Separation of zirconium and hafnium

Claim 2

A continuous process for the separation of the tetrahalides of hafnium and zirconium comprising dissolving a crude feed consisting essentially of hafnium tetrahalide and zirconium tetrahalide in a solvent comprising a near eutectic mixture of zirconium tetrahalide and at least one alkaline metal halide selected from the group consisting of sodium, potassium and lithium to form a first solution, introducing said first solution of an elevated temperature into a distillation tower, withdrawing hafnium tetrahalide vapor from the said solution as the overhead product, adding at least one alkaline metal halide selected from the group consisting of sodium, lithium and potassium to a portion of said hafnium tetrahalide vapor at an elevated temperature to form an eutectic second solution, introducing said second solution into the distillation tower as a reflux, withdrawing an eutectic third solution of zirconium tetrahalide and at least one alkaline metal halide selected from the group consisting of sodium, potassium and lithium as a bottoms fraction from said distillation tower, and separating from said third solution a portion of zirconium tetrahalide.

Claim 3

The process of claim 1 wherein said halide is chloride.

Claim 4

The process of claim 2 wherein said alkaline metal halide consists of a mixture of sodium chloride and potassium chloride.

Claim 5

The process of claim 1, wherein zirconium tetrahalide is separated from the eutectic third solution by vaporization.

Claim 6

The process of claim 1, wherein a fraction of the remainder of said third solution after said separation of a portion of zirconium tetrahalide therefrom is reduced to produce zirconium metal.

Claim 7

The process of claim 4 further including recycling substantially the remainder of said third solution, after separation of zirconium tetrahalide therefrom, as solvent to dissolve said crude zirconium tetrahalide feed, the said remainder containing zirconium tetrahalide.

Claim 8

The process of claim 4 further including recycling a portion of pure zirconium tetrahalide vapor to the bottom of said distillation tower to improve the separation efficiency in the lower portions of the tower.

Claim 9

The process of claim 6, wherein said halides are chlorides.

Claim 10

The process of claim 8, wherein said alkaline salt consists of sodium chloride and potassium chloride.

Claim 11

A continuous process for the separation of the tetrahalides of hafnium and zirconium and for the production of pure zirconium metal comprising mixing crude zirconium tetrachloride containing hafnium tetrachloride with sodium chloride and potassium chloride to form an eutectic salt containing about 65 mole percent zirconium tetrachloride and hafnium tetrachloride, about 29 mole percent potassium chloride and about 8 mole percent sodium chloride, melting the mixture at a temperature less than about 220°C to form a molten salt mixture, feeding the molten salt mixture to a distillation tower and withdrawing pure hafnium tetrachloride vapor as an overhead product, removing a bottoms product from said tower comprising a molten hafnium-free salt containing about 85 percent by weight zirconium tetrachloride, heating said bottoms product to remove a portion of the pure zirconium tetrachloride, reducing said pure zirconium tetrachloride with magnesium to provide pure zirconium metal, recycling the remainder of the bottoms product to said eutectic salt and combining a portion of the hafnium tetrachloride overhead product with a mixture of sodium chloride and potassium chloride to form an eutectic reflux which is introduced to said column.

Claim 12

A continuous process for the separation of the tetrahalides of hafnium and zirconium and for the production of pure zirconium metal comprising mixing crude zirconium tetrachloride containing hafnium tetrachloride with sodium chloride and potassium chloride to form an eutectic salt containing about 65 mole percent zirconium tetrachloride and hafnium tetrachloride, about 29 mole percent potassium chloride and about 8 mole percent sodium chloride, melting the mixture at a temperature less than about 220°C to form a molten salt mixture, feeding the molten salt mixture to a distillation tower and withdrawing pure hafnium tetrachloride vapor as an overhead product, removing a bottoms product from said tower comprising a molten hafnium-free salt containing about 85 percent by weight zirconium tetrachloride, heating said bottoms product to remove a portion of the pure zirconium tetrachloride, reducing said pure zirconium tetrachloride with magnesium to provide pure zirconium metal, recycling the remainder of the bottoms product to said eutectic salt and combining a portion of the hafnium tetrachloride overhead product with a mixture of sodium chloride and potassium chloride to form an eutectic reflux which is introduced to said column.

Claim 13

A process according to claim 1, further including reducing the hafnium tetrachloride product with magnesium to provide pure hafnium metal.

Claim 14

The process of claim 2, wherein the separated tetrachloride streams are respectively reduced with magnesium to provide pure metals.

Claim 15

The process of claim 1 wherein the temperature of the distillation column is maintained at about 325°C at the upper portion of the column and about 400°C at the lower portion of the column, and the pressure is maintained at about one atmosphere.