• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The present invention relates to a process for the preparation of calcium monohydrogenphosphate comprising an attack in an aqueous medium, for a predetermined period of time, of a phosphate source by an acid with formation of a pulp comprising an aqueous phase containing phosphate of calcium in solution and a solid phase containing impurities, a first separation between said aqueous phase and said solid phase, during a predetermined period of time, a neutralization of said aqueous phase at a pH sufficient to obtain a precipitation of said calcium monohydrogenphosphate, a second separation between said aqueous medium and said calcium monohydrogenphosphate, characterized in that said first separation of said step b) is carried out at a filtration rate of at least 0.1 tons of P2O5 / √ △ P / m2 / day .
    公开号:BE1025288B1
    申请号:E2017/5456
    申请日:2017-06-27
    公开日:2019-01-15
    发明作者:Tibaut THEYS；Thomas Henry
    申请人:Prayon Technologies；
    IPC主号:
    专利说明:

    ’’ PROCESS FOR THE PREPARATION OF MONÇHYDROGENOPHOSPHATE DEÇALÇjUM
    The present invention relates to a process for the preparation of calcium monohydrogen phosphate or dicalcium phosphate comprising the steps of:
    a) digestion in an aqueous medium, for a predetermined period of time, of a source of phosphate with an acid with the formation of a pulp comprising an aqueous phase containing calcium phosphate in solution and a solid phase containing impurities,
    b) a first separation between said aqueous phase containing calcium phosphate in solution and said solid phase containing impurities, during a predetermined period of time,
    c) neutralization of said aqueous phase containing calcium phosphate in solution at a pH sufficient to obtain precipitation in an aqueous medium of insoluble calcium phosphate as the above-mentioned calcium monohydrogen phosphate, and
    d) a second separation between said aqueous medium and said calcium monohydrogenphosphate.
    The attack on a source of phosphate, such as phosphate ore, by an acid has been known for many years, for example US Patents 3304157 and GB 105 15 21.
    Document WO 2004002888 discloses a method for manufacturing calcium monohydrogen phosphate (DCP) and also a method for producing phosphoric acid from DCP obtained according to the method described in this patent document.
    This document provides for an attack on a phosphate ore in a digestion tank with a hydrochloric acid solution, having a concentration of the order of 5% by weight, to form a pulp comprising an aqueous phase containing phosphate of calcium
    B E2017 / 5456 and chloride ions in solution and a solid phase containing impurities.
    Passing the aforementioned pulp through a filter press makes it possible to separate the aqueous phase containing calcium phosphate and chloride ions in solution from the solid phase containing impurities.
    Neutralization of the separated aqueous phase containing calcium phosphate and chloride ions is carried out by means of the addition of a calcium compound to precipitate the DCP insoluble in the aqueous phase, following a rise in pH.
    An additional separation is carried out to recover a wet cake of DCP at the end of the process.
    Concerning the production of a phosphoric acid using the DCP thus obtained, this is carried out by a liquid-liquid extraction and requires several stages of implementation.
    it is, in fact, necessary to carry out a step of dissolving the wet cake of FADs, obtained according to the method described above, by a new attack with more concentrated hydrochloric acid which can range up to 20% by weight. This solubilization allows the formation of an aqueous solution containing phosphate ions, calcium ions and chloride ions, to be extracted with an organic extracting agent.
    More specifically, this extraction step is carried out in an extraction column using an organic solvent and makes it possible to produce an aqueous extraction phase containing chloride ions and calcium ions and an organic extraction phase containing phosphoric acid.
    The organic extraction phase containing phosphoric acid is re-extracted using an aqueous re-extraction agent so as to isolate an aqueous re-extraction phase containing phosphate ions.
    a concentration
    B E2017 / 5456
    This phosphoric acid production process is complex and requires several expensive steps to provide sufficient quality phosphoric acid for the intended applications.
    Furthermore, the use of organic extraction solvents makes such a process unattractive in terms of ecological impact.
    WO 2005 066 070 relates to a process for attacking phosphate ore with an aqueous hydrochloric acid solution having an HCl concentration of less than 10% by weight, with the formation of a pulp consisting of an aqueous phase containing calcium phosphate in solution and chloride ions and an insoluble solid phase containing impurities.
