Patent Number: 042773636
Section: description

The different processing units for carrying out the successive steps of the method according to the invention are shown diagrammatically in FIG. 1 and in the following order: at 1: the unit for the first processing step of removal of impurities from the gas mixture produced by the nuclear fuel reprocessing plant; this initial purification step makes it possible to obtain a mixture consisting of air which practically contains no constituents other than xenon and krypton and is carried out in three successive stages respectively within three units shown diagrammatically at 1a, 1b and 1c; PA1 at 2: a column for the second step of concentration of xenon and krypton in liquid argon, thus making it possible to remove mainly the nitrogen from the mixture and to collect a concentrated mixture of xenon and krypton in argon; PA1 at 3: a column for the third step of removal of argon by cryogenic distillation of the mixture of argon, xenon and krypton; PA1 at 4: a column for the separation of xenon and krypton by cryogenic distillation in order to remove the krypton and to collect pure xenon. In more precise terms, the first step of removal of any impurities contained in the initial gas mixture comprises a first stage of removal of hydrocarbons by catalytic oxidation (and also of catalytic dissociation of nitrogen oxide N.sub.2 O) which is performed within the unit shown at 1a; a second stage of removal of oxygen and nitrogen oxides by catalytic reduction which takes place within the unit shown at 1b; and a third stage of removal of carbon dioxide gas and of water vapor by passing through a molecular sieve and/or silica gel which takes place within the unit shown at 1c. Thus the gas mixture to be processed is first introduced at 5 into the unit 1a and discharged from said unit after removal of the hydrocarbons. The mixture is then introduced at 6 into the unit 1b in which a catalytic reduction is carried out in the presence of palladium by the action of hydrogen supplied at 7. Said mixture passes out of said 1b after removal of the oxygen and nitrogen oxides and is introduced at 8 into the unit 1c in which it is freed from the carbon dioxide gas and water vapor by passing it through a molecular sieve. Thus the mixture introduced into the column 2 at 9 is a mixture of nitrogen, xenon and krypton which first receives an addition of argon at 10 prior to admission into the column 2. The cryogenic distillation which permits removal of the nitrogen at 11 is carried out within the column 2, thus making it possible to recover a mixture of argon, xenon and krypton at 12. This mixture of argon, xenon and krypton is then introduced at 13 into the column 3 in which removal of argon is performed at 14 by cryogenic distillation and recovery of a mixture of krypton and xenon at 15. Said mixture of krypton and xenon is then introduced at 16 into the column 4 in which the krypton is removed at 17 by cryogenic distillation and in which pure xenon is recovered at 18. In a preferred embodiment of the invention, part of the krypton removed at 17 can be recycled at 19 and fed back to the inlet of column 2 in order to permit cryogenic distillation at a lower pressure. In accordance with the invention, the pressure at which cryogenic distillation is carried out within column 2 has a maximum value of 18 bar; the pressure at which cryogenic distillation is carried out within column 4 is approximately 3 bar; and the pressure at which cryogenic distillation is carried out within column 3 is comprised between the pressure of column 4 and the pressure of column 2. FIG. 2 shows in greater detail the different elements and circuits for interconnecting the units 1a, 1b, 1c, in which the first step of removal of impurities according to the method of the invention is carried out. The gas mixture to be processed and derived from the irradiated fuel reprocessing plant is first introduced at 20 into a compressor 21, then cooled by a circulation of water within a cooler 22. After passing through a heat exchanger 23, said gas mixture is introduced at 5 into the unit 1a which contains a platinum or rhodium catalyst: within said unit 1a, the hydrocarbons are removed from the gas mixture by catalytic oxidation and removal of the nitrous oxide N.sub.2 O also takes place by catalytic dissociation of this latter. An external heating device serves to maintain a maximum temperature 700.degree. C. within said unit 1a. At the outlet of the unit 1a, the gas mixture from which hydrocarbons have been removed passes into the heat exchanger 23 and then, after mixing with part of the gas mixture which comes from the water separator 27, passes into an electric reheating system 24 in which said mixture is brought to a temperature of 100.degree. C. and is introduced into the unit 1b at 6. The oxygen and the nitrogen oxides are removed by catalytic reduction within said unit 1b which contains a palladium catalyst and may also contain a rhodium catalyst, and hydrogen is introduced at 7 in order to maintain a slight excess quantity of said gas at the outlet of said unit 1b. After passing out of the unit 1b, the gas mixture from which oxygen and nitrogen oxides have been removed is cooled in a water cooler 25 and then passes into a