PROCESS AND APPARATUS FOR PRODUCING ALLOY CONTAINING TERBIUM AND/OR GADOLINIUM

Abstract: The process includes the steps of: (a) preparing a bath of molten electrolyte (44) which consists essentially of 20-95% by weight of TbF₃ and/or GdF₃, 5-80% of LiF, up to 40% of BaF₂ and up to 20% of CaF₂; (b) reducing the TbF₃ and/or GdF₃ in the bath, with carbon anode (42) and with cathode (40) made of a metal such as iron or cobalt, so as to electrodeposit Tb and/or Gd on the cathode, and alloying the electrodeposited Tb and/or Gd with metal of the cathode so as to produce the alloy containing Tb and/or Gd in a liquid state on the cathode; (c) adding the TbF₃ and/or GdF₃ to the bath so as to maintain the composition of the bath, for compensating for consumption of the TbF₃ and/or GdF₃ during production of the alloy; (d) dripping the liquid alloy from the cathode into a receiver (50) having a mouth which is open upward in a lower portion of the bath below the cathode, and thereby collecting the liquid alloy in the form of a molten pool (52) in the receiver; and (e) withdrawing the molten pool of the liquid alloy from the receiver.

Description: The present invention relates to a process and an apparatus for producing an alloy containing terbium and/or gadolinium, and more particularly to such a process of continuously producing an alloy of high content of terbium and/or gadolinium, and of low harmful impurities and non-metallic inclusions. Terbium (Tb) and gadolinium (Gd) are utilised in the form of thin-layered amorphous alloys of TbFe, TbCo, GdFe, GdCo, TbFeCo, TbGdFe, TbGdCo, etc., as materials for magnetooptical discs of the rare earth type which have been recently studied and developed. These elements are also added to other kinds of material and the demand for terbium and gadolinium will be increased in the future. Although terbium and gadolinium can be used in the form of the pure metal to obtain an alloy containing the same, for the addition thereof to other materials it is preferable to use the element in the form of an alloy with iron, cobalt, or other alloying metal, since metallic terbium and metallic gadolinium have a comparatively high melting point, 1365°C for terbium and 1313°C for gadolinium. Four processes of manufacturing an alloy of a rare earth metal with a metal of high melting point are described below, which are commonly known in the art. All of them can, however, not be satisfactory, because of having some inherent disadvantages or problems, as the practical and industrial process operable continuously. (A) A method wherein rare earth metal or its alloy is prepared beforehand by means of electrowinning the same in a bath of electrolyte or by means of reducing a rare earth compound with an active metal, and the obtained rare earth or its alloy is melted together with another metal for alloying them: The method, however, is problematical in the first step of preparing the rare earth or its alloy. In the electrowinning method, two techniques can be named as a prior art: electrolysis in an electrolyte bath of fused chlorides (raw materials), and electrolysis of rare earth oxide (raw material) dissolved in an electrolyte bath of fused fluorides. The former technique suffers the problem of difficult handling of the fused chrorides, and a further problem resulting from the batch style which is not suitable for a continuous operation in a large scale. On the other hand, the latter technique has the problem of low solubility of the oxide in the electrolyte bath, which hinders a continuous electrolysis operation and results in an accumulation of sludge on the bottom of the electro­ winning cell. For continuous and large scale production it is recommended that the rare earth or its alloy is produced in a liquid state, but it is impractical to operate at the excessively high electrolysis temperatures at which the electrolysis operation has to be conducted in view of the high melting point of the rare earth to be obtained, since at such higher temperatures impurities and non-metallic inclusions more easily enter into the rare earth or its alloy produced. On the other hand, the reduction method utilising an active metal belongs to a batch system and is therefore not suitable for a continuous and large scale production. Further, this method has the disadvantage of using an expensive active metal (reducing agent) and expensive materials for the exclusive apparatus. This method has the further disadvantage of involving an additional step for removing the residual active agent. (B) Another method wherein alloying is executed by means of reducing a mixture of a rare earth compound and a compound of the metal to be alloyed with the rare earth by utilising a reducing agent (e.g., calcium hydride for a Sm-Co alloy): This method needs an expensive reducing agent, and cannot be, either, an exception of the batch-style method, being unsuitable for a continuous and large scale operation. (C) Still another method wherein an alloy of rare earth and a metal to be alloyed with the rare earth is electrodeposited on the cathode by electrolytic reduction which is carried out in a bath of electrolyte dissolving both a compound of the rare earth and a compound of the metal to be alloyed with the rare earth (U.S. patent No. 3298935 can be referred), therein. This method is problematical in that it is difficult to keep the chemical composition of the alloy produced on the cathode uniform over a long period of time during the electrolysis operation. Further, in the case where oxide is used as a raw material, the method has a problem of a low solubility of the oxide in the electrolyte bath, which hinders a continuous electrolysis operation. (D) So-called consumable cathode method, wherein rare earth is electrodeposited by electrolytic reduction on a consumable cathode of a metal and alloyed with the metal of the cathode, in one step which is executed in a suitable bath of electrolyte of fused salts (can be referred "U.S. Bur. of Min., Rep. of Invest.", No. 7146, 1968, and Japanese patents No. 837401 and 967389): The shortcomings will be described below: in the case where a rare earth oxide is used as a raw material to be reduced, the method suffers problems, as stated previously, of a low solubility of the rare earth oxide in the selected electrolyte bath and of an accumulated sludge of the oxide; moreover, conducting the electrolysis operation at increased temperatures for overcoming those problems results in producing a deteriorated alloy containing an increased amount of impurities and non-metallic inclusions as coming from the structural materials of the electrowinning cell. Further, the recovery of the produced alloy is carried out in a batch style which is unsuitable for a continuous and large-scale operation. Metallic terbium and metallic gadolinium have been, in fact, almost useless, and the industrial manufacturing process of obtaining the same has not been settled, yet, except for the above-mentioned reduction method of (A) in which terbium or gadolinium can be produced in a small quantity. However, the reduction method is not satisfactory in that the residual reducing agent (calcium) and the impurities (e.g., oxygen) are harmful to the "target" product, terbium or gadolinium. Therefore, it can be said that no industrially practical process is firmly established for continuously producing such metals. It is therefore an object of the present invention to provide a process and apparatus, suitable for continuous and large-scale production, for producing an alloy containing terbium and/or gadolinium, and in particular a reliable, economical industrial process and apparatus for producing such an alloy with a high content of terbium and/or gadolinium, and with a low content of non-metallic inclusions and impurities such as calcium and oxygen. According to a first aspect of the present invention, there is provided a process of producing an alloy containing terbium and/or gadolinium, comprising the steps of: (a) preparing a bath of molten electrolyte which has a composition consisting essentially of 20-95% by weight of terbium fluoride and/or gadolinium fluoride, 5-80% by weight of lithium fluoride, up to 40% by weight of barium fluoride and up to 20% by weight of calcium fluoride; (b) effecting electrolytic reduction of the terbium and/or gadolinium fluoride in the bath of molten electrolyte, with at least one carbon anode and at