralization tank and subjected to the neutralization 1 treatment.
  • a neutralizing agent is added to the acid leached solution, and the pH of the solution is adjusted to the range of 3.5 to 5 to form a neutralized precipitate.
  • the treatment temperature may be from normal temperature to 80 ° C.
  • a neutralizing agent use of calcium carbonate aqueous solution is desirable.
  • the treated liquid is directly sent to the neutralization step to carry out the treatment of neutralization 1 without taking treatment or operation to separate the leaching residue from the liquid.
  • the neutralized precipitate generated by the treatment is separated simultaneously with the leaching residue from the previous hydrochloric acid leaching treatment and separated simultaneously. It was found that the filterability is greatly improved by the simultaneous solid-liquid separation compared to the case where the acid leaching residue and the neutralized precipitate are separated individually (Comparative Example 1 described later). It is believed that this is because the leaching residue acts as a filter aid.
  • This solid-liquid separation can be performed, for example, using a filter-press, and this solid-liquid separation gives a filtrate L 1 and a residue P 1 (a gangue-based residue).
  • Filtrate L 1 is then subjected to the treatment of neutralization 2 which adds a neutralizing agent to neutralize in the region of pH> 5, preferably to a pH greater than 5 to 9.
  • the treatment temperature may be from normal temperature to 80 ° C. It is preferable to use an aqueous solution of calcium hydroxide as a neutralizing agent. By the treatment of this neutralization 2, heavy metal ions in the solution are precipitated, and Ca ions remain dissolved in the solution as calcium chloride.
  • the slurry obtained after neutralization 2 treatment is subjected to solid-liquid separation to obtain filtrate L 2 and residue P 2.
  • the filtrate L 2 contains a large amount of calcium chloride and metal ions such as Zn, P b and C u.
  • the species contains only traces, and these heavy metals such as Zn, Pb, and Cu shift to residue P2 with high yield.
  • the residue P 2 contains a high concentration of Z n, It is useful as a raw material or concentrate for zinc wet steelmaking because it is accompanied by P b and C u and contains almost no C a, S i and alkali components. For this reason, residue P 2 can be subjected to zinc kneading as a raw material having economic value, and Z n in fly ash is recovered as high purity Z n, and heavy metals such as P b and C u are also recovered. Collected together.
  • the filtrate L2 contains a large amount of calcium chloride. Therefore, by adding sulfuric acid to this filtrate L2, gypsum is deposited, and the solution after the deposition of gypsum becomes a hydrochloric acid solution. This gypsum suspension is separated into solid and liquid to obtain filtrate L 3 and 2 hydrogypsum.
  • the filtrate L 3 can be reused in the leaching step as a regenerated hydrochloric acid aqueous solution.
  • solid content can be recovered as high-quality, high-quality dihydrate gypsum.
  • it is preferable to control the concentration of hydrochloric acid so that the solubility of gypsum decreases as the filtrate L3.
  • the solubility of gypsum in the hydrochloric acid regeneration solution can be reduced, and this regenerated hydrochloric acid is repeatedly used in the leaching step. Also, less gypsum is precipitated in the leaching residue, and the amount of residue generation can be reduced.
  • Fly ash A and B generated from a melting furnace that slags incinerated ash and fly ash, and fly ash derived from a direct melting furnace that enables direct melting and slagging of incinerated ash generated during general waste incineration C And D were mixed equally to make a mixed fly ash.
  • the grade of these fly ash A to E is shown in Table 1.
  • the process was carried out according to the flow shown in Fig.2.
  • the mixed fly ash E was washed with water to obtain the washed fly ash of the grade shown in Table 3.
  • the washing water used for washing was waste water generated from the zinc-making process, and hydrochloric acid was added so that the pH of the treatment solution was 1 Q.
  • the pulp concentration at washing was 300 g / L.
  • the water removal process resulted in a removal rate of 27.2%, a removal rate of Na of 74.1%, and a removal rate of K of 76%, as shown in Table 3. Heavy metals are not eluted.
