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WO2013066957A1 - Extraction de l'uranium de l'acide phosphorique produit par voie humide - Google Patents

Extraction de l'uranium de l'acide phosphorique produit par voie humide Download PDF

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Publication number
WO2013066957A1
WO2013066957A1 PCT/US2012/062711 US2012062711W WO2013066957A1 WO 2013066957 A1 WO2013066957 A1 WO 2013066957A1 US 2012062711 W US2012062711 W US 2012062711W WO 2013066957 A1 WO2013066957 A1 WO 2013066957A1
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WO
WIPO (PCT)
Prior art keywords
uranium
wpa
ion exchange
stream
species
Prior art date
Application number
PCT/US2012/062711
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English (en)
Inventor
Marcus Worsley Richardson
James Andrew Davidson
Bryn Llywelyn Jones
Jessica Mary Page
Karin Helene Soldenhoff
Tomasz Artur SAFINSKI
Manh Toan TRAN
Original Assignee
Urtek, Llc
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 Urtek, Llc filed Critical Urtek, Llc
Priority to MX2014005312A priority Critical patent/MX2014005312A/es
Priority to EP12846133.2A priority patent/EP2773783A4/fr
Priority to CA2854145A priority patent/CA2854145A1/fr
Priority to BR112014010334A priority patent/BR112014010334A2/pt
Priority to KR1020147014379A priority patent/KR20140123040A/ko
Priority to PH1/2014/500971A priority patent/PH12014500971A1/en
Publication of WO2013066957A1 publication Critical patent/WO2013066957A1/fr
Priority to TNP2014000183A priority patent/TN2014000183A1/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B25/00—Phosphorus; Compounds thereof
    • C01B25/16—Oxyacids of phosphorus; Salts thereof
    • C01B25/18—Phosphoric acid
    • C01B25/234—Purification; Stabilisation; Concentration
    • C01B25/237—Selective elimination of impurities
    • C01B25/238—Cationic impurities, e.g. arsenic compounds
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G43/00—Compounds of uranium
    • C01G43/003—Preparation involving a liquid-liquid extraction, an adsorption or an ion-exchange
    • 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
    • C22B60/00—Obtaining metals of atomic number 87 or higher, i.e. radioactive metals
    • C22B60/02—Obtaining thorium, uranium, or other actinides
    • C22B60/0204—Obtaining thorium, uranium, or other actinides obtaining uranium
    • C22B60/0217—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes
    • C22B60/0252—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries
    • C22B60/0278—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries by chemical methods
    • C22B60/0282—Solutions containing P ions, e.g. treatment of solutions resulting from the leaching of phosphate ores or recovery of uranium from wet-process phosphoric acid

