EP0008552B1 - Procédé de récupération de l'uranium contenu dans une phase organique - Google Patents

Procédé de récupération de l'uranium contenu dans une phase organique Download PDF

Info

Publication number
EP0008552B1
EP0008552B1 EP79400553A EP79400553A EP0008552B1 EP 0008552 B1 EP0008552 B1 EP 0008552B1 EP 79400553 A EP79400553 A EP 79400553A EP 79400553 A EP79400553 A EP 79400553A EP 0008552 B1 EP0008552 B1 EP 0008552B1
Authority
EP
European Patent Office
Prior art keywords
uranium
process according
aqueous
organic phase
agent
Prior art date
Legal status (The legal status 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 status listed.)
Expired
Application number
EP79400553A
Other languages
German (de)
English (en)
French (fr)
Other versions
EP0008552A1 (fr
Inventor
Thomas Nenner
Dominique Foraison
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Rhone Poulenc Chimie de Base SA
Original Assignee
Rhone Poulenc Chimie de Base SA
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 Rhone Poulenc Chimie de Base SA filed Critical Rhone Poulenc Chimie de Base SA
Priority to AT79400553T priority Critical patent/ATE187T1/de
Publication of EP0008552A1 publication Critical patent/EP0008552A1/fr
Application granted granted Critical
Publication of EP0008552B1 publication Critical patent/EP0008552B1/fr
Expired legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • 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
    • C22B60/026—Obtaining thorium, uranium, or other actinides obtaining uranium by wet processes treatment or purification of solutions or of liquors or of slurries liquid-liquid extraction with or without dissolution in organic solvents
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals

Definitions

  • the present invention relates to a process for recovering uranium contained in a complexing organic phase and it relates more particularly to the concentration and purification of uranium extracted from a wet phosphoric acid.
  • the extraction agent as defined above can be combined with a well-known synergistic extraction agent such as, for example, alkylphosphates, alkylphosphonates, alkylphosphinates or trialkylphosphine oxides.
  • a well-known synergistic extraction agent such as, for example, alkylphosphates, alkylphosphonates, alkylphosphinates or trialkylphosphine oxides.
  • a well-known synergistic extraction agent such as, for example, alkylphosphates, alkylphosphonates, alkylphosphinates or trialkylphosphine oxides.
  • a well-known synergistic extraction agent such as, for example, alkylphosphates, alkylphosphonates, alkylphosphinates or trialkylphosphine oxides.
  • the organic phase contains, where appropriate, an organic diluent which is inert towards the extractants in order to improve the hydrodynamic properties of the organic phase.
  • organic diluent which is inert towards the extractants in order to improve the hydrodynamic properties of the organic phase.
  • many organic solvents or their mixtures can be used as a diluent.
  • aliphatic hydrocarbons such as kerosene, aromatic, halogenated and petroleum ethers, etc.
  • the characteristics of the inert diluent are not critical although some have advantages under particular conditions. 'use.
  • the starting organic phase contains uranium at the oxidation state (VI), taking into account the conditions for producing this solution. It also contains other chemical species depending on its production conditions. Especially in the case of a solution obtained by liquid-liquid extraction of a crude wet phosphoric acid, it usually contains phosphoric acid and other anions and metal cations such as AI, Fe, Ti, V , etc ... in the weakly concentrated state.
  • the uranium concentration of the organic phase is generally between 20 and 3000 mg expressed as metal uranium per liter of phase, preferably between 50 and 500 mg per liter.
  • the aqueous solution contains iron with the degree of oxidation (II).
  • the solution In order to shift the equilibrium of the reaction between the ions U (VI) and Fe (II) on the one hand and U (IV) and Fe (III) on the other hand, in the direction favorable to the production of ions U (IV), the solution should contain a large excess of iron (II) ion compared to uranium ions.
  • the concentration of the iron solution in the oxidation state (II) is usually between 0.5 and 100 grams per liter.
  • the concentration of strong acid in the solution can vary within wide limits.
  • the organic phase containing the uranium at the oxidation state (VI) and the aqueous solution which have been described above, are brought into contact in a conventional liquid-liquid extraction apparatus.
  • This contacting can be carried out in mixers- decanters, packed or pulsed columns, or any other suitable device, the contact being co-current or counter-current.
  • the temperature during contacting is not critical but for practical reasons it is preferred to operate between 20 ° C and 80 ° C, preferably in the vicinity of 50 ° C.
  • the iron of this added solution can be in the form of iron (II) or iron (III) ions and can come from either iron present in phosphoric acid, or iron (II) or iron (III) salt added to this solution, or iron attack by phosphoric acid.
  • Anodic compartments (13) leaves an aqueous solution which is sent to a storage not shown and containing, where appropriate, the complexing acid, uranium in the concentrated state substantially in U (VI) and l oxidizing agent in the oxidized state, which constitutes the production. This solution then undergoes subsequent treatments to recover the uranium.
  • the aqueous contact extraction solution comprises a strong and complexing acid and an oxidoreducing agent consisting of iron ions.
  • an oxidoreducing agent consisting of iron ions.
  • another redox agent it is possible to use another redox agent provided that it satisfies the requirements required above.
  • an aqueous phase (35) containing uranium (IV), iron (II) and iron (III) is removed.
  • This stream is divided into two streams (36) and (37).
  • Current (36) feeds the cathode compartments of a first battery of electrolytic elements schematically represented by (38).
  • This current after reduction, constitutes the current (39) which partially supplies the first contact zone (31).
  • the current (37) successively supplies the anode compartments of a second battery of electrolysis elements represented diagrammatically by (40) and then by the current (41) the anode compartments (42) of the first battery of electrolytic elements already mentioned. From the compartments (42) there flows a current (43) which constitutes the production and which is sent to storage, not shown.
  • the organic phase stream (32) is brought into contact with an aqueous solution (44) containing the complexing acid, iron (II) and iron (III) and a small proportion of 'uranium (IV).
  • an aqueous phase is removed from the zone (33) which is divided into a current (45) which feeds together with the current (39) described above, the first contact zone, and into a current (46), which after adding a fresh current containing the complexing acid and iron ions supplies the cathode compartments of the second battery of electrolytic elements already mentioned, and represented schematically by (48).
  • the material balance requires that the amounts of complexing acid and iron entering by the stream (47) are equal to those leaving in the production stream (43).
  • aqueous phase (61) enriched in uranium (IV) which is sent entirely into the anode compartments of the battery of electrolytic elements represented diagrammatically by (62), from which an aqueous stream (63) enriched in uranium (VI) is recovered which constitutes the production and which is sent to a storage not shown.
  • this mode may include the optional variant of processing the production by means of a very small quantity of chemical oxidizing agent.
  • a derivative current (75) is withdrawn from the last mixer-settler which is reintroduced into the first mixer-settler of said battery in order to form a loop. recycling (75-74).
  • the current (76) feeds the anode compartments of said battery of electrolytic elements, which are schematically represented by (77) and exits by the current (78) which constitutes the production.
  • This stream enriched in uranium (VI) is sent to storage for further processing.
  • the embodiment of FIG. 5 can optionally comprise the treatment of the production stream (78) by means of a very small quantity of chemical oxidizing agent.
  • the current (18) feeds the anode compartment (24) of the electrolysis cell.
  • Phase (30) is brought into contact with an aqueous solution which is the union of two streams, on the one hand stream (39) with a flow rate of 5 liters per hour of the following composition: and on the other hand, of a current (45) which will be explained below.
  • a solution of kerosene containing 0.5 mol / l of di (ethyl-2-hexyl) phosphoric acid, 0.125 mol / l of trioctylphosphine oxide and 150 mg / l of U (VI) ions is introduced in (70). ).
  • the flow rate is 41 / h, the temperature 55 ° C.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Metallurgy (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Mechanical Engineering (AREA)
  • Geology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • Inorganic Compounds Of Heavy Metals (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Extraction Or Liquid Replacement (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Electrolytic Production Of Metals (AREA)
  • Ceramic Products (AREA)
  • Stabilization Of Oscillater, Synchronisation, Frequency Synthesizers (AREA)
  • Processing Of Solid Wastes (AREA)
EP79400553A 1978-08-17 1979-08-03 Procédé de récupération de l'uranium contenu dans une phase organique Expired EP0008552B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT79400553T ATE187T1 (de) 1978-08-17 1979-08-03 Verfahren zur rueckgewinnung von uran aus einer organischen phase.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR7823950A FR2433587A1 (fr) 1978-08-17 1978-08-17 Procede de recuperation de l'uranium contenu dans une phase organique
FR7823950 1978-08-17

Publications (2)

Publication Number Publication Date
EP0008552A1 EP0008552A1 (fr) 1980-03-05
EP0008552B1 true EP0008552B1 (fr) 1981-09-02

Family

ID=9211858

Family Applications (1)

Application Number Title Priority Date Filing Date
EP79400553A Expired EP0008552B1 (fr) 1978-08-17 1979-08-03 Procédé de récupération de l'uranium contenu dans une phase organique

Country Status (16)

