PROCESS FOR STABILIZATION TREATMENT OF FERROMAGNETIC METAL POWDERS

Abstract: Apparatus for the stabilizing treatment of ferromagnetic metal powders comprises a horizontal, cylindrical, rotatable reactor body (1) having a feed port (2) for introducing ferromagnetic metal powder into the reaction body, a withdrawal port (2) for removing treated ferromagnetic metal powder from the body; an inlet conduit (3) for introducing an oxidizing gas into the reactor body; and an outlet conduit (4) for removing oxidizing gas from the reactor body. Ferromagnetic metal powder is subjected to surface oxidation in the apparatus by passing oxidising gas through the reactor body whilst rotating it.

Description: This invention relates to a process for the stabilization treatment of ferromagnetic metal powders, and more particularly it relates to a process for the stabilization treatment of ferromagnetic metal powders composed mainly of iron. Recently there has been marked developments in magnetic recording and in magnetic powders for use in magnetic recording media. In order to achieve high density magnetic recording, there have been developments in ferromagnetic metal powders having a high coersive force and high saturation magnetization. However, since such ferromagnetic metal powders have a very high chemical activity due to their fine particle size, the powders, if untreated, are at once oxidized upon exposure to air with consequent less of desirable properties. In addition heat generation or ignition may occur due to the sudden oxidation to give rise to problems of handling and safety. There is also the problem of corrosion resistance which is most important for magnetic tapes (hereinafter simply referred to as "tape"). In order to overcome such problems it has been proposed to apply organic substances onto the surface of the ferromagnetic metal powders or to submit them to a surface oxidation treatment. In the case of surface treatment with organic substances, some effect upon the stability of powder itself is observed, but when coating with the resulting powder, the width of choice of surfactant, solvent etc. is narrowed so as to make dispersing of the coating very difficult; hence a high quality tape could not be obtained and, also, the treatment is not effective with regard to the corrosion resistance of a tape. The surface oxidation treatment process (i.e. an oxidized coating-forming process using diluted oxygen as an oxidizing gas) has been most widely employed and is an effective process. An apparatus for carrying out the process there have been prepared stirred vessel type (Japanese laid-open patent application No. Sho. 55-164001/1980); a fluidized bed type vessels (U.S.P. 4420330), and fixed type vessel (Japanese patent application laid-open No. Sho. 57-19301/1982), but problems have arisen in the formation of a uniform and dense oxidized coating to give a powder of good quality. Treatment using a stirred vessel reactor is effected by dispersing the ferromagnetic metal powder in an organic solvent and stirring and blowing an oxidizing gas into the resulting dispersion to form an oxidized film on the ferromagnetic metal powder. In order to uniformly disperse the ferromagnetic metal powder in the organic solvent, it is necessary to grind the powder granules into primary or secondary particles. However, the surface energy of ferromagnetic metal powders is so large that when the powder is ground, agglomeration occurs; hence the surface oxidation not only becomes uneven, but also the agglomerate does not wholly disintegrate so that it has an unwanted influence upon the physical properties of a tape. Further, since it is necessary to carry out agitation inside the reactor vessel, a stirrer is provided therein. The resulting agitation causes collision of particles with one another, resulting in pulverization and further agglomeration to thereby adversely affect the physical properties of the powder. Treatment using a fluidized bed type reactor is carried out by fluidizing the ferromagnetic metal powder in the gas to form an oxidized film, but it is difficult to establish fludizing conditions and it is necessary to carry out food fluidization for uniform coating. Pulverization and agglomeration due to particle collision occurs so that, not only is a non-uniform oxidized film formed, but also the physical properties of ferromagnetic metal powder are reduced. When using a reactor of the fixed vessel type, since the ferromagnetic metal powder is not moved, pulverization due to particle collision does not occur, but non-uniform oxidation due to uneven flow of gas occurs and, in extreme cases, reaction may abruptly proceed due to local oxidation heat-generation; so that the operation