    The above-mentioned aqueous phase is neutralized at a first pH at which a significant proportion of calcium phosphate is maintained in the aqueous phase in order to precipitate impurities.
    Then, the aforementioned insoluble solid phase is separated from the aqueous phase while the precipitated impurities are isolated.
    Additional neutralization of the aqueous phase is carried out at a second pH higher than the above-mentioned first pH to precipitate DCP which is then separated from the aqueous medium.
    This process is limited by the fact that an aqueous hydrochloric acid solution having a concentration of less than 10% by weight must be used.
    More recently, a process for attacking a source of phosphate with an aqueous solution of hydrochloric acid was the subject of patent application WO 2015 082 468.
    According to this disclosure, digestion of the rock in the presence of the aqueous hydrochloric acid solution makes it possible to form a pulp consisting of an aqueous phase containing calcium phosphate and
    Chlorine ions in solution, and an insoluble solid phase containing impurities.
    B E2017 / 5456
    The aqueous phase is then separated from the solid phase by filtration so that the aqueous phase can be neutralized at a sufficient pH to form an aqueous medium comprising chloride ions and in order to precipitate the calcium phosphate in the form of said phosphate salt. Subsequent separation isolates the phosphate salt.
    According to this process, the attack and filtration steps are carried out at a temperature between 50 ° C and 70 * 0 and the first aqueous solution of hydrochloric acid has an HCl concentration less than or equal to 15% by weight.
    Unfortunately, the known methods are impractical for industrialists since they do not exhibit an extraction yield of P 2 Q 5 which is sufficient relative to the amount of P 2 Q 5 present in the starting phosphate source. and that the phosphate salt obtained is not sufficiently pure, which nevertheless determines its potential for use in several fields of application, such as agriculture or food and technical applications with high added value.
    There is therefore a real need to provide a process for manufacturing calcium monohydrogen phosphate which ultimately solves this problem linked to the purity of calcium monohydrogen phosphate, while limiting the losses of P 2 Og in the waste generated by the process for the purpose to improve the general performance of the process.
    The object of the invention is to provide a process for the manufacture of calcium monohydrogen phosphate which can be simpler to implement and reliable, while taking due account of the compromise between the desired degree of purity of the calcium monohydrogen phosphate obtained at the end of the process. , limitation of P 2 O 5 losses and the duration of the process.
    To solve this problem, there is provided according to the invention a method as indicated at the beginning, in which said first separation of said step b) is carried out at a filtration speed of at least 0.1 tonnes
    B E2017 / 5456 of P ^ g / VAP / mF / day. preferably between 0.1 and 5 tonnes of P 2 Os / VAP / m 2 / day, more preferably between 0.15 and 3 tonnes of PgOgA / AP / m ^ day, more preferably still between 0.3 and
    0.9 tonnes of PgOg / VAP / rrF / day, in particular between 0.4 and 0.7 tonnes of 5 P 2 O5 / VAP / m 2 / day, said filtration speed being calculated using the following equation:
    Filtration speed
    Qpws fëP £ lT f where
    Qp2O5 corresponds to the quantity of P 2 O 5 collected in the filtrate and is expressed in tonnes,
    Ω is the area of the filter expressed in m 2 ,
    ΔΡ is the difference between the pressure leaving the filtrate and the pressure applied to the pulp at the time of said first separation and is expressed in bar, and
    T] is the duration of said first separation and is expressed in days.
    The filtration speed indicated above is calculated, in a manner known to a person skilled in the art, as described in particular in Albert Rushton, Anthony S. Ward and Richard G. Holdich, Solid-Liquid Filtration and Separaten Technology, p. 35-93, ed. John Wiley & Sons, 2008.
    Surprisingly, it appeared that it was possible to obtain in a simple manner an extraction yield of P 2 O "for steps a and b greater than 90% by weight, preferably greater than 93 % by weight, advantageously greater than 95%, by applying rapid and economical filtration rates on an industrial scale.
    It has been found that the process according to the invention makes it possible to carry out said step b) of first separation at a filtration speed which is particularly advantageous in that it allows, at the same time, to reduce the filtration times while still 'not increasing the size of the filter, which is required for industrial application.
    B E2017 / 5456
    Said predetermined period of time in said step a) of digestion may be greater, less or equal to that of step a) of abovementioned first separation.