Country Link
US (1) US4341602A (xx)
EP (1) EP0008552B1 (xx)
JP (1) JPS5541992A (xx)
AT (1) ATE187T1 (xx)
BR (1) BR7905261A (xx)
CA (1) CA1127995A (xx)
DE (1) DE2960742D1 (xx)
EG (1) EG14862A (xx)
ES (1) ES483424A1 (xx)
FI (1) FI68664C (xx)
FR (1) FR2433587A1 (xx)
GR (1) GR69708B (xx)
IL (1) IL58056A (xx)
MA (1) MA18565A1 (xx)
SU (1) SU1058511A3 (xx)
ZA (1) ZA794288B (xx)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2450233A1 (fr) * 1979-02-28 1980-09-26 Rhone Poulenc Ind Procede de recuperation de l'uranium contenu dans un acide phosphorique impur
US4397820A (en) * 1980-07-24 1983-08-09 Wyoming Mineral Corporation Method to maintain a high Fe+2 /Fe+3 ratio in the stripping system for the recovery of uranium from wet process phosphoric acid
US4578249A (en) * 1983-09-02 1986-03-25 International Minerals & Chemical Corp. Process for recovery of uranium from wet process H3 PO4
DE3345199A1 (de) * 1983-12-14 1985-06-27 Kernforschungszentrum Karlsruhe Gmbh, 7500 Karlsruhe Verfahren zur reduktiven plutonium-rueckextraktion aus einer organischen wiederaufarbeitungsloesung in eine waessrige, salpetersaure loesung unter anwendung eines elektrolysestromes
GB8719045D0 (en) * 1987-08-12 1987-10-07 Atomic Energy Authority Uk Liquid treatment process
US8883096B2 (en) 2008-07-31 2014-11-11 Urtek, Llc Extraction of uranium from wet-process phosphoric acid
KR101389877B1 (ko) 2008-07-31 2014-04-29 우르텍, 엘엘씨 습식 공정 인산으로부터 우라늄의 추출
FR2965056B1 (fr) * 2010-09-16 2013-05-10 Areva Nc Procede de mesure de la concentration en uranium d'une solution aqueuse par spectrophotometrie

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2843450A (en) * 1955-01-18 1958-07-15 Jr Harold W Long Method of recovering uranium mineral values
US2790702A (en) * 1955-06-21 1957-04-30 Robert F Mccullough Acid treatment of phosphate rock to recover phosphates and uranium
FR1397587A (fr) * 1964-05-04 1965-04-30 Le Ministre De La Defense Perfectionnements apportés aux procédés pour l'extraction d'uranium
US3616276A (en) * 1969-04-14 1971-10-26 Allied Chem Process for changing the valence of a metal of variable valence in an organic solution
US3737513A (en) * 1970-07-02 1973-06-05 Freeport Minerals Co Recovery of uranium from an organic extractant by back extraction with h3po4 or hf
US3711591A (en) * 1970-07-08 1973-01-16 Atomic Energy Commission Reductive stripping process for the recovery of uranium from wet-process phosphoric acid
US3770612A (en) * 1970-08-24 1973-11-06 Allied Chem Apparatus for electrolytic oxidation or reduction, concentration, and separation of elements in solution
BE771349R (en) * 1971-08-16 1971-12-31 Allied Chem Concentrating metals - by preferential soln for different valencies of the metal
BE771350R (en) * 1971-08-16 1971-12-31 Allied Chem Metal transfer - from organic soln to aqs soln by electrochemical oxidation or reduction
DE2261018C3 (de) * 1972-12-13 1981-02-05 Kernforschungszentrum Karlsruhe Gmbh, 7500 Karlsruhe Gegenstromextraktrionskolonne zur Flüssig-Flüssig-Extraktion bei gleichzeitiger Elektrolyse
DE2449590C3 (de) * 1974-10-18 1980-06-12 Kernforschungszentrum Karlsruhe Gmbh, 7500 Karlsruhe Verfahren zur Reinigung von in niedrigen Oxidationszuständen befindlichen Aktiniden
US4234393A (en) * 1979-04-18 1980-11-18 Amax Inc. Membrane process for separating contaminant anions from aqueous solutions of valuable metal anions

Also Published As

Publication number Publication date
EG14862A (en) 1985-06-30
GR69708B (xx) 1982-07-09
FI68664C (fi) 1985-10-10
ES483424A1 (es) 1980-05-16
JPS6135256B2 (xx) 1986-08-12
FI792545A (fi) 1980-02-18
ATE187T1 (de) 1981-09-15
SU1058511A3 (ru) 1983-11-30
IL58056A (en) 1983-05-15
US4341602A (en) 1982-07-27
FR2433587A1 (fr) 1980-03-14
EP0008552A1 (fr) 1980-03-05
ZA794288B (en) 1980-09-24
CA1127995A (fr) 1982-07-20
FI68664B (fi) 1985-06-28
JPS5541992A (en) 1980-03-25
DE2960742D1 (en) 1981-11-26
MA18565A1 (fr) 1980-04-01
BR7905261A (pt) 1980-05-06
FR2433587B1 (xx) 1981-01-09

