Process for producing an alkylenamine by using a mixing oxide catalyst.

Abstract: A mixed oxide catalyst comprising niobium oxide and titania, alumina, silica, zirconia and/or an oxide of an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table. A process for producing an alkylenamine, which comprise reacting ammonia and/or an alkylenamine with an alkanolamine in the presence of such a mixed oxide.

Description: The present invention relates to a process for producing alkylenamines using a mixed oxide catalyst. Heretofore, a number of industrial processes are known wherein sulfuric acid, phosphoric acid, aluminum chloride, etc. are used as acid catalysts. In general, when such a catalyst is used in a system where water is present, for example, in a homogeneous system with such a catalyst dissolved in water, it is difficult to separate the catalyst from the reaction product, and there will be a problem such as corrosion of the apparatus. Whereas in the case of a heterogeneous system, there is a problem in the useful life of the catalyst, such as a decrease in the activities due to flowing away of the catalyst, and there still remains a problem of corrosion of the apparatus just like in the case of the homogeneous system. Under the circumstances, various studies have been made for solid acids as acid catalysts, and ion exchange resins have been proposed as solid acid catalysts which are hardly decomposed in a system where water is present. However, such ion exchange resins are expensive, and they are inferior in heat resistance. As a solid acid catalyst useful in the presence of water, JP-A-44039/1975 discloses a water-containing niobium oxide. However, this catalyst is also inadequate in heat resistance from the industrial point of view, since the activities deteriorate substantially at a temperature of 500°C or higher. On the other hand, as a process for producing alkylenamines, particularly ethylenamines which are particularly important from the industrial point of view, a process is known wherein ethylene dichloride is reacted with ammonia. By this process, the production of piperazine and piperazine ring-containing cyclic ethylenamines is small. Namely, it is possible to obtain ethylenamines having high non-cyclic rates and industrially preferred quality. This process is practically widely used. However, it has a problem that a large amount of sodium chloride is formed as a by-product, and its separation and treatment are costly. Another process wherein a monoethanolamine is used as starting material, and ammonia is reacted thereto in the presence of hydrogen and a hydrogenation catalyst to obtain an ethylamine, is also widely practically employed. However, piperazine ring-containing cyclic ethylenamines which are undesirable from the viewpoint of quality, are produced in a substantial amount although ethylenediamines may be produced with high efficiency. Therefore, it is difficult to produce polyethylenepolyamines having high molecular weights. In addition to these processes, a process has been proposed wherein monoethanolamine is used as starting material, and ammonia or/and ethylenamine are reacted thereto by using a phosphorus-containing substance as catalyst to produce an ethylenamine. For example, JP-A-147600/1976 discloses a process wherein phosphoric acid or phosphorous acid is used as catalyst. However, these catalysts are soluble in the reaction solution containing water. Therefore, a special step for the separation and recovery from the reaction solution is required. Under the circumstances, processes for the production of ethylenamines have been proposed wherein various salts of phosphoric acid and supported phosphoric acid insoluble in the reaction solution containing water are used as catalysts. US-A-4,448,997 discloses a process for producing ethylenamines wherein aluminum phosphate is used as catalyst, and JP-A-41641/1985 discloses such a process wherein a phosphate of a metal of Group IIIb such as lanthanum phosphate is used as catalyst. Further, JP-A-150538/1984 discloses a process wherein phosphoric acid supported on e.g. titanium dioxide is used as catalyst. However, these phosphates and supported phosphoric acid are substantially poorer in the catalytic activities than free phosphoric acid. Further, by the use of these phosphoric acid type catalysts, it is not possible to reduce piperazine ring-containing cyclic amines undesirable from the viewpoint of quality to a level sufficiently low for the industrial purpose. As a phosphoric acid catalyst having high activities, there is a phosphorus-containing ion exchanger resin. However, this catalyst is poor in heat resistance and thus has a problem in the catalytically useful life. As a non-phosphorus catalyst, silica-alumina is disclosed in JP-A-38329/1980, but the catalytic activities of this catalyst are very low. As described in the foregoing, some solid acid catalysts have been disclosed as catalysts which may be used in a system containing water. However, they have a problem that they are inferior in heat resistance, and they are still inadequate from the industrial point of view. Therefore, it is desired to develop a solid acid catalyst useful in a system containing water, which is excellent in heat resistance. As described above, many processes have been disclosed for the production of alkylenamines. However, such processes are still inadequate from the industrial point of view. Thus, the technical problem underlying the present invention is to develop a process for producing high quality alkylenamines having high non-cyclic rates by using a solid catalyst having high catalytic activities and high heat resistance and being hardly soluble in the reaction solution, for the production of alkylenamines using alkanolamines as starting material. This technical problem could be solved by a process for producing alkylenamines having alkylene chains increased over ammonia and/or alkylenamines as starting material by the reaction of the ammonia and/or alkylenamines with alkanolamines