|Publication number||USH857 H|
|Application number||US 07/562,187|
|Publication date||Dec 4, 1990|
|Filing date||Jul 26, 1990|
|Priority date||Jul 26, 1990|
|Publication number||07562187, 562187, US H857 H, US H857H, US-H-H857, USH857 H, USH857H|
|Inventors||Paul A. Haas|
|Original Assignee||The United States Of America As Represented By The United States Department Of Energy|
|Export Citation||BiBTeX, EndNote, RefMan|
|Referenced by (8), Classifications (14), Legal Events (1)|
|External Links: USPTO, USPTO Assignment, Espacenet|
This invention was developed pursuant to a contract with the U.S. Department of Energy.
This invention relates to a process for preparing uranium and more particularly an electrolytic process for preparing uranium using fluoride and chloride salt mixtures.
A standard method for making uranium metal is the reduction of UF4 with magnesium as a reducing agent. The high cost of such a process has directed efforts at alternatives. One alternative is the use of electrochemical methods similar to the Hall-Heroult process used in making aluminum. These approaches presented major difficulties.
First, the high density and low solubility of uranium oxides resulted in fouled cells that prevented metal coalescence. Also, less than 50% of recovered metal is from uranium oxides, the rest being from UF4 which not only must first undergo conversion from the UO2 form before electrolytic reduction, but also produces an undesirable CF4 waste gas emission. The efficiencies are low, rarely exceeding 30% and usually lower than 20% for production from UO2. Cell capabilities are low due to low current efficiencies and because the maximum current is limited by the "critical current density" that gives an "anode effect" when CF4 is produced. Finally, in order to maintain continuous operation at 1200° C., consumed carbon anodes must be repeatedly replaced, a difficult and dangerous job.
Therefore there is a continuing need to develop new, safe and efficient process for making uranium metal.
In view of the above needs, it is an object of this invention to provide a process for making uranium that eliminates oxide fouling of the cell.
It is another object of this invention to provide a process for making uranium that has a high uranium yield and is thus more efficient than present processes.
An additional object of this invention is to provide an electrolytic process for making uranium wherein current capacities are maximized.
A further object of this invention is to provide a process for making uranium that is safe, having no hazardous by products.
Additional objects, advantages and novel features of the invention will be set forth in part in the description which follows, and in part will become apparent to those skilled in the art upon examination of the following or may be learned by practice of the invention. The objects and advantages of the invention may be realized and attained by means of the instrumentalities and combinations particularly pointed out in the appended claims.
To achieve the foregoing and other objects and in accordance with the purpose of the present invention, as embodied and broadly described herein, the process of this invention may comprise: in an electrolytic cell having an anode and cathode electrodes, contacting in the molten state uranium chloride and a mixture of salts comprising chloride salts of metals selected from the group consisting of K, Na and Ba, the fluoride salts of metals selected from the group consisting of K, Na and Ba in sufficient amounts to minimize volatility of uranium chlorides; and introducing an electric current across the electrodes thus resulting in the production of uranium metal. This process is safer and more efficient than prior electrolytic processes.
The theory of this invention is to produce at one electrode a byproduct that can be recycled to a feed reactor containing UO2 feed material to produce a uranium compound that can be electrolytically reduced, thus eliminating the problem of having UO2 in the reaction vessel and also recycling a byproduct. The composition of the reactants is formulated so that Cl2 forms at the anode. This reacts with UO2 in a the feed reactor to form uranium chlorides as the uranium compounds to be reduced.
The anode reaction is
4Cl- →2Cl2 +4e
The reaction at the cathode is
The net overall cell reaction is
UCl4 →2Cl2 +U°
The reactions listed using uranium chlorides are known and were used in batch-type processes to prepare dendritic uranium metal solids at 750° to 900° C. The process was inefficient and uneconomical because of the large amount of waste solids and the steps for recovery of the uranium metal powder. Operations to prepare molten uranium were not practical because of the excessive volatility of uranium chlorides.