may prove impossible. It is an object of the present invention to provide apparatus for stabilizing ferromagnetic magnetic powders by a surface oxidization treatment process, which apparatus makes it possible to form a surface-oxidized film which is as uniform and dense as possible and to give a ferromagnetic metal powder of good quality. According to the invention there is provided a process for treating ferromagnetic metal powders which comprises the steps of: molding said ferromagnetic metal powders into granules having an average diameter of 0.25 to 10 mm; feeding said granules into apparatus comrpising having a horizontal, cylindrical, rotatable reactor body (1) having a feed port (2) for introducing ferromagnetic metal powder into the reactor body, a withdrawal port for removing ferromagnetic metal powder from the reactor body which port may be the same as the feed port (2), an inlet conduit (3) for introducing gas into the reactor body, and an outlet conduit (4) for removing oxidizing gas from the reactor body, the reactor not being provided with a stirrer; oxidizing the surface of said granules by passing an oxygen-containing gas through the reactor at a temperature of 0 to 90°C and at a speed of 0.01 to 2 m/sec. In the following description reference will be made to the accompanying drawings in which:- Figs. 1, 2, 4 and 6 are each schematic longitudinal sections through various embodiments of apparatus for use in the present invention; Fig. 3 is cross-sectional view along the line III-III of Fig. 2'; Fig. 5 is cross-sectional view along the line V-V of Fig. 4; and Fig. 7 is cross-sectional view along the line VII-VII of Fig. 6. DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS In the accompanying drawings, numeral 1 shows the body of a reactor; 2, a feeding port for raw material (ferromagnetic metal powder) in common to a withdrawing port for ferromagnetic metal powder after stabilization treatment; 3,4, inlet and exit for oxidizing gas (either of which may be inlet or exit; 3, inlet and 4, exit, in Figs. 1, 2, 4 and 6); and 5, a pipe located at the central part of the body through which an oxidizing gas passes. The pipe 5 is supported by a pedestal (not shown) onto the body of the reactor 1. The numeral 6 shows a shaft supporting the body; 7, a supporting roller; 8, a ground packing and a bearing. A gas or a liquid is sealed by the ground packing and the body of the reactor or the pipe located at the central part of the body through which an oxidizing gas passes is supported by the bearing. Numeral 9 shows a box supporting the body of the reactor and 10, a gas duct. The inlet or exit 3 for the oxidizing gas and the pipe 5 located at the central part of the body through which the oxidizing gas passes constitute a passageway for blowing or withdrawing the oxidizing gas. The exit or inlet 4 of the oxidizing gas, the box supporting the body of the reactor 9, the gas duct 10 and ground packings and bearings 8 between the box supporting the body of the reactor 9, the gas duct 10 and the pipe 5 at the central part of the body through which an oxidizing gas passes, constitute the withdrawing passageway or the blowing-in passageway for the oxidizing gas. Numeral 11 shows a driving motor for rotating the body of the reactor; 12, a support for the reaction apparatus; 13, a scraping-up plate; and 14, 15, inlet or exit for heating medium or cooling medium (either of which may be inlet or exit; and in Figs. 1, 2, 4 and 6, numeral 14 shows inlet and 15, exit); 16, a jacket; 17, a box supporting the body of the reactor; 18, an outer side duct for heating (or cooling) medium; 19, an inner side duct for heating (or cooling) medium; and 20, granules of ferromagnetic metal powder. Arrow marks indicate the passing direction of the oxidizing gas, the passing direction of heating or cooling medium and the rotating direction of the body of the reactor. A raw material composed mainly of iron and also containing at least one component of metal elements other than iron such as Ni, Si, Aℓ, Mn, Cu, Cr, Ti, Mg, Co, Zn, Ba, Sn, etc. and compounds of these metal elements, the content of the metal element being in the range of 0 to 50% by weight based on the weight of iron, is molded into granules having a minimum diameter of 0.25 to 10 mm. If the proportion of the metal elements other than iron and compounds thereof exceeds 50% by weight based on the weight of iron, there is a fear that the ferromagnetic characteristics are lost. Further, if the minimum diameter of granules of ferromagnetic metal powder is less than 0.25 mm, the granules are scattered by an oxidizing gas to the outside of the body of the reactor 1. If the minimum diameter of the granules exceeds 10 mm, there is a fear