least one metal cathode, so as to electrodeposit terbium and/or gadolinium on the at least one metal cathode, and alloying the electrodeposited terbium and/or gadolinium with metal of the at least one metal cathode so as to produce the alloy containing terbium and/or gadolinium in a liquid state on the at least one metal cathode; (c) adding the terbium and/or gadolinium fluoride to the bath of molten electrolyte so as to maintain the composition of the bath of molten electrolyte, for compensating for consumption of the terbium and/or gadolinium fluoride during production of the alloy; (d) dripping the liquid alloy from the at least one metal cathode into a receiver having a mouth which is open upward in a lower portion of the bath of molten electrolyte below the metal cathode, and thereby collecting the liquid alloy in the form of a molten pool in the receiver; and (e) withdrawing the molten pool of the liquid alloy from the receiver. In the above-mentioned process according to the present invention, an alloy containing terbium and/or gadolinium can be manufactured in only one step of electrolytic reduction. And in this one step of electrolytic reduction, an alloy of high content of terbium and/or gadolinium and of low content of impurities (e.g., oxygen) and non-metallic inclusions that adversely affect the properties of magnetooptical disks, permanent magnets, or other end products, can be manufactured in an economical, continuous and large-scale operation. According to the present invention, are advantageously produced alloys such as a terbium-iron alloy, terbium-cobalt alloy, gadolinium-iron alloy, gadolinium-cobalt alloy, terbium-gadolinium-iron alloy, and terbium-gadolinium-­ cobalt alloy. The invented method is additionally provided with various advantages: use of a solid cathode allows easy handling of the same; siphoning the produced alloy in a liquid state in the course of the electrolysis or electrowinning makes it possible to continue the electrolysis substantially without interruption, i.e. a continuous operation of the electrolysis is attainable; the advantage of using a so-called consumable cathode is fully attainable, i.e. a continuous operation of the electrolysis under lower temperatures remarkably improves the electrolysis results or yields, and also improves the grades of the produced alloys owing to a decreased amount of impurities such as oxygen. This method according to the present invention allows the scale of the operation to be enlarged and the time duration of the operation to be enlarged, which has been regarded as impossible in the reduction processes using an active metal such as calcium, and also allows the entering of impurities such as the active metal into the produced alloy to be effectively restricted. It further allows the fundamental elimination of difficulties observed in the continuous operation of the electrolytic manufacturing method executed in a mixture of fused salts of fluoride and oxide(s), terbium oxide and/or gadolinium oxide as the raw material. The method of the present invention allows the electrolysis operation to be effected at lower temperatures than the method using terbium oxide and/or gadolinium oxide as the raw material. Operation at lowered temperatures is advantageous in that the entering of impurities and non-metallic inclusions, such as coming from the structural materials of the electrowinning cell, is effectively restricted. Another advantage of this method resides in the capability of using a higher anode current density than the method using the oxide or oxides, at the same temperature. That is, in the case where the present method and the method using the oxide(s) employ an anode with the same dimensions, a higher current density can be used with the present method thereby assuring a better productivity. In an advantageous embodiment of the above mentioned process of the present invention, the at least one metal cathode is formed of a metal which is easily alloyed with terbium and/or gadolinium; for example, iron, cobalt, copper, nickel, manganese, chromium, or titanium is used. According to a preferred embodiment of the above-mentioned process of the present invention, the terbium and/or gadolinium fluoride is terbium fluoride, the at least one metal cathode is formed of iron, and the alloy containing terbium and/or gadolinium is a terbium-iron alloy. In this case, the bath of molten electrolyte is preferably held at temperatures within a range of 860-1000°C, and the electrolytic reduction may be effected at those temperatures. According to another embodiment of the invention process, the terbium and/or gadolinium fluoride is terbium fluoride, the at least one metal cathode is formed of cobalt, and the alloy is a terbium-cobalt alloy. In this case, the bath of molten electrolyte is preferably held at temperatures within a range of 710-1000°C, and the electrolytic reduction may be effected at those temperatures. According to still another embodiment of the process, the terbium and/or gadolinium fluoride is gadolinium fluoride, the at least one metal cathode is formed of iron, and the alloy is a gadolinium-iron alloy. In this case, the bath of molten electrolyte is preferably held at temperatures within a range of 850-1000°C, and the electrolytic reduction may be effected at those temperatures. According to yet another embodiment of the process of the present invention, the terbium and/or gadolinium fluoride is gadolinium fluoride, the at least one metal cathode is formed of cobalt, and the alloy is a gadolinium-cobalt alloy. In this case, the bath of molten electrolyte is preferably held at temperatures within a range of 800-1000°C, and the electrolytic reduction may be effected at those temperatures. According to a further embodiment of the process, the terbium and/or gadolinium fluoride is a mixture of terbium fluoride and gadolinium fluoride, the at least one metal cathode is formed of iron, and the alloy is a terbium-gadolinium-iron alloy. In this case, the bath of molten electrolyte is preferably held at temperatures within a range of 850-1000°C, and the electrolytic reduction is effected at those temperatures. According to a yet further embodiment of the process, the terbium and/or gadolinium fluoride is a mixture of terbium fluoride and gadolinium fluoride, the at least one metal cathode is formed of cobalt, and the alloy is a terbium-gadolinium-cobalt alloy. In this case, the bath of molten electrolyte is preferably held at temperatures within a range of 710-1000°C, and the electrolytic reduction is effected at those temperatures. According to an embodiment of the process of the present invention, the terbium and/or gadolinium fluoride is terbium fluoride, and the electrolytic reduction is effected by applying a direct current to the at least one carbon anode with a current density of 0.05-10.0 A/cm², and to the at least metal one cathode with a current density of 0.50-80 A/cm². According to another embodiment of the process of the present invention, the terbium and/or gadolinium fluoride is gadolinium fluoride, and the electrolytic reduction is effected by applying a direct current to the at least one carbon anode with a current density of 0.05-4.0 A/cm², and to the at least one cathode with a current density of 0.50-80 A/cm². According to another embodiment of the process of the present invention, the terbium and/or gadolinium fluoride is a mixture of terbiun fluoride and gadolinium fluoride, and the electrolytic reduction is effected by applying a direct current to the at least one carbon anode with a current density of 0.05-10.0 A/cm², and to the at least one cathode with a current density of 0.50-80 A/cm². In a further embodiment of the process, the at least one carbon anode is formed of graphite. In a yet further embodiment of the process, the at least one metal cathode is an elongate solid member having a substantially constant transverse cross sectional shape over its length. In a preferred embodiment of the process, the at least one metal cathode is an elongate tubular member having a substantially constant transverse cross sectional shape over its length. According to an embodiment of the process of the present invention, the bath of electrolyte containing the terbium and/or gadolinium fluoride consists essentially of at least 25% by weight of terbium fluoride and/or gadolinium fluoride, and at least 15% by weight of lithium