Uranium recovery from wet process phosphoric acid

Claim 2

A process for the recovery of uranium from wet-process phosphoric acid derived from the acidification of uraniferous phosphate ores which comprises: (a) reducing the uranium to the uranous form; (b) contacting the reduced solution with a liquid-liquid solvent extraction agent which is a mixture of a mono- and di- (alkyl-phenyl) esters of orthophosphoric acid dissolved in an inert organic diluent, to effect transfer of the uranium into the organic phase; (c) stripping the uranium from the organic phase of step (b) with a phosphoric acid solution containing a sufficient amount of an oxidizing agent to convert uranous uranium to uranyl uranium; (d) contacting the diluted strip solution of step (c) with an organic phase containing as the liquid-liquid solvent extraction agent di(2-ethylhexyl) phosphoric acid and a synergistic agent dissolved in an inert organic diluent to effect transfer of the uranyl uranium into the organic phase; (e) stripping the loaded agent of step (d) with an alkali metal carbonate solution; (f) acidifying the strip solution of step (e) to precipitate iron, vanadium, and other impurities; (g) adding ammonia to the purified acidic solution of step (f) to precipitate the uranium, and (h) calcining the precipitated product of step (g) to a purified uranium oxide product.

Claim 3

The process of claim 1 in which the alkali metal carbonate is sodium carbonate.

Claim 4

The process of claim 1 in which the loaded agent of step (d) is scrubbed prior to stripping step (e).

Claim 5

The process of claim 3 in which the scrubbing is performed with at least a portion of the acidified strip solution of step (f).

Claim 6

The process of claim 1 in which the liquid-liquid solvent extraction agent in the stripped organic of step (e) in the sodium form is converted to the hydrogen form with a mineral acid and recycled to step (d).

Claim 7

The process of claim 5 in which the acid is sulfuric acid.

Claim 8

The process of claim 1 in which the oxidizing agent of step (c) is hydrogen peroxide.

Claim 9

The process of claim 1 in which uranium process organics from the aqueous raffinate resulting from the first uranium extraction step utilizing the OPPA-esters as extractants are removed from the raffinate of step (b).

Claim 10

The process of claim 8 in which the removed organics are returned to the organic phase of step (b) to substantially maintain the required balance of mono- and di- (alkyl-phenyl) esters of orthophosphoric acid in the liquid-liquid solvent extraction agent.

Claim 11

The process of claim 8 in which the process organics-free raffinate is returned to a wet-process phosphoric acid circuit.

Claim 12

The process of claim 8 in which the organics are removed by subjecting the raffinate sequentially to a flotation step and an absorption step on hydrophobic polystyrene beads.

Claim 13

The process of claim 11 in which the process organics are removed from the polystyrene beads by elution with methanol.

Claim 14

The process of claim 3 in which the ion exchange agent in the stripped organic of step (e) in the sodium form is converted to the hydrogen form with sulfuric acid and recycled to step (d).

Claim 15

The process of claim 3 in which the scrub is performed with at least a portion of the acidified strip solution of step (f) and the liquid-liquid solvent extraction agent in the stripped organic of step (e) in the sodium form is converted to the hydrogen form with sulfuric acid and recycled to step (d).

Claim 16

The process of claim 1 in which in step (a) the feed solution has been reduced to an emf more reducing than about -250 mv.

Claim 17

The process of claim 1 in which in step (c) the strip solution contains from about 39 to about 55 percent phosphoric acid, a stripping time of about 1/2 to about 5 minutes is used and an organic to aqueous ratio of about 0.1 to about 20 is used.

Claim 18

The process of claim 2 in which in step (e) a concentration of about 50 to about 200 gpl sodium carbonate is used, a contact time of about 1/2 to about 5 minutes is used and an organic to aqueous ratio of about 0.5 to about 10 is used.

Claim 19

The process of claim 2 in which in step (e) the molarity of the strip solution varies from about 0.5 to about 3.

Claim 20

The process of claim 18 in which the molarity of the strip solution is about 1.

Claim 21

The process of claim 1 in which in step (d) the synergistic agent is a member selected from the group consisting of trioctylphosphine oxide, di-butyl butylphosphonate and tributyl phosphate.

Claim 22

The process of claim 20 in which the synergistic agent is trioctylphosphine oxide.

Claim 23

The process of claim 20 in which the synergistic agent is di-butyl butylphosphonate.

Claim 24

The process of claim 20 in which the synergistic agent is tributyl phosphate.