Definitions

  • the invention relates to the field of extracting uranium from wet-process phosphoric acid.
  • Phosphoric acid (H3PO 4 ) for use in fertilizer production is typically produced by a wet-process during which naturally occurring phosphate rock is reacted with sulphuric acid to provide so called wet-process phosphoric acid (WPA) .
  • WPA wet-process phosphoric acid
  • it may contain valuable metals such as uranium, vanadium and yttrium, which are dissolved by the sulphuric acid and form impurity constituents of the WPA.
  • the invention provides a process for extracting uranium from wet-process phosphoric acid (WPA) , the process comprising: (a) separating uranium from WPA to produce a loaded uranium solution stream and a uranium depleted WPA stream; (b) contacting the loaded uranium solution stream with an ion exchange resin; (c) eluting uranium species bound to the ion exchange resin by contacting the resin with a solution comprising anions to produce a loaded uranium eluant stream; and (d) treating the loaded uranium eluant stream to provide a uranium containing product.
  • WPA wet-process phosphoric acid
  • the anions used to elute the uranium species in step (c) are selected from the group consisting of chloride anions, sulphate anions, nitrate anions, and combination thereof.
  • step (a) is preceded by a valency reduction step comprising reducing the valency of ferric ions in the WPA.
  • the valency reduction step may be carried out by chemical reduction, such as by the addition of metallic iron, ferro- phosphorus alloy or ferro-silicon alloy; or by electrochemical reduction (ER) .
  • step (a) and/or the valency reduction step (if used) may be preceded by an iron removal step.
  • the iron removal step comprises lowering the concentration of iron in the WPA by decreasing the amount of dissolved iron species in the WPA relative to the amount of uranium species in the WPA to produce a lowered iron content WPA having uranium species therein.
  • the concentration of iron in the WPA may be lowered by precipitating at least some of the iron present in the WPA as iron ammonium phosphate.
  • the invention provides a process for extracting uranium from wet-process phosphoric acid (WPA) , the process comprising: (a) contacting uranium laden WPA with a first ion exchange resin to form uranium depleted WPA; (b) separating the uranium depleted WPA from the first ion exchange resin; (c) oxidizing uranium species on the first ion exchange resin by contacting the first ion exchange resin with an oxidant; (d) contacting the first ion exchange resin with ammonia to remove impurities from the resin, the impurities being vanadium ions, organic species, or a combination thereof; (e) separating the impurities from the first ion exchange resin; (f) removing the oxidized uranium species from the first ion exchange resin by contacting the resin with ammonium carbonate to form a uranium enriched ammonium carbonate stream; (g) contacting the
  • the oxidant is selected from the group consisting of: air, oxygen, hydrogen peroxide, WPA, and combinations thereof.
  • the elution in step (i) is carried out using a solution comprising anions selected from the group consisting of chloride anions, nitrate anions, sulphate anions, and combinations thereof.
  • step (a) may be preceded by a valency reduction step comprising reducing the valency of ferric ions in the WPA.
  • the valency reduction step may be carried out by chemical reduction, such as by the addition of metallic iron, ferro- phosphorus alloy or ferro-silicon alloy; or by electrochemical reduction (ER) .
  • step (a) and/or the valency reduction step (if used) may be preceded by an iron removal step.
  • the iron removal step comprises lowering the concentration of iron in the WPA by decreasing the amount of dissolved iron species in the WPA relative to the amount of uranium species in the WPA to produce a lowered iron content WPA having uranium species therein.
  • the concentration of iron in the WPA may be lowered by precipitating at least some of the iron present in the WPA as iron ammonium phosphate.
  • the invention provides a process for extracting uranium from wet-process phosphoric acid (WPA) , the process comprising: (a) contacting uranium laden WPA with an oxidant to form an oxidized WPA stream; (b) contacting the oxidized WPA stream with an organic solvent; (c) separating a uranium enriched organic solvent stream from an aqueous WPA stream; (d) contacting the uranium enriched organic solvent stream with an ammonium carbonate stream to form a uranium enriched ammonium carbonate stream; (e) contacting the uranium enriched ammonium carbonate stream with an ion exchange resin;
  • the organic solvent used in step (b) comprises a di (2-ethylhexyl) phosphoric acid and trioctylphosphine oxide (i.e. a "DEHPA TOPO" system).
  • the valency reduction step is preceded by an iron removal step.
  • the iron removal step comprises lowering the concentration of iron in the WPA by decreasing the amount of dissolved iron species in the WPA relative to the amount of uranium species in the WPA to produce a lowered iron content WPA having uranium species therein.
  • the concentration of iron in the WPA may be lowered by precipitating at least some of the iron present in the WPA as iron ammonium phosphate.