Similar Documents

Publication Publication Date Title
EP0015811B1 (fr) Procédé de récupération de l'uranium contenu dans un acide phosphorique impur
IE43467B1 (en) Treatment of sulphur-and-zinc containing ore or concentrate
EP0008552B1 (fr) Procédé de récupération de l'uranium contenu dans une phase organique
EP0198736B1 (fr) Procédé de séparation du cérium et de terres rares
KR101528507B1 (ko) 리튬계 전지로부터 코발트 및 망간의 동시 회수 방법
JPS5940490B2 (ja) ウラニウムアイソト−プ濃縮法
EP0026132B1 (fr) Procédé permettant la récupération globale de l'uranium, des terres rares, du thorium et de l'yttrium contenus dans une solution acide
AU2017265940B2 (en) A process for recovering gold from ores
AT520723B1 (de) Aufbereitung von Wolframcarbidzusammensetzungen
EP0014111B1 (fr) Procédé de fabrication de composés oxhydrylés de nickel et composés ainsi obtenus
CA1136423A (fr) Procede de recuperation de l'uranium d'un acide phosphorique impur
EP0299838B1 (fr) Procédé de réduction par électrolyse et de séparation de l'europium
FR2628408A1 (fr) Procede d'oxydation electrochimique du cerium 3+ en cerium 4+, en emulsion
KR840001196B1 (ko) 습식 인산으로부터 우라늄을 회수하는 방법
FR2589885A1 (fr) Procede de separation et de recuperation de metaux, dans des melanges de sulfures metalliques, tels que des minerais de plomb
KR840001065B1 (ko) 유기상에 포함되어 있는 우라늄의 회수방법
RU2534093C2 (ru) Способ переработки медеэлектролитного шлама
CN112210790B (zh) 一种铜阳极泥分铜液的处理方法
EP0251399A1 (fr) Procédé de séparation ou de récupération de plutonium et plutonium ainsi obtenu
RU2164554C1 (ru) Способ выделения благородных металлов из раствора
FR2463201A1 (fr) Procede de production d'electrolytes au cobalt exempts de chlore
KR840002457B1 (ko) 불순 인산중에 함유된 우라늄의 회수방법
BE875539A (fr) Procede de recuperation de valeurs metalliques a partir de boues d'anode

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Designated state(s): AT BE DE GB IT NL

17P Request for examination filed
ITF It: translation for a ep patent filed

Owner name: D. PERROTTA & C. S.A.S.

GRAA (expected) grant

Free format text: ORIGINAL CODE: 0009210

AK Designated contracting states

Designated state(s): AT BE DE GB IT NL

REF Corresponds to:

Ref document number: 187

Country of ref document: AT

Date of ref document: 19810915

Kind code of ref document: T

REF Corresponds to:

Ref document number: 2960742

Country of ref document: DE

Date of ref document: 19811126

RAP2 Party data changed (patent owner data changed or rights of a patent transferred)

Owner name: RHONE-POULENC RECHERCHES

RAP2 Party data changed (patent owner data changed or rights of a patent transferred)

Owner name: RHONE-POULENC CHIMIE DE BASE

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: DE

Payment date: 19840713

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: BE

Payment date: 19840930

Year of fee payment: 6

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: AT

Payment date: 19860828

Year of fee payment: 8

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: NL

Payment date: 19870831

Year of fee payment: 9

PGFP Annual fee paid to national office [announced via postgrant information from national office to epo]

Ref country code: GB

Payment date: 19890630

Year of fee payment: 11

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: AT

Effective date: 19890803

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: BE

Effective date: 19890831

BERE Be: lapsed

Owner name: RHONE-POULENC INDUSTRIES

Effective date: 19890831

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: NL

Effective date: 19900301

NLV4 Nl: lapsed or anulled due to non-payment of the annual fee
PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: DE

Effective date: 19900501

PG25 Lapsed in a contracting state [announced via postgrant information from national office to epo]

Ref country code: GB

Effective date: 19900803

GBPC Gb: european patent ceased through non-payment of renewal fee
PLBE No opposition filed within time limit

Free format text: ORIGINAL CODE: 0009261

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: NO OPPOSITION FILED WITHIN TIME LIMIT