fluoride. According to a second aspect of the present invention, there is provided an apparatus for producing an alloy containing terbium and/or gadolinium, comprising: (A) an electrowinning cell formed of refractory materials for accommodating a bath of electrolyte consisting essentially of terbium fluoride and/or gadolinium fluoride, and lithium fluoride, and optionally barium fluoride and calcium fluoride as needed; (B) a lining applied to the inner surface of the electrowinning cell and contacting the bath of electrolyte; (C) at least one elongate carbon anode having a substantially constant transverse cross sectional shape over its length, and projecting into the electrowinning cell such that a lower free end portion of the at least one carbon anode is immersed in the bath of electrolyte; (D) at least one elongate metal cathode having a substantially constant transverse cross sectional shape over its length, and projecting into the electrowinning cell such that a lower free end portion of the at least one metal cathode is immersed in the bath of electrolyte; (E) a receiver having a mouth which is open upward in a lower portion of the electrowinning cell below the free end portion of the at least one metal cathode, the receiver reserving a molten pool of the alloy containing terbium and/or gadolinium which is produced on the at least one metal cathode by means of electrolytic reduction of the terbium and/or gadolinium fluorides with a direct current applied between the at least one carbon anode and the at least one metal cathode, the produced alloy being dripped off the at least one metal cathode into the receiver; (F) siphoning means for withdrawing the molten pool of the alloy from the receiver out of the electrowinning cell; and (G) feeding means for feeding the at least one metal cathode into the bath of electrolyte so as to apply the direct current to the at least one metal cathode with a predetermined current density, for compensating for a wear length of the at least one metal cathode during production of the alloy. In a preferred embodiment of the above-mentioned apparatus of the present invention, the at least one metal cathode is formed of iron or cobalt. In another embodiment of the apparatus, the at least one metal cathode is an elongate solid member. In yet another embodiment of the apparatus, the at least one metal cathode is an elongate tubular member. In this case, the tubular metal cathode may be connected to a protection gas supplying means from which a protection gas is blown into the bath of electrolyte through an opening at a lower end of the at least one metal cathode. In a further embodiment of the apparatus of the present invention, the apparatus further comprises raw material-supply means for adding the terbium and/or gadolinium fluoride to the bath of electrolyte. In this case, the at least one metal cathode is an elongate tubular member through which the terbium and/or gadolinium fluorides are supplied into the bath of electrolyte, and which thus serves as part of the raw material-supply means. According to a yet further embodiment of the apparatus, the apparatus further comprises ascent-and-­ descent means for positioning the at least one carbon anode into the bath of electrolyte so as to apply the direct current to the at least one carbon anode with a predetermined current density, for compensating for a wear length of the at least one carbon anode during production of the alloy. According to a still further embodiment of the apparatus, the siphoning means comprises a siphon pipe which is disposed so that one end thereof is immersed in the molten pool of the produced alloy in the receiver, the siphoning means further comprising suction means for sucking the liquid alloy under vacuum from the receiver out of the electrowinning cell. This is advantageous in a case of industrialization. According to another embodiment of the apparatus of the present invention, the lining is formed of a ferrous material. This is advantageous in that the ferrous material costs less than other refractory metals such as molybdenum and tungsten. According to a still another embodiment of the apparatus, the at least one carbon anode is formed of graphite. These and other objects, and many of the attendant features and advantages of this invention will be readily appreciated, as the same becomes better understood by reference to the following detailed description of illustrative embodiments when considered in connection with the accompanying drawings, in which: Fig. 1 is a schematic diagram of an arrangement of the electrolysis system for the process of the present invention; and Fig. 2 is a sectional view showing the structure of an example of electrowinning cell with which the present invention is realized. To further clarify the present invention, illustrative embodiments of the present invention will be described in detail with reference to the accompanying drawings, in which Embodiment (A) relates to a process of producing an alloy of terbium and an apparatus therefor, Embodiment (B) relates to a process of producing an alloy of gadolinium and an apparatus therefor, and Embodiment (C) relates to a process of producing an alloy of terbium and gadolinium (i.e., an alloy containing terbium and gadolinium) and an apparatus therefor. An electrowinning cell 2, which is a principal part of the electrolysis or electrowinning system illustrated in the schematic diagram of Fig. 1, is to contain in it a solvent 4 constituting an electrolyte bath or mixed molten salts. As the solvent 4, a mixture of terbium fluoride (TbF₃) and lithium fluoride (LiF) is used for Embodiment (A), while a mixture of gadolinium fluoride (GdF₃) and lithium fluoride (LiF) is used for Embodiment (B). For Embodiment (C), a mixture of terbium fluoride, gadolinium fluoride and lithium fluoride is used as the solvent 4. In each of the three embodiments, it is possible to optionally add barium fluoride (BaF₂) and calcium fluoride (CaF₂), individually or in combination as needed. The electrolysis raw material is supplied from a raw material-supply means 6 into the electrolyte bath in the electrowinning cell 2. As the raw material, terbium fluoride is used for Embodiment (A), in place of the traditional raw material, terbium oxide (Tb₄O₇), and the terbium fluoride is at the same time one component of the electrolyte bath. For Embodiment (B), gadolinium fluoride is used as the raw material, in place of the traditional gadolinium oxide (Gd₂O₃), while for Embodiment (C) a mixture of terbium fluoride and gadolinium fluoride is used, in place of terbium oxide and gadolinium oxide, as the raw material. The gadolinium fluoride for Embodiment (B) and the terbium fluoride and gadolinium fluoride for Embodiment (C) is(are) at the same time a component(s) of the electrolyte bath for Embodiment (B) and Embodiment (C), respectively. In the electrolyte bath contained in the electrowinning cell 2, an anode or anodes 8 and a cathode or cathodes 10 are respectively inserted to be immersed therein. The anodes 8 are made of carbon, and the cathodes 10 are made of metal, such as iron and cobalt. Between the anodes 8 and the cathodes 10 direct current is applied with a power source 12 so as to carry out electrolytic reduction of the raw material, terbium fluoride, gadolinium fluoride, or the mixture of terbium fluoride and gadolinium fluoride. Metallic terbium, metallic gadolinium, or metallic terbium and metallic gadolinium, electrodeposited on the cathodes 10, will immediately produce an alloy, in a liquid state, together with the alloying metal constituting the cathodes 10. The liquid alloy produced on the cathodes 10 will drip one after another into a receiver placed in the electrolyte bath in the electrowinning cell 2 and will make a molten pool therein. Since the produced alloy on the cathodes 10 becomes liquid at the temperature where the electrolyte is fused, and specific gravity of the electrolyte bath is chosen smaller than that of the produced alloy, the liquid alloy drips readily one after another off the surface of each cathode 10 as it is formed there. The liquid alloy, collected in this matter in the receiver which is located below the cathodes 10 and the mouth of which is open upward, is withdrawn from the electrowinning cell 2 with a suitable siphoning means, i.e., alloy-withdrawing means 14 so as to be recovered. In Embodiment (C) for producing an alloy