CN103889906A - Method for processing contaminated brine solutions for chlor-alkali electrolysis - Google Patents

Method for processing contaminated brine solutions for chlor-alkali electrolysis Download PDF

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CN103889906A
CN103889906A CN201280028114.6A CN201280028114A CN103889906A CN 103889906 A CN103889906 A CN 103889906A CN 201280028114 A CN201280028114 A CN 201280028114A CN 103889906 A CN103889906 A CN 103889906A
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CN103889906B (en
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沃尔特·坎茨勒
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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
    • C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/14—Purification
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D3/00—Halides of sodium, potassium or alkali metals in general
    • C01D3/14—Purification
    • C01D3/16—Purification by precipitation or adsorption
    • 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
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C02F1/727—Treatment of water, waste water, or sewage by oxidation using pure oxygen or oxygen rich gas
    • 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
    • C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers
    • 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
    • C02F2101/30—Organic compounds
    • C02F2101/34—Organic compounds containing oxygen
    • 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
    • C02F2101/30—Organic compounds
    • C02F2101/36—Organic compounds containing halogen
    • 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
    • C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
    • C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
    • 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
    • C02F2209/02—Temperature
    • 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
    • C02F2209/03—Pressure
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/06—Pressure conditions
    • C02F2301/066—Overpressure, high pressure
    • 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
    • C02F2303/16—Regeneration of sorbents, filters
    • 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
    • C02F2303/18—Removal of treatment agents after treatment
    • 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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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
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  • Environmental & Geological Engineering (AREA)
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Abstract

The invention relates to a novel method for removing TOC and AOX from brine, which arises for example in the production of epichlorohydrin, by means of high-pressure wet oxidation with iron(II) salts as catalysts and oxygen as an oxidant at temperatures of 170 to 260 DEG C. The pH value of the brine is set to less than 2 and the brine is brought to a pressure of 30 to 60 bar. Said oxidation leads to acetic acid, which in a second method step is adsorbed from the brine onto synthetic activated carbon, while the catalyst salts are precipitated in a last method step. After the pH value has been raised, the iron salts are removed.