using a mixed oxide catalyst comprising niobium oxide and titania, niobium oxide and alumina, niobium oxide and silica, niobium oxide and zirconia, or niobium oxide and an oxide of an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except elements Fe, Cr and W which has high activities as catalyst and is a solid hardly soluble in a reaction solution containing water, and it is also excellent in heat resistance. The present invention this provides a process for producing alkylenamines, which comprises reacting ammonia and/or an alkylenamine with an alkanolamine in the presence of such a mixed oxide catalyst to obtain alkylenamines having an increased number of alkylene moieties over the ammonia and/or the alkylenamine used as starting material, wherein said mixed oxide catalyst comprises niobium oxide and titania, alumina, silica or zirconia and/or an oxide of an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except oxides of the elements Fe, Cr and W. Now, the present invention will be described in further detail. The catalyst used in the present invention is a mixed oxide comprising niobium oxide and titania, niobium oxide and alumina, niobium oxide and silica, niobium oxide and zirconia, or niobium oxide and an oxide of an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except oxides of the elements Fe, Cr and W. The mixed oxide catalyst is a substance obtained by converting a compound containing niobium and a compound containing titanium, aluminium, silicon, zirconium or an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except Fe, Cr and W simultaneously to the oxide or hydroxide of niobium and to the oxide or hydroxide of titanium, aluminium, silicon, zirconium or an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except oxides of Fe, Cr and W. There is no particular restriction as to the oxidized state of niobium, and it may be pentavalent, tetravalent, trivalent, bivalent or monovalent. However, tetravalent niobium is preferred. Titanium, silicon and zirconium are preferably tetravalent, and aluminum is preferably trivalent. The mixed oxide to be used in the present invention may be used alone by itself, or may be combined with other substances in the form of a mixture or in the form of a mixed oxide with other oxides. The mixed oxide catalyst can be obtained by converting a compound containing niobium and a compound containing titanium, aluminium, silicon, zirconium or an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except Fe, Cr and W simultaneously to the oxide or hydroxide of niobium and to the oxide or hydroxide of titanium, aluminum, silicon, zirconium or an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except the oxides of Fe, Cr and W. Various methods are available for the conversion, including: 1) A method wherein the pH of a solution of a niobium-containing compound and a compound containing titanium, aluminum, silicon, zirconium or an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except elements Fe, Cr and W is changed to convert them to insoluble hydroxides, which are then dehydrated to obtain a mixed oxide; 2) A method wherein an organic substance such as an alkoxide of niobium and an organic substance such as an alkoxide of titanium, aluminum, silicon, zirconium or an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except elements Fe, Cr and W, are hydrolyzed; and 3) A method wherein an organic substance such as an alkoxide of niobium and an organic substance such as an alkoxide of titanium, aluminum, silicon, zirconium or an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except elements Fe, Cr and W are thermally decomposed. Any one of such methods may be employed. The ratio of the respective components of the mixed oxide to be used in the present invention is as follows. The molar ratio of niobium to titanium (Nb/Ti) is from 0.01 to 100, preferably from 0.1 to 100, more preferably from 0.1 to 10. The molar ratio of niobium to aluminum (Nb/Al), niobium to silicon (Nb/Si), or niobium to zirconium (Nb/Zr) is from 0.001 to 100, preferably from 0.01 to 100, more preferably from 0.01 to 10. The molar ratio of the niobium to the element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table substantially varies depending upon the element and may not generally be defined. For example, in the case of Ca of Group IIA in the Periodic Table, the molar ratio of Nb/Ca is from 10 to 1,000. In the case of Bi of Group VA, the molar ratio of Nb/Bi is from 0.1 to 1,000. In the case of Te of Group VIA, the molar ratio of Nb/Te is from 0.1 to 1,000. In the case of Cu of Group IB, the molar ratio of Nb/Cu is from 0.1 to 1,000. In the case of Zn of Group IIB, the molar ratio of Nb/Zn is from 0.1 to 1,000. In the case of La of Group IIIB, the molar ratio of Nb/La is from 0.01 to 100. In the case of Ta of Group VB, the molar ratio of Nb/Ta is from 0.001 to 1,000. In the case of Mn of Group VIIB, the molar ratio of Nb/Mn is from 0.1 to 1,000. If Nb is less than these ranges, the quality of the resulting alkylenamine tends to be inferior, and if it exceeds the above ranges, the heat resistance of the catalyst tends to deteriorate. In the present invention, there is no particular restriction as to the shape of the catalyst. Depending upon the reaction system, it may be used as powder, or may be used in a molded form. For example, in a suspension bed system, it is used in a powder or granular form. In a fixed bed system, it is used in a molded form of pellets or beads. The molding method of the catalyst includes extrusion molding, tablet molding or granule molding. For the molding, silica, alumina, alumina-silica, clay or the like may be added as a binder. Further, in order to increase the surface area of the catalyst, the mixed oxide may be supported on a carrier such as silica, alumina, titania, zirconia or porous vycor glass. The catalyst may be used after calcination or without sintering. When calcination is applied, there is no particular restriction as to the calcination temperature. However, the