• 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:
    Wet-processed phosphoric acid is decontaminated. To this end, the phosphoric acid and an organic solvent, which is partially miscible with water and capable of absorbing phosphoric acid, are contacted countercurrently with respect to one another. The resulting organic phosphoric acid solution is separated from contaminants unabsorbed by the solvent, termed primary raffinate, decontaminated phosphoric acid is recovered either in the form of free acid by re-extracting the organic phosphoric acid solution with water, or in the form of an alkali metal phosphate by reacting the organic phosphoric acid solution with an alkali, and the primary raffinate is treated countercurrently with a solvent containing a mineral acid. More specifically, the organic phosphoric acid extract, which orginates from the primary raffinate treatment and contains more than 0 up to at most 10 weight% of water, is mixed with an anhydrous solvent in a ratio by weight necessary to ensure the formation of a mixture containing more than 0 and less than 50% of water than would correspond to the saturation concentration of water in the solvent; and the mixture is contacted countercurrently with the phosphoric acid which is to be decontaminated.
    公开号:SU888812A3
    申请号:SU772547802
    申请日:1977-11-30
    公开日:1981-12-07
    发明作者:Элерс Клаус-Петер；Шайбитц Вольфганг；Шредтер Клаус；Хеймер Геро
    申请人:Хехот Аг(Фирма)；
    IPC主号:
    专利说明:

    The invention relates to methods of purifying extractive phosphoric acid used in the chemical industry. A known method of purification of diluted phosphoric acid by treating it with activated carbon to remove organic impurities, followed by extraction with phosphoric acid-dissolving organic solvent, which uses n-butanol, ketone with 4-10 carbon atoms in chain 1. The disadvantage of this method is its multiphase. A known method of purification of phosphoric acid extraction by treating crude phosphoric acid with a partially organic water-miscible solvent, which uses alcohol with 5 carbon atoms in the chain, dissolves the solvent countercurrently to phosphoric acid, and then separates the insoluble impurities with the raffinate and reextrates phosphoric acid with water and alkalis with the circulation of the solvent 2. The disadvantage of this method is the low yield of the product — up to 92.8%; obtaining a precipitate in the form of thin gypsum slime which cannot be stored in this form, but must be filtered out, with the problem of using a filtrate. The aim of the invention is to increase the yield of the product and obtain a dehydrated sludge, which allows it to be stored without additional processing operations. The goal is achieved in that the phosphoric acid is treated with a solvent in two separate extraction zones to obtain primary and secondary extract and raffinate, the insoluble impurities with the raffinate are separated, and the recycled solvent is divided into two parts in a ratio. The first part of the solvent is dehydrated and mixed with a secondary extract containing 0.1-10.0 wt.% Water, and the solvent and the secondary extract are mixed in such a proportional ratio that the resulting mixture contains 0.1-50.0 wt.% Water, .and serves it in the first zone of the extract, the primary raffinate is fed to the second extraction zone, where, in 2-10 stages, the countercurrent is treated with a mixture consisting of the second part of the recirculating solvent and concentrated sulfuric acid, the volume ratio of solvent to the primary raffinate taken equal to 47-8: 1, and sulfuric acid was introduced in such an amount that 1 g-atom of phosphorus was added to one acid equivalent, phosphoric acid was reextracted with water or alkalis with solvent circulation. The water released during the dehydration of the solvent is used to rinse the primary extract before it is stripped, and the thus obtained wash solution is mixed with phosphoric acid prior to feeding into the first extraction zone. Table 1 shows the data characterizing the method with different process parameters. The feasibility of the temperature limits established in the second extraction zone follows from the fact that the conversion into soluble form of the primary raffinate should occur due to the acid supplied