  • the hydrochloric acid solution was prepared as follows. First, measure 4 g of sodium chloride 41 g and 222 g of calcium chloride to make an 8-litre aqueous solution. To this, add 22 9 mL of 98% concentrated sulfuric acid, mix and stir well, and then solid-liquid separate (filter) the formed white precipitate (gypsum: C a S 0 4 ⁇ 2 H 20). Obtain 6.5 liters of filtrate. Perform the same operation 3 times to obtain a total filtrate of 19.5 liters. It can be said that this solution contains hydrogen chloride with an acid concentration of 1N (standard: molar ZL).
  • Table 4 shows the grade and volume of the acid leaching simulant used.
  • the acid leaching treatment leached the washed fly ash in a stirred tank using the above-mentioned simulated hydrochloric acid solution in an amount of 6.5 L per 1 kg of dry washed fly ash.
  • a hydrochloric acid solution was added to maintain the pH of the treatment solution at 2.0.
  • the treated solution after leaching with hydrochloric acid was subsequently subjected to the treatment of neutralization 1.
  • neutralization 1 an aqueous solution of calcium carbonate of 16.7 wt% was added so that the pH of the treatment solution would be 4.0.
  • an aqueous solution of calcium carbonate was used in an amount of 0.33 75 liters per 1 kg of the washed and washed fly ash.
  • the solution after this neutralization treatment was introduced into a pressure filter, and solid-liquid separation was carried out by this pressure filter into a filtrate L1 and a residue P1 as shown in FIG.
  • the quality and quantity of the filtrate L 1 are shown in Table 5, and the grade and quantity of the residue P 1 (unwashed) are shown in Table 6.
  • zinc in fly ash remains in the filtrate L 1 side, and copper and lead also remain in the filtrate L 1 side in a large amount, but Si and C a are residues P 1 side Migrate to a lot.
  • the residue P 1 is a gangue-type residue having a high content of Si and Ca.
  • This gangue-based residue can be disposed of for disposal, but it can also be subjected to leaching treatment to further recover Zn, Pb, Cu, etc. coexisting in it.
  • Table 7 shows the grade and quantity of filtrate L2
  • Table 8 shows the grade and quantity of residue P2 (after water washing).
  • zinc shifts to residue P2 and only trace amount remains in filtrate L2.
  • Si, Na, and K in the residue P 2 are all less than 0.2%, and about 0.3% of Ca. Therefore, the residue P 2 is a zinc-rich residue rich in heavy metals, and is similar to high-grade zinc concentrates with less algal components and gangue components, and is suitable as a raw material for wet production of zinc is there.
  • Table 11 shows the recovery rates of Z n, P b and C u at each step performed in this example.
  • Z n, P b and C u in fly ash are collected with high recovery in residue P2.
  • the second treatment was performed in the same manner as described above except that the filtrate L 3 was used instead of the hydrochloric acid simulation solution used initially, but it was confirmed that the same result as the first was obtained. It was done.
  • the results of recovery of Z n, P b and C u at the second acid leaching and neutralization two steps were similar to those of the first one from the values shown in Table 11 as well. I understand.
  • Example 1 After acid leaching treatment, solid-liquid separation (referred to as intermediate solid-liquid separation) with a pressure filter is carried out prior to neutralization 1 treatment, and the filtrate obtained by this intermediate solid-liquid separation is neutralized 1 Example 1 was repeated, except that the process was performed.
  • the filtration rate under pressure of 0.3 MPa in the intermediate solid-liquid separation is 3 to 10 L / mVmin
  • the water content in the residue is 30 to 40%
  • the solid after the neutralization 1 treatment is
  • the filtration rate under a pressure of 0.5 MPa was 1.5 to 5.5 L / m 2 / min
  • the water content in the residue was 45 to 70%.
  • the filtration rate of the both is very slow as compared with the filtration rate of 15 to 18 L / mV min in solid-liquid separation after the neutralization 1 treatment of Example 1.
  • Example 1 rather than performing neutralization after separation of the acid leaching residue as in this example, it can be seen that if the acid leaching residue and the neutralized precipitate are simultaneously separated by solid-liquid separation, the filterability will be better and the operability will be improved.