calcination temperature is preferably not higher than 700°C. If calcination is conducted at a temperature exceeding 700°C, the surface area tends to be small, whereby the catalytic activities tends to be reduced. The amount of the mixed oxide catalyst used in the present invention may be at any level so long as it is sufficient to have the reaction proceeded at an industrially useful reaction rate. Ammonia or the alkylenamine to be used in the process of the present invention is a compound represented by the general formula I: wherein a is a number of from 2 to 6, r is a number of from 0 to 6, R₁ is hydrogen or an alkyl group having from 1 to 4 carbon atoms, R₁' is a group represented by the general formula (1): -[(CH₂) b (NH) d ] s -H (1) wherein b is a number of from 2 to 6, d is 0 or 1, and s is a number of from 0 to 4, or a compound represented by the general formula II: wherein e is a number of from 2 to 6, f is a number of from 2 to 6, and each of R₂ and R₂' is a group represented by the general formula (2): -[(CH₂) g NH] t -H (2) wherein g is a number of from 2 to 6, and t is a number of 0 to 5. Either the compound of the formula I or the compound of the formula II may be employed. Preferably, however, ammonia or an alkylenamine of the formula I is employed. When an alkylenamine of the general formula I is used, high quality alkylenamines having a high non-cyclic rate is obtainable. Ammonia and the alkylenamine of the general formula I include ammonia, ethylenamines such as ethylenediamine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, pentaethylenehexamine and hexaethyleneheptamine, propyleneamines such as propylenediamine and dipropylenetriamine, butyleneamines such as butylenediamine and dibutylenetriamine, alkylenamines such as hexamethylenediamine and alkylated products thereof such as N-methylethylenediamine and N-ethylethylenediamine. Among them ethylenamines such as ethylenediamine and diethylenetriamine are preferred as starting material to be used in the process of the present invention. Ammonia and alkylenamines to be used in the process of the present invention may be used alone or in combination as a mixture of two or more different kinds. The alkanolamine to be used in the process of the present invention is a compound represented by the general formula III: wherein h is a number of from 2 to 6, u is a number of from 0 to 5, R₃ is hydrogen or an alkyl group having from 1 to 4 carbon atoms, and R₃' is a group represented by the general formula (3): -[(CH₂) i -(NH) j ] v -H (3) wherein i is a number of from 1 to 6, j is 0 or 1, and v is a number of from 0 to 4, or a compound represented by the general formula IV: wherein k is a number of from 2 to 6, l is a number of from 2 to 6, m is a number of from 2 to 6, and R₄ is a group represented by the general formula (4): -[(CH₂) n -NH] w -H (4) wherein n is a number of from 2 to 6, and w is a number of from 0 to 5. Either a compound of the general formula III or a compound of the general formula IV may be employed. However, an alkanolamine of the general formula III is preferably employed. When a alkanolamine of the general formula III is used, high quality alkylenamines having a high non-cyclic rate are obtainable. The alkanolamines of the general formula III include alkanolamines such as monoethanolamine, N-(2-aminoethyl)ethanolamine, monopropanolamine and N-(3-aminopropyl)propanolamine. As the starting material to be used in the process of the present invention, ethanolamines such as monoethanolamine and N-(2-aminoethyl)ethanolamine are preferred. The alkanolamines to be used in the process of the present invention may be used alone or in combination as a mixture of two or more different kinds. The combination of starting materials supplied for the reaction in the process of the present invention includes the following three types: 1) Ammonia and an alkanolamine; 2) An alkylenamine and an alkanolamine; and 3) Ammonia, an alkylenamine and an alkanolamine. The reaction may be conducted for any one of such combinations. Preferred combinations of starting materials include: 1) Ammonia and an alkanolamine of the general formula III; 2) An alkylenamine of the general formula I other than ammonia and an alkanolamine of the general formula III; and 3) Ammonia and an alkylenamine of the general formula I and an alkanolamine of the general formula III. More preferred combinations of starting materials include: 1) Ammonia and an ethanolamine; 2) An ethylenamine and an ethanolamine; and 3) Ammonia, an ethylenamine and an ethanolamine. Preferred molar ratios of the starting materials to be supplied in the process of the present invention are as follows: 1) In the case where ammonia and an alkanolamine are used as starting materials, the molar ratio of ammonia/the alkanolamine is from 2 to 30; 2) In a case where an alkylenamine and an alkanolamine are used as starting materials, the molar ratio of the alkylenamine/the alkanolamine is from 0.5 to 10; and 3) In a case where ammonia, an alkylenamine and an alkanolamine are used as starting materials, the molar ratio of (ammonia + the alkylenamine)/the alkanolamine is from 0.5 to 30. In each case, the quality of the resulting alkylenamine varies depending upon the molar ratio of the starting materials. If the molar ratio is smaller than the above-mentioned ranges, piperazine ring-containing amines will be produced in a substantial amount, whereby alkylenamines having undesirable quality tend to form. If the molar ratio is larger than the above range, the reaction rate tends to decrease, and the pressure is required to be extremely high, such being not practical. In the process of the present invention, the resulting alkylenamines differ depending upon the types of the starting materials. When an alkanolamine is reacted with ammonia and/or an alkylenamine, the resulting alkylenamine has alkylene chains increased over the ammonia or the alkylenamine as starting material. Namely, when the alkanolamine of the general formula III is reacted with the