  • the uranyl solution may be further treated to provide a uranium containing product. The further treatment may comprise a precipitation step.
  • FIG. 1 illustrates a general flow chart for a process according to a first exemplary embodiment of the invention
  • FIG. 2 illustrates a general flow chart for a process according to a second exemplary embodiment of the invention
  • FIG. 3 illustrates a general flow chart for a process according to a third exemplary embodiment of the invention .
  • FIG. 4 illustrates a general flow chart for a process according to a fourth exemplary embodiment of the invention .
  • FIG. 5 illustrates a general flow chart for a process according to a fifth exemplary embodiment of the invention.
  • FIG. 6 illustrates a general flow chart for a process according to a sixth exemplary embodiment of the invention .
  • FIG. 1 is a flow chart of a first exemplary embodiment of the invention, which is a process 10 for extracting uranium from wet-process phosphoric acid (WPA) 12.
  • the process 10 comprises a first separation step 14 in which uranium is separated from the WPA in a first ion exchange (IX) or solvent extraction (SX) step.
  • the first separation step 14 provides a loaded uranium solution stream 16 and a uranium depleted WPA stream 18.
  • the loaded uranium solution stream 16 is then contacted with an anion exchange resin in a secondary ion exchange step 20.
  • uranium species are bound to the anion exchange resin.
  • the bound uranium species are then eluted from the anion exchange resin by contacting the resin with a solution comprising chloride ions 22 to produce a loaded uranium eluant stream 24.
  • Other anions that could be used to elute the bound uranium species from the anion exchange resin include nitrate and sulphate.
  • the secondary ion exchange step 20 may be carried out using a cation exchange resin or a chelating resin.
  • the loaded uranium eluant stream 24 is then treated in a further treatment step 26 to provide a uranium containing product 28.
  • the wet-process phosphoric acid (WPA) 12 may be any WPA feed.
  • WPA is typically produced by reacting phosphate rock with sulphuric acid.
  • the WPA Prior to it being fed into the process of the present invention, the WPA may be treated in one or more pre-treatment steps.
  • the WPA feed 12 at a concentration of approximately 30% WPA may contain a significant amount of suspended solids, mostly sodium fluorosilicates and gypsum, which may cause issues for later stages of the process. In these cases, the WPA may be clarified.
  • the clarification step may comprise filtering the WPA to remove insoluble matter.
  • the clarification step may use an existing clarifier in a WPA plant and additional clarifiers, complementing the pre ⁇ existing clarifiers, are used to reduce the total suspended solids (TSS) and decrease process fluctuations due to upstream changes.
  • WPA can, for instance, be clarified in conventional clarifiers.
  • the clarifiers are dosed with flocculant to encourage precipitation of suspended solids. Underflow from the clarifier may be transferred back to the clarifier with the overflow being transferred to the next stage of the process.
  • the WPA 12 is an aqueous solution comprising from about 20% by weight to about 40% by weight WPA. In some embodiments, the WPA 12 is an aqueous solution comprising about 30% by weight WPA.
  • the first separation step 14 may be an ion exchange (IX) step or a solvent exchange (SX) step.
  • the first separation step 14 is an ion exchange step.
  • WPA feed 12 (which may or may not be a lowered iron content WPA or a valency reduced WPA as described in more detail below) is transferred to one or more ion exchange (IX) columns containing a chelating ion exchange resin.
  • IX ion exchange
  • each train of IX columns will nominally have one lead column, one catch (or tail) column and one column in elution/idle mode at any one time.
  • the uranium depleted WPA stream 18 is returned to WPA holding tanks to be used for fertilizer production, etc.
  • the elution procedure comprises eluting the IX column with eight Bed Volumes (BV) of ammonium carbonate solution.
  • Uranium forms a stable, soluble uranyl tricarbonate complex in the ammonium carbonate solution, whereas impurities such as iron will form insoluble compounds.
  • Precipitated iron can be removed from the eluate using filters prior to entering secondary IX where further rejection of impurities takes place.
  • the loaded uranium solution stream 16 containing uranyl carbonate from the first separation step 14 is then passed to the secondary anion exchange step 20, to extract the uranium onto the resin, and to recycle the ammonium carbonate.
  • a nominal 10% bleed may be removed to control impurity build up in the eluant and may be replaced with fresh ammonium carbonate solution.
  • the uranium bound to the IX column in the secondary anion exchange step 20 is then eluted using a solution containing chloride ions 22 to produce a uranium containing product 28.
  • Other anions that can be used for this step include sulphate and nitrate.
  • the first separation step 14 is a solvent extraction step.