containing terbium and gadolinium, a mixture of terbium fluoride and gadolinium fluoride is used as the electrolysis raw material, instead of terbium oxide and gadolinium oxide, as stated previously. The studies conducted by the inventors et al. have revealed that, in Embodiment (C), the alloy produced on the cathode has a chemical composition whose terbium relative to gadolinium is slightly richer than terbium fluoride relative to gadolinium fluoride of the electrolyte bath. Therefore, a desired alloy whose composition has a desired ratio of terbium to gadolinium, can be continuously obtained by supplying to the electrolyte bath a mixture of terbium fluoride and gadolinium fluoride having the same ratio of terbium fluoride to gadolinium fluoride as that of the electrolyzed or consumed mixture of the two fluorides, and thereby maintaining the terbium to gadolinium ratio of the electrolyte bath during the electrolysis operation. Further, protection gas 16 is introduced into the electrowinning cell 2 for the purpose of preventing the electrolyte bath, the produced alloy, the anodes 8 and the cathodes 10, and the structural materials of the cell from deterioration, and also of avoiding the pickup of harmful impurities and non-metallic inclusions in the produced alloy. A gas or gases produced in the electrowinning cell 2 in the course of the electrolytic reduction are introduced into an exhaust gas-treating means 18 together with the protection gas 16 for being placed under a predetermined treatment. In the electrolysis system of the present invention, terbium fluoride, gadolinium fluoride, or a mixture of terbium fluoride and gadolinium fluoride is used as the electrolysis raw material, instead of terbium oxide gadolinium oxide, or a mixture of terbium oxide and gadolinium oxide. Since the terbium fluoride, the gadolinium fluoride, or the mixture of terbium fluoride and gadolinium fluoride, being the raw material, is in this system a principal component of the electrolyte bath at the same time, supplementing the same in the bath as it is consumed in the course of electrolysis is relatively easy. Another merit of use of the fluoride or fluorides, used as the raw material, is that it allows continuation of the electrolysis in a far wider range of raw material concentrations in the bath as compared with in the oxide(s) electrolysis. As to the way of supplementing the raw material, sprinkling powder of terbium fluoride, gadolinium fluoride, or the mixture of the two fluorides over the surface of the electrolyte bath is quite common and preferable because of its easier dissolution into the bath. It is, however, allowable to introduce it into the bath together with a gas, or to immerse a compressed powder briquette. Another advantage of the use of the fluoride or fluorides superior to the oxide or oxides as the raw material is a far wider range of allowance in the electrolytic raw material concentration observed within the interpolar electrolysis region in the bath. Continuation of the electrolytic operation, being provided with a wider allowance range in the raw material concentration in the bath, it is not affected so much by a delay of raw material feed to this interpolar region. In comparison with the traditional operation using the oxide or oxides, the invented method using the fluoride or fluorides, with far wider a region of allowance in regards to its concentration, is relieved to a large extent from restrictions on the raw material supply position and on the raw material supply rate depending upon the current applied. In the manufacturing of alloys of terbium, alloys of gadolinium, or alloys of terbium and gadolinium, according to the invention, of low content of impurities and of low content of non-metallic inclusions, it is required to maintain the electrolysis temperature as low as practicable. For this purpose, a mixture of molten salts consisting substantially of 29-95% by weight of terbium fluoride, gadolinium fluoride, or a mixture of terbium fluoride and gadolinium fluoride, 5-80% by weight of lithium fluoride, 0-40% by weight of barium fluoride and 0-20% by weight of calcium fluoride (total of the terbium fluoride or the gadolinium fluoride or the two fluorides mixture, the lithium fluoride, the barium fluoride, and the calcium fluoride amounts to substantially 100%) is selected as the electrolyte bath. Even when the raw material of terbium fluoride, gadolinium fluorde, or the fluorides mixture is added to the electrolyte bath, the bath must be adjusted so as to maintain during the entire process of electrolysis the above-mentioned composition. In regard to the composition of the components of the electrolyte bath, lowering of the concentration of the terbium fluoride, gadolinium fluoride, or the two fluorides mixture below the lowest limit, i.e., less than 20% will adversely affect the electrolysis results, and raising beyond the highest limit, i.e., higher than 95% will problematically increase the melting point of the bath. As to the concentration of lithium fluoride, excessive lowering thereof will raise the melting point of the bath, and excessive raising thereof will make the mutual interaction between the produced alloy and the bath too vigorous, causing thereby deterioration of the electrolysis results. The concentration of the lithium fluoride must be therefore adjusted in the range of 5-80%. Adding the barium fluoride and/or the calcium fluoride is aimed at decreasing the amount of use of the expensive lithium fluoride and also aimed at the adjustment of the melting point of the mixed electrolyte bath. Excessive addition of them tends to raise the melting point of the bath, so the concentration of the former must be limited up to 40% and that of the latter to 20%, although they may be used either singly or together. Anyway, the electrolyte bath must always be so constituted as to make the sum of the components, i.e., terbium and/or gadolinium fluoride(s), lithium fluoride, barium fluoride and calcium fluoride, to be substantially 100%. It is preferable again, when the electrolyte bath is composed only of terbium and/or gadolinium fluoride(s) and lithium fluoride, to adjust the concentration of the former to more than 25% and that of the latter more than 15%. The composition of the electrolyte bath must be selected, so that the specific gravity of the bath may be smaller than that of the produced alloy such as a terbium-iron alloy, terbium-cobalt alloy, gadolinium-iron alloy, gadolinium-­ cobalt alloy, terbium-gadolinium-iron alloy, and terbium-gadolinium-cobalt alloy. The alloy produced on the cathode can drip off the cathode into the alloy receiver with an opening, located below the cathode, because of this difference of the specific gravity between the two. The temperature of the electrolyte bath is preferably adjusted during electrolysis depending upon what kind of alloy to be produced. The temperature is maintained at 860-1000°C for a terbium-iron alloy; 710-1000 for a terbium-cobalt alloy; 850-1000 for a gadolinium-iron alloy; 800-1000 for a gadolinium-cobalt alloy; 850-1000 for a terbium-gadolinium-iron alloy; and 710-1000 for a terbium-gadolinium-cobalt alloy. At an excessively high termperature, impurities and foreign matters can enter into the products beyond the allowable limit. On the other hand, at an excessively low temperature and in the case of use of iron cathodes, the metal(s) produced on the cathode, that is, terbium, gadolinium, or terbium and gadolinium is(are) not fully fused with the iron of the cathode, since the eutectic temperature of the terbium-iron alloy, gadolinium-iron alloy, and terbium-gadolinium-iron alloy is about 845°C, about 850°C, and about 850°C (estimated), respectively. In this case, metallic terbium, or metallic gadolinium, or metallic terbium and gadolinium, each having a relatively high melting point, is electrodeposited in a solid state on the cathode. The solid metal produced on the cathode often causes interpolar short-circuiting, and finally hinders continuation of the electrolysis operation. Further, in the case where alloys of cobalt, such as terbium-cobalt alloy, gadolinium-cobalt alloy, and terbium­ gadolinium-cobalt alloy, are produced using cobalt cathodes, it becomes difficult at an excessively low temperature to maintain the composition of the electrolyte bath to be uniform, thereby adversely affecting the nature of the bath and finally