Zirconium isotope separation process

The present process is a process for separation of the zirconium 91 isotope from other isotopes in zirconium and uses a photo-assisted solvent extraction system.
It has been disclosed, for example, in U.S. Pat. No. 4,389,292 and U.S. Pat. No. 4,612,097, both of which are assigned to the assignee of the present invention, to separate isotopes of zirconium by a photochemical method based upon electronic excitation of zirconium complexes. The isotope effect arises from the interaction of nuclear magnetic moment with the excited electronic state. For zirconium, only the isotope with mass 91 has a nonzero nuclear magnetic moment, so the molecules in a supply of zirconium may be separated into two portions by photochemical excitation. The two portions differ by the lifetime of the excited state, so that the portion containing .sup.91 Zr has a longer excited state lifetime than the portion containing the other isotopes of zirconium (having masses of 90, 92, 94 and 96 amu).
In U.S. Pat. No. 4,389,292, which is incorporated by reference herein, a chemical isotope separation process involves initially forming a zirconium complex or chelate and exposing the same to selected wavelength photons such that the metal ligand bond may rupture and then reform. The photon excited states of the metal-ligand bond for even and odd zirconium isotopes are a singlet and triplet which drop back to the ground state at slightly different rates. If a scavenger, or second chelate or complexing liquid, is available to react with the excited metal-ligand molecule, then the product of this reaction would become enriched with the .sup.91 Zr isotope since the triplet state is expected to remain in the excited state for a longer time.
In U.S. Pat. No. 4,612,097, which is incorporated by reference herein, the zirconium 91 isotope content of zirconium is reduced by forming a solution of a zirconium compound and a scavenger of 8-hydroxyquinoline or its derivatives, and irradiating the solution with light at wavelength that excites the zirconium compound such that it reacts with the scavenger. Since the zirconium 91 isotope remains excited longer, the same reacts disproportionately with the scavenger. The reaction product is precipitated from the solution and is enriched in the .sup.91 Zr isotope.
In order to achieve a significant isotope separation, the two above-described photochemical processes preferably use a zirconium complex such as zirconium tetraacetylacetonate [Zr(AcAc).sub.4 ], which is soluble in a variety of solvents, including acidic water,, methanol or cyclohexanol, with a scavenger, or molecular, present which will react with the electronically excited zirconium complex. As described above, since the zirconium complexes containing the mass 91 isotope have a longer excited state lifetime, the probability of reaction is higher for such excited species than is the probability of reaction for the zirconium complexes containing the other isotopes. In these previous systems, the photochemical product was a precipitate. A minimum degree of enrichment of the precipitate resulted in a precipitate with about 11.45 percent .sup.91 Zr and the remaining solution contained a fraction of zirconium with about 11.05 percent .sup.91 Zr, compared to the natural abundance of about 11.23 percent of that isotope in zirconium. The parameter used to characterize such a separation is the heads to tails separation factor, ##EQU1## where X.sub.h is the mole fraction of a given isotope in the heads fraction and X.sub.t is the mole fraction of the same isotope in the tails fraction.
An overall separation that reduces the .sup.91 Zr isotope content of zirconium to less than one percent is desired. The necessary alpha depends on the cut, or fraction of feed resulting in the desired product. For a cut of one-third, an overall alpha of 18.5 is requied. The dependence of alpha on cut, for production of zirconium with less than one percent .sup.91 Zr, is shown in FIG. 1. It is clear that an overall alpha of 15 to 20 will be required in order to obtain the necessary isotope separation with a reasonable cut. Since the observed photochemical separation factor for the precipitation process is only 1.05, it is necessary to find a way to increase the same.
Solvent extraction is a common industrial process with applications for separation of similar chemical species, and with known application to isotope separation. For example, uranium isotopes can be separated by solvent extraction, as described by S. Villani in Isotope Separation, American Nuclear Society, 1976, P. 53, but the single stage separation factor is .alpha.=1.0016. No economic solvent extraction process for uranium enrichment has been developed. Also, as described in U.S. Pat. No. 4,584,183, assigned to the assignee of the present invention, and which is incorporated by reference herein, a solvent extraction-exchange process is usable to separate a feed stream of an aqueous solution of a mixture of .sup.90 Zr salts into two aqueous product streams, each containing both a .sup.90 Zr isotopic portion and a .sup.91 to .sup.96 Zr isotopic portion, but in different ratios. The zirconium salts usable are thiocyanate, nitrate, sulfate, chloride, and perchlorate salts and mixtures thereof.
SUMMARY OF THE INVENTION
A process for separating the zirconium 91 isotope in zirconium is provided wherein a first solution of solvent, scavenger and zirconium compound, which compound reacts with the scavenger when exposed to light, is formed and irradiated to photoreact a disproportionate amount of the zirconium compound containing the 91 isotope with the scavenger to form a reaction product. At the same time, the irradiated first solution is contacted with a second solvent that is immiscible with the first solvent and is a preferential solvent for the zirconium reaction product, with reaction product thus transferred to the second solvent to form a second solution, and the two solutions are then separated.
