# US 5,344,623 A · Process for the extraction of strontium from acidic solutions

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- Number: US 5,344,623 A
- Document ID: US5344623A
- Status: Granted
- Kind: A
- Application number: 08/076,881
- Filed: 1993-06-15
- Granted: 1994-09-06
- Earliest claimed: 1993-06-15
- Assignees: The United States of America as represented by the United States Department of Energy
- Inventors: E. Philip Horwitz; Mark L. Dietz
- Web page: https://patentgrep.com/patent/US5344623A

## CPC

- C01B 21/46: Purification; Separation {; Stabilisation (C01B21/40 takes precedence)}
- C22B 26/20: Obtaining alkaline earth metals or magnesium
- C01B: NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; {METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C}
- C22B: PRODUCTION AND REFINING OF METALS (electrolytic C25); PRETREATMENT OF RAW MATERIALS

## Abstract

The invention is a process for selectively extracting strontium values from aqueous nitric acid waste solutions containing these and other fission product values. The extractant solution is a macrocyclic polyether in an aliphatic hydrocarbon diluent containing a phase modifier. The process will selectively extract strontium values from nitric acid solutions which are up to 6 molar in nitric acid.

## Claims

### Claim 1

A process of recovering strontium values from an aqueous nitric acid feed solution contain this and other fission product values comprising:
contacting the aqueous feed solution containing from about 1 to 6 molar nitric acid with an organic extractant solution consisting of a crown ether in a diluent, the diluent being selected from the group consisting of a neat phase modifier and a paraffinic hydrocarbon having from 10 to 15 carbons containing a phase modifier;
maintaining the contact for a period of time sufficient for the strontium values in the feed solution to be taken up by the extractant; and
separating the extractant from the feed solution, thereby separating the strontium values from the aqueous acid feed solution.

### Claim 2 (depends on 1)

The process of claim 1 wherein the crown ether has the formula: 4,4'(5')[(R,R')Cyclohexano]-18-crown-6, where R and R' are one or more members selected from the group consisting of H, methyl, propyl, t-butyl, hexyl and octyl.

### Claim 3 (depends on 2)

The process of claim 2 wherein the extractant solution is from 0.1 to 0.5M in crown ether.

### Claim 4 (depends on 3)

The process of claim 3 wherein the diluent is selected from the group consisting of neat tri-n-butyl phosphate, and normal and iso-paraffinic hydrocarbons consisting of 10 to 15 carbons containing an organophosphorous compound as a phase modifier.

### Claim 5 (depends on 4)

The process of claim 4 wherein the phase modifier is selected from the group consisting of tri-n-butyl phosphate, diamyl amylphosphonate, bis(2-, 4, 4-trimethylpentylphosphinic acid and a mixture of trialkylphosphine oxides of the formulas R.sub.3 P(O) , R.sub.2 R'P(O), RR'.sub.2 P(O) and R'.sub.3 P(O), where R=CH.sub.3 (CH.sub.2).sub.7 and R'=CH.sub.3 (CH.sub.2).sub.5, said mixture having a molecular weight of about 348 and a flash point of about 182.degree. C.

### Claim 6 (depends on 5)

The process of claim 5 wherein the extractant solution contains about 1.0 to 3.0M phase modifier.

### Claim 7 (depends on 6)

The process of claim 6 wherein the crown ether is selected from the group consisting of dicyclohexano-18-crown-6, bis[methylcyclohexano]-18-crown-6 and bis 4, 4'(5')[(t-butyl)cyclohexano]-18-crown-6.

### Claim 8 (depends on 7)

The process of claim 7 wherein the extractant solution consists of about 0.2M bis-4,4'(5')[(t-butyl)cyclohexano]-18-crown-6 in dodecane containing about 1.2M tri-butylphosphate as a phase modifier.

### Claim 9 (depends on 8)

The process of claim 8 including the additional step of contacting the loaded extractant solution with an aqueous stripping solution containing up to about 0.5M nitric acid thereby recovering the strontium values from the extractant solution.

### Claim 10

A process of recovering strontium values from an aqueous acid feed solution containing these and other fission product values comprising:
contacting the aqueous feed solution containing from about 1M to about 6M nitric acid with an extractant solution of about 0.2M bis-4, 4'(5')[(t-butyl)cyclohexano]-18-crown-6 in dodecane and about 1.2M tri-n-butyl phosphate at a temperature between about 25.degree. and about 60.degree. C.;
maintaining the contact for at least 1 minute for the strontium values to be taken up by the extractant solution; and
separating the loaded extractant solution from the aqueous solution, thereby separating the strontium from the aqueous acid feed solution.

### Claim 11 (depends on 10)

The process of claim 10 including the additional step of contacting the loaded extractant solution with an aqueous stripping solution containing up to about 0.05 H nitric acid thereby recovering the strontium values from the extractant solution.