hindering a continuous electrolysis operation. It goes without saying that at the lowest possible temperature within the above-mentioned range can be manufactured the purest possible alloy that has the least possible impurities and non-metallic inclusions as coming from the structural materials of the electrowinning cell. Within the above-mentioned temperature limits, alloys of high content of terbium, such as a terbium-iron alloy and a terbium-cobalt alloy each containing more than 80% by weight of terbium, can be manufactured, and the produced alloy forms liquid metal in the receiver. Similarly, alloys of high content of gadolinium, such as a gadolinium-iron alloy and a gadolinium-cobalt alloy each containing more than 60% by weight of gadolinium, and alloys of high content of terbium and gadolinium, such as a terbium-gadolinium-iron alloy and a terbium-gadolinium-­ cobalt alloy each containing more than 70% (in total) by weight of terbium and gadolinium, can be manufactured. Each of the molten alloys can be effectively siphoned or withdrawn from the electrowinning cell by vacuum suction. It is also possible to tap it from the bottom of the cell by flowing-down by gravity. In either way of the withdrawing of the alloy, it needs not to be heated at all, because it can be withdrawn easily in the liquid state as it is. As to the electrodes used in the electrolysis in the present invention, it is preferable to use a cathode made of a metal that can give an alloy with terbium and/or gadolinium. Iron or cobalt is preferably used as material for the cathode. For the anode, carbon, in particular graphite, is used. Metal used for the cathode must be of low content of impurities because such impurities are easily introduced into the produced alloy. In all Embodiments (A), (B), and (C), the cathode is consumed during the electrolysis operation so as to form the alloy. Compensation for the consumption of the cathode by means of gradual immersion of the same into the electrolyte bath will, however, enable the electrolysis, i.e. manufacture of the alloy, to continue without interruption. In this case the metallic components to be used as the cathode may be connected one after another by forming threadings on both the ends, which makes it easy to continuously compensate for the consumption of the cathode. Use of such a solid cathode is, in comparison with a molten metal cathode, far more convenient in handling and is very advantageous for simplifying the structure of the electrowinning cell. It naturally allows enlarging of the electrowinning cell, to a great advantage, in the case of industrialization. In the electrolysis of the terbium fluoride using carbon anodes in this invention, it is desirable to maintain the current density over the whole immersion surface of the anodes within the range of 0.05-10.0 A/cm² during all the time of the electrolysis operation. Similarly, the current density of the anodes is maintained under the same conditions withing the range of 0.05-4.0 A/cm² for the electrolysis of the gadolinium fluoride and the mixture of terbium fluoride and gadolinium fluoride. When the current density is excessively small, it means either that the immersion surface of the anode is too large or that the current per unit area of the anode surface is too small, which lowers the productivity, with a result of industrial demerit. On the other hand, raising the current density to too high a level tends to bring about the anode effect which has been observed in the electrolysis using the oxide or oxides as the raw material, or some other similar abnormal phenomena. It is therefore recommendable in the invention to maintain the anode current density within the above-mentioned range, as one of the required conditions for the electrolysis, so as to effectively prevent occurrence of such abnormal phenomena. In Embodiment (B), it is more preferable to keep the current density between 0.1 and 3.0 A/cm² over the whole immersion surface of the anodes, from the consideration of possible variation of the current density on a local area thereof. Similarly, in Embodiments (A) and (C) it is more preferable to keep the current density between 0.1 and 8.0 A/cm² over the whole immersion surface of the anodes, from the same consideration. At the same temperature, the fluoride or fluorides, used as the raw material for the electrolysis, permits the anode to have a higher current density than the oxide or oxides. This is advantageous in a case of industrialization. As to the current density on the cathode in this invention a fairly broad range such as 0.50-80 A/cm² is allowed over the whole immersion surface thereof, for the three embodiments. When the current density on the cathode is too low, however, the current per unit surface area of the cathode becomes too small, lowering the productivity to the extent of being industrially impractical; when it excessively rises, on the other hand, electrolytic voltage rises so much as to affect adversely the electrolysis results. In the actual electrolysis operation in the production line it is preferable, for all the embodiments, to keep the cathode current density in a narrower range, 1.0-30 A/cm², which facilitates keeping the voltage fluctuation small and makes the electrolysis operation easy and smooth. Regarding the electrodes, the anode is in the present invention provided as a carbon anode independently, not letting the bath container or crucible, which is made of a material resistant to the corrosive action of the bath, function simultaneously as the anode, so consumption of the anode does not necessarily require stoppage or interruption of the operation as in the case of the crucible anode. A separately provided anode may be compensated for the consumption thereof by immersing the same deeper into the bath as it shortens. When more than one is provided, they can be replaced one by one as they shorten. As to the cathode, consumption can be compensated similarly in all the embodiments only by the deeper immersion of the same or by the replacement thereof. As to the arrangement or configuration of both electrodes, it is preferable in the present invention, to set a plurality of anodes around each cathode so that the former can face the latter, taking advantage of the fairly large difference of the current density between the anode and the cathode. In that case, replacement of the anodes is an easy task, allowing their successive replacement and thereby never interrupting alloy-producing operation. The benefits of the electrolysis process can be herewith fully realized. It is also practically very convenient that both the anodes and cathodes have constant and uniform shapes in their longitudinal direction, which facilitates their continuous and successive use, by being replaced in turn. An electrowinning cell of the above-described embodiments will be further described with reference to a preferred form illustrated in a schematic sectional view of Fig. 2. The cell which is allotted the reference numeral 20 is composed of a lower main cell 22 and a lid body 24 covering the opening of the former. The outer sides of these two members 22 and 24 are covered by metallic outer shells 26, 28, respectively. Usually, the outer shells 26, 28 are made of steel or the like. Both the lower main cell 22 and the lid body 24 are respectively provided, inside the outer shells 26, 28, with double lining layers laid one on the other, the outer being a refractory heat-insulating layer 30, 32 made of brick or castable alumina, etc., and the inner being a layer 34, 36 which is resistant to the bath and is made of graphite, carbonaceous stamping mass, or the like. The inner side of the corrosion-resistant material layer 34 is further provided with a lining member 38 for covering the potentially bath-contacting surface thereof. The lining member 38 functions to prevent entry of trace impurities coming from the corrosion-resistant layer 34, and when it is made of a refractory metal such as tungsten, molybdenum, etc., it can work at the same time as the earlier mentioned receiver for the dipping alloy. However, it is recommended in the present invention to use an inexpensive iron material for the lining member 38. Studies of the inventors et al. came to a discovery that the inexpensive iron has unexpectedly excellent corrosion resistance to the action of the electrolyte bath, i.e., fused fluoride salts, and that it can