  • WPA feed 12 (which may or may not be a lowered iron content WPA or a valency reduce WPA as described in more detail below) may be transferred to an oxidation stage in which the WPA is oxidized with an air/oxygen mixture and/or with a chemical oxidant, such as hydrogen peroxide or a WPA stream.
  • the oxidized WPA is then transferred to a solvent extractor.
  • the solvent extraction step 14 uses any organic solvent that has a high affinity for uranium. Examples of solvents of this type include a DEHPA TOPO (di-2-ethylhexyl phosphoric acid and trioctylphosphine oxide) system.
  • the solvent extraction step 14 is a multi-extraction DEHPA TOPO (di-2-ethylhexyl phosphoric acid and trioctylphosphine oxide) system, nominally with a concentration of 0.5M DEHPA and 0.125M TOPO in a kerosene based organic diluent, operated at around 40°C. Further details of the DEHPA TOPO can be found in Hurst et al . , Ind. Eng. Chem. Process Des . Develop., 1972, 11, 122-128, the details of which are incorporated herein by reference.
  • the uranium depleted WPA stream 18 is returned to WPA holding tanks to be used for fertilizer production, etc.
  • the pregnant organic phase is stripped with ammonium carbonate to provided loaded uranium solution stream 16.
  • FIG. 2 is a flow chart describing a second exemplary embodiment of the invention which is a process 40 for extracting uranium from wet-process phosphoric acid (WPA) 12.
  • the process 40 comprises contacting uranium laden WPA 12 with a first ion exchange resin in a first ion exchange step 42.
  • the first ion exchange resin is a chelating resin.
  • a uranium depleted WPA stream 44 is separated from the first ion exchange resin and the resin is then contacted with an oxidant 52 in an oxidation step 54 under conditions to oxidize substantially all of the uranium species on the resin.
  • the first ion exchange resin is then contacted with a stream comprising ammonia 46 in a stripping step 48 under conditions to remove at least some of any bound vanadium ions and/or organic species from the resin.
  • a vanadium and/or organic species enriched stream 50 is then separated from the first ion exchange resin.
  • the first ion exchange resin is subsequently contacted with an ammonium carbonate stream 56 in an elution step 58 under conditions to remove the oxidized uranium species from the resin and provide a uranium enriched ammonium carbonate stream 60.
  • the uranium enriched ammonium carbonate stream 60 is then contacted with an anion exchange resin in a second ion exchange step 62 and a uranium depleted ammonium carbonate stream 64 is separated from the second ion exchange resin.
  • the uranium species are then eluted from the second ion exchange resin in an elution step 66 to provide a uranyl solution 68.
  • the elution step 66 may be carried out using a solution comprising suitable anions, such as chloride, nitrate or sulphate.
  • FIG. 3 is a flow chart describing a third exemplary embodiment of the invention which is a process 40 for extracting uranium from wet-process phosphoric acid (WPA) 12.
  • WPA wet-process phosphoric acid
  • Process steps 42, 48, 54, 58, 62 and 64 in this embodiment are the same as those described in respect of the second exemplary embodiment and shown FIG. 2.
  • the first ion exchange step 42 is preceded by a valency reduction step 70.
  • the valency reduction step 70 comprises reducing the valency of ferric ions in the WPA 12 to produce a valency reduced WPA 72 which is then subjected to first ion exchange step 42.
  • the valency reduction step 70 may be important because any ferric iron has a deleterious effect on subsequent process steps of the uranium extraction process.
  • the ion exchange (IX) resin used in subsequent step(s) for the extraction of uranium has a high affinity to load ferric (Fe 3+ ) ions, which inhibits uranium loading. For this reason, it is preferable for the iron in the WPA feed 12 to be in the ferrous (Fe 2+ ) state.
  • the valency reduction in valency reduction step 70 may be carried out by contacting the WPA containing ferric (Fe 3+ ) ions with a suitable reducing agent.
  • suitable agents for this purpose include (but are not limited to) : metallic iron; ferro-phosphorus alloy; and ferro-silicon alloy.
  • the valency reduction in valency reduction step 70 may be carried out by reducing the ferric (Fe 3+ ) ions in the WPA in an electroreduction step.
  • the valency reduction step 70 comprises adding metallic iron to a reactor containing WPA 12 in order to reduce the ferric iron to ferrous iron.
  • metallic iron For example, concentrate may be pumped into three agitated tanks with a total residence time of three hours. Powdered or granular iron may be added into the first of two reactors at 120% stoichiometric equivalent (relative to the amount of ferric iron) .
  • the metallic iron could be substituted with or used in combination with ferro-phosphorus alloy or ferro-silicon alloy.
  • the valency reduction step 70 comprises electroreduction. Electroreduction may be advantageous because no chemical species are added to the WPA and it is easy to control electrolytic reduction. In one form of the electroreduction stage WPA feed is transferred to continuously operated electroreduction cells.
  • FIG. 4 is a flow chart describing a fourth exemplary embodiment of the invention which is a process 40 for extracting uranium from wet-process phosphoric acid (WPA) 12.