that the surface oxidation of the ferromagnetic powder becomes non-uniform. As the oxidizing gas, an inert gas containing oxygen is preferred to use. The oxygene concentration of the oxidizing gas has no particular limitation, but if the gas is too much diluted, the reaction is so retarded that it is practically undesirable. Thus, 0.5% by volume or more is preferred. On the other hand, when a solvent is used, the upper limit should be restricted to its explosion range or less for safety. As to the dilution of oxygen in the oxidizing gas, use of an inert gas raises no problem, and nitrogen gas may be advantageously used. Further, the gas quantity is preferred to be adjusted so that 5 to 30 hours may be required for making the quantity of the surface layer oxidized (hereinafter referred to "conversion") 10 to 25%. If the oxidation rate is too high, there is a fear of deterioration of the physical properties due to local heat generation. As to the body of the reactor 1, a horizontal, cylindrical, rotating type reactor is used, since this horizontal, rotating type reactor can uniformly mix granules of ferroelectric metal powder. In short, the granules within the layer of the granules ascend with rotation of the body of the reactor 1, and after the granules reach the upper end of the granule layer, they drop on the surface of the granule layer. When they are dropping, they are exposed to the oxidizing gas. Thus, the moving of the granules is uniformly carried out. The granules within the granule layer in the reactor are moved and uniformly mixed as described above, whereby it is possible to form a dense surface-oxidized film on the surface of the ferromagnetic metal powder. Further, another important point of the apparatus of the present invention consists in that the apparatus is utterly not provided with any means such as stirrer, etc., which resultantly mechanically pulverizes the granules of ferromagnetic metal powder. When the granules of ferroelectric metal powder are pulverized, the powder particles are broken, and further, sintering of the powder particles due to contact thereof with oxidizing gas, agglomeration, etc. occur to deteriorate the physical properties of the powder particles. In the case of the horizontal reactor of the present invention, the factor of causing pulverization is nothing but contact of the granules of ferromagnetic metal powder with one another; hence the reactor constitutes a structure by which pulverization hardly occurs so that it is possible to restrain the pulverization which deteriorates the physical properties of finally obtained, stabilized ferromagnetic metal powder, to a minimum; thus the resulting powder has a good quality. Oxygen as an oxidizing gas is removed from the inside of the body of the reactor 1 using nitrogen gas or the like in advance of introducing the granules of ferromagnetic metal powder into the body. Next, the granules of ferromagnetic metal powder are introduced into the body of the reactor 1 through a valve 2 positioned upward lest the granules should be contacted with air. The quantity of the granules introduced is preferred to be 50% or less, preferably 40% or less of the capacity of the body of the reactor 1, in order to obtain a uniform mixing effect. The granules of ferromagnetic metal powder may be either in a state where they are immersed in an organic solvent or in a state where they are not immersed therein, in the body of the reactor 1. In the case where they are immersed therein, the mixed quantity of the granules of ferromagnetic metal powder and the organic solvent is preferred to be 40% or less of the capacity of the reactor. Examples of usable organic solvents are aromatic hydrocarbons such as benzene, toluene, xylene, etc., fluorine compound solvents such as trifluoroethanol, perfluorooctane, etc., and lower alcohols such as methanol, ethanol, etc. The introduced granules of ferromagnetic metal powder are uniformly mixed by rotation of the body of the reactor 1 by means of a driving motor 9. By uniformly mixing the granules of ferromagnetic metal powder, it is possible to form a dense and uniform oxidized film on the surface of the granules through their contact with the oxidizing gas. In order to further improve the uniformity and denseness of the oxidized film, it is preferred to provide a scraping-up plate 13 on the inner wall of the body of the reactor 1 in parallel to the generatrix thereof, as shown in Figs. 2, 3, 6 and 7. The scraping-up plate yields a scraping-up effect and the amount of the mixture increases to thereby increase the uniformity of oxidation. Further, since oxidation reaction at the part where the mixture is scraped up by means of the scraping-up plate can also be carried