    It has appeared particularly advantageous that the first separation step is no longer restrictive for the user since it is rapid and efficient. This has the consequence that the process according to the present invention is sufficiently profitable since it does not does not require repeated and consequent washing of the separation means.
    In practice, whether according to a continuous or discontinuous process, these advantages provided by the process clearly reduce the filtration area required. Thus, the first separation step is simpler and more efficient, which ultimately makes it possible to provide a more profitable process than the processes known in the prior art.
    As explained, ie calcium monohydrogenphosphate obtained according to the process of the present invention can be used in the field of agriculture, food or even in a composition intended for agriculture or food. The field of agriculture notably includes fertilizers, such as fertilizers. It can also be used for the production of phosphoric acid.
    Advantageously, the above steps a) and b) are carried out in a predetermined duration of less than 2 hours, preferably a duration of between 30 and 100 minutes, preferably between 30 and 70 minutes, more preferably between 40 and 65 minutes.
    More advantageously still, said predetermined time period of said step a) is advantageously between 75 and 100 minutes, preferably between 80 and 95 minutes, or between 20 and 45 minutes, in particular between 24 and 40 minutes, preferably between 30 and 35 minutes.
    According to a preferred embodiment, said source of phosphate and said acid are introduced into a first reactor comprising said aqueous medium simultaneously or successively, in order to carry out said step a)
    B E2017 / 5456 for digestion and said pulp comprising said aqueous phase containing calcium phosphate in solution and said solid phase containing impurities is transferred from the first reactor to a separation means to implement said first separation taken up in step b ) of the above-mentioned first separation,
    More preferably, said separation means is located between said first reactor and a second reactor.
    Even more preferably, said separation means is present in a second reactor into which is introduced said pulp comprising an aqueous phase containing calcium phosphate in solution and a solid phase containing impurities, to implement said first separation taken up at step b ) above.
    In addition, said separation means can preferably be a filter chosen from the group consisting of a rotary filter, preferably with tilting cells, filter press, band filter, drum filter.
    According to a preferred mode, said acid is chosen from the group consisting of hydrochloric acid (HCl), nitric acid, sulfuric acid, phosphonic acid and their mixtures.
    Advantageously, said acid is an aqueous solution of acid, preferably hydrochloric acid, having an acid concentration less than or equal to 15% by weight.
    Even more preferably, steps a) and b) are carried out at a temperature between 5 (TC and 70 ° C, preferably equal to 6 (TC.
    Preferably, said phosphate source is chosen from the group consisting of a phosphate rock, a phosphate ore, secondary phosphate sources such as ash (for example from sludge from a treatment plant or from bone or pig llslers) had their mixtures.
    Advantageously, the neutralization step is carried out using a neutralizing agent chosen from the group consisting of
    B E2017 / 5456 calcium-based compounds such as calcium oxide or hydroxide, calcium carbonate and water-soluble calcium salts.
    Other embodiments of the process according to the invention are indicated in the appended claims.
    The present invention also relates to a use of the calcium monohydrogenphosphate obtained according to the present invention for producing phosphoric acid.
    Such production of phosphoric acid can involve an attack of calcium monohydrogen phosphate obtained with sulfuric acid.
    Preferably, the calcium monohydrogen phosphate obtained according to the process according to the present invention is used in the food industry or in the agricultural or horticultural field.
    Other embodiments of the use according to the invention are indicated in the appended claims.
    Other characteristics, details and advantages of the method and of the use according to the invention will emerge from the description given below, without implied limitation.
    In the context of the present invention, the expression “digestion is carried out during a predetermined period of time” should be understood to mean that digestion ends at the moment when the first separation step is initiated, which corresponds to the moment where the pulp is introduced into a separation means, such as a filter.
    In the context of the present invention, the expression “first separation carried out during a predetermined period of time” must be understood to mean that the duration linked to this first separation is determined from the moment when the pulp to be filtered is introduced into a separation means, such as a filter.
    According to a practical example, a phosphate ore and an aqueous solution of hydrochloric acid are introduced simultaneously or
    B E2017 / 5456 successively in an aqueous medium contained in a first reactor.
    After digestion during a predetermined period of time, a pulp is obtained in the first reactor and is introduced into a separation means with a view to carrying out step b) of first separation during a predetermined period of time which may be less than that corresponding in step a) of digestion.