The first solvent is preferably an acidic aqueous media, and the second solvent an immiscible organic solvent such as benzene or kerosene containing an extractant medium. The scavenger may be an additional chemical compound in the aqueous acidic media or an excess of acid may be used to provide anions which act as scavengers.

BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a graphic illustration between cut (heads/feed) and overall process .alpha. for production of zirconium with .sup.91 Zr of less than 1 percent for a photochemical process that specifically removes .sup.91 Zr;
FIG. 2 graphically illustrates a maximum single state separation factor (.alpha..sub.ss) calculated for photochemical zirconium isotope separation, as a function of excited state lifetime ratio. .alpha..sub.ss is less than 1 because .sup.91 Zr is being depleted;
FIG. 3 is a graphical illustration of a calculated overall alpha required for production of zirconium with less than 1 percent of .sup.91 Zr for a solvent extraction process (A) and the present photo-assisted solvent extraction process (B) as a function of cut;
FIG. 4 is an illustration of absorption spectrum of a zirconium reaction system, and emission spectrum of high pressure sodium vapor lamp (HPS) used for isotope enrichment, illustrating that a mercury bromide lamp (HgBr.sub.2) would be a better match to the absorption spectrum;
FIG. 5 illustrates the isotopic enrichment of a zirconium tetrachloride/4M HCl/H.sub.2 C.sub.2 O.sub.4 : thenoyltrifluoroacetone/xylene system following two hours of photolysis with a 200 W HPS lamp, with .alpha..sub.s for each isotope calculated from analysis of aqueous phase, assuming a distribution coefficient K=1; and
FIG. 6 is a process diagram for a 3-stage shakeout experiment. Aqueous feed loaded with zirconium is contacted with organic solvent and extractant at A1. The mixture is stirred and irradiated for a selected time, and then allowed to separate. The separated phases are propogated through the diagram as shown, with fresh organic introduced at A1, A2 and A3, and fresh aqueous at A1, B1 and C1.

DETAILED DESCRIPTION
In the present solvent extraction-photochemical zirconium isotope separation process, distribution of zirconium between the two phases, or solvent streams, is accomplished by having the zirconium present as two distinct chemical species, one of which is preferentially soluble in a first solvent (e.g. acidic water) and the other of which is preferentially soluble in the immiscible second solvent (e.g. xylene). The two zirconium species are in thermodynamic equilibrium governed by the zirconium distribution coefficient: ##EQU2## where for the sake of the argument ZrX is the preferentially aqueous phase soluble species and ZrY is the species preferentially dissolved in the organic solvent. The brackets indicate concentration.
In order for solvent extraction isotope separation to occur, it is necessary for K in Eq. 2 to vary slightly depending on which isotope of zirconium is involved, and for kinetic exchange of Zr between phases to proceed at a viable rate. In principle, the faster the exchange rate, the better.
The exchange reaction can be written as follows:
ZrX+Y.revreaction.ZrY+X (3)
The effect of photochemistry is that one of the zirconium species, for instance ZrX, absorbs light of a selected wavelength with the result tht the rate of reaction is increased for conversion of ZrX to ZrY, and furthermore that the increase is greater if a .sup.91 Zr atom is involved. The overall equilibrium still applies, so the back conversion of ZrY to ZrX also is speeded up, but this process is not isotope selective. The effect is to deplete the ZrX phase in .sup.91 Zr and to enrich the ZrY phase in .sup.91 Zr. The efficiency of this enrichment step should be the same as was observed in the previously described precipitation process of U.S. Pat. No. 4,612,097.
Under steady illumination conditions, the isotope ratio in the excited state can be calculated. Zr is considered to consist of two fractions, X.sub.o being the fraction of .sup.91 Zr in the ground state, and (1-X.sub.o) the fraction of the other isotopes in the ground state. When a sample of mixed Zr isotopes is excited, the .sup.91 Zr relaxes to the ground state with a characteristic lifetime t.sub.o, and the other isotopes relax with lifetime t.sub.e. The ratio k=t.sub.o /t.sub.e only needs to be different from 1 to produce an isotope effect. If light is being absorbed at a rate I.sub.o, then .sup.91 Zr excited states are being created at the rate X.sub.o I.sub.o and excited states of the other isotopes are being created at the rate (1-X.sub.o)I.sub.o. The excited state populations obey the equations: ##EQU3## At steady state, the rate of change is zero, so ##EQU4## The fraction of .sup.91 Zr in the excited state, then, is given by ##EQU5## Notice that the excited state isotope ratio depends only on the ground state ratio and the ratio, k, of excited state lifetimes. Furthermore, when k is small and the isotope composition is typical of .sup.91 Zr(X.sub.o .about.0.1), the excited state isotope ratio depends almost linearly on k.