Description

Pre-treatment is for the method for chloro-basic metal-electrolytical contaminated salt brine solution
In saponification-process, for example, in preparing epoxy chloropropane, concentrated salt-the solution of main generation more or less, be salt solution, this salt solution does not allow to be discharged in drainage tray, because wherein also have the impurity of hydrocarbonaceous or halon (mostly time be chlorinated hydrocarbon) except salts contg.On the other hand, salt solution-solution is not usually containing inorganic impurity, and this makes to be become a kind of for chloro-basic metal-electrolytical potential raw material.
Therefore, the object of the invention is, such salt solution is purified, it can be served as for electrolytical raw material.
In preparing epoxy chloropropane, can produce salt solution, described saline bag is polluted containing the NaCI of about 20 % by weight and the about 8000mg/L TOC being caused by glycerine, epoxy chloropropane and dichlorohydrine.Due to high salts contg, salt solution only just can enter among traditional biological sewage refining plant after being diluted about 20-100 times.
In preparing epoxy resin, also can produce similar salt solution-solution, wherein by sodium hydroxide solution, chlorine atom be split off from epoxy chloropropane equally.The traditional wet oxidation style and the electrolytic oxidation method that for example utilize superoxide, hypochlorite, UV and ozone to carry out are eliminated because efficiency is low.In these methods,, in the time being applied to salt solution, preferably producing chlorine and TOC and AOX and be only decomposed with faint degree.
The pressure oxidation method corresponding to prior art according to for example DE102006001955 is to work by solid catalyst, does not possess required transformation efficiency for salts solution, because catalyzer is because the hydrochloric acid forming can not reach time limit of service.Those adopt the method for hydrogen peroxide as oxygenant, for example, according to EP0680931, can not in salt brine solution, realize significant transformation efficiency.
US6139755 utilizes free radical-initiator, catalyzer and oxygen at the temperature of 80-140 DEG C, to process community's waste water, wherein uses metal-salt as catalyzer and uses hydrogen peroxide as free radical-initiator.Relate to significantly one " Fenton-reaction " here.This method is invalid for salt solution.But surprisingly find according to the present invention, iron (II)-salt (>220 DEG C) at higher temperature also can make TOC and AOX, especially glycerine, epoxy chloropropane and dichlorohydrine oxidation in salt solution by oxygen.
According to the present invention by utilizing at least one oxygen containing gas, preferably oxygen, the method of the hydrocarbon in salt solution and chlorinated hydrocarbon oxidation can be realized this purpose by high-pressure oxidation by catalysis, described method is characterised in that, by at least one acid, preferred hydrochloric acid is adjusted to pH value by the pH-value of salt solution and is less than 2, add the iron(ic) chloride (II) of 40-400mg/L to salt solution, salt solution is placed in to the pressure of 30-60 bar, by one or more interchanger (W1, W2) brine preheating is had to oxygen containing gas to 170-260 DEG C and salt solution, preferably having the mode with direct current in the reactor (R1) of oxygen flows from bottom to top, salt solution by reaction be heated to 240-275 DEG C and the reaction product that produces in oxidising process (preferably acetic acid) cooling in interchanger (W1) after, preferably by untreated salt solution or crude brine, decompression (V1) and degassed (B1) is attracted to adsorber (A11, A12) on, then by add alkali pH-value is increased to after 10, by iron (II)-and iron (III)-salt separate.
The test of being undertaken by interpolation strong oxidizer in subcritical range shows, also can in the situation that not generating chlorine, in salt solution, decompose TOC.But the shortcoming of this method is, salt does not dissolve and stops up reactor and there is no in addition to meet the material of these conditions in subcritical range.
Therefore, finding effective catalyst moderate and that can again be separated after reaction always.Wherein the iron of chloride form (II) proves best solution.Until reaction finishes, the major part of catalyzer own is converted to iron (III).Can the reaction end temp in reactor be dropped to 240-275 DEG C according to component by adding iron(ic) chloride (II) in either case.Because the reaction heat in the time decomposing TOC and AOX can improve 10-100 DEG C (depending on the pollution level of salt solution) by the temperature in reactor, so the input temp entering in reactor must be only between 170-250 DEG C.
For the salt solution from epoxy chloropropane preparation process, be 200 DEG C and be 260 DEG C at reactor outlet in the optimum temps situation of Reactor inlet.Concentration the best of catalyzer is about 100mg/L iron(ic) chloride (II).Higher concentration can not brought obviously higher transformation efficiency.
Temperature in reactor can not be brought up to more than 270 DEG C, even if because best titanium alloy also can lose efficacy in the time exceeding this temperature.
The transformation efficiency of AOX is actual is in these trials that 100%, TOC only has 90% to be decomposed.This is because oxidising process is in most of the cases to be undertaken by acetic acid by different intermediate stages and approach, and acetic acid is because the stability of molecule is just partly oxidized under set condition.After reaction, starting ingredient, for example glycerine, epoxy chloropropane and dichlorohydrine can only be detected more micro-ly.
In known wet oxidation process, do not have a kind of method can make the acetic acid oxidation in salt solution.
Can be further by 90% acetic acid separated by liquid-liquid-extraction process separating acetic acid.99% TOC is separated still still very little, because chloro-basic metal now-electrolytical diaphragm can only bear at most 5-10mg/LTOC.
Therefore, attempted various commercial sorbent material, but they can not realize this purpose economically.Therefore surprisingly, synthetic " gac ", especially can make the content of acetic acid reach maximum 3 % by weight taking hot coking ion-exchanger LewatitAF5 as basic composite reactive charcoal by absorption.This is due to due to its synthetic preparation, uniformly pore structure and high internal surface area.Wherein absorption must be that in acid range, to carry out and regenerate be that sodium hydroxide solution by diluting carries out according to conventional adsorption method, 2-bed-exchange process that for example those skilled in the art are familiar or have the 3-bed-method of adsorber, polisher, revivifier.
According to the present invention or by ion-exchanger or by filtering, iron is separated.In both cases, for being separated completely, iron (II) pH-value must be increased to 7.5-8.
Advantage according to the inventive method is, except iron-ion not among hetero-ion enters system, thereby can be reduced at widely the salt water pretreatment (Soleaufbereitung) in chloro-basic metal-ionogen.
For the application that only need to purify 90% salt solution, for example, in the time can not using salt solution and for example salt solution be entered in seawater, can cancel the absorption phase of acetic acid.
Preferably in salt solution, add 80-100mg/L iron(ic) chloride (II) within the scope of the present invention.
In addition can be by with reacting of oxygen, salt solution being heated to 250-270 DEG C, preferably 260 DEG C.
As mentioned above, advantageously use composite reactive charcoal, especially using hot coking ion exchange resin (LewatitAF5) as basic composite reactive charcoal is as sorbent material.
In addition advantageously, after being adsorbed on sorbent material, the pH-value of salt solution is adjusted to 3-10, especially 5-10, and preferably 7.5.
Advantageously verified aspect oxygen-conveying, add a small amount of, preferred maximum 20% oxygen containing gas of total amount, preferably oxygen to crude brine before crude brine being put into interchanger (W1).
For reproducing adsorbent preferred design, described salt solution is cooled to below 40 DEG C after degassed (B1), especially below 30 DEG C and alternately by the sodium hydroxide solution of dilution, especially use the NaOH of 1-5 % by weight, preferably make the adsorbent reactivation in adsorber with the sodium hydroxide solution of 4 % by weight.As for iron is separated, effectively, by the ion-exchanger of alternately regenerating, for example (Lewatit TP207) carries out.
In addition, also advantageously design, the pH-value of salt solution is increased to 1-2.5, preferably 1.3-1.5, make in the first ion-exchange stage, iron (III) composition to be isolated from salt solution, afterwards the pH-value of salt solution is increased to 3.0-5.0, preferably 3.3-4 and iron (II) being separated from salt solution in the second ion-exchange stage.
Can, after improving the pH-value of salt solution, especially after neutralization, by filtering, iron be separated as a supplement.
Finally it is pointed out that when salt solution be to be discharged into drainage tray and the conversion that realizes in high pressure-oxidising process fully time, can cancel absorption phase, especially charcoal absorption-stage.
Application example:
From epoxy resin preparation process, salt-content is the 1m of 21 % by weight 3/ h salt solution is polluted by the TOC of 4000mg/L.TOC respectively accounts for half by glycerine and epoxy chloropropane and forms.To iron(ic) chloride (II) and the adjusting pH<2 of salt solution admixture 100mg/L.High pressure-pump P1 pressure is increased to 50 bar and before aheat exchanger W1 under the pressure of 55 bar with 5Nm 3the flow of/h adds content and reaches 98% oxygen.Be increased to 210 DEG C and be increased to 215 DEG C in the mesohalobic temperature of well heater W2 of the saturated vapo(u)r with 40 bar in the mesohalobic temperature of interchanger W1 from 40 DEG C.Salt solution after heating enters in reactor now, in the ingress of reactor again with 15Nm 3the flow of/h adds content and reaches 98% oxygen.It is 2.8 hours with the residence time that the height of reactor is 9 meters.Salt solution is heated to 260 DEG C by reaction heat.At this moment the TOC transforming reaches 89%, and the AOX transforming reaches >99.9%.
The treated salt solution that carrys out autoreactor is cooled to heat release to be less than 90 DEG C to crude brine and in this process in interchanger W1, the gas comprising, the CO for example forming 2be separated in pressure reduction vessel B1 with excessive oxygen, salt solution enters and is filled with taking hot coking ion-exchanger (LewatitAF5) in the adsorber A11 of basic composite reactive charcoal.TOC before adsorber A11 (acetic acid) is 440mg/L and after adsorber, is 3mg/L.In the time that adsorber A11 moves, utilize the sodium hydroxide solution of 4 % by weight to make adsorber A12 regeneration.After moving 8 hours, between adsorber, switch.Adsorber A11 is in reproduced state, and adsorber A12 adsorbs.After adsorber, make pH-value rise to 7.5 and iron-ion is separated from salt solution by the sodium hydroxide solution of 4 % by weight, until its content is less than 0.3mg/L.Separation is to carry out on ion-exchanger (Lewatit TP207).Ion-exchanger is to be equally to be undertaken by 2% hydrochloric acid with the operation of 2-bed-exchange process and regeneration with adsorber.