    This separation means can be present in the first reactor or in a second reactor.
    When the separation means is present in the first reactor, the latter can be in fluid communication with this reactor.
    Thus, the predetermined duration of digestion ends from the moment when the pulp is introduced into the separation means.
    The separation means can also be present in a second reactor possibly in fluid communication with the first reactor.
    It is also possible to use a first reactor, a second reactor and a separation means which can be arranged between said first and second reactors so as to be in fluid communication with the latter.
    In the context of the present invention, the process can be carried out continuously or discontinuously.
    The step of neutralizing said aqueous phase comprising calcium phosphate and chloride ions in solution, when the attack is carried out with hydrochloric acid, is carried out at a pH sufficient to precipitate the calcium phosphate in the form of said monohydrogen phosphate calcium.
    A second separation is provided between said aqueous medium comprising the chloride ions and the calcium monohydrogenphosphate so as to provide the calcium monohydrogenphosphate obtained by the process according to the present invention.
    B E2017 / 5456
    The neutralization and second separation steps are known to those skilled in the art, in particular from document WO 2015 082 468, which is incorporated by reference in the present patent application.
    We start with a phosphate ore with the characteristics of Table 1 below:
    Amount phosphate I1000.0 g IHumidity | 1.93% 19.3 gCaO I 48.90% 489.0 g IP 2 O S 31.00% 310.0 gï
    An amount of 120.8 g of demineralized water is introduced into a berlin and then an amount of 75 g of phosphate from Table 1 is added to the demineralized water, with stirring, to form a mixture. The berlin is then covered with a watch glass and the mixture is brought to a temperature of 60 ° C.
    120.8 g of demineralized water are mixed with an aqueous solution of hydrochloric acid, which has an HCl concentration of 37%, so as to obtain 357.7 g of an aqueous solution of HCl at 12%. The latter is then added to the hot mixture of phosphate and demineralized water.
    The duration of digestion is measured from the moment when the aqueous solution of dilute acid is added to the hot mixture containing phosphate and demineralized water.
    The solution obtained after digestion is filtered, at a filtration temperature of 60 ° C., by means of a polyester fiber filter 25 having a diameter of 90 mm and a thickness of 0.17 mm placed on Buchner type equipment. previously evacuated.
    B E2017 / 5456
    The filtration pressure used is 0.4 bar, which represents a difference in driving pressure of 0.6 bar compared to the atmospheric pressure of 1 bar.
    The filtration time corresponds to the time necessary to obtain a wet cake from the pulp formed during the previous steps. After filtration, the cake is subjected to a drying step during which the ambient air is sucked through the cake, the drying step lasting 5 minutes. According to this first exemplary embodiment, the filtration time is 5 minutes.
    The weight of the wet cake obtained is then measured as well as the weight of the filtrate. The filtrates and the cake are then subjected to analysis.
    The wet cake is then dried at a temperature of 60 ° C. and its weight, after drying, is also measured.
    In this example, the digestion time is 30 minutes and the filtration time is 5 minutes, as shown in Table 2 below. Table 2
    Free 1
    Amount of starting phosphate 75 grams Amount of aqueous solutionof HC112% 357.7 grams Ore digestion temperature 60 ° C Digestion time 30 minutes Filtration temperature 60 ° C Filtration time 5 minutes Filtration speed 1.3 tonnes of PsOg / mV ^ AP / day
    The yield of P 2 O 5 in the final product obtained at the end of the process after steps a and b is equal to 94.03%. The yield is calculated on the basis of the quantity of P 2 O 5 present in the ore of
    B E2017 / 5456 phosphate. H represents the percentage of P 2 O 5 in the filtrate after the first separation step b with respect to this quantity.
    Free 2
    This example is carried out under the same operating conditions as those described in Example 1, except that the digestion time is 45 minutes and the filtration time is 5.5 minutes, as illustrated in Table 3 below.
    12%
    Ore digestion temperature
    Digestion time
    Filtration temperature
    Filtration time
    Filtration speed
    The yield of P 2 O 5 after steps a and b of the process is 93.02%.
    Free 3
    This exemption is carried out under the same operating conditions as those described in Example 1, with the exception that the digestion time is 60 minutes and the filtration time is 4.75 minutes, as illustrated in the table. 4 below.