It is possible to calculate the single-stage enrichment produced by photochemial excitation of Zr complexes. The process was modeled by computer in the following manner. Starting with the natural composition, the excited state isotope mixture was calculated, and it was assumed that 10% of the total Zr reacted under those conditions. The result is a shift in the isotope ratio and of the total concentration of Zr in each solvent. Overall equilibrium (Eq. 2) was then restored by shift of 10% of the Zr back into the first solvent. The process was repeated iteratively until no further change resulted. .alpha..sub.SS was then calculated from the isotope composition of each solvent phase. The single stage enrichment factor thus calculated is independent of the distribution constant, and nearly linearly dependent on the lifetime ratio, k. Results are given in FIG. 2.
In solvent extraction mode the two Zr complexes are being carried along with the counter current flowing solvents. The photochemical exchange process is continually shifting Zr from one solvent to the other. The overall equilibrium is also being maintained. The result is continuous enrichment, similar to normal solvent extraction. However, coupling the photochemical process to counter-current solvent extraction gives a single-stage separation factor that is determined by the optical properties of the system. The result can be a photochemical separation factor that is much larger than the normal solvent extraction separation factor, resulting in a much smaller system. If the number of stages is cut by a factor of 10, in general the corresponding inventories of solvents and reagents will also be cut by a factor of 10.
Solvent extraction separation, in general, is based on distribution of a chemical system between two immiscible solvents, so a distribution constant of the type ##EQU6## applies. As a sample moves through a solvent extraction column, the components repeatedly exchange between the counterflowing solvents, and enrichment or depletion in a particular stream occurs on the basis of different values of K. Thus, for isotope separation by solvent extraction it is necesary to find solvents and extractants that give isotope dependent K values.
The single-stage separation factor is the key parameter for design of a multi-stage solvent extraction column. For the present process, such a column would have a number of theoretical stages sufficient to give the desired final product composition. This number of stages is determined by the cut, which defines the tails composition, and the Fenske equation which relates the number of stages to the overall process alpha, .alpha., and the single stage alpha, .alpha..sub.s :
N+1=log .alpha./ log .alpha..sub.s (10)
If the cut is designated as
Z=H/F (11)
then the tails composition can be calculated from the feed composition, the desired heads composition and the cut: ##EQU7## where again the summation is over all the isotopes in the tail.
.alpha.is now calculated as a function of cut, using Equation 9 with the overall heads and tails compositions calculated from Eqs. 12-14. The number of theoretical stages required to achieve the required separation, as a function of z and .alpha..sub.s is shown in FIG. 3, for solvent extraction (A) and for the present process (B).
In solvent extraction isotope separation, the isotope effect on the distribution ratio is found to be proportional to the mass difference between isotopes, and usually depends on the ratio .DELTA.M/M where .DELTA.M is the difference between the isotope masses and M is the average mass. For solvent extraction separation of Zr, it is necessary to concentrate on the separation of .sup.90 Zr from .sup.91 Zr. The other (heavier) isotopes would be expected to separate more efficiently from .sup.90 Zr because of their larger M values. Thus, a solvent extraction process to produce Zr with <1% .sup.91 Zr must enrich .sup.90 Zr to approximately 99% purity. Pure solvent extraction has a limit on cut of z=0.5 and will produce a waste stream enriched in all the other isotopes. A large number of theoretical stages are required because the required overall separation factor is large and the stage separation factor is small.