  • WPA wet-process phosphoric acid
  • Process steps 42, 48, 54, 58, 62, 64 and 70 in this embodiment are the same as those described in respect of the third exemplary embodiment and shown FIG. 3.
  • the valency reduction step 70 is preceded by an iron removal step 74.
  • the iron removal step 74 comprises decreasing the amount of dissolved iron species in the WPA relative to the amount of uranium species in the WPA to produce a lowered iron content WPA 76 having uranium species therein 76.
  • the lowered iron content WPA 76 has a lower amount of dissolved iron species than the raw WPA 12.
  • the lowered iron content WPA 76 is then subjected to the valency reduction step 70, which involves subjecting the lowered iron content WPA 76 to a reduction step, wherein the valency of dissolved iron species remaining in the lowered iron content WPA 76 is reduced .
  • the aim of the iron removal stage 74 is to lower the iron content. This can be done by removing the majority of the total iron present through precipitation of an iron ammonium phosphate (IAP) compound from the feed or pretreated WPA.
  • IAP iron ammonium phosphate
  • the IAP precipitation step is designed to remove a portion of the ferric iron, as a partial step prior to the valency reduction step. Additionally IAP precipitation reduces scaling species
  • WPA is transferred to a small pre-mix tank ammonia is added at a stoichiometric excess of approximately 300 - 1000% of the calculated ammonia requirements for formation of IAP.
  • the treated stream is transferred to overflow reactors.
  • the treated stream has a total residence time of 7 to 12 hours in the overflow reactors to allow completion of the IAP precipitation process.
  • the overflow from the overflow reactor is transferred to a centrifuge, or other solid liquid separation device, where IAP is separated from the WPA.
  • FIG. 5 is a flow chart describing a fifth exemplary embodiment of the invention which is a process 80 for extracting uranium from wet-process phosphoric acid (WPA) 12.
  • the process 80 comprises an oxidation step 82 in which uranium laden WPA 12 is contacted with an oxidant 84 to provide an oxidized WPA stream 86.
  • the oxidized WPA stream 86 is then contacted with a solvent 88 comprising di (2- ethylhexyl ) phosphoric acid and trioctylphosphine oxide in a solvent extraction step 90.
  • a uranium enriched organic solvent stream 92 is then separated from a WPA containing aqueous stream 94 and the uranium enriched organic solvent stream 92 is contacted with an ammonium carbonate solution 94 in a stripping step 96 under conditions to provide a uranium enriched ammonium carbonate stream 98.
  • the uranium enriched ammonium carbonate stream 98 is then contacted with an ion exchange resin in an ion exchange step 100.
  • a uranium depleted ammonium carbonate stream 102 is separated from the ion exchange resin and the resin is contacted with a solution containing chloride ions 104 and a uranyl solution 106 is separated from the ion exchange resin.
  • FIG. 6 is a flow chart describing a sixth exemplary embodiment of the invention which is a process 80 for extracting uranium from wet-process phosphoric acid (WPA) 12.
  • Process steps 82, 90, 96 and 100 in this embodiment are the same as those described in respect of the fifth exemplary embodiment and shown FIG. 5.
  • the solvent extraction step 90 is preceded by an iron removal step 108.
  • the iron removal step 108 comprises lowering the concentration of iron in the WPA 12 to produce a lowered iron content WPA 110 that is then subjected to the solvent extraction step 90.
  • the iron removal step may be carried out as described previously.
  • the uranium containing product 28 or uranyl solution 106 may be further treated to produce a commercial uranium product.
  • the uranium may be precipitated from the uranium containing product 28 or uranyl solution 106.
  • the step of precipitating the uranium from the uranium containing product 28 or uranyl solution 106 comprises acidification and removal of carbon dioxide generated, formation of a uranyl peroxide through the addition of hydrogen peroxide, as well as caustic soda as required for maintaining a suitable pH for the precipitation reaction.
  • the step of drying the precipitated product involves thickening the precipitate in a high rate thickener and drying in a low temperature dryer at 260° C.
  • the uranium containing product 28 or uranyl solution 106 is pumped into the first of three tanks in series. Hydrogen peroxide and caustic soda is added to enable precipitate uranium of oxides. The total residence time in the precipitation reactors is three hours. The underflow is transferred to a thickener, followed by drying of the precipitate at around 260° C and subsequent drumming into drums and finally packaging into shipping containers.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Inorganic Chemistry (AREA)
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  • General Chemical & Material Sciences (AREA)
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  • Metallurgy (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Treatment Of Water By Ion Exchange (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Extraction Or Liquid Replacement (AREA)