    B E2017 / 5456
    The yield of P 2 0g in the product after steps a and b of the process is $) 3.16%.
    Example 4
    This example is carried out under the same operating conditions as those described in Example 1, except that the digestion time is 90 minutes and the filtration time is 2.33 minutes, as illustrated in the table. 5 below.
    Example 4
    Amount of starting phosphate i 75 i
    I Amount of ia
    Digestion temperature 7kTmkïëraï ~ y6 (rC
    Digestion time ΓοοΈτί
    I
    Filtration temperature! 60 ° C filtration time i 2.33 i
    B E2017 / 5456
    The yield of P 2 0 s in the product obtained after steps a and b of the process is 91.96%.
    This example is carried out under the same operating conditions as those described in Example 1, except that the digestion time is 10.5 minutes and the filtration time is 25 minutes, as illustrated in Table 6 below.
    Table 6
    Free 5 Amount of starting phosphate 75 grams Amount of aqueous solution 357.7 grams of HC112%Ore digestion temperature 60 ° C Digestion time 0.5 minutes Filtration temperature 60 ° C Filtration time 25 minutes Filtration speed 0.3 tonnes of PaOg / mVVâP / day
    The yield of P 2 O 5 in the product obtained after steps a and b of the process is $) 6.33%.
    This example is carried out under the same operating conditions as those described in Example 1, except that the digestion time is 15 minutes and the filtration time is 13 minutes as illustrated in Table 7.
    B E2017 / 5456
    Board exam plaice 6 Amount of starting phosphate d 75 grams Amount of the aqueous HCl solution I 357.7 grams 12%Ore digestion temperature i 60 ° C Digestion time D 15 minutes Filtration temperature | 60 ° C Filtration time 13 minutes Filtration speed 0.5 tonnes of P 2 C
    ί
    i free i quantity of starting phosphate 75 grams ί quantity of aqueous solution of HCl 357, i grouirr I 12%
    E "..........................................
    I Ore digestion temperature 60 ° C
    I Digestion time i Filtration temperature i Filtration time i Filtration speed
    21.5 minutes ο, d
    B E2017 / 5456
    The yield of P2O5 in the product obtained after your steps a and b of the process is 96.09%.
    This example is carried out under the same operating conditions as those described in example 1, except that the digestion time is 26.33 minutes and the filtration time is 7.33 minutes, as illustrated in table 9 below.
    The yield of P 2 Os in the product obtained after steps a and b of the process is 95.85%.
    It is understood that the present invention is in no way limited to the embodiments described above and that many modifications can be made thereto without departing from the scope of the appended claims.
    权利要求:
    Claims (14)
    [1]
    1. Process for the preparation of calcium monohydrogen phosphate comprising the steps of:
    a) digestion in an aqueous medium, for a predetermined period of time, of a source of phosphate with an acid with the formation of a pulp comprising an aqueous phase containing calcium phosphate in solution and a solid phase containing impurities,
    b) a first separation between said aqueous phase containing calcium phosphate in solution and said solid phase containing impurities, during a predetermined period of time,
    c) neutralization of said aqueous phase containing calcium phosphate in solution at a pH sufficient to obtain precipitation in an aqueous medium of insoluble calcium phosphate as the above-mentioned calcium monohydrogen phosphate, and
    d) a second separation between said aqueous medium and said calcium monohydrogenphosphate, characterized in that said first separation of said step b) is carried out at a filtration rate of at least 0.1 tonnes of PgOsA / AP / mViour, preferably between 0.1 and 5 tonnes of PzOgA / AP / mVday, more preferably between 0.15 and 3 tonnes of P2O5 / vAP / m 2 / day, more preferably still between 0.3 and 0.9 tonnes of PsOs / VAP / m ^ / day, in particular between 0.4 and 0.7 tonnes of PaOg / vAP / mVday, said filtration speed being calculated according to the following equation:
    Filter ffies.se = .....