To get around that problem, the cell charge is a mixture of chloride and fluoride salts with one or more of the fluoride salts selected to give a high degree of conversion of uranium chlorides to uranium fluorides. The preferred fluoride is KF and some conversion reactions are
Thermodynamic data shows a value of -255 Kj/mol UCl4 =f G°=-RT InKf at 1500° C. for the first reaction. This value indicates a very high equilibrium conversion to KCl and UF4 and results in a very fast conversion in the molten cell charge. Other possible fluoride salts for exchange with uranium chlorides are NaF and BaF2, however, NaCl is more volatile than KCl, and the exchange reaction with BaF2 is less favorable thermodynamically.
Another reason to use the salt mixture is that it will have a lower melting point resulting in easier more convenient operation. The composition is selected so that UCl4 concentration in the melt is low to enable the cell to be operated above the boiling point of UCl4 without the production of excessive amounts of UCl4 vapor. Because the chlorine is in the melt, as KCl, the anode product is Cl2 in spite of the low UCl4 concentration.
The electrode reaction depend on the ions present at the electrode and not on the melt constituents that do not ionize. The KCl and UF4 and UF3 all ionize. The anode reaction to form Cl2 occurs first and the undesirable reaction of F- to form CF4 requires a higher voltage and does not occur until the chloride at the anode is depleted to a low concentration. At the cathode, U metal is formed in preference to K metal. The net reactions in the cell when the uranium is mostly UF4 are
UF4 +4KCl→2Cl2 +U°+4KF
UF3 +3KCl→3/2Cl2 +U°+3KF
In combination with the exchange reactions for KF with uranium chloride feed, the net reactions starting with uranium chloride feed are
UCl4 →2Cl2 +U°
UCl3 →3/2Cl2 +U°
One reaction for chloride recycle in a chlorinator is
UO2 +2Cl2 +2CO→UCl4 +2CO2
Then the overall net process reaction is
UO2 +2CO→2CO2 +U°
This process provides many benefits over prior art processes. Uranium fluoride and chlorides are molten and soluble in the cell melt at 1200° C.; therefore, there are no interfering solids to foul the cell. The cell can be operated without UF4 feed material or having to deal with CF4 waste. The current efficiencies are higher since low efficiencies can be attributed to parasitic U(III)←→U(IV) cycle and large amounts of UF4 needed to give useful solubilities UO2. Lower UF4 concentrations and resulting higher current efficiencies are possible when the anode product is Cl2. Higher anode current densities and higher cell capacities are possible with Cl2 as the anode product since Cl2 does not give the critical anode effect that occurs when CF4 is a product. In addition, the carbon anode is not consumed as it is when CO and CF4 are the anode product. This allows for a continuous process for uranium manufacture since the anode does not need to be periodically replaced.
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US5164050 *||Jul 3, 1990||Nov 17, 1992||Compagnie Europeenne Du Zirconium Cezus||Method of obtaining uranium from oxide using a chloride process|
|US5380406 *||Oct 27, 1993||Jan 10, 1995||The United States Of America As Represented By The Department Of Energy||Electrochemical method of producing eutectic uranium alloy and apparatus|
|US5421855 *||May 27, 1993||Jun 6, 1995||The United States Of America As Represented By The United States Department Of Energy||Process for continuous production of metallic uranium and uranium alloys|
|US7011736 *||Aug 5, 2003||Mar 14, 2006||The United States Of America As Represented By The United States Department Of Energy||U+4 generation in HTER|
|US7097747 *||Aug 5, 2003||Aug 29, 2006||Herceg Joseph E||Continuous process electrorefiner|
|US20040244533 *||Jun 6, 2002||Dec 9, 2004||Lewin Rober Glynn||Actinide production|
|WO2001041152A2 *||Dec 4, 2000||Jun 7, 2001||British Nuclear Fuels Plc||Actinide production|
|WO2002099815A2 *||Jun 6, 2002||Dec 12, 2002||British Nuclear Fuels Plc||Actinide production|
|U.S. Classification||205/47, 75/398, 423/253, 423/19, 423/5, 423/254, 75/399|
|International Classification||C25C3/34, G21C19/48|
|Cooperative Classification||G21C19/48, C25C3/34, Y02W30/884|
|European Classification||G21C19/48, C25C3/34|
|Apr 23, 1991||AS||Assignment|
Owner name: UNITED STATES OF AMERICA, THE, AS REPRESENTED BY T
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:HAAS, PAUL A.;REEL/FRAME:005682/0396
Effective date: 19900424