out, it is possible to shorten the reaction time. When a solvent is used, the reaction in the solvent is heterogeneous and retarded and hence not practical; thus it is necessary to fix a scraping-up plate onto the inner wall, and then advance the reaction while the granules are scraped up from the solvent by means of the scraping-up plate and drop into the solvent. Thus, in this case, it is indispensable to provide the scraping-up plate. The revolution number of the body of the reactor 1, and the width, the number and the angle against the central line of the body of the reactor 1, of the scraping-up plate are optional, but these are preferred to be determined taking it into consideration that the oxidation rate and pulverization due to rotation of ferromagnetic metal powder which somewhat occurs due to drop of the granules from the scraping-up plate, friction of the granules between one another, etc., is to be made as least as possible and also the granules are to be uniformly dispersed within the body of the reactor 1. An oxidizing gas for oxidizing the granules of ferromagnetic metal powder is blown into the body through a port 3 or 4. It is necessary for the blow-in of the oxidizing gas to uniformly blow the gas toward the granules of ferromagnetic metal powder being uniformly mixed by the rotation of the body of the reactor 1 or the rotation and the scraping-up plate to thereby form a uniform and dense oxidized film. If the oxidizing gas is locally blown toward the granules of ferromagnetic metal powder or oxygen in the oxidizing gas is non-uniform, then the resulting oxidized film becomes non-uniform, however uniformly the granules are mixed. If the speed of the oxidizing gas is low, the oxygen concentration in the oxidizing gas in the length direction within the body of the reactor 1 varies depending on the oxygen consumption by the reaction and hence is liable to be non-uniform. On the other hand, if the blowing speed is high, local heat generation occurs to deteriorate the physical properties of the granules. Thus, the speed of the oxidizing gas blown toward the granules of ferromagnetic metal powder is in the range of 0.01 to 2m/sec. As described above, due to the effect of the rotation of the body of the reactor 1 or the rotation and the scraping-up plate 13, the granules of ferromagnetic metal powder are uniformly mixed and the oxidizing gas is blown through the port 3 or 4 to form a uniform oxidized film on the surface of the powder; however, in order to control the reaction temperature optionally and with safety, it is further preferred to provide a jacket 16 on the body of the reactor 1 as shown in Figs. 4, 5, 6 and 7. As to the heat generation due to the oxidization, when iron is oxidized into magnetite (Fe₃O₄), the quantity of heat generated is 1,600 Kcal per Kg of iron. Due to the reaction heat, the granules of ferromagnetic metal powder generate heat and due to overheat at that time, there is a fear that the reaction abruptly proceeds to be thereby liable to deteriorate the physical properties of the granules. Further, even in the case of weak overheat, the oxidized film on the surface of the ferromagnetic metal powder is liable to becomes non-uniform. Thus, in order to prevent such overheat to thereby form a dense oxidized film, it is preferred to control the reaction temperature. On the other hand, when a solvent is used, if the temperature is low, the reaction does not proceed to the contrary so that it is necessary to raise the temperature. Thus, it is preferred to provide a jacket 16 on the body of the reactor 1. The efficiency of contact of the ferromagnetic metal powder with the oxidizing gas varies depending on the structure and the rotation number of the body of the reactor 1, the quantity of the raw material fed, the size of the scraping-up plate 13, the quantity and concentration of the oxidizing gas blown through the port 3 or 4 and use or nonuse of the solvent, and hence an adequate inner temperature of the reactor (the temperature referring to the temperature of the granules in the reactor; and this applying to the subsequent); thus it is possible to afford a desired temperature by by adjusting the jacket temperature. The inner temperature of the of the reactor is in the range of 0 to 90°C. If the temperature is lower than 0°C, a problem is raised that the cooling cost is high and the reaction time is prolonged; hence such low temperature is commercially unadvantageous. On the other hand, if the temperature is higher than 90°C, the oxidization reaction rapidly proceeds so that the oxidized film cannot be dense to thereby deteriorate the physical properties of the ferromagnetic metal powder. When an organic solvent is used, the organic