Photochemical enhancement of solvent extraction according to the present process will improve the separation of .sup.90 Zr from .sup.91 Zr by introducing an effect that specifically removes the one undesirable isotope. The present process will produce product that has .sup.90 Zr enriched by solvent extraction to an overall degree determined by .alpha..sub.s, Z and the number of stages, N.sub.s. Because of the photochemical effect, depleting .sup.91 Zr to 1% requires fewer stages than a straight solvent extraction process to achieve the same .sup.90 Zr/.sup.91 Zr ratio. As a result, some of the heavier isotopes will be left in the product and a larger cut is possible. Because the product can contain all the even-mass isotopes, maximum theoretical cut is increased to 90% and fewer theoretical stages are required. These benefits do, however, require capital investment and operating expense for lamps and electrical power. Straight solvent extraction will produce a product with a neutron capture cross section of 38 mbarn, compared to the natural value of 97 mbarn. The present process produces a product that contains all even-mass isotopes and a slightly larger cross section of 50 mbarn will result. The following table lists the predicted properties of a "pure solvent extraction" product and of a "pure photochemical" product, although it must be remembered that the present process will combine some solvent extraction-type enrichment of .sub.90 Zr relative to the other even-mass isotopes, so the present product will be intermediate in properties between the two limiting cases:
______________________________________COMPARISON OF CALCULATED PRODUCT COMPO-SITION AND ENRICHMENT FACTORS FOR PHOTO-CHEMICAL PROCESS (ASSUMING NO SOLVENT EX-CHANGE CONTRIBUTION) AND FOR SOLVENTEXCHANGEISOTOPE 90.sub.Zr 91.sub.Zr 92.sub.Zr 94.sub.Zr 96.sub.Zr______________________________________Natural 0.5145 0.1132 0.1789 0.1728 0.0278PHOTOCHEMICAL RESULT, CUT = 0.8X.sub.H 0.5698 0.0099 0.1981 0.1914 0.0308X.sub.T 0.3612 0.3723 0.1256 0.1213 0.0195 2.3420 0.0169 1.7200 1.7140 1.59571/ 0.4270 59.3110 0.5814 0.5834 0.6267SOLVENT EXTRACTION RESULT, CUT = 0.3X.sub.H 0.9887 0.0099 0.0010 0.0003 0.0001X.sub.T 0.3077 0.1560 0.2527 0.2444 0.0393 197.3439 0.0540 0.0029 0.0009 0.00241/ 0.0051 18.5027 341.6445 1089.8515 413.5830______________________________________
It is also worthy of note that the amount of waste Zr produced by the two processes is quite different. The production of 954,000 lbs/yr of enriched Zr by a solvent extraction process, at a cut of 0.3, will leave 2.2 million pounds of Zr waste with a neutron capture cross section of 127 mbarn. Production of the same amount of Zr product by the present process, operating at a cut of 0.8, will give only 0.24 million pounds of waste Zr, with a net neutron capture cross section of 228 mbarn.
The two solvents used in the present photo-assisted solvent extraction process must be immiscible to enable ready separation thereof. The first solution will generally use acidic water as a solvent and will contain the zirconium compound being treated and a scavenger for the zirconium compound when exposed to light of the designated wavelength. The water should be acidified in order to serve as a solvent for the zirconium compound and the scavenger and is a 0.5 to 8.0 molar acidic aqueous solution. Acids that are suitable in forming the 0.5 to 8.0 molar solution are preferably hydrochloric, nitric and sulfuric acids.
The acidic solution contains a zirconium compound that is soluble therein and which is excitable by the light of the designated range. Examples of such zirconium compounds are zirconium sulfate, Zr(SO.sub.4).sub.2 ; zirconyl chloride, ZrOCL.sub.2 ; zirconium perchlorate, Zr(ClO.sub.4).sub.2, and zirconium tetrachloride, ZrCl.sub.4 ; as well as zirconium oxide, ZrO.sub.2, which will form a salt and dissolve in an acidic aqueous solution, for example forming zirconyl chloride (ZrOCl.sub.2) upon dissolving in an aqueous hydrochloric acid medium.
Scavengers that may be added to the first solvent, in formation of the first solution, may be the complexing agents such as citric acid, tartaric acid and beta diketones, such as acetylacetone, dibenzoylmethane, benzoylacetone, trifluoroacetylacetone and other beta diketones. 8-hydroxy quinoline ("oxine") and its derivatives such as chloro, bromo, fluoro and hydroxy derivatives are also useful, as described in U.S. Pat. No. 4,612,097. Or, an excess of the ions from the acid in the aqueous solution, such as chloride ions, or other ions, may serve as a scavenger. By adjustment of the pH of the aqueous solution to a value where the ratio of such ion to zirconium present in the first solution is greater than 1:1, the excess anions resulting can serve as a scavenger.
The first solution, containing the zirconium compound in a first solvent and a scavenger therefor is irradiated with light at a wavelength of between about 220-600 nm. Experiments have been made to demonstrate that photochemical systems could produce isotope separation using conventional light sources. A sodium vapor lamp was used for this purpose (exposure to sunlight has also been shown to cause similar Zr isotope separations). FIG. 4 shows the emission spectrum of a sodium vapor lamp (left side of figure), as well as that for a mercury halide lamp (HgBr.sub.2). Isotope separation was observed with the sodium vapor lamp even though the lamp spectrum barely overlaps the absorption spectrum of the Zr complexes. Better separation should result from the use of a mercury halide lamp since its spectrum would give a better match to the Zr absorption.