Abstract

L'invention concerne un procédé de traitement par voie humide d'une cendre volante, qui consiste à soumettre une cendre volante provenant d'un gaz de carneau produit lors de l'incinération de déchets urbains ou analogues à un traitement de lixiviation au moyen d'une solution acide d'acide chlorhydrique à pH de 3 ou moins, à ajouter un agent neutralisant dans le fluide obtenu et à neutraliser le fluide afin d'obtenir un pH supérieur à 3,5 et 5 ou inférieur et à soumettre ce fluide à une séparation solide-liquide en vue d'obtenir un filtrat (L1) et un résidu à base de gangue (P1); à ajouter un agent neutralisant au filtrat susmentionné (L1) afin de neutraliser le filtrat de sorte à atteindre un pH supérieur à 5 et 9 ou inférieur et à soumettre le fluide obtenu à une séparation liquide-solide afin d'obtenir un filtrat (L2) et un résidu riche en zinc (P2); à ajouter de l'acide sulfurique au filtrat susmentionné (L2) et à soumettre le fluide obtenu à une séparation liquide-solide afin d'obtenir un filtrat (L3) et un résidu à base de gypse (P3). Le résidu précipité de neutralisation susmentionné (P2) est riche en zinc ainsi qu'en d'autres métaux lourds, et contient une faible quantité de Si, de La et analogue, c'est pourquoi il présente une qualité suffisante à alimenter en matériau brut le procédé de raffinage de zinc par voie humide.
PCT/JP2004/016202 2003-10-27 2004-10-26 Procede de traitement par voie humide de cendres volantes WO2005040437A1 (fr)

Applications Claiming Priority (2)

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JP2003-365706 2003-10-27
JP2003365706A JP4431767B2 (ja) 2003-10-27 2003-10-27 飛灰の湿式処理法

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Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2921715A1 (fr) * 2007-09-28 2009-04-03 Lab Sa Sa Procede pour la detoxification et pour l'extraction des metaux de machefers et de cendres volantes issus de l'incineration
CN104388685A (zh) * 2014-10-30 2015-03-04 株洲冶炼集团股份有限公司 从氧化锌烟灰中回收碲铜铋的方法
WO2018029290A1 (fr) * 2016-08-11 2018-02-15 Stena Recycling International Ab Co-traitement de déchets de nettoyage de gaz de combustion et de liquide épurateur acide
EP3556468A1 (fr) * 2018-04-19 2019-10-23 OiW Process AS Procédé et appareil de formation d'une suspension de cendres volantes partiellement dissoutes dans un acide minéral
NO20210383A1 (en) * 2021-03-24 2022-09-26 Noah Solutions As Method and apparatus for neutralizing and stabilizing of fly ash

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110607454B (zh) * 2019-09-29 2021-03-23 新中天环保股份有限公司 一种从垃圾焚烧二次飞灰中提取重金属的方法
KR102186054B1 (ko) * 2020-05-25 2020-12-07 (주)에코이노베이션 중금속을 포함하는 비산재의 재활용 처리장치 및 그 처리방법

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JPS49110518A (fr) * 1973-02-24 1974-10-21
JPH06170354A (ja) * 1992-12-02 1994-06-21 Dowa Mining Co Ltd 焼却炉および溶融炉からの飛灰の処理方法
JPH08117724A (ja) * 1994-10-26 1996-05-14 Dowa Mining Co Ltd 焼却炉または溶融炉からの飛灰の処理方法
JPH09316557A (ja) * 1996-05-29 1997-12-09 Mitsubishi Heavy Ind Ltd 飛灰からの有価物回収方法
JPH11128872A (ja) * 1997-10-29 1999-05-18 Furukawa Co Ltd 溶融飛灰の水洗い処理設備
JP2000054038A (ja) * 1998-08-10 2000-02-22 Ebara Corp カルシウム含有焼却飛灰及び溶融飛灰の処理方法
JP2000109938A (ja) * 1998-10-01 2000-04-18 Mitsubishi Materials Corp 飛灰からの有価金属回収方法
JP2000140795A (ja) * 1998-11-13 2000-05-23 Dowa Mining Co Ltd 重金属含有飛灰の処理方法
JP2000354843A (ja) * 1999-06-16 2000-12-26 Chiyoda Corp 重金属類を含む固体の処理方法および処理システム
JP2001087739A (ja) * 1999-09-27 2001-04-03 Dowa Mining Co Ltd 飛灰からの重金属回収方法
JP2002316123A (ja) * 2002-02-15 2002-10-29 Dowa Mining Co Ltd 焼却炉および溶融炉からの飛灰の処理方法
JP2003027153A (ja) * 2001-07-19 2003-01-29 Hitachi Zosen Corp 飛灰からの重金属の回収方法