solvent vaporizes into the oxidizing gas and is withdrawn from the body of the reactor to the outside of the system, accompanying the gas. At that time, the solvent may be either withdrawn as it is, or condensed by a condenser, recovered and returned to the body of the reactor 1. Further, it is also possible to adequately withdraw the solvent midway through a valve 2 positioned below. The reaction can be adjusted so as to give a conversion of 10 to 25% and a reaction time of 5 to 30 hours, through uniform mixing of the granules of ferromagnetic metal powder by the rotation of the body of the reactor 1 and if desired, the rotation of the scraping-up plate 13, and uniform oxidation is obtained by blowing the oxidizing gas through the port 3 or 4, and if desired, through the control of the inner temperature by adjusting the temperature of the jacket 16. Thus it is possible to form a uniform and dense oxidized film on the ferromagnetic metal powder. The resulting granules of ferromagnetic metal powder having a uniform and dense oxidized film formed thereon are withdrawn through the valve 2, and as to the withdrawing manner, the body 1 is tilted and rotated and the granules are collected onto the side of the valve 2 and withdrawn through the valve 2 positioned below. As described above, according to the present invention, the granules of ferromagnetic metal powder are not only uniformly mixed due to the effect of the rotation of the body of the reactor or the rotation and the scraping-up plate, but also almost no pulverization having a bad influence upon the physical properties of the ferromagnetic metal powder occurs; hence a uniform and dense oxidized film is formed on the surface of the powder so that it is possible to obtain granules of ferromagnetic metal powder having a good quality and a stabilized surface. The effectiveness of the present invention will be described in more detail by way of Reference examples and Comparative examples. Reference example 1 Into the body of a reactor 1 in a stabilization apparatus having its inside purged with nitrogen gas in advance, as shown in Figs. 6 and 7, which body has a length of 1,200 mm and a diameter of 400 mm and is provided with 4 scraping-up plates 13 each having a width of 75 mm, were fed granules of ferromagnetic metal powder of 1 to 2 mm in diameter and 2 to 5 mm long (10 Kg on the basis of dry weight) through a valve 2, which granules were immersed in toluene (35 Kg) and which ferromagnetic metal powder contained 10% by weight of Ni, 1.5% by weight of Aℓ, 2.5% by weight of Si, each weight based on the weight of iron and the remainder being iron. A motor 11 was driven and the body of the reactor 1 was rotated at 2 rpm. Warm water was passed through a jacket 16 to raise the temperature of the jacket up to 40°C. When 40°C was attained, nitrogen gas containing 5% by volume of oxygen was blown into the body through a gas inlet 3 at a rate of 30 Nm³/Hr. In such a state, reaction was carried out for 15 hours. During the period, toluene distilled out accompanying the oxidizing gas was condensed by a condenser fixed onto the outer part and returned into the inside of the apparatus. After the reaction for 15 hours, while the reaction conditions were kept, the toluene distilled out accompanying the oxidizing gas was withdrawn to the outside of the reaction system and drying of the granules of ferromagnetic metal powder was started. Ten hours were required until toluene in the apparatus was entirely freed. At this point, the reaction was stopped and the resulting treated granules of ferromagnetic metal powder were withdrawn through a valve 2 positioned downward. The physical properties and conversions of the ferromagnetic metal powder forming the granules prior to the treatment and that posterior to the treatment are shown in Table 1. In addition, the conversion was sought regarding the iron as having been converted into magnetite and also regarding this magnetite as having no magnetic properties (this applies to the subsequent conversion). Reference example 2 Into the same apparatus as used in Reference example 1 was fed the same granules of ferromagnetic metal powder as used in Reference example 1 in the same quantity and immersed in toluene (35 Kg). In the same manner as in Reference example 1, the jacket temperature was made 40°C, nitrogen gas containing 5% by volume of oxygen was blown into the body at a rate of 30 Nm³/Hr and the body of the reactor was rotated at 2 rpm. Under such conditions, reaction was carried out for 15 hours. During the period, toluene distilled out accompanying the oxidizing gas was recovered and returned into the apparatus. After the reaction for 15 hours, the rotation of the body of the reactor was