Claim 25

The process of claim 1 in which in step (e) the alkali metal carbonate solution has an equilibrium pH between about 8 and 10.7.

Claim 26

The process of claim 2 in which in step (e) the alkali metal carbonate solution has an equilibrium pH between about 8 and about 10.7.

Claim 27

A process for the recovery of uranium from a wet-process phosphoric acid derived from the acidification of uraniferous phosphate ore which comprises: (a) reducing the uranium to the uranous form; (b) contacting the reduced solution of (a) with a liquid-liquid solvent extraction agent which is a mixture of mono- and di-(alkyl-phenyl) esters of orthophosphoric acid dissolved in an inert organic diluent, to effect transfer of the uranium into the organic phase; (c) removing uranium process organics from the raffinate of step (b) and returning at least some of them to the organic phase of step (b) to substantially maintain the required balance of mono- and disubstituted phenyl esters of orthophosphoric acid in the ion exchange agent; (d) stripping the uranium from the organic phase of step (b) with a phosphoric acid solution containing a sufficient amount of hydrogen peroxide to convert the uranous to uranyl uranium; (e) contacting the diluted strip solution of step (d) with an organic phase containing as the liquid-liquid solvent extraction agent di(2-ethylhexyl) phosphoric acid and a synergistic agent dissolved in an inert diluent to effect transfer of the uranyl uranium to the organic phase; (f) scrubbing the organic phase of step (e) with at least a portion of the acidified strip solution of step (i) below to remove phosphorus and other impurities; (g) stripping the scrubbed organic phase of step (e) with an alkali metal carbonate solution; (h) converting the liquid-liquid solvent extraction agent in the stripped organic of step (g) in the sodium form to the hydrogen form with sulfuric acid and recycling it to step (e); (i) acidifying the strip solution of step (g) with sulfuric acid to precipitate iron, vanadium, and other impurities; (j) adding ammonia to the purified acidic solution of step (i) to precipitate the uranium, and; (k) calcining the precipitated product of step (j) to a purified uranium oxide product.

Claim 28

A process for the recovery of uranium from a wet-process phosphoric acid derived from the acidification of uraniferous phosphate ore which comprises: (a) reducing the uranium to the uranous form; (b) contacting the reduced solution of (a) with a liquid-liquid solvent extraction agent which is a mixture of mono- and di-(alkyl-phenyl) esters of orthophosphoric acid dissolved in an inert organic diluent, to effect transfer of the uranium into the organic phase; (c) removing uranium process organics from the raffinate of step (b) and returning at least some of them to the organic phase of step (b) to substantially maintain the required balance of mono- and disubstituted phenyl esters of orthophosphoric acid in the ion exchange agent; (d) stripping the uranium from the organic phase of step (b) with a phosphoric acid solution containing a sufficient amount of hydrogen peroxide to convert the uranous to uranyl uranium; (e) contacting the diluted strip solution of step (d) with an organic phase containing as the liquid-liquid solvent extraction agent di(2-ethylhexyl) phosphoric acid and a synergistic agent dissolved in an inert diluent to effect transfer of the uranyl uranium to the organic phase; (f) scrubbing the organic phase of step (e) with at least a portion of the acidified strip solution of step (i) below to remove phosphorus and other impurities; (g) stripping the scrubbed organic phase of step (e) with an alkali metal carbonate solution; (h) converting the liquid-liquid solvent extraction agent in the stripped organic of step (g) in the sodium form to the hydrogen form with sulfuric acid and recycling it to step (e); (i) acidifying the strip solution of step (g) with sulfuric acid to precipitate iron, vanadium, and other impurities; (j) adding ammonia to the purified acidic solution of step (i) to precipitate the uranium, and; (k) calcining the precipitated product of step (j) to a purified uranium oxide product.

Claim 29

The process of claim 26 in which in step (g) the alkali metal carbonate solution has an equilibrium pH between about 8 and about 10.7.