    VÄÄßT) where
    Qp2os corresponds to the quantity of P2O5 collected in the filtrate and is expressed in tonnes,
    2017/5456
    BE2017 / 5456
    Ω is the area of the filter expressed in m 2 ,
    ΔΡ is the difference between the pressure leaving the filtrate and the pressure applied to the pulp at the time of said first separation and is expressed in bar, and
    5 T f is the duration of said first separation and is expressed in days.
    [2]
    2. Method according to claim 1, wherein said predetermined period of time of said step a) of digestion is greater, less or equal to that of step b) of said first separation,
    [3]
    3. Method according to claim 1 or 2 S wherein the steps
    A) and b) above are carried out in a predetermined duration of less than 2 hours, preferably a duration of between 30 and 100 minutes, in particular between 30 and 70 minutes, more preferably between 40 and 65 minutes.
    [4]
    4. Method according to any one of the claims
    15, in which said source of phosphate and said acid are introduced into a first reactor comprising said aqueous medium simultaneously or successively, in order to carry out said step a) of digestion and in which said pulp comprising said aqueous phase containing calcium phosphate in solution and said solid phase
    20 containing impurities is transferred from the first reactor to a separation means to implement said first separation taken up in step b) above.
    [5]
    5. The method of claim 4, wherein said separation means is located between said first reactor and a second reactor.
    25
    [6]
    6. The method of claim 4, wherein said separation means is present in a second reactor into which is introduced said pulp comprising an aqueous phase containing calcium phosphate in solution and a solid phase containing impurities, for implementing said first separation resumed at
    30 step b) above.
    2017/5456
    BE2017 / 5456
    [7]
    7. Method according to any one of claims 4 to 6, wherein said separation means is a filter chosen from the group consisting of a rotary filter, preferably with tilting cells, filter press, band filter, drum filter.
    [8]
    8. Method according to any one of the preceding claims, in which the said acid is chosen from the group consisting of hydrochloric acid (HCl), nitric acid, sulfuric acid, phosphoric acid and their mixtures,
    [9]
    9. The method according to claim 8, wherein said acid is an aqueous solution of acid having an acid concentration less than or equal to 15% by weight, preferably in the first reactor,
    [10]
    10. Method according to any one of the preceding claims, in which steps a) and b) are carried out at a temperature between 50 ° C and 70 ° C, preferably equal to 60 ° C,
    [11]
    11. Method according to any one of the preceding claims, in which said source of phosphate is chosen from the group consisting of a phosphate rock, a phosphate ore, secondary phosphate sources such as ash, for example from sludge from sewage treatment plants or from bone or pig manure, or mixtures thereof.
    [12]
    12. Method according to any one of the preceding claims, in which the neutralization step is carried out by means of a neutralizing agent chosen from the group consisting of calcium-based compounds such as oxide, hydroxide, calcium carbonate and water-soluble calcium salts.
    [13]
    13. Use of the calcium monohydrogen phosphate obtained according to any one of the preceding claims for producing phosphoric acid.
    2017/5456
    BE2017 / 5456
    [14]
    14. Use of the silicon monohydrogen phosphate obtained according to any one of claims 1 to 12 in the food industry or in the agricultural or horticultural field.
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    FR2273760A1|1974-06-05|1976-01-02|Israel Chemicals Ltd|IMPROVED PROCESS FOR THE PREPARATION OF FOOD GRADE DICALCIUM PHOSPHATE AND PHOSPHORIC ACID|
    WO2015082468A1|2013-12-02|2015-06-11|Ecophos S.A.|Source of phosphate for agriculture and the food industry|
    GB953156A|1961-08-20|1964-03-25|Makhtsavei Israel|Improvements in or relating to the recovery of phosphoric acid by solvent extraction|
    GB1051521A|1964-02-20|1966-12-14|Israel Mining Ind Inst For Res|Improvements in or relating to a process for the production of substantially iron free aqueous solution of phosphoric acid|
    BE1015013A3|2002-06-28|2004-08-03|Ecophos|Process phosphoric acid production and / or salt thereof and products obtained.|
    BE1015840A3|2003-12-24|2005-10-04|Ecophos|Process leading ore phosphate.|CN111533099B|2020-05-22|2021-12-07|四川大学|Production method of water-soluble monoammonium phosphate|
    法律状态:
    2019-02-04| FG| Patent granted|Effective date: 20190115 |
    优先权:
    申请号 | 申请日 | 专利标题
    BE2016/5485|2016-06-28|
    BE201605485|2016-06-28|
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