stopped, and toluene inside the apparatus was withdrawn through a valve 2 positioned downward and provided with a wire gauze. However, toluene attached onto the inner wall of the body of the reactor and onto the granules of ferromagnetic metal powder remained inside the body of the reactor. Thereafter, the rotation of the body of the reactor was again carried out at 2 rpm. The same reaction conditions such as the jacket temperature, the quantity of the gas blown, etc. as above were employed. The distilled-out toluene was withdrawn to the outside of the system and the granules of ferromagnetic metal powder inside the apparatus were dried over 8 hours. After the drying, the granules of ferromagnetic metal powder were withdrawn through the valve 2. The physical properties and conversions of the ferromagnetic metal powder forming the granules prior to the treatment and that posterior to the treatment are shown in Table 1. Reference example 3 The same apparatus and granules of ferromagnetic metal powder as in Reference example 1 were used and reaction was carried out under the same conditions as in Reference example 1 except that distilled-out toluene was not returned and all withdrawn to the outside of the system and when the granules of ferromagnetic metal powder were dried (10 hour since the start of the reaction), the granules were withdrawn. The physical properties and conversions of the ferromagnetic metal powder forming the granules prior to the treatment and that posterior to the treatment are shown in Table 1. Reference example 4 The same apparatus and granules of ferromagnetic metal powder as in Reference example 1 were used, and reaction was carried out under the same conditions as in Reference example 1 except that the jacket temperature was made 60°C. After the reaction for 15 hours, the granules of ferromagnetic metal powder were dried over 7 hours in the same manner as in Reference example 1 except that the jacket temperature was made 60°C, and withdrawn. The physical properties and conversions of the ferromagnetic metal powder forming the granules prior to the treatment and that posterior to the treatment are shown in Table 1. Reference example 5 Using the same apparatus and granules of ferromagnetic metal powder and under the same conditions as in Reference example 4, reaction was carried out for 15 hours. After 15 hours, toluene was withdrawn in the same manner as in Reference example 2 and drying was then carried out under the initial reaction conditions. After the granules of ferromagnetic metal powder were dried for 5 hours, they were withdrawn. The physical properties, and conversions of the ferromagnetic metal powder forming the granules prior to the treatment and that posterior to the treatment are shown in Table 1. Reference example 6 Reaction was carried out using the same apparatus and under the same conditions as in Reference example 4 except that distilled-out toluene was not returned and withdrawn to the outside of the system. After the granules of ferromagnetic metal powder was dried for 7 hours, they were withdrawn through the valve 2. The physical properties and conversions of the ferromagnetic metal powder prior to the treatment and that posterior to the treatment are shown in Table 1. Reference example 7 Into the same apparatus as in Reference example 1 were fed the same granules of ferromagnetic metal powder in the same quantity together with toluene in the same quantity each as in Reference example 1. Next, toluene was withdrawn through the valve 2 positioned downward and having a wire gauze attached thereto, in advance of the reaction. However, toluene attached onto the inner wall of the body of the reactor and granules of ferromagnetic metal powder remained inside the body of the reactor. The body of the reactor was rotated at 2 rpm. N₂ gas containing 1% by volume of oxygen was blown into the body through a gas inlet 3. Reaction was continued until the granules of ferromagnetic metal powder was dried. Seventeen hours were required. The granules were then withdrawn. The physical properties and conversions of the ferromagnetic metal powder prior to the treatment and that posterior to the treatment are shown in Table 1. Reference example 8 Reaction was carried out using the same apparatus and granules and under the same conditions each as in Reference example 7 except that the jacket temperature was made 20°C. However, the reaction was carried out until the granules were dried. Fifteen hours were required. The physical properties and conversions of the ferromagnetic metal powder forming the granules prior to the treatment and that posterior to the treatment are shown in Table 1. Reference example 9 The same granules of ferromagnetic