Claim 30

In the process for recovery of uranium from wet process phosphoric acid derived from the acidification of uraniferous phosphate ore in which the uranium in the solution is reduced to uranous uranium, recovered from the solution in a first liquid-liquid solvent extraction circuit with a liquid-liquid solvent extraction agent consisting essentially of a mixture of mono- and di-(alkyl-phenyl) esters of orthophosphoric acid dissolved in an inert organic diluent, the raffinate recycled to the wet process plant, oxidatively stripping the uranium from the agent with phosphoric acid solution containing a sufficient amount of an oxidizing agent to convert the uranous to uranyl ions, recovering the uranyl ions from the strip solution in a second liquid-liquid solvent extraction circuit with an liquid-liquid solvent extraction agent consisting essentially of di(2-ethylhexyl) phosphoric acid and a synergistic concentration of trioctylphosphine oxide dissolved in an inert organic diluent, scrubbing the loaded agent of the second circuit with water to remove phosphate ions, stripping the scrubbed agent with ammonium carbonate solution to form a solution or slurry of ammonium uranyl tricarbonate, recycling the stripped agent to the second liquid-liquid solvent extraction step and calcining the ammonium uranyl tricarbonate to a uranium oxide product, the improvement which comprises removing uranium process organics from the aqueous raffinate resulting from the first uranium extraction step utilizing the OPPA-esters as extractants before recycling it to the wet process plant, adding the recovered organics to the first liquid-liquid solvent extraction step to maintain the proper ratio of mono- and disubstituted components in the liquid-liquid solvent extraction mixture, using phosphoric acid stripping solution containing about 39-55 percent phosphoric acid, a stripping time of about 1/2 to 5 minutes and an organic to aqueous ratio of about 0.1 to 20, the stripping solution containing hydrogen peroxide as the oxidizing agent in an amount of about 0.4 to 3.4 grams per liter of organic feed, scrubbing the loaded liquid-liquid solvent extraction agent of the second circuit with loaded sodium carbonate stripping solution from the immediately succeeding step which has been acidified, stripping the scrubbed agent with sodium carbonate solution having a concentration of about 50-200 grams per liter sodium carbonate in a strip contact time of about 1/2 to 5 minutes using an organic to aqueous ratio of about 0.5 to about 10, regenerating the stripped agent of the second circuit with sulfuric acid before recycling it to the second liquid-liquid solvent extraction step, acidifying the loaded sodium carbonate strip solution to remove impurities, adding ammonia to the acidified sodium carbonate strip solution to precipitate the uranium, and calcining the precipitated product to a purified uranium oxide product.

Claim 31

In the process for recovery of uranium from wet process phosphoric acid derived from the acidification of uraniferous phosphate ore in which the uranium in the solution is reduced to uranous uranium, recovered from the solution in a first liquid-liquid solvent extraction circuit with a liquid-liquid solvent extraction agent consisting essentially of a mixture of mono- and di-(alkyl-phenyl) esters of orthophosphoric acid dissolved in an inert organic diluent, the raffinate recycled to the wet process plant, oxidatively stripping the uranium from the agent with phosphoric acid solution containing a sufficient amount of an oxidizing agent to convert the uranous to uranyl ions, recovering the uranyl ions from the strip solution in a second liquid-liquid solvent extraction circuit with an liquid-liquid solvent extraction agent consisting essentially of di(2-ethylhexyl) phosphoric acid and a synergistic concentration of trioctylphosphine oxide dissolved in an inert organic diluent, scrubbing the loaded agent of the second circuit with water to remove phosphate ions, stripping the scrubbed agent with ammonium carbonate solution to form a solution or slurry of ammonium uranyl tricarbonate, recycling the stripped agent to the second liquid-liquid solvent extraction step and calcining the ammonium uranyl tricarbonate to a uranium oxide product, the improvement which comprises removing uranium process organics from the aqueous raffinate resulting from the first uranium extraction step utilizing the OPPA-esters as extractants before recycling it to the wet process plant, adding the recovered organics to the first liquid-liquid solvent extraction step to maintain the proper ratio of mono- and disubstituted components in the liquid-liquid solvent extraction mixture, using phosphoric acid stripping solution containing about 39-55 percent phosphoric acid, a stripping time of about 1/2 to 5 minutes and an organic to aqueous ratio of about 0.1 to 20, the stripping solution containing hydrogen peroxide as the oxidizing agent in an amount of about 0.4 to 3.4 grams per liter of organic feed, scrubbing the loaded liquid-liquid solvent extraction agent of the second circuit with loaded sodium carbonate stripping solution from the immediately succeeding step which has been acidified, stripping the scrubbed agent with sodium carbonate solution having a concentration of about 50-200 grams per liter sodium carbonate in a strip contact time of about 1/2 to 5 minutes using an organic to aqueous ratio of about 0.5 to about 10, regenerating the stripped agent of the second circuit with sulfuric acid before recycling it to the second liquid-liquid solvent extraction step, acidifying the loaded sodium carbonate strip solution to remove impurities, adding ammonia to the acidified sodium carbonate strip solution to precipitate the uranium, and calcining the precipitated product to a purified uranium oxide product.