in countercurrent. This process accelerates with increasing temperature, but it is not possible to bring the temperature to the boiling point of water. As regards the volume ratio of solvent to first raffinate, large ratios than 8: 1, inevitably, also large quantities of solvent, which also need to be dehydrated, are bound to with energy costs, ratios less than 1: 1 result in terms of terms. Pij. the amount of injected mineral acid is due to the fact that to convert the phosphate in a soluble state in the primary raffiate to an i-g atom of phosphorus, an equivalent of acid is required. More acids lead to contamination of the primary extract, while introducing a smaller holistic; secondary raffinate and is lost. The proposed method allows to increase the yield of the product to 98.1% and to obtain a dehydrated precipitate in an easily stored form. Example. 23.12 tons extraction. phosphoric acid, NO, content (wt.%): 50.2 2.48 Fe; l, 60 A1; 0.56 MD; 0.12 Ca; 0.15 SDH for 60 hours along with 3.2 tons of recirculating wash solution is treated in a two-stage countercurrent unit in the presence of 49.62 tons of anhydrous ami of ethyl alcohol and 14.03 tons of organic secondary extract coming from the second stage of a three-stage countercurrent extraction of the primary raffinate . The mixture of these two organic media contains 2.1% by weight of water. 3.45 tons of almost solid primary raffinate are fed to the second stage of countercurrent extraction, and at 25 ° C, 13.82 tons of amyl alcohol is extracted into which 0.52 tons of concentrated sulfuric acid (96%) are preliminarily introduced. the second stage of extraction is used as described above. On the whole, 86.43 tons of primary extract with a content of 15.1% by weight are obtained by countercurrent treatment of the crude acid, from which, after washing and stripping with water, 32.36 tons of purified phosphoric acid with a content of 36.4% by weight are extracted. The content of impurities at the level of 1-0-20 ppm. Besides; in the process, 3.85 tons of a secondary raffinate containing in wt.% RoP5 is obtained. The total loss is 1.9 wei.%, i.e. yield of acids 98.1%. To the secondary raffinate in the mixer, 0.53 tons of calcined lime is added, which absorbs the evaporated water, and 3.93 tons of sediment are obtained, suitable for storage. The water-saturated amyl alcohol obtained during reextraction is mixed with sulfuric acid and fed back into the battery. Most of the silyl alcohol is dehydrated by adsorption distillation. The water separated during the distillation is directed to a flush battery.
    805
    1.6 620 2.1 610
    4.7
    97.1
    2 2 2 98.1 96.8
    权利要求:
    Claims (2)
    [1]
    1. A method for purifying an extraction phosphoric acid by treating it with a partially water-miscible organic solvent, which is introduced counter-current to phosphoric acid, followed by separating the extract from the raffinate, and re-extracting the phosphoric acid with water or alkali with solvent circulation, characterized by the fact that In order to increase the yield of the product and to obtain a dehydrated sludge, the treatment of phosphoric acid with an organic solvent is carried out in two separate extraction zones to obtain primary and secondary extras. kta and raffinate, the recycled solvent is divided into two parts in a ratio of 6-1: 1, the first part of the solvent is dehydrated and mixed with a secondary extract containing 0.1-10.0 wt.% water, and the solvent and the secondary extract are mixed in such a quantitative ratio that the resulting mixture contains 0.1-50.0 wt.% water, and
    Table continuation
    it is fed to the extraction zone, the primary raffinate is fed to the second extraction zone, where at 0-98 ° C the countercurrent is treated in stages with a mixture consisting of the second part of the recycled solvent and concentrated sulfuric acid, at a volume ratio of solvent to the primary raffinate 4f8: l, and sulfuric acid is introduced in such an amount that one acid equivalent is per g of phosphorus atom.
    [2]
    2. The POP.1 method, characterized in that the water, Brought on by the dehydration of the solvent, is used to rinse the primary extract before re-extraction and the resulting washing solution is mixed with phosphoric acid before cleaning.