Claims (11)

1. by least one oxygen containing gas, preferably oxygen, by the high-pressure oxidation of catalysis by the method for the hydrocarbon in salt solution and chlorinated hydrocarbon oxidation, it is characterized in that, by at least one acid, preferably hydrochloric acid, the pH-value of described salt solution is adjusted to the pH-value that is less than 2, add the iron(ic) chloride (II) of 40-400mg/L to described salt solution, described salt solution is placed in to the pressure of 30-60 bar, passed through one or more interchanger (W1, W2) be preheating to 170-260 DEG C and there is oxygen containing gas, preferably in the reactor (R1) of oxygen, flow with direct current from bottom to top, be heated to 240-275 DEG C and by the reaction product producing by described reaction in oxidation, preferably acetic acid, preferably by untreated salt solution or crude brine, after decompression (V1) and degassed (B1) is cooling in interchanger (W1), be attracted to adsorber (A11, A12) on, then by add alkali pH-value is increased to after 10, by iron (II)-and iron (III)-salt separate.
2. method according to claim 1, is characterized in that, adds 80-100mg/L iron(ic) chloride (II) to described salt solution.
3. method according to claim 1 and 2, is characterized in that, by described salt solution being heated to 250-270 DEG C with reacting of oxygen, preferably 260 DEG C.
4. according to the method described in any one in claim 1-3, it is characterized in that, use composite reactive charcoal, especially using hot coking ion exchange resin (LewatitAF5) as basic composite reactive charcoal is as sorbent material.
5. according to the method described in any one in claim 1-4, it is characterized in that, after being adsorbed onto on sorbent material, the pH-value of described salt solution is adjusted to 3-10, especially 5-10, and preferably 7.5.
6. according to the method described in any one in claim 1-5, it is characterized in that, add a small amount of, preferred maximum 20% oxygen-containing gas of total amount, preferably oxygen to crude brine before crude brine being put into interchanger (W1).
7. according to the method described in any one in claim 1-6, it is characterized in that, described salt solution is cooled to and is less than 40 DEG C after described degassed (B1), especially be less than 30 DEG C and alternately by dilution sodium hydroxide solution, especially the sodium hydroxide solution of 1-5 % by weight, preferably the sodium hydroxide solution of 4 % by weight makes the adsorbent reactivation in adsorber.
8. according to the method described in any one in claim 1-7, it is characterized in that, by the ion-exchanger of alternately regenerating, for example Lewatit TP207 separates iron (iron-II, iron-HI).
9. according to the method described in any one in claim 1-8, it is characterized in that, the pH-value of described salt solution is increased to 1-2.5, preferably 1.3-1.5, make in the first ion-exchange stage, iron (III) composition to be separated from salt solution, afterwards the pH-value of described salt solution is increased to 3.0-5.0, preferably 3.3-4, and in the second ion-exchange stage, iron (II) is separated from described salt solution.
10. according to the method described in any one in claim 1-9, it is characterized in that, after improving the pH-value of described salt solution, especially after the described salt solution of neutralization, by filtering, iron is separated.
11. according to the method described in any one in claim 1-10, it is characterized in that, when the conversion that described brine discharge is realized to drainage tray and in high pressure-oxidising process is fully time, cancels absorption phase, especially gac-stage.
CN201280028114.6A 2011-06-07 2012-06-06 Method for processing contaminated brine solutions for chlor-alkali electrolysis Active CN103889906B (en)