Patent Citations (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS49110518A (fr) * 1973-02-24 1974-10-21
JPH06170354A (ja) * 1992-12-02 1994-06-21 Dowa Mining Co Ltd 焼却炉および溶融炉からの飛灰の処理方法
JPH08117724A (ja) * 1994-10-26 1996-05-14 Dowa Mining Co Ltd 焼却炉または溶融炉からの飛灰の処理方法
JPH09316557A (ja) * 1996-05-29 1997-12-09 Mitsubishi Heavy Ind Ltd 飛灰からの有価物回収方法
JPH11128872A (ja) * 1997-10-29 1999-05-18 Furukawa Co Ltd 溶融飛灰の水洗い処理設備
JP2000054038A (ja) * 1998-08-10 2000-02-22 Ebara Corp カルシウム含有焼却飛灰及び溶融飛灰の処理方法
JP2000109938A (ja) * 1998-10-01 2000-04-18 Mitsubishi Materials Corp 飛灰からの有価金属回収方法
JP2000140795A (ja) * 1998-11-13 2000-05-23 Dowa Mining Co Ltd 重金属含有飛灰の処理方法
JP2000354843A (ja) * 1999-06-16 2000-12-26 Chiyoda Corp 重金属類を含む固体の処理方法および処理システム
JP2001087739A (ja) * 1999-09-27 2001-04-03 Dowa Mining Co Ltd 飛灰からの重金属回収方法
JP2003027153A (ja) * 2001-07-19 2003-01-29 Hitachi Zosen Corp 飛灰からの重金属の回収方法
JP2002316123A (ja) * 2002-02-15 2002-10-29 Dowa Mining Co Ltd 焼却炉および溶融炉からの飛灰の処理方法

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2921715A1 (fr) * 2007-09-28 2009-04-03 Lab Sa Sa Procede pour la detoxification et pour l'extraction des metaux de machefers et de cendres volantes issus de l'incineration
EP2042246A3 (fr) * 2007-09-28 2014-02-19 Lab Sa Procédé pour la détoxification et pour l'extraction des métaux de machefers et de cendres volantes issus de l'incinération
CN104388685A (zh) * 2014-10-30 2015-03-04 株洲冶炼集团股份有限公司 从氧化锌烟灰中回收碲铜铋的方法
WO2018029290A1 (fr) * 2016-08-11 2018-02-15 Stena Recycling International Ab Co-traitement de déchets de nettoyage de gaz de combustion et de liquide épurateur acide
EP3556468A1 (fr) * 2018-04-19 2019-10-23 OiW Process AS Procédé et appareil de formation d'une suspension de cendres volantes partiellement dissoutes dans un acide minéral
WO2019201919A1 (fr) * 2018-04-19 2019-10-24 Oiw Process As Procédé et appareil pour former une suspension de cendres volantes partiellement dissoutes dans un acide minéral
NO20210383A1 (en) * 2021-03-24 2022-09-26 Noah Solutions As Method and apparatus for neutralizing and stabilizing of fly ash
WO2022203517A1 (fr) * 2021-03-24 2022-09-29 Noah Solutions As Procédé et appareil de neutralisation et de stabilisation de cendres volantes

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JP4431767B2 (ja) 2010-03-17

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