While beinbg irradiated with the light of the required wavelength, the first solution is contacted with a second solvent that is immiscible with the first solvent, and which is a preferential solvent for the reaction product formed in the first solution by the irradiation. The second solvent is preferably selected from benzene, toluene, xylene, a kerosene, or other water immiscible organic solvent. The solvent preferably contains an extractant medium for the zirconium reaction product formed in the first solution, such as benzyoylactone (BzAc), 2-thenoyltrifluoracetone (HTTA), dibenzoylmethane (DBM), a primary amine such as that sold under the tradename PRIMENE JMT sold by Rohm & Haas, a phosphoric acid such as bis(2, 4, 4')trimethylpentyl phosphoric acid sold under the tradename Cyanex 272 sold by American Cyanamid, or quaternary ammonium salts such as tricaprylyl methyl ammonium chloride (Aliquat 336). Such extractant mediums are liquid ion exchange compounds which will preferentially effect the extraction of the zirconium reaction product from the aqueous feed stream. The extractant medium should be present in the organic solvent as a solution of about a 0.05 to 1.0 molar solution.
EXAMPLE I
As an example of the present process, the aqueous solutions of zirconium compound listed on Table I were irradiated as indicated and contacted with the organic phase indicated, using Aliquat 336 as an extractant medium. The results were:
Table I
TABLE I__________________________________________________________________________ Sample Organic Phase Aqueous Phase SystemOptical Exp. 91/90 Ratio ##STR1## K__________________________________________________________________________ 0.1 M Aliquat 336 0.05 M ZrOCl.sub.2 a L f = 0.21863 0.9977 0.491 Xylene 8 M HCl h = 0.218582 t = 0.219093 0.1 M Aliquat 336 0.05 M ZrOCl.sub.2 a c h = 0.21852 0.9966 0.564 Xylene 8 M HCl t = 0.21926 SV L f = 0.218595 0.1 M Aliquat 336 0.05 M ZrOCl.sub.2 h = 0.21823 0.9930 0.526 Xylene 8 M HCl t = 0.21977 SV c f = 0.218597 0.1 M Aliquat 336 0.05 M ZrOCl.sub.2 h = 0.21856 0.9962 0.548 Xylene 8 M HCl t = 0.21940__________________________________________________________________________ a = 200 W tungsten Filament Lamp c = 2 hours L = 1 hour SV = Sodium Vapor 300 mW 300-400 nm Exp. = Exposure K = Distribution K =Org/Aq EF = Enrichment Factor
EXAMPLE II
As a further example of the present process, a series of runs were made where a Zr(SO.sub.4).sub.2 solution (0.05M) in 0.5M H.sub.2 SO.sub.4, which was deoxygenated, was irradiated with an argon ion laser (0.5 W at 363 nm) and contacted with a second solvent (xylene containing 0.1M benzoylacetone) for the times listed in Table II-A and with the results listed therein:
Table II-A
A second set of runs using the same feed solution composition and other parameters gave the following results:
Table II-B
TABLE II__________________________________________________________________________ Aqueous Organic Weight Weight Distribution PhotonExposure M(i) Fraction Fraction .alpha. s K = Org/Aq Dose__________________________________________________________________________Run No. (Aqueous 90 0.5054 Feed) 91 0.1116 92 0.1731 94 0.1800 96 0.0297 9 5 min. 90 0.5054 0.5055 1.000 0.03 0.50 91 0.1116 0.1116 1.000 92 0.1731 0.1731 1.000 94 0.1800 0.1800 1.000 96 0.0297 0.0297 1.00010 10 min. 90 0.5063 0.5055 1.003 0.10 1.00 91 0.1118 0.1116 1.002 92 0.1729 0.1731 0.998 94 0.1794 0.1800 0.996 96 0.0296 0.0297 0.99611 30 min. 90 0.5060 0.5055 1.002 0.12 3.00 91 0.1118 0.1116 1.002 92 0.1730 0.1731 0.999 94 0.1795 0.1800 0.996 96 0.0296 0.0297 0.99612 1 hour 90 0.5056 0.5055 1.000 0.14 6.00 91 0.1120 0.1116 1.004 92 0.1728 0.1731 0.998 94 0.1804 0.1800 1.002 96 0.0295 0.0297 0.99313 2 hours 90 0.5068 0.5055 1.005 0.14 