    Sources of information1 “ation taken into account during the examination
    1. Japanese Patent 22403, cl. 15 B 63, 09/25/1969.
    2. US patent 2885265, cl. 23-165, 1959 (prototype).
    类似技术:
    公开号 | 公开日 | 专利标题
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    SU888812A3|1981-12-07|Method of purifying extraction phosphoric acid
    US3953581A|1976-04-27|Purification of wet-processed phosphoric acid using anhydrous solvents
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    US4271128A|1981-06-02|Apparatus for recovering alcoholic phosphoric acid solutions from acid phosphates
    GB1563760A|1980-04-02|Effluent treatment
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    SU858572A3|1981-08-23|Method of uranium extraction
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    IL32320A|1973-07-30|Process for the recovery of phosphoric acid from the aqueous liquors obtained by the decomposition of rock phosphate with hydrochloric or nitric acid
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    EP0009849B1|1983-03-09|A process for the purification of phosphoric acid
    US3497329A|1970-02-24|Production of phosphoric acid
    US4203956A|1980-05-20|Process and apparatus for recovering alcoholic phosphoric acid solutions from acid phosphates
    US4207303A|1980-06-10|Method for producing pure phosphoric acid
    US3518071A|1970-06-30|Production of nitrophosphate fertilizer and ammonium nitrate-calcium carbonate fertilizers
    同族专利:
    公开号 | 公开日
    ATA898277A|1979-07-15|
    JPS5383993A|1978-07-24|
    FI773803A|1978-06-18|
    FI65610B|1984-02-29|
    SE7714259L|1978-06-18|
    FR2374263B1|1982-10-08|
    FI65610C|1984-06-11|
    DE2657190C2|1982-11-04|
    DK149229B|1986-03-24|
    DK149229C|1986-08-18|
    GB1554379A|1979-10-17|
    DE2657190A1|1978-06-22|
    BE861920A|1978-06-16|
    BR7708375A|1978-08-08|
    CH631418A5|1982-08-13|
    DK562677A|1978-06-18|
    US4200620A|1980-04-29|
    NL7713608A|1978-06-20|
    PH14335A|1981-05-29|
    AT354978B|1980-02-11|
    FR2374263A1|1978-07-13|
    MX146999A|1982-09-22|
    NL184945B|1989-07-17|
    IT1090568B|1985-06-26|
    CA1084238A|1980-08-26|
    SE429752B|1983-09-26|
    DD136258A5|1979-06-27|
    JPS5734203B2|1982-07-21|
    IL53618D0|1978-03-10|
    NL184945C|1989-12-18|
    ES463603A1|1978-07-16|
    TR19331A|1978-12-07|
    ZA777470B|1978-11-29|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    DE884358C|1951-09-20|1953-07-27|Gerardo Collardin|Process for the purification of technical phosphoric acid|
    BE757550A|1969-10-16|1971-03-16|Giulini Gmbh Geb|PROCESS FOR PREPARING PURE PHOSPHATES FROM IMPURE PHOSPHORIC ACIDS|
    US3956465A|1970-06-12|1976-05-11|Azote Et Produits Chimiques S.A.|Solvent purification of wet process phosphoric acid|
    SE366972B|1970-06-12|1974-05-13|Azote & Prod Chim|
    FR2093372A5|1970-06-12|1972-01-28|Azote & Prod Chim|Purification of wet-process phosphoric acid - by extraction - with part water-misc organic solvent|
    DE2029564C3|1970-06-16|1978-06-22|Giulini Chemie Gmbh, 6700 Ludwigshafen|Process for the production of pure alkali phosphates from rock phosphoric acid|
    US3684439A|1970-09-22|1972-08-15|Monsanto Co|Handling of raffinates from wet phosphoric acid purification|
    FR2128968A6|1971-03-10|1972-10-27|Azote & Prod Chim|Purification of wet-process phosphoric acid - by extraction - with part water-misc organic solvent|
    DE2321751C3|1973-04-30|1981-11-19|Hoechst Ag, 6000 Frankfurt|Process for purifying wet phosphoric acid|
    DE2605106C2|1976-02-10|1984-06-14|Hoechst Ag, 6230 Frankfurt|Process and device for the production of alcoholic phosphoric acid solutions from acidic phosphates|US4197280A|1978-10-02|1980-04-08|Stauffer Chemical Company|Wet process phosphoric acid purification|
    DE2909572A1|1979-03-12|1980-09-25|Hoechst Ag|METHOD FOR CONVERTING EXTRACTION RESIDUES FROM PHOSPHORIC ACID CLEANING IN SOLID DEPOSITE PRODUCTS|
    DE2926943C2|1979-07-04|1988-01-28|Hoechst Ag, 6230 Frankfurt, De|
    US4751066A|1986-05-08|1988-06-14|Fmc Corporation|Process for preparing alkali metal phosphate|
    GB9124353D0|1991-11-15|1992-01-08|Albright & Wilson|Immobilisation of metal contaminants from a liquid to a solid metal|
    IL211043D0|2010-02-06|2011-04-28|Aharon Eyal|A method for the separation of a non-volatile strong acid from a salt thereof and compositions produced thereby|
    EP2948230A4|2013-01-28|2016-03-16|Solex Water Ltd|Methods and systems for water recovery|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2657190A|DE2657190C2|1976-12-17|1976-12-17|Process for purifying wet process phosphoric acid|
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