metal powder (10 Kg) as in Reference example 1 was fed as they were, without being immersed in toluene, into the same apparatus as in Reference example 1, purged with nitrogen gas, through the valve 2. The body of the reactor was rotated by means of a driving motor 11 at 2 rpm. Water was passed through the jacket 16 to make the jacket temperature 20°C. Nitrogen gas containing 0.5% of oxygen was blown into the body through the inlet 3 at a rate of 30 Nm³/Hr and reaction was carried out for 20 hours. The body of the reactor was then tilted and the granules of the surface-treated ferromagnetic metal powder was withdrawn through the valve 2. The physical properties and conversions of the ferromagnetic metal powder prior to the treatment and that posterior to the treatment are shown in Table 1. Any of the treated granules of ferromagnetic metal powder were unchanged in the state from those prior to the treatment and free-flowing and there was almost no pulverization. Comparative example 1 The same granules of ferromagnetic metal powder (10 Kg) as in Reference example 1 were ground by means of a mill in toluene into particles of about 0.05 mm in diameter, and the particles were fed into a vertical, cylindrical reactor of 400 mm in diameter and 1,000 mm high equipped with a jacket and having a stirrer. The height of the particle layer was 160 mm. Toluene was additionally added up to a height of 800 mm in the reactor. While the stirrer was rotated at 180 rpm and the particles were dispersed, the jacket temperature was raised up to 60°C and N₂ gas containing 5% by volume of oxygen was blown into the reactor at a rate of 30 Nm³/Hr to carry out oxidation. At that time, toluene accompanying the gas was condensed by a condenser and returned to the reactor. After the reaction for 20 hours, the gas feed was stopped and the jacket temperature was lowered down to 20°C. The stirrer was also stopped. Particles after the surface oxidation-treatment were filtered off and toluene was vaporized at room temperature in N₂ current to dry the particles, followed by measuring the physical properties and conversion of the particles. The results are shown in Table 1. As compared with Reference example 1, it is evident that notable deterioration in the physical properties occurred. Comparative example 2 The same granules of ferromagnetic metal powder (10 Kg) as in Reference example 1 were fed as they were, without being immersed in toluene, into a fixed bed reactor of 400 mm in diameter and 800 mm high equipped with a jacket and designed so as to blow an oxidizing gas from its lower part thereinto. The reactor was purged with nitrogen gas in advance. The height of the layer of the granules was 20 cm. The jacket temperature was made 20°C and nitrogen gas containing 0.5% by volume of oxygen was blown into the reactor from its lower part at a rate of 10 Nm³/Hr to carry out reaction for 30 hours. After the reaction, the resulting granules of the surface-treated ferromagnetic metal powder were withdrawn from the reactor into the air. As a result, the granules immediately became red hot.

Claims: A process for treating ferromagnetic metal powders which comprises the steps of: molding said ferromagnetic metal powders into granules having an average diameter of 0.25 to 10 mm; feeding said granules into apparatus comrpising having a horizontal, cylindrical, rotatable reactor body (1) having a feed port (2) for introducing ferromagnetic metal powder into the reactor body, a withdrawal port for removing ferromagnetic metal powder from the reactor body, which port may be the same as the feed port (2), an inlet conduit (3) for introducing gas into the reactor body, and an outlet conduit (4) for removing oxidizing gas from the reactor body, the reactor not being provided with a stirrer; oxidizing the surface of said granules by passing an oxygen-containing gas through the reactor at a temperature of 0 to 90°C and at a speed of 0.01 to 2 m/sec. A process according to claim 1, wherein said ferromagnetic metal powder comprises, besides iron, at least one of Ni, Si, Aℓ, Mn, Cu, Cr, Ti, Mg, Co, Zn, Ba, Sn, and compounds thereof. A process for treating ferromagnetic metal powders according to claim 1 or claim 2 wherein the oxygen-containing gas is passed in such a quantity that the conversion of the surface of the granules by oxidizing reaches to 10 to 25% thereof. A process for treating ferromagnetic metal powders according to any one of the preceding claims in which the reactor is provided with scraping-up plates on the inner wall thereof.

Inventors: NAKAGAWA, ETSUO, NIWANO, MASARU, YAMAMOTO, TETSUSHI
Applicants: CHISSO CORPORATION
Application year: 1988
Main classification: H01F1
IPC codes: C23C8, B22F1, H01F1, G11B5