12.0 91 0.1122 0.1116 1.006 92 0.1727 0.1731 0.997 94 0.1789 0.1800 0.992 96 0.0294 0.0297 0.989Sample14 5 min 90 0.5068 0.5055 1.005 0.15 0.5 91 0.1120 0.1116 1.004 92 0.1727 0.1731 0.997 94 0.1790 0.1800 0.989 96 0.0294 0.0297 0.98915 1 hour 90 0.5066 0.5066 1.004 0.16 6.0 91 0.1121 0.1116 1.005 92 0.1730 0.1731 0.999 94 0.1800 0.1800 1.000 96 0.0286 0.0297 0.96116 2 hours 90 0.5072 0.5055 1.007 0.16 12.0 91 0.1122 0.1116 1.006 92 0.1721 0.1731 0.993 94 0.1789 0.1800 0.992 96 0.0294 0.0297 0.989__________________________________________________________________________
EXAMPLE III
A series of runs were made as in Example I, except that 0.0015M Triton was added to the aqueous solution, the results being:
Table III
TABLE III__________________________________________________________________________ Aqueous Organic Weight Weight Distribution PhotonSample Exposure M(i) Fraction Fraction .alpha. s K = Org/Aq Dose__________________________________________________________________________17 5 min 90 0.5054 0.5055 1.000 0.02 0.5 91 0.1117 0.1116 1.001 92 0.1731 0.1731 1.000 94 0.1800 0.1800 1.000 96 0.0297 0.0297 1.00018 10 min 90 0.5063 0.5055 1.003 0.12 1.0 91 0.1118 0.1116 1.002 92 0.1729 0.1731 0.998 94 0.1794 0.1800 0.996 96 0.0296 0.0297 0.99619 30 min 90 0.5063 0.5055 1.003 0.16 3.0 91 0.1118 0.1116 1.002 92 0.1730 0.1731 0.999 94 0.1795 0.1800 0.996 96 0.0296 0.0297 0.99620 1 hour 90 0.5069 0.5055 1.006 0.19 6.0 91 0.1122 0.1116 1.006 92 0.1728 0.1731 0.998 94 0.1793 0.1801 0.995 96 0.0294 0.0297 0.98921 2 hours 90 0.5072 0.5055 1.007 0.19 12.0 91 0.1124 0.1116 1.008 92 0.1724 0.1731 0.995 94 0.1787 0.1801 0.991 96 0.0294 0.0297 0.98922 5 min 90 0.5049 0.5055 0.998 0.25 1.8 91 0.1116 0.1116 1.000 92 0.1731 0.1731 1.000 94 0.1806 0.1801 1.004 96 0.0298 0.0297 1.00323 10 min 90 0.5049 0.5055 0.998 0.15 3.6 91 0.1116 0.1116 1.000 92 0.1732 0.1731 1.000 94 0.1806 0.1800 1.004 96 0.0298 0.0297 1.00324 30 min 90 0.5049 0.5055 0.998 0.20 11.0 91 0.1115 0.1116 0.999 92 0.1731 0.1731 1.000 94 0.1806 0.1800 1.004 96 0.0298 0.0297 1.00325 1 hour 90 0.5045 0.5055 0.996 0.27 20.0 91 0.1124 0.1116 1.008 92 0.1727 0.1731 0.997 94 0.1802 0.1801 1.001 96 0.0295 0.0297 0.99326 2 hours 90 0.5041 0.5055 0.995 0.30 40.0 91 0.1126 0.1116 1.010 92 0.1729 0.1731 0.998 94 0.1803 0.1801 1.002 96 0.0294 0.0297 0.989__________________________________________________________________________Samples 22 to 26 have organic phases, aqueous phasesand optical systems as follows:Organic Phase Aqueous Phase Optical System__________________________________________________________________________0.10 M BzAc 0.05 M Zr(SO.sub.4).sub.2 Ar ion laserXylene 0.05 M H.sub.2 SO.sub.4 335 nm 0.0015 M Triton 351 nm 363 nm 1.8 W__________________________________________________________________________
EXAMPLE IV
A series of runs were made using the aqueous solutions, organic phases (second solvents), optical systems and times of exposure listed in Table IV, using thenoyltrifluoroacetone (HTTA) as an extractant medium:
Table IV
TABLE IV__________________________________________________________________________ Sample Organic Phase Aqueous Phase SystemOptical Exp. 91/90 Ratio ##STR2## K__________________________________________________________________________27 0.5 M HTTA 0.05 M ZrOCL.sub.2 a b f = 0.2185028 Benzene 0.1 M H.sub.2 C.sub.2 O.sub.4 h = 0.21829 0.9978 0.6729 2 M HCl t = 0.2187730 c h = 0.21835 0.9939 0.7531 t = 0.2197032 0.5 M HTTA 0.05 M ZrOCl.sub.2 a c f = 0.2185333 Xylene 0.4 M H.sub.2 C.sub.2 O.sub.4 h = 0.21829 0.9983 0.3534 2 M HCl t = 0.21866 0.2 M HTTA 0.05 M ZrOCl.sub.2 a c f = 0.2185735 Xylene 0.2 M H.sub.2 C.sub.2 O.sub.4 h = 0.21838 0.9989 0.6136 4 M HCl t = 0.21863 0.2 M HTTA 0.05 M ZrOCl.sub.2 a c f = 0l.2185737 Xylene 0.2 M