ammonia and/or the alkylenamine of the formula I, the resulting alkylenamine will be a compound represented by the general formula V: wherein o is a number of from 2 to 6, x is a number of 1 to 7, R₅ is hydrogen or an alkyl group having from 1 to 4 carbon atoms, and R₅' is a group of the general formula (5): -[(CH₂) p (NH) q ] y -H (5) wherein p is a number of from 1 to 6, q is 0 or 1, and y is a number of 0 to 4, wherein x and/or y in the resulting alkylenamine is a number larger at least by one than r and/or s of the ammonia or the alkylenamine as starting material. Thus, an alkylenamine having an increased number of alkylene chains over the starting material is obtainable. For example, when ammonia is reacted with monoethanolamine, ethylenediamine and non-cyclic polyethylenepolyamines such as diethylenetriamine, triethylenetetramine, tetraethylenepentamine and pentaethylenehexamine will be formed. When ethylenediamine is reacted with monoethanolamine, the above-mentioned non-cyclic polyethylenepolyamines will be formed. When ammonia and ethylenediamine are reacted with monoethanolamine, ethylenediamine and the above-mentioned non-cyclic polyethylenepolyamines will be formed. In the process of the present invention, the reaction is conducted usually at a temperature within a range of from 200 to 400°C, preferably from 240 to 350°C. If the temperature is less than 200°C, the reaction rate tends to be substantially low, and if it exceeds 400°C, the resulting alkylenamine tends to undergo decomposition, such being not practical. In the process of the present invention, the reaction may be conducted in the gas phase or in the liquid phase. However, it is preferred to conduct it in the liquid phase in order to produce a high quality alkylenamine. In the process of the present invention, the reaction may be conducted by a suspended batch, semi-batch or continuous system, or by a fixed bed system. However, the fixed bed system is industrially advantageous from the viewpoint of the operation, apparatus and economy. In the process of the present invention, the pressure for the reaction varies substantially depending upon whether the reaction is a gas phase reaction or a liquid phase reaction, or whether or not ammonia is used. Therefore, it is difficult to define the pressure range. However, for example, in the case of a liquid phase reaction using no ammonia, the pressure is within a range of from about 1.96 (1) to about 295 bar (300 kg/cm²G). In the process of the present invention, the catalyst will usually be separated and recovered from the reaction solution, and then the starting material is separated and recovered by distillation. The separated and recovered starting material is recycled to the reaction zone, as the case requires. A part of the reaction product may be recycled to the reaction zone in order to change the composition of the reaction product. The separation of the starting material and the product is usually conducted by distillation. Such distillation may be conducted by a continuous system or by a batch system. The reaction product may be treated with active carbon or sodium borohydride in order to improve the purity or color tone of the reaction product. The color tone, odor, etc. of the reaction product may be improved by conducting the reaction in the presence of hydrogen. The formed water may be removed from the reaction zone in order to reduce the formation of amines undesirable from the viewpoint of quality such as hydroxyl group-containing amines or to improve the reaction rate. Otherwise, the reaction may be conducted with addition of water in order to prolong the catalytically useful life or to make it easy to handle ammonia or the alkylenamine. The mixed oxide catalyst is stable in a system containing water and excellent in heat resistance, and thus it is industrially very useful. Further, the present invention provides a process for producing a high quality alkylenamine in good yield by using a mixed oxide catalyst, which is highly active, resistant to corrosion by the reaction solution and excellent in the heat resistance, and thus it is industrially extremely significant. Now, the present invention will be described in further detail with reference to Examples. However, it should be understood that the present invention is by no means restricted to such specific Examples. Alkylenamines as reaction products and alkylenamines and alkanolamines as starting materials will be represented by the following abbreviations: EDA: Ethylenediamine MEA: Monoethanolamine PIP: Piperazine AEP: N-(2-aminoethyl)piperazine DETA: Diethylenetriamine AEEA: N-(2-aminoethyl)ethanolamine TETA: Triethylenetetramine (linear, branched or cyclic isomer) TEPA: Tetraethylenepentamine (linear, branched or cyclic isomer) EXAMPLE 1: Preparation of catalysts CATALYST 1: Into a 500 ml flask, 15.3 g (48.1 mmol) of niobium pentaethoxide and 13.6 g (48.1 mmol) of titanium tetraisopropoxide were charged under a nitrogen stream and dissolved in 40 ml of 1-butanol. This solution was refluxed, and 300 ml of water was dropwise added thereto under stirring. Formed precipitates were collected by filtration and washed with water. They were calcined at 400°C for 2 hours under a dry air stream to obtain niobium-titania mixed oxide. As a result of the elemental analysis, the molar ratio of Nb/Ti was 1. The BET specific surface area thereof was 309 m²/g. The mixed oxide was not crystallized, and no X-ray diffraction pattern was observed in the X-ray diffraction analysis. To the niobium-titanium mixed oxide catalyst, 100 ml of distilled water was added, and the mixture was refluxed for 2 hours. Then, the catalyst was collected by filtration and calcined at 400°C under a dry air stream, whereby the mixed oxide was recovered 100%. CATALYST 2: 10.0 g (37 mmol) of niobium pentachloride and 7.2 g (38 mmol) of titanium chloride were dissolved in 50 ml of methanol. To this solution, 200 ml of 7% aqueous ammonia was added. Formed precipitates were collected by filtration, washed with water and then calcined at 400°C for 2 hours under a dry air stream. The BET specific surface area was 45 m²/g. As a result of the elemental analysis, the molar ratio of Nb/Ti was 1. CATALYST 3: 25.2 g (79 mmol) of niobium pentaethoxide and 2.5 g (8.8 mmol) of titanium tetraisopropoxide were dissolved in 20 ml of 1-butanol, and the solution was refluxed. To this solution, 350 ml of water was dropwise added. Formed precipitates were collected by filtration, washed with water and then calcined at 400°C for 2 hours under a dry air stream. The BET specific surface area was 295 m²/g. As a result of the elemental analysis, the molar ratio of Nb/Ti was 9. CATALYST 4: 10.5 g (33 mmol) of niobium pentaethoxide and 84.4 g (297 mmol) of titanium tetraisopropoxide were dissolved in 20 ml of 1-butanol, and the solution was refluxed. To this solution, 350 ml of water was dropwise added. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream. As a result of the elemental analysis, the molar ratio of Ti/Nb was 9. The BET surface area was 179 m²/g. CATALYST 5: Catalyst 1 was calcined at 600°C for 2 hours under a dry air stream. The BET specific surface area was 110 m²/g. From the X-ray diffration, this catalyst was found to be not crystallized. CATALYST 6: Into a 500 ml flask, 13.2 g (41.5 mmol) of niobium pentaethoxide and 8.5 g (41.8 mmol) of aluminum isopropoxide were introduced under a nitrogen stream and dissolved in 1-butanol under reflux. Then, 300 ml of water was dropwise added thereto over a period of 20 minutes, and the mixture was heated for one hour and 40 minutes. The mixture was left to stand still overnight. Then, formed precipitates were collected by filtration and washed with water. They were calcined at 400°C for 2 hours to obtain a catalyst. As a result of the elemental analysis, the molar ratio of Nb/Al was 1. The BET specific surface area thereof was 296 m²/g. This mixed oxide was not crystallized, and no X-ray diffraction pattern was observed by the X-ray diffraction analysis. To this oxidized niobium-alumina mixed oxide catalyst, 100 ml of distilled water was added, and the mixture was refluxed for 2 hours. Then, the catalyst was collected by filtration and calcined at 400°C under a dry air stream, whereby the mixed oxide was recovered 100%. CATALYST 7: 10.0 (37 mmol) of niobium pentachloride an 4.9 g (37 mmol) of aluminum chloride were dissolved in 50 ml of methanol. To this solution, 7% aqueous ammonia was added until the solution became pH 7. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 7. As a result of the elemental analysis, the molar ratio of Nb/Al was 1. CATALYST 8: Under a nitrogen stream, 20.0 g (62.9 mmol) of niobium pentaethoxide and 1.4 g (6.85 mmol) of aluminum isopropoxide were dissolved in 1-butanol under reflux. To this mixture, 300 ml of water was dropwise added over a period of 20 minutes, and the mixture was heated for one hour and 40 minutes. The mixture was left to stand overnight. Then, formed precipitates were collected by filtration and washed with water. Then, they were calcined at 400°C for 2 hours to obtain a catalyst, which is designated as Catalyst 8. As a result of the elemental analysis, the molar ratio of Nb/Al was 9. CATALYST 9: Under a nitrogen stream, 5.0 g (15.7 mmol) of niobium pentaethoxide and 28.9 g (141 mmol) of aluminum isopropoxide were dissolved in 1-butanol under reflux. To this solution, 300 ml of water was dropwise added. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 9. As a result of the elemental analysis, the molar ratio of Nb/Al was 0.11. CATALYST 10: Under a dry air stream, Catalyst 6 was calcined at 600°C for 2 hours to obtain a catalyst which is designated as Catalyst 10. The BET specific surface area was 195 m²/g. CATALYST 11: Into a 500 ml flask, 13.0 g (40.9 mmol) of niobium pentaethoxide and 8.51 g (40.9 mmol) of tetraethoxysilane were introduced under a nitrogen stream and dissolved in 40 ml of 1-butanol. This solution was refluxed, and 200 ml of water was dropwise added thereto over a period of 40 minutes. The heating was continued for further 35 minutes, and then the mixture was cooled and left to stand overnight. The supernatant was removed, and formed precipitates were collected by filtration and washed with water. The precipitates were calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 11. As a result of the elemental analysis, the molar ratio of Nb/Si was 1. The BET specific surface area was 274 m²/g. This mixed oxide was not crystallized, and no X-ray diffraction pattern was observed by the X-ray diffraction analysis. To the oxidized niobium-silica mixed oxide catalyst, 100 ml of distilled water was added, and the mixture was refluxed for 2 hours. Then, the catalyst was collected by filtration and calcined at 400°C under a dry air stream, whereby the mixed oxide was recovered 100%. CATALYST 12: 5.2 g (16.3 mmol) of niobium pentaethoxide and 45.3 g (297.4 mmol) of tetramethoxysilane were dissolved in 50 ml of methanol, and the solution was refluxed. To this solution, 50 ml of water was dropwise added in 10 minutes, and then the mixture was refluxed for 30 minutes. The mixture was left to stand overnight, and then the solvent was distilled off. The residue was dried at 130°C for 16 hours to obtain a catalyst, which is designated as Catalyst 12. As a result of the elemental analysis, the molar ratio of Nb/Si was 0.055. CATALYST 13: 15.9 g (49.9 mmol) of niobium pentaethoxide and 1.15 g (5.5 mmol) of tetraethoxysilane were dissolved in 1-butanol, and the solution was refluxed. To this solution, 500 ml of water was dropwise added. After the dropwise addition, the refluxing was continued for 1.5 hours. Then, formed precipitates were collected by filtration, washed with water and calcined at 300°C for 2 hours to obtain a catalyst which is designated as Catalyst 13. As a result of the elemental analysis, the molar ratio of Nb/Si was 9.1. CATALYST 14: 10.0 g (37 mmol) of niobium pentachloride and 6.3 g (37 mmol) of silicon tetrachloride were dissolved in 50 ml of methanol. To this solution, 200 ml of 7% aqueous ammonia was added. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 14. The BET specific surface area was 45 m²/g. As a result of the elemental analysis, the molar ratio of Nb/Si was 1. CATALYST 15: Catalyst 11 was calcined at 600°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 15. The BET specific surface area was 113 m²/g. CATALYST 16: Into a 500 ml flask, 13.5 g (42.4 mmol) of niobium pentaethoxide and 16.5 g (43.0 mmol) of zirconium tetrabutoxide were charged under a nitrogen stream and dissolved in 1-butanol under reflux. To the solution, 300 ml of water was dropwise added over a period of one hour and 20 minutes. The mixture was heated for further one hour and 20 minutes. The mixture was left to stand still overnight. Then, formed precipitates were collected by filtration and washed with water. They were calcined at 400°C for 2 hours to obtain a catalyst, which is designated as Catalyst 16. As a result of the elemental analysis, the molar ratio of Nb/Zr was 1. The BET specific surface area was 241 m²/g. This mixed oxide was not crystallized, and no X-ray diffraction pattern was observed by the X-ray diffraction analysis. To the oxidized niobium-zirconia mixed oxide catalyst, 100 ml of distilled water was added, and the mixture was refluxed for 2 hours. Then, the catalyst was collected by filtration and calcined at 400°C under a dry air stream, whereby the mixed oxide was recovered 100%. CATALYST 17: 10.0 g (37 mmol) of niobium pentachloride and 8.6 g (37 mmol) of zirconium chloride were dissolved in 50 ml of methanol. To this solution, 7% aqueous ammonia was added until the solution became pH 7. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as catalyst 17. As a result of the elemental analysis, the molar ratio of Nb/Zr was 1. CATALYST 18: Under a nitrogen stream, 20.0 g (62.9 mmol) of niobium pentaethoxide and 2.7 g (7.04 mmol) of zirconium tetrabutoxide were added to 1-butanol and dissolved under reflux. To this solution, 300 ml of water was dropwise added over a period of 20 minutes, and the mixture was heated for further one hour and 40 minutes. The mixture was left to stand still overnight, and formed precipitates were collected by filtration and washed with water. They were calcined at 400°C for 2 hours to obtain a catalyst, which is designated as Catalyst 18. As a result of the elemental analysis, the molar ratio of Nb/Zr was 9. CATALYST 19: Under a nitrogen stream, 5.0 g (15.7 mmol) of niobium pentaethoxide and 54.2 g (141 mmol) of zirconium tetrabutoxide were added to 1-butanol and dissolved under reflux. To this solution, 300 ml of water was dropwise added. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 19. As a result of the elemental analysis, the molar ratio of Nb/Zr was 0.11. CATALYST 20: Under a dry air stream, Catalyst 16 was calcined at 600°C for 2 hours to obtain a catalyst, which is designated as Catalyst 20. The BET specific surface area was 152 m²/g. CATALYST 21: 5 g of niobium pentachloride was dissolved in 10 ml of methanol. To this solution, a solution obtained by dissolving 2 g of calcium chloride in 50 ml of water, was added. Further, the mixture was diluted with 300 ml of water, and 50 ml of 15% aqueous ammonia was dropwise added thereto. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 21. CATALYST 22: 5 g of niobium pentachloride and 5.8 g of bismuth trichloride were dissolved in 100 ml of methanol. This solution was dropwise added to 100 ml of 15% aqueous ammonia. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 22. CATALYST 23: 5 g of niobium pentachloride and 5 g of tellurium tetrachloride were dissolved in 100 ml of methanol. This solution was dropwise added to 100 ml of 15% aqueous ammonia. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 23. CATALYST 24: 5 g of niobium pentachloride and 3.1 g of copper (II) chloride dihydrate were dissolved in methanol. The solution was dropwise added to 300 ml of a 2% sodium hydroxide aqueous solution. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 24. CATALYST 25: 5 g of niobium pentachloride was dissolved in 10 ml of methanol. To this solution, a solution prepared by dissolving 2.5 g of zinc (II) chloride in 100 ml of water, was added. This solution was dropwise added to 350 ml of a 2% sodium hydroxide aqueous solution. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 25. CATALYST 26: 5 g of niobium pentachloride was dissolved in 10 ml of methanol. To this solution, a solution prepared by dissolving 8 g of lanthanum nitrate hexahydrate in 50 ml of water, was added. This mixture was diluted with 300 ml of water, and 100 ml of 15% aqueous ammonia was added thereto. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 26. CATALYST 27: 5 g of tantalum pentachloride and 15 g of niobium pentachloride were dissolved in 500 ml of methanol. The solvent was distilled off under reduced pressure. To the residue, 1-butanol was added, and the mixture was refluxed. Then, 500 ml of water was added thereto, and the mixture was refluxed for 5 hours. Then, the mixture was neutralized by an addition of 15% aqueous ammonia. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 27. CATALYST 28: 30 ml of methanol was added to 5 g of niobium pentachloride and 4.9 g of chromium (III) chloride hexahydrate. This solution was dropwise added to 300 ml of 5% aqueous ammonia. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 28. CATALYST 29: 5 g of niobium pentachloride was dissolved in 10 ml of methanol. To this solution, 10 ml of concentrated hydrochloric acid was added. To this solution, a solution prepared by dissolving 4.5 g of manganese acetate hexahydrate in 50 ml of water, was added. Water was added thereto to bring the total volume to 300 ml. Then, 300 ml of the solution was dropwise added to 150 ml of 15% aqueous ammonia. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 29. CATALYST 30: 5 g of niobium pentachloride was dissolved in 10 ml of methanol. To this solution, a solution prepared by dissolving 3 g of iron (III) chloride in 50 ml of water, was added. This solution was dropwise added to 550 ml of 3% aqueous ammonia. Formed precipitates were collected by filtration, washed with water and calcined at 400°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Catalyst 30. COMPARATIVE CATALYST A: 10 g of water-containing niobium oxide (AD-378) manufactured by CBMM Co. was calcined at 400°C for 2 hours under a dry air stream. The BET specific surface area was 99 m²/g. This was found to be not crystallized from the X-ray diffration. This was further calcined at 500°C for 2 hours under a dry air stream to obtain a catalyst, which is designated as Comparative Catalyst A. The BET specific surface area was 17 m²/g. From the X-ray diffraction, this Comparative Catalyst was found to be crystalline. COMPARATIVE CATALYST B: 130 g of lanthanum nitrate hexahydrate was dissolved in deionized water under stirring. Separately, 79.2 g of diammonium hydrogen phosphate was dissolved in deionized water under stirring. While vigorously stirring the aqueous diammonium hydrogen phosphate solution, the aqueous lanthanum nitrate solution was added at once, whereby thick bulky precipitates formed. A thick creamy suspension was obtained by stirring, and the precipitates were collected by filtration under suction. The paste-like solid thus obtained was thoroughly washed with deionized water and then dried at a temperature of from 80 to 90°C to obtain a catalyst, which is designated as Comparative Catalyst B. COMPARATIVE CATALYST C: To 67.6 g of aluminum oxide trihydrate, 279.4 g of 85% phosphoric acid was added portionwise in several times. The mixture was left to stand at room temperature. Before the temperature became constant, the mixture was heated abruptly to 120°C to obtain a viscous uniform solution. The hot reaction solution was poured into distilled water under stirring to obtain a colorless transparent solution having a pH of from 2 to 3. To this solution, a 30% ammonium hydroxide solution was added, whereby white precipitates formed. Ammonium hydroxide was added until precipitates no longer formed. Then, white precipitates were collected by filtration under suction. The precipitates were thoroughly washed with distilled water and then with methanol, and then dried in an evacuated deccicator at a temperature of from 80 to 100°C for 16 hours. Then, the precipitates were calcined at 250°C for 7 hours to obtain aluminum phosphate, which is designated as Comparative Catalyst C. EXAMPLE 2 1.6 g of Catalyst 1, 60.0 g of EDA and 30.0 g of MEA were charged into a 200 ml stainless steel autoclave equipped with an electromagnetic stirrer. After flushing with nitrogen, the mixture was heated to 300°C and maintained at that temperature for 5 hours. The reaction pressure was 42.63 bar (42.5 kg/cm²G). Then, the reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 70.0%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 4.3% by weight, DETA: 53.1% by weight, AEEA: 3.6% by weight, AEP: 3.1% by weight, and TETA: 21.6% by weight. The recovery rate of the catalyst was 100%. EXAMPLE 3 The reaction was conducted under the same condition as in Example 2 except that the reaction was conducted for 2.7 hours by using 3.0 g of Catalyst 1. The results are shown in Table 1. COMPARATIVE EXAMPLE 1 The reaction was conducted under the same condition as in Example 1 except that the reaction was conducted for 3.0 hours by using 3.0 g of Comparative Catalyst C. The results are shown in Table 1. COMPARATIVE EXAMPLE 2 The reaction was conducted under the same condition as in Example 2 except that the reaction was conducted for 3.0 hours by using 3.0 g of Comparative Catalyst B. COMPARATIVE EXAMPLE 3 The reaction was conducted under the same condition as in Example 2 except that the reaction was conducted for 6.3 hours by using 12.0 g of silica manufactured by Nikki Kagaku K.K. as the catalyst. The results are shown in Table 1. EXAMPLE 4 Into a 200 ml stainless steel autoclave equipped with an electromagnetic stirrer, 4.8 g of Catalyst 1 was charged, and 30.0 g of EDA and 15.0 g of MEA were added thereto. After flushing with nitrogen, 52.6 g of ammonia was added, and the mixture was reacted at 280°C for 2 hours. After cooling, the reaction solution was taken out and analyzed by gas chromatography. As a result, the conversion of MEA was 62.8%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 5.1% by weight, DETA: 34.1% by weight, AEEA: 0.7% by weight, and TETA: 12.0% by weight. EXAMPLE 5 The reaction was conducted under the same condition as in Example 2 except that 1.0 g of Catalyst 2 was used as the catalyst. The conversion of MEA was 47.1%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 2.7% by weight, DETA: 42.6% by weight, and TETA: 11.2% by weight. EXAMPLES 6 and 7 The reactions were conducted under the same condition as in Example 2 except that as the catalyst, those as identified in Table 2 were used in the amounts as identified in Table 2, and the reactions were conducted for the periods of time as identified in Table 2. The results are shown in Table 2. Catalyst Amount of catalyst (g) Reaction time (hr) Conversion of MEA (%) Example 6 Catalyst 3 1.1 5.0 62.5 Example 7 Catalyst 4 6.4 3.0 50.8 EXAMPLES 8 and 9 The reactions were conducted under the same condition as in Example 2 except that as the catalyst, 3.0 g of the catalysts as identified in Table 3 were used, and the reactions were conducted for the periods of time as identified in Table 3. The results are shown in Table 3. COMPARATIVE EXAMPLE 4 The reaction was conducted under the same condition as in Example 2 except that as the catalyst, 3.0 g of Comparative Catalyst A was used, and the reaction was conducted for 3.0 hours. The results are shown in Table 3. Catalyst Amount of catalyst (g) Reaction time (hr) Conversion of MEA (%) Example 8 Catalyst 1 3.0 2.7 64.5 Example 9 Catalyst 5 3.0 2.5 35.4 Comparative Example 4 Comparative Catalyst A 3.0 3.0 8.8 EXAMPLE 10 The reaction was conducted under the same condition as in