ventilator 26. At the outlet of the ventilator 26, pat of the gas mixture first passes thorugh a water separtor 27 to be recycled at 28 to the unit 1b and the other part is directed at 8 towards the unit 1c. the mixture which is introduced into the unit 1c at 8 is freed from the water vapor and from traces of CO.sub.2 by passing through a molecular sieve and/or a silica gel within one of the two absorbers 29 which are placed in parallel; these two absorbers 29 are subjected periodically and in alternate sequence to regeneration by heating and circulation of nitrogen. There are again shown in FIG. 3 the columns 2, 3 and 4 which serve respectively to carry out the second, the third and fourth steps of the method according to the invention. The gas mixture containing nitrogen, argon, krypton and xenon derived from the unit 1 is first cooled within a heat exchanger 30, then introduced into the column 2 at 9. The distillation column 2 operates at a maximum pressure of 18 bar. The lower portion of the column 2 is maintained at the necessary temperature by means of an electric heating device 31. At the head of the column 2, a reflux is carried out by a condenser 32 which is cooled by liquid nitrogen supplied at 33. A mixture containing mainly nitrogen and possibly a fraction of argon is withdrawn from the top of the column 2 at 11; this mixture can be recycled to the fuel element shearing or decladding sweep circuit or discharged to the atmosphere; the mixture is heated beforehand by passing through the heat exchanger 30 from which it is discharged at 34. A liquid mixture of argon concentrated in krypton and xenon is withdrawn from the bottom of the column 2 and introduced at 13 into the distillation column 3. Within column 3 which operates at a pressure comprised between the pressure of column 4 and the pressure of column 2, the argon is separated by cryogenic distillation at 14 and the mixture of krypton and xenon is collected at the bottom of the column 3. If necessary, the argon which leaves the column 3 at 14 can be recycled to the inlet of column 2. The mixture of krypton and xenon which leaves the bottom of the column 3 is fed into the column 4 and 16 in which separation of the krypton and the xenon is carried out by cryogenic distillation: the krypton is obtained at 17 at the head of column 4 and the xenon is obtained at 18 at the bottom of column 4. If necessary, part of the krypton obtained at 17 is recycled at 19 to the inlet of column 2; this makes it possible to increase the relative proportion of krypton contained in the feed gas mixture and to carry out the initial cryogenic distillation within column 2 at a pressure which is appreciably lower than 18 bar. For example, in the case of a krypton to xenon ratio of 1 obtained with a reflux of krypton from 10, the operating pressure of column 2 can be reduced to a value of 10 bar. The pure xenon obtained at 18 is a marketable product. One example of circulation of products is given hereinafter by way of indication together with particulars on the concentrations of the mixtures and the different flow rates. For the sake of convenience, reference will be made to FIG. 1. The gas mixture to be processed and to which has been added a predetermined quantity of argon has the following composition: 81% nitrogen, 11% oxygen, 8% argon, 150 ppm of krypton, and 1500 ppm of xenon, hydrocarbons, nitrogen oxides, water vapor and carbon dioxide gas. The mixture is introduced into the unit 1a at 5 at a flow rate of 21.8 m.sup.3 per hour. At the outlet of the unit 1a, the mixture which has been freed from hydrocarbons is introduced into the unit 1b at 6 and hydrogen is introduced at 7 at a flow rate of 4.8 m.sup.3 per hour. At the outlet of the unit 1b, the mixture from which oxygen and nitrogen oxides have been removed is introduced into the unit 1c at 8. At the outlet of said unit 1c, the gas mixture from which water vapor and CO.sub.2 have been removed is introduced into column 2 at 9: at this moment, the mixture has the following composition: 88% nitrogen, 12% argon, 150 ppm of krypton and 1500 ppm of xenon; the mixture is then introduced into column 2. At the head of column 2, a mixture containing 91% nitrogen and 9% argon is recovered at 11. A mixture containing 94.5% argon, 0.5% krypton and 5% xenon is recovered at the base of column 2. This mixture is introduced into column 3 at 13. At the head of column 3, argon is recovered at 14 at a flow rate of 600 l/hr and a mixture containing 10% krypton and 90% xenon is recovered at the base of column 3. This mixture is introduced into column 4 at 16. Krypton is recovered at a flow rate of 1 l/hr at the head of column 4 at 17 and xenon is withdrawn at a flow rate of 30 l/hr from the bottom of column 4. The values given in the foregoing relate to the case in which recycling of part of the krypton obtained at 17 to the inlet of column 12 is not carried out. If said recycling of part of the krypton is effected at the end of the process at 19, for example at a flow rate of 27 l/hr, the gas mixture fed to the inlet of column 2 at 9 then has the following composition: 88% nitrogen, 12% argon, 1500 ppm of krypton and 1500 ppm of xenon. This permits operation of the column 2 at a pressure of the order of 10 bar instead of 18 bar.