H.sub.2 C.sub.2 O.sub.4 h = 0.21846 0.9983 0.2538 6 M HCl t = 0.21883 0.2 M HTTA 0.05 M ZrCl.sub.2 a c f = 0.2185939 Xylene 0.2 M H.sub.2 C.sub.2 O.sub.4 h = 0.21838 0.9989 0.4340 4 M HNO.sub.3 t = 0.2186341 0.5 M HTTA 0.05 M Zr(SO.sub.4).sub.2 a c h = 0.21825 0.9982 0.2542 Benzene 0.7 M H.sub.2 SO.sub.4 t =43 d h = 0.21837 0.9977 1.0044 t = 0.2188845 c h = 0.21801 0.9940 1.5046 t = 0.21932 0.2 M HTTA 0.05 M ZrOCl.sub.2 SV c f = 0.2185047 Xylene 0.2 M H.sub.2 C.sub.2 O.sub.4 h = 0.21799 0.9922 0.6748 4 M HCl t = 0.2197149 g h = 0.21679 0.9839 0.6950 t = 0.22037 0.2 M HTTA 0.05 M ZrOCl.sub.2 SV j f = 0.2185951 Xylene 0.2 M H.sub.2 C.sub.2 O.sub.4 h = 0.21848 0.9993 0.5452 Deoxygenated 4 M HCl t = 0.2186353 10-2 M Triton L h = 0.21832 0.9943 0.6754 t = 0.2195855 p h = 0.21779 0.9895 0.6756 t = 0.2201057 q h = 0.21795 0.9901 0.6758 t = 0.22013 0.05 M ZrOCl.sub.2 0.05 M H.sub.2 C.sub.2 O.sub.4 p f = 0.2186459 4 M HCl h = 0.21823 0.9917 2.7060 10-2 M Triton t = 0.2200561 q h = 0.21805 0.9895 2.7062 t = 0.2203763 0.05 M ZrOCl.sub.2 p h = 0.21733 0.9882 5.6764 0.025 M H.sub.2 C.sub.2 O.sub.4 t = 0.21993 4M HCl65 10-2M Triton q h = 0.21741 0.9873 4.5666 t = 0.22021__________________________________________________________________________ a = 200 W Tungsten Filament Lamp b = 1/2 hour c = 2 hours d = 2 min. e = 5 min. f = feed g = 3.5 hours h = heads j = shake only K = Distribution K = Org/Aqu L = 1 hour p = 3 hours q = 6 hours t = tails Exp. = Exposure EF = Enrichment Factor SV = Sodium Vapor 300 mW 300-400 nM
EXAMPLE V
A series of runs were made using dibenzoylmethane as an extractant medium:
Table V
TABLE V__________________________________________________________________________ Aqueous Organic Weight Weight Distribution PhotonSample Exposure M(i) Fraction Fraction .alpha. s(i) K = Org/Aq Dose__________________________________________________________________________ feed 90 0.5059 91 0.1116 92 0.1729 94 0.1800 96 0.029567 3 min 90 0.5055 0.5105 1.0203 91 0.1116 0.1117 1.0013 92 0.1731 0.1711 0.9858 0.10 0.33 94 0.1800 0.1802 1.0014 96 0.0298 0.0265 0.886168 5 min 90 0.5056 0.5084 1.0113 91 0.1120 0.1099 0.9787 92 0.1728 0.1737 1.0066 0.20 0.50 94 0.1803 0.1789 0.9906 96 0.0296 0.0291 0.981669 10 min 90 0.5063 0.5059 0.9982 91 0.1120 0.1115 0.9951 92 0.1727 0.1730 1.0019 3.76 1.0 94 0.1794 0.1802 1.0053 96 0.0296 0.0295 0.995770 60 min 90 0.5072 0.5058 0.9945 91 0.1124 0.1115 0.9912 92 0.1721 0.1730 1.0064 9.00 6.0 94 0.1789 0.1801 1.0085 96 0.0294 0.0295 1.004071 3 min 90 0.5062 0.5059 0.9989 91 0.1122 0.1115 0.9928 92 0.1727 0.1730 0.0019 4.56 0.33 94 0.1795 0.1801 1.0043 96 0.0296 0.0295 0.995972 5 min 90 0.5062 0.5059 0.9989 91 0.1122 0.1115 0.9935 92 0.1725 0.1730 1.0033 9.00 0.5 94 0.1797 0.1808 1.0024 96 0.0296 0.0295 0.996373 10 min 90 0.5063 0.5059 0.9984 91 0.1122 0.1115 0.9934 92 0.1725 0.1730 1.0033 9.00 1.0 94 0.1794 0.1801 1.0047 96 0.0296 0.0295 0.996274 60 min 90 0.5068 0.5059 0.9963 91 0.1124 0.1115 0.9913 92 0.1725 0.1730 1.0033 9.00 6.0 94 0.1793 0.1801 1.0055 96 0.0294 0.0294 1.0041__________________________________________________________________________Samples 67 and 71 have organic phases, aqueousphases and optical systems as follows:Sample Organic Phase Aqueous Phase Optical System__________________________________________________________________________67 0.05 M DBM 0.025 M ZrCl.sub.4 Ar ion laser Xylene 2 M HCl 0.55 W at 363 nm Deoxygenated 0.01 M Triton71 0.05 M DBM 0.025 M ZrCl.sub.4 Ar ion laser Xylene 2 M HCl 0.55 W at 363 nm Deoxygenated 0.01 M Triton 30 min Prestir before Photolysis__________________________________________________________________________
EXAMPLE VI
A series of runs were made using Cyanex 272 and Primene JMT as extractant mediums as follows:
Table VI