Abstract

La présente invention se rapporte, dans un mode de réalisation préféré, à un procédé permettant d'extraire l'uranium de l'acide phosphorique produit par voie humide, ledit procédé consistant à séparer l'uranium de l'acide phosphorique produit par voie humide afin de produire un courant de solution chargé d'uranium et un courant acide phosphorique produit par voie humide appauvri en uranium. Le courant de solution chargé d'uranium est ensuite mis en contact avec une résine échangeuse d'ions. Les types d'uranium liés à la résine échangeuse d'ions sont élués par mise en contact de la résine avec une solution qui comprend des anions pour produire un courant d'éluant chargé en uranium. Le courant d'éluant chargé en uranium est traité pour donner un produit qui contient de l'uranium.
PCT/US2012/062711 2011-10-31 2012-10-31 Extraction de l'uranium de l'acide phosphorique produit par voie humide WO2013066957A1 (fr)

Priority Applications (7)

Application Number Priority Date Filing Date Title
MX2014005312A MX2014005312A (es) 2011-10-31 2012-10-31 Extraccion de uranio a partir de acido fosforico de procedimiento en humedo.
EP12846133.2A EP2773783A4 (fr) 2011-10-31 2012-10-31 Extraction de l'uranium de l'acide phosphorique produit par voie humide
CA2854145A CA2854145A1 (fr) 2011-10-31 2012-10-31 Extraction de l'uranium de l'acide phosphorique produit par voie humide
BR112014010334A BR112014010334A2 (pt) 2011-10-31 2012-10-31 extração de urânio de ácido fosfórico de processo a úmido
KR1020147014379A KR20140123040A (ko) 2011-10-31 2012-10-31 습식 인산으로부터의 우라늄의 추출
PH1/2014/500971A PH12014500971A1 (en) 2011-10-31 2012-10-31 Extraction of uranium from wet-process phosphoric acid
TNP2014000183A TN2014000183A1 (en) 2011-10-31 2014-04-30 Extraction of uranium from wet-process phosphoric acid

Applications Claiming Priority (2)

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US201161553742P 2011-10-31 2011-10-31
US61/553,742 2011-10-31

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WO2013066957A1 true WO2013066957A1 (fr) 2013-05-10

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EP (1) EP2773783A4 (fr)
KR (1) KR20140123040A (fr)
BR (1) BR112014010334A2 (fr)
CA (1) CA2854145A1 (fr)
MX (1) MX2014005312A (fr)
PH (1) PH12014500971A1 (fr)
TN (1) TN2014000183A1 (fr)
WO (1) WO2013066957A1 (fr)

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CN109399591A (zh) * 2018-12-26 2019-03-01 江苏新宏大集团有限公司 一种净化湿法磷酸的制备方法

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US11708286B2 (en) 2020-08-19 2023-07-25 Marmon Industrial Water Llc High rate thickener and eductors therefor

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US4199470A (en) * 1977-05-13 1980-04-22 Koei Chemical Co., Ltd. Material for recovering uranium and method for recovering a uranium solution of high purity and high concentration, using the same
US4599221A (en) * 1983-08-01 1986-07-08 The State Of Israel, Atomic Energy Commission, Nuclear Research Center Negev Recovery of uranium from wet process phosphoric acid by liquid-solid ion exchange
US20100028226A1 (en) * 2008-07-31 2010-02-04 Urtek, Llc Extraction of uranium from wet-process phosphoric acid

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US6645453B2 (en) * 2001-09-07 2003-11-11 Secretary, Department Of Atomic Energy, Government Of India Solvent extraction process for recovery of uranium from phosphoric acid (25-55% P205)

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Publication number Priority date Publication date Assignee Title
US4199470A (en) * 1977-05-13 1980-04-22 Koei Chemical Co., Ltd. Material for recovering uranium and method for recovering a uranium solution of high purity and high concentration, using the same
US4599221A (en) * 1983-08-01 1986-07-08 The State Of Israel, Atomic Energy Commission, Nuclear Research Center Negev Recovery of uranium from wet process phosphoric acid by liquid-solid ion exchange
US20100028226A1 (en) * 2008-07-31 2010-02-04 Urtek, Llc Extraction of uranium from wet-process phosphoric acid

Non-Patent Citations (1)

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Title
See also references of EP2773783A4 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109399591A (zh) * 2018-12-26 2019-03-01 江苏新宏大集团有限公司 一种净化湿法磷酸的制备方法
CN109399591B (zh) * 2018-12-26 2021-06-29 江苏新宏大集团有限公司 一种净化湿法磷酸的制备方法

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BR112014010334A2 (pt) 2017-05-09
TN2014000183A1 (en) 2015-09-30
KR20140123040A (ko) 2014-10-21
EP2773783A1 (fr) 2014-09-10
PH12014500971A1 (en) 2014-06-09
EP2773783A4 (fr) 2015-09-23
MX2014005312A (es) 2015-01-19
CA2854145A1 (fr) 2013-05-10

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