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AT8392011A AT511354B1 (en) 2011-06-07 2011-06-07 METHOD FOR THE PREPARATION OF POLLUTED SOLUTIONS FOR CHLORINE ALKALI ELECTROLYSIS
ATA839/2011 2011-06-07
PCT/AT2012/000163 WO2012167297A1 (en) 2011-06-07 2012-06-06 Method for processing contaminated brine solutions for chlor-alkali electrolysis

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CN105621764A (en) * 2016-03-17 2016-06-01 浙江奇彩环境科技股份有限公司 Treatment process of epoxy chloropropane production wastewater
CN105645624A (en) * 2014-11-13 2016-06-08 中国科学院大连化学物理研究所 Resource utilization method for high-salt wastewater from epichlorohydrin preparation through glycerol method
CN109071288A (en) * 2016-04-27 2018-12-21 沃尔特·坎茨勒 Method for aoxidizing hydrocarbon in saline solution etc.
CN114684966A (en) * 2022-04-02 2022-07-01 浙江晶立捷环境科技有限公司 Resource system and method for rosemary lipid solubility extraction wastewater

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CN110316808B (en) * 2019-07-16 2021-05-07 北京理工大学 Method and apparatus for treating organic wastewater by catalytic wet oxidation
CN112159037B (en) * 2020-09-25 2021-08-24 南京大学 Dai serge high concentration organic wastewater pretreatment device
CN112591767B (en) * 2020-12-03 2022-12-20 山东智永化工产业技术研究院有限公司 Method for treating chemical waste salt by high-temperature melting

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CN101601998A (en) * 2009-06-11 2009-12-16 浙江省环境保护科学设计研究院 A kind of Preparation of catalysts method that is used for treating high-concentration organic wastewater through catalytic oxidation
CN101798154A (en) * 2009-12-30 2010-08-11 宁波东港电化有限责任公司 Method for processing wastewater produced in saponification cyclization step in epoxy chloropropane production method

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CN105645624A (en) * 2014-11-13 2016-06-08 中国科学院大连化学物理研究所 Resource utilization method for high-salt wastewater from epichlorohydrin preparation through glycerol method
CN105621764A (en) * 2016-03-17 2016-06-01 浙江奇彩环境科技股份有限公司 Treatment process of epoxy chloropropane production wastewater
CN105621764B (en) * 2016-03-17 2018-05-15 浙江奇彩环境科技股份有限公司 A kind for the treatment of process of epoxychloropropane production waste water
CN109071288A (en) * 2016-04-27 2018-12-21 沃尔特·坎茨勒 Method for aoxidizing hydrocarbon in saline solution etc.
CN109071288B (en) * 2016-04-27 2022-06-03 沃尔特·坎茨勒 Method for oxidizing hydrocarbons and the like in brine solution
CN114684966A (en) * 2022-04-02 2022-07-01 浙江晶立捷环境科技有限公司 Resource system and method for rosemary lipid solubility extraction wastewater
CN114684966B (en) * 2022-04-02 2023-10-20 浙江晶立捷智能科技有限公司 Recycling system and method for rosemary fat-soluble extraction wastewater

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AT511354B1 (en) 2012-11-15

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