TABLE VI__________________________________________________________________________ Sample Organic Phase Aqueous Phase SystemOptical Exp. 91/90 Ratio ##STR3## K__________________________________________________________________________75 0.1 M Cyanex 272 0.05 M ZrOCl.sub.2 SV q h = 0.21838 0.9970 0.2076 Xylene 0.2 M H.sub.2 C.sub.2 O.sub.4 t = 0.21903 Deoxygenated 4 M HCl77 0.1 M Primene JMT 0.04 M Zr(SO.sub.4).sub.2 a c h = 0.21832 0.9968 0.6178 Kerosene 0.7 M H.sub.2 SO.sub.4 t = 0.21901 3% Tridecanol79 0.1 M Primene JMT 0.05 M ZrOCl.sub.2 j b h = 0.21860 0.9995 0.4380 Kerosene 0.1 M H.sub.2 C.sub.2 O.sub.4 t = 0.21871 0.7 M H.sub.2 SO.sub.4 a c f = 0.2186081 h = 0.21821 0.9966 0.5482 t = 0.21896__________________________________________________________________________ a = 200 W Tungsten Filament Lamp b = 1/2 hour c = 2 hours f = feed h = heads j = shake only K = Distribution K = Org/Aq t = tails EF = Enrichment Factor Exp. = Exposure SV = Sodium Vapor 300 mW 300-400 nm
An early, key result of the runs of Examples I-VI was the confirmation of the proposed photochemical mechanism, as illustrated by FIG. 5 of the drawings. The confirmation of the mechanism is based on the fact that the isotope with a non-zero nuclear moment, .sup.91 Zr, is clearly affected differently than the trend obeyed by the set of the other isotopes. The present photo-assisted solvent extraction process is indicated; the solvent extraction contribution produces a trend in .alpha..sub.s vs. isotope mass that slopes from 90 to 96. On top of the solvent extraction process is a photochemical effect that produces additional shift of .sup.91 Zr from the aqueous to the organic phase. This result confirms the proposed photochemical mechanism involved in solvent extraction with photochemical assist.
EXAMPLE VII
A series of three stage runs were made using an aqueous solution of Zr(SO.sub.4).sub.2, H.sub.2 SO.sub.4 (to pH 3.63) and 0.0025M Triton, with an organic phase of xylene containing benzoylacetone. The runs used a three-stage photochemical shakeout, an experiment which requires eight contact operations as shown in the diagram in FIG. 6. These operations are required to create the properly loaded phases for the contacts which simulate the behavior in theoretical stages of a multi-stage column. Results of two such runs are shown in Table VII, for systems which differ only in the irradiation wavelength:
Table VII
TABLE VII______________________________________Experiment Sample 90.sub.Zr 91.sub.Zr 92.sub.Zr 94.sub.Zr 96.sub.Zr______________________________________ Zr-feed 0.5051 0.1116 0.1735 0.1800 0.029883 A3R 0.5078 0.1116 0.1729 0.1798 0.0291 .alpha. 1.02 1.00 0.992 0.997 0.953Argon ion B3R 0.5098 0.1100 0.1713 0.1790 0.0299laser .alpha. 1.034 0.968 0.970 0.987 1.007363 nm C2R 0.5063 0.1113 0.1726 0.1799 0.02980.5 W .alpha. 1.01 0.994 0.987 0.999 1.0084 A3R 0.5059 0.1112 0.1729 0.1801 0.0298 .alpha. 1.006 0.992 0.992 1.004 1.000Argon ion B3R 0.5113 0.1098 0.1718 0.1774 0.0297laser .alpha. 1.051 0.964 0.977 0.965 0.993458 nm C2R 0.5060 0.1116 0.1726 0.1800 0.0298 .alpha. 1.015 1.000 0.990 0.999 0.976______________________________________
These three-stage runs show two important results. One is that the big isotope shift comes after the second photolysis step, while the first photolysis seems to have been dominated by overall extraction with a small isotope shift. Secondly, the shift in the .sup.90 Zr isotope is unexpectedly large, and may indicate a synergistic effect.

Number	Name	Date
3069232	Greenberg et al.	Dec 1962
4389292	Phillips et al.	Jun 1983
4578165	Peterson et al.	Mar 1986
4584183	Chiang et al.	Apr 1986
4612097	Jackovitz et al.	Sep 1986

Zirconium isotope separation process

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