be a suitable lining member in the case of fluoride electrolyte baths. It is permissible to omit the layer 34, since the lining member 38 can be directly applied on the refractory heat-insulating layer 30. Passing through the lid body 24, one or more metal cathodes 40 and a plurality of carbon anodes 42, arranged to face each cathode 40, are set such that both 40, 42 may be immersed into the electrolyte bath of predetermined molten salts contained in the lower main cell 22 by the length or distance appropriate to produce a predetermined current density on each of the electrodes. Only two of the carbon anodes 42, 42, which should be arranged to face the cathode 40, are illustrated in the drawing. As the material for the cathodes, a metal which is easily alloyed with terbium and/or gadolinium is used, such as iron, cobalt, copper, nickel, manganese, chromium, and titanium. As the material for the anodes, graphite is recommendable. Those carbon anodes 42 may be used in a variety of shapes, such as a rod form, a plate form, a pipe form, etc. They may also be fluted, as is well known, with the object of lowering the anode current density by enlarging the anode surface area of the immersed portion thereof in an electrolyte bath 44. The carbon anodes 42 in Fig. 2 are slightly tapered on the immersed portion thereof in order to show trace of the anode consumption. Those anodes 42 may be provided with a suitable electric lead-bar of metal or a like conductive material for the purpose of power-­ supplying. They are also equipped with an ascent-and-­ descent device 46, with which they can be moved up and down into the bath and also adjusted continuously or intermittently as to the length of the immersed portion thereof so as to surely maintain the required anode current density. In other words, the surface area of the immersed portion, on which the anode current density under a continuous and constant current depends, is adjusted through the length thereof. The ascent-and-descent device 46 may be imparted the function, at the same time, of electric contact for the anode. The cathode or cathodes 40 are, on the other hand, made of cobalt, iron or other metal that is alloyed with the metallic terbium and/or gadolinium electrodeposited on the cathode through the electrolytic reduction. In Fig. 2 only one cathode 40 is illustrated, and its immersed portion is shown as a cone, as a sign of the cathode consumption due to dripping of the produced alloy. The cathode 40 takes a solid form, as the electrolysis temperature is selected below the melting point of the iron cathode 40, and may be a wire, a rod, or a plate in its shape. This cathode 40 is also equipped with an ascent-and-descent device 48, with which it is introduced into the bath 44 continuously or intermittently so as to compensate for the consumption thereof due to the alloy formation. The ascent-and-descent device 48 can simultaneously work as an electric contact. It is permissible to protect the non-immersed portion thereof with a sleeve or the like, from corrosion. For the purpose of receiving the alloy thus produced on the tip of the cathode 40, a receiver 50 is placed, in the bath 44, on the bottom of the lower main cell 22, with an opening or mouth thereof just below the cathode 40. A drop-formed liquid alloy 52, produced on the tip of the cathode 40 by the electrolytic reduction, drips off the cathode 40 and falls down to be collected in the receiver 50. This receiver 50 may be made of a refractory metal such as tungsten, tantalum, molybdenum, niobium, or their alloy, with small reactivity to the produced alloy 52. As its material, ceramics made of borides like boron nitride or of oxides or cermet is also permissible. The electrolyte bath 44 is a fused salt solution of a fluorides mixture containing terbium fluoride and/or gadolinium fluoride therein with an adjusted composition according to the present invention, and its composition is so selected as to make the specific gravity thereof to be smaller than that of the produced alloy. The electrolysis raw material which is consumed through the electrolytic operation is supplemented by feeding it from a raw material-supply means 54 through a material-supply hole 56 formed in the lid body 24 so as to prepare and maintain the electrolyte bath 44 of a predetermined preferable composition. As mentioned earlier the produced alloy 52, which drips off the metal cathode 40 to be reserved in the receiver 50, is, when the reserved amount reaches to a predetermined value, withdrawn in a liquid state from the electrowinning cell 20 by a predetermined alloy siphoning or tapping system. An alloy-siphoning system such as illustrated in Fig. 2 is preferably used for this purpose, wherein a pipe-like vacuum suction nozzle 58 is inserted, through a produced alloy-suction hole 60 formed in the lid body 24, into the electrolyte bath 44, such that the lower end of the nozzle 58 can be immersed into the produced alloy 52 in the alloy receiver 50, and the alloy 52 is withdrawn, through sucking action of a vacuum means (not illustrated), from the electrowinning cell 20. It is also permissible here to install an alloy tapping or flowing-out system, in place of the alloy siphoning system for withdrawing the alloy 52 by evacuation, which is provided with a tapping pipe, passing through the wall of the electrowinning cell 20 (lower main cell 22) and further passing through the wall of the alloy receiver 50, for having its opening in the alloy receiver 50, so as to flow the alloy 52 down out of the lower main cell 22 by gravity. There is a not-illustrated protection gas-­ supplying device, in the present invention, for supplying protection gas into the cell 20 such that possibly generated gas or gases in the course of electrolysis operation may be discharged together with the protection gas through an exhaust gas outlet port 62. It goes without saying that a heating device may be equipped with, when needed, inside or outside the cell 20 for maintaining the electrolysis temperature to a desired level, although it is not shown in the figure. There will be described some examples of the present invention, which however are shown for illustrative purpose only, and in which Examples 1 and 2 relate to Embodiment (A) for producing alloys of terbium, Examples 3 and 4 relate to Embodiment (B) for producing alloys of gadolinium, and Examples 5 and 6 relate to Embodiment (C) for producing alloys of terbium and gadolinium. The present invention can be practised in a variety of ways other than the above-mentioned description and the disclosed embodiments as well as the following examples, based on the knowledge of those skilled in the art, within the limit and spirit thereof. All of those varieties and modifications should be understood to be included in this invention. Example 1 A rare earth-iron (RE-Fe) alloy, 0.49 kg, with a composition of 89% by weight of rare earth metals including terbium for the most part and 11% by weight of iron was obtained by the following process: An electrolyte bath consisting substantially of two fluorides, i.e., terbium fluoride and lithium fluoride was electrolyzed, at an average temperature 900°C, in an inert gas atmosphere with an electrowinning cell of the type shown in Fig. 2. As the cell, was used a graphite crucible which is lined by a lining member made of a ferrous material resistive to the bath. An alloy receiver made of boron nitride (BN) was placed in the middle portion of the bottom of the graphite crucible. A single wire-like vertical iron cathode with 6 mm was immersed in the bath in the middle portion of the graphite crucible, while four rod-like vertical graphite anodes with 40 mm were immersed in the bath in a concentric (in the plane view) arrangement around the single cathode. Powdered terbium fluoride as the raw material was continuously supplied so as to maintain the electrolysis operation for 8 hours under the operation conditions shown in Table I. All the time during this operation, the electrolysis was satisfactorily continued, producing drips of liquid alloy of rare earth (terbium) with iron collected one by one in the BN receiver placed in the bath. The alloy was siphoned from the cell with a vacuum suction type alloy siphoning system having a nozzle. The electrolysis results and the analysis results of the obtained alloy are shown in Table I and Table II, respectively. Values of current efficiency (%) shown in Table I were determined based upon the weight of rare earth metals obtained, on the assumption that the rare earth metals include terbium only. Example 2 A rare earth(terbium)-cobalt alloy, 0.58 kg, with a composition of 80% of rare earth metals consisting substantially of terbium and 20% of cobalt, was obtained by way of the undermentioned electrolysis operation: A lining of iron was applied inside a container of graphite crucible in the cell. An alloy receiver made of molybdenum was placed in the middle portion of the bottom of the graphite crucible. A mixture substantially consisting of terbium fluoride and lithium fluoride, as the electrolyte bath, was electrolyzed at an average temperature 790°C in an inert gas atmosphere. A single rod-like vertical cobalt cathode with 6 mm was arranged in the similar manner as in Example 1. Four rod-like vertical graphite anodes with 40 mm were used just like in Example 1. The raw material of terbium fluoride was continuously supplied into the bath during the electrolysis operation of 8 hours under the conditions in Table I. The process progressed satisfactorily, and the produced rare earth(terbium)-cobalt alloy was collected in the molybdenum receiver, in the form of drips during the operation. The alloy could be siphoned in a liquid state as in Example 1. The electrolysis results and the analysis results of the produced alloy are shown respectively in Table I and Table II. Example 3 A rare earth-iron (RE-Fe) alloy, 0.54 kg, with a composition of 87% by weight of rare earth metals including gadolinium for the most part and 13% by weight of iron was obtained by the following process: An electrolyte bath consisting substantially of two fluorides, i.e., gadolinium fluoride and lithium fluoride was electrolyzed, at an average temperature 885°C, in an inert gas atmosphere with an electrowinning cell of the type shown in Fig. 2. As the cell, was used a graphite crucible which is lined by a lining member made of a ferrous material resistive to the bath. An alloy receiver made of boron nitride (BN) was placed in the middle portion of the bottom of the graphite crucible. A single wire-like vertical iron cathode with 6 mm was immersed in the bath in the middle portion of the graphite crucible, while four rod-like vertical graphite anodes with 40 mm were immersed in the bath in a concentric (in the plane view) arrangement around the single cathode. Powdered gadolinium fluoride as the raw material was continuously supplied so as to maintain the electrolysis operation for 8 hours under the operation conditions shown in Table III. All the time during this operation, the electrolysis was satisfactorily continued, producing drips of liquid alloy of rare earth (gadolinium) with iron collected one by one in the BN receiver placed in the bath. The alloy was siphoned from the cell with a vacuum suction type alloy siphoning system having a nozzle. The electrolysis results and the analysis results of the obtained alloy are shown in Table III and Table IV, respectively. Values of current efficiency (%) shown in Table III were determined based upon the weight of rare earth metals obtained, on the assumption that the rare earth metals include gadolinium only. Example 4 A rare earth(gadolinium)-cobalt alloy, 0.53 kg, with a composition of 83% of rare earth metals consisting substantially of gadolinium and 17% of cobalt, was obtained by way of the undermentioned electrolysis operation: A lining of iron was applied inside a container of graphite crucible in the cell. An alloy receiver made of tungsten was placed in the middle portion of the bottom of the graphite crucible. A mixture substantially consisting of gadolinium fluoride and lithium fluoride, as the electrolyte bath, was electrolyzed at an average temperature 831°C in an inert gas atmosphere. A single rod-like vertical cobalt cathode with 6 mm was arranged in the similar manner as in Example 3. Four rod-like vertical graphite anodes with 40 mm were used just like in Example 3. The raw material of gadolinium fluoride was continuously supplied into the bath during the electrolysis operation of 8 hours under the conditions in Table III. The process progressed satisfactorily, and the produced rare earth(gadolinium)-cobalt alloy was collected in the tungsten receiver, in the form of drips during the operation. The alloy could be siphoned in a liquid state as in Example 3. The electrolysis results and the analysis results of the produced alloy are shown respectively in Table III and Table IV. Example 5 A rare earth-cobalt (RE-Co) alloy, 0.52 kg, with a composition of 80% by weight of rare earth metals including terbium and gadolinium for the most part and 20% by weight of cobalt was obtained by the following process: An electrolyte bath made substantially of three fluorides, i.e., terbium fluoride, gadolinium fluoride and lithium fluoride was electrolyzed, at an average temperature 840°C, in an inert gas atmosphere with an electrowinning cell similar to that shown in Fig. 2. As the cell, was used a graphite crucible. An alloy receiver made of boron nitride was placed in the middle portion of the bottom of the graphite crucible. A single wire-like vertical cobalt cathode with 6 mm was immersed in the bath in the middle portion of the graphite crucible, while four rod-like vertical graphite anodes with 40 mm were immersed in the bath in a concentric (in the plane view) arrangement around the single cathode. Powder of a mixture of terbium fluoride and gadolinium fluoride as the raw material was continuously supplied so as to maintain the electrolysis operation for 8 hours under the operation conditions shown in Table V. All the time during this operation, the electrolysis was satisfactorily continued, producing drips of liquid alloy of rare earth (terbium and gadolinium) with cobalt collected one by one in the boron-nitride receiver placed in the bath. The alloy was siphoned from the cell with a vacuum suction type alloy siphoning system having a nozzle. The electrolysis results and the analysis results of the produced alloy are shown respectively in Table V and Table VI. Example 6 A rare earth(terbium and gadolinium)-iron alloy, 0.41 kg, with an average composition of 88% of rare earth metals including terbium and gadolinium for the most part and 12% of iron was obtained by way of the undermentioned electrolysis operation: A lining of iron was applied inside a container of graphite crucible in the cell. An alloy receiver made of boron nitride was placed in the middle portion of the bottom of the graphite crucible. A mixture substantially consisting of three fluorides, i.e., terbium fluoride, gadolinium fluoride, and lithium fluoride, as the electrolyte bath, was electrolyzed at an average temperature 900°C in an inert gas atmosphere. A single wire-like vertical iron cathode with 6 mm was arranged in the similar manner as in Example 5. Four of rod-like vertical graphite anodes with 40 mm were used just like in Example 5. The raw material, a mixture of terbium fluoride and gadolinium fluoride, was continuously supplied into the bath during the electrolysis operation of 8 hours under the conditions in Table V. The process progressed satisfactorily, and the produced alloy of rare earth (terbium and gadolinium) with iron was collected in the boron-nitride receiver, in the form of drips during the operation. The alloy could be siphoned in a liquid state as in Example 5. The electrolysis results and the analysis results of the produced alloy are shown respectively in Table V and Table VI. As can be evidently observed from Tables I to Table VI, alloys rich in terbium and gadolinium, such as a terbium-iron alloy, terbium-cobalt alloy, gadolinium-iron alloy, gadolinium-cobalt alloy, terbium-­ gadolinium-iron alloy, and terbium-gadolinium-cobalt alloy, can be produced easily through electrolysis of terbium fluoride and/or gadolinium fluoride, in a single step. It is also clearly recognized in these tables, that the alloys produced by the invented method contain little impurities such as calcium or oxygen which are known to have the detrimental effect on the properties of the produced alloys. With regard to all the examples described above, it is easy to continue the experiments longer, exceeding the time durations shown in the tables, and similar results to those tabulated in the tables have been ascertained even in the said elongated experiment.

Claims: 1. A process of producing an alloy containing terbium and/or gadolinium, comprising the steps of: preparing a bath of molten electrolyte which has a composition consisting essentially of 20-95% by weight of terbium fluoride and/or gadolinium fluoride, 5-80% by weight of lithium fluoride, up to 40% by weight of barium fluoride and up to 20% by weight of calcium fluoride; effecting electrolytic reduction of said terbium and/or gadolinium fluoride in said bath of molten electrolyte, with at least one carbon anode and at least one metal cathode, so as to electrodeposit terbium and/or gadolinium on said at least one metal cathode, and alloying the electrodeposited terbium and/or gadolinium with metal of said at least one metal cathode so as to produce said alloy containing terbium and/or gadolinium in a liquid state on said at least one metal cathode; adding said terbium and/or gadolinium fluoride to said bath of molten electrolyte so as to maintain said composition of the bath of molten electrolyte, for compensating for consumption of the terbium and/or gadolinium fluorides during production of said alloy; dripping the liquid alloy from said at least one metal cathode into a receiver having a mouth which is open upward in a lower portion of the bath of molten electrolyte below said metal cathode, and thereby collecting said liquid alloy in the form of a molten pool in said receiver; and withdrawing said molten pool of the liquid alloy from said receiver. 2. A process according to claim 1, wherein said at least one metal cathode is formed of a metal selected from iron, cobalt, copper, nickel, manganese, chromium, and titanium. 3. A process according to claim 1 or claim 2, wherein said at least one metal cathode is formed of iron or cobalt and said alloy is a terbium-iron alloy, a terbium-cobalt alloy, a gadolinium-iron alloy, a gadolinium-cobalt alloy, a terbium-gadolinium-iron alloy or a terbium-gadolinium-cobalt alloy. 4. A process according to claim 3, wherein where said fluoride is terbium fluoride and said at least one metal cathode is formed of iron, said bath of molten electrolyte is held at temperatures within the range of 860-1000°C, said electrolytic reduction is effected at said temperatures and said alloy is a terbium-iron alloy; where said fluoride is terbium fluoride and said at least one metal cathode is formed of cobalt, said bath of molten electrolyte is held at temperatures within the range of 710-1000°C, said electrolytic reduction is effected at said temperatures and said alloy is a terbium-­ cobalt alloy; where said fluoride is gadolinium fluoride and said at least one metal cathode is formed of iron, said bath of molten electrolyte is held at temperatures within the range of 850-1000°C, said electrolytic reduction is effected at said temperatures and said alloy is a gadolinium-­ iron alloy; where said fluoride is gadolinium fluoride and said at least one metal cathode is formed of cobalt, said bath of molten electrolyte is held at temperatures within the range of 800-1000°C, said electrolytic reduction is effected at said temperatures and said alloy is a gadolinium-cobalt alloy; where said fluoride is a mixture of terbium fluoride and gadolinium fluoride and said at least one metal cathode is formed of iron, said bath of molten electrolyte is held at temperatures within the range of 850-1000°C, said electrolytic reduction is effected at said temperatures and said alloy is a terbium-gadolinium-iron alloy; and where said fluoride is a mixture of terbium fluoride and gadolinium fluoride and said at least one metal cathode is formed of cobalt, said bath of molten electrolyte is held at temperatures within the range of 710-1000°C, said electrolytic reduction is effected at said temperatures and said alloy is a terbium-gadolinium-cobalt alloy. 5. A process according to any one of claims 1 to 4, wherein when said terbium and/or gadolinium fluoride is terbium fluoride, said electrolytic reduction is effected by applying a direct current to said at least one carbon anode with a current density of 0.05-10.0 A/cm², and to said at least one metal cathode with a current density of 0.50-­ 80 A/cm²; when said terbium and/or gadolinium fluoride is gadolinium fluoride, said electrolytic reduction is effected by applying a direct current to said at least one carbon anode with a current density of 0.05-4.0 A/cm², and to said at least one cathode with a current density of 0.50-80 A/cm²; and when said terbium and/or gadolinium fluoride is a mixture of terbium fluoride and gadolinium fluoride, said electrolytic reduction is effected by applying a direct current to said at least one carbon anode with a current density of 0.05-10.0 A/cm², and to said at least one cathode with a current density of 0.50-80 A/cm². 6. A process according to any one of claims 1 to 5, wherein said at least one carbon anode is formed of graphite. 7. A process according to any one of claims 1 to 6, wherein said at least one metal cathode is an elongate solid member having a substantially constant transverse cross sectional shape over its length or an elongate tubular member having a substantially constant transverse cross sectional shape over its length. 8. A process according to any one of claims 1 to 7, wherein said bath of electrolyte containing said terbium and/or gadolinium fluoride consists essentially of at least 25% by weight of terbium fluoride and/or gadolinium fluoride, and at least 15% by weight of lithium fluoride. 9. An apparatus for producing an alloy containing terbium and/or gadolinium, comprising: an electrowinning cell formed of refractory material for accommodating a bath of electrolyte consisting essentially of terbium fluoride and/or gadolinium fluoride, and lithium fluoride, and optionally barium fluoride and calcium fluoride as needed; a lining applied to the inner surface of said electrowinning cell and adapted to contact said bath of electrolyte; at least one elongate carbon anode having a substantially constant transverse cross sectional shape over its length, and projecting into said electrowinning cell such that a lower free end portion of said at least one carbon anode is adapted to be immersed in said bath of electrolyte; at least one elongate metal cathode having a substantially constant transverse cross sectional shape over its length, and projecting into said electrowinning cell such that a lower free end portion of said at least one metal cathode is adapted to be immersed in said bath of electrolyte; a receiver having a mouth which is open upward in a lower portion of said electrowinning cell below said free end portion of said metal cathode, said receiver being adapted to receive a molten pool of said alloy containing terbium and/or gadolinium which is produced on said at least one metal cathode by means of electrolytic reduction of said terbium and/or gadolinium fluoride with a direct current applied between said at least one carbon anode and said at least one metal cathode, the produced alloy being dripped off said at least one metal cathode into said receiver; means for withdrawing said molten pool of the alloy from said receiver out of said electrowinning cell; and feeding means for feeding said at least one metal cathode into said bath of electrolyte so as to apply the direct current to said at least one metal cathode with a predetermined current density, for compensating for consumption of said at least one metal cathode during production of said alloy. 10. An apparatus according to claim 9, wherein said at least one metal cathode is formed of iron or cobalt. 11. An apparatus according to claim 9 or claim 10, wherein said at least one metal cathode is an elongate solid member or an elongate tubular member. 12. An apparatus according to claim 11, wherein said metal cathode is tubular and is connected to a protection gas supplying means from which a protection gas is blown into said bath of electrolyte through an opening at a lower end of said at least one metal cathode. 13. An apparatus according to any one of claims 9 to 12, further comprising raw material-supply means for adding said terbium and/or gadolinium fluoride to said bath of electrolyte. 14. An apparatus according to claim 27, wherein said at least one metal cathode is an elongate tubular member through which said terbium and/or gadolinium fluoride is supplied into said bath of electrolyte, and which thus serves as part of said raw material-supply means. 15. An apparatus according to any one of claims 9 to 14, further comprising raising-and-lowering means for positioning said at least one carbon anode into said bath of electrolyte so as to apply the direct current to said at least one carbon anode with a predetermined current density, for compensating for wearing away of said at least one carbon anode during production of said alloy. 16. An apparatus according to any one of claims 9 to 15, wherein said siphoning means comprises a siphon pipe which is disposed so that one end thereof is immersed in said molten pool of the produced alloy in said receiver, said siphoning means further comprising suction means for sucking the liquid alloy under vacuum from said receiver out of said electrowinning cell. 17. An apparatus according to any one of claims 9 to 16, wherein said lining is made of a ferrous material. 18. An apparatus according to any one of claims 9 to 17, wherein said at least one carbon anode is made of graphite.

Inventors: ITOH, KATSUHISA, NAKAMURA, EIJI, NISHIO, MASAHIRO, SAKAKIBARA, MIKIO, SASAKI, SHIGEAKI
Applicants: SUMITOMO LIGHT METAL INDUSTRIES, LTD.
Application year: 1987
Main classification: C25C3
IPC codes: C25C3