Example 2 except that as the catalyst, 1.4 g of Catalyst 6 was used. The reaction pressure was 40.67 bar (40.5 kg/cm²G). Then, the reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 48.3%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 3.0% by weight, DETA: 43.5% by weight, AEEA: 9.3% by weight, AEP: 1.2% by weight, and TETA: 13.6% by weight. The non-cyclic rate of TETA i.e. (branched + linear)/(branched + linear + cyclic isomer) x 100, was 85.9%. EXAMPLE 11 The reaction was conducted under the same condition as in Example 2 except that 3.0 g of Catalyst 7 was used, and the reaction was conducted for 2 hours. The conversion of MEA was 43.2%. EXAMPLE 12 3.0 g of Catalyst 8, 30.1 g of EDA and 15.0 g of MEA were charged into a 200 ml stainless steel autoclave equipped with an electromagnetic stirrer. After flushing with nitrogen, 55.6 g of ammonia was added, and the mixture was heated to 280°C and maintained at that temperature for 3 hours. The reaction pressure was 350.8 bar (357 kg/cm²G). Then, the reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 67.8%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 3.9% by weight, DETA: 34.7% by weight, AEEA: 0.0% by weight, AEP: 4.3% by weight, and TETA: 12.8% by weight. EXAMPLES 13 and 14 The reactions were conducted under the same condition as in Example 2 except that as the catalyst, 3.0 g of the catalysts as identified in Table 4 were used, and the reactions were conducted for 2 hours. The results are shown in Table 4. Catalyst Reaction time (hr) Conversion of MEA (%) Example 13 Catalyst 9 2.5 56.1 Example 14 Catalyst 10 2.5 43.0 EXAMPLE 15 The reaction was conducted under the same condition as in Example 2 except that as the catalyst, 1.5 g of Catalyst 11 was used. The reaction pressure was 36.26 bar (36.0 kg/cm²G). Then, the reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 26.1%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 3.7% by weight, DETA: 40.8% by weight, AEEA: 15.8% by weight, and TETA: 5.1% by weight. The recovery rate of the catalyst was 100%. EXAMPLE 16 The reaction was conducted under the same condition as in Example 2 except that 3.0 g of Catalyst 12 was used, and the reaction was conducted for 2 hours. The results are shown in Table 5. Amount of catalyst (g) Reaction time (hr) Conversion of MEA (%) Non-cyclic TETA (%) Example 16 3.0 2.0 34.0 93.3 EXAMPLE 17 Into a 200 ml stainless steel autoclave equipped with an electromagnetic stirrer, 3.0 g of Catalyst 13, 15.0 g of MEA and 54.4 g of ammonia were charged and reacted at 280°C for 3 hours. The reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 93.1%, and the composition of the reaction solution was as follows: EDA: 16.4% by weight, MEA: 6.9% by weight, PIP: 5.1% by weight, DETA: 4.9% by weight, AEEA: 0.06% by weight, and TETA: 7.8% by weight. EXAMPLE 18 Into a 200 ml stainless steel autoclave equipped with an electromagnetic stirrer, 3.0 g of Catalyst 13, 60.0 g of EDA, 30.0 g of MEA and 16.5 g of ammonia were charged and reacted at 280°C for 5 hours. The reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 46.5%, and the composition of the reaction solution was as follows: EDA: 51.4% by weight, MEA: 17.8% by weight, PIP: 0.7% by weight, DETA: 14.9% by weight, AEEA: 0.4% by weight, and TETA: 2.9% by weight. EXAMPLES 19 and 20 The reaction was conducted under the same condition as Example 2 except that as the catalyst, 3.0 g of the catalysts as identified in Table 6 were used, and the reaction time was changed to 2.5 hours. The reaction solution was cooled and analyzed by gas chromatography. The results are shown in Table 6. Catalyst Reaction time (hr) Conversion of MEA (%) Example 19 Catalyst 14 2.5 26.1 Example 20 Catalyst 15 2.5 19.5 EXAMPLE 21 The reaction was conducted under the same condition as in Example 2 except that as the catalyst, 1.9 g of Catalyst 16 was used. The reaction pressure was 42.63 bar (42.5 kg/cm²G). Then, the reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 51.8%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 2.8% by weight, DETA: 38.8% by weight, AEEA: 8.7% by weight, AEP: 1.3% by weight, and TETA: 12.7% by weight. The non-cyclic rate of TETA i.e. (branched + linear)/(branched + linear + cyclic isomer) x 100, was 86.3%. EXAMPLE 22 The reaction was conducted under the same condition as in Example 2 except that 3.0 g of Catalyst 17 was used, and the reaction was conducted for 2 hours. The conversion of MEA was 46.0%. EXAMPLE 23 3.0 g of Catalyst 18, 30.1 g of EDA and 15.0 g of MEA were charged into a 200 ml stainless steel autoclave equipped with an electromagnetic stirrer. After flushing with nitrogen, 52.3 g of ammonia was charged thereto, and the mixture was heated to 280°C and maintained at that temperature for 3 hours. The reaction pressure was 310.7 bar (316 kg/cm²G). Then, the reaction solution was cooled and analyzed by gas chromatography. The conversion of MEA was 44.8%, and the composition of the reaction solution excluding the starting materials and formed water was as follows: PIP: 2.4% by weight, DETA: 33.4% by weight, AEEA: 2.3% by weight, AEP: 2.1% by weight, and TETA: 7.7% by weight. EXAMPLES 24 and 25 The reactions were conducted under the same condition as in Example 2 except that 3.0 g of the catalysts as identified in Table 7 were used, and the reactions were conducted for 2 hours. The reaction solutions were cooled and analyzed by gas chromatography. The results are shown in Table 7. Catalyst Reaction time (hr) Conversion of MEA (%) Example 24 Catalyst 19 3.0 45.1 Example 25 Catalyst 20 3.0 39.3 EXAMPLE 26 The reaction was conducted under the same condition as in Example 2 except that 1 g of Catalyst 23 was used, and the reaction was continued for 3 hours. The reaction pressure was 89.2 bar (90.0 kg/cm²G). The reaction solution was cooled, withdrawn and analyzed by gas chromatography. As a result of the analysis, the conversion of MEA was 43.5%, and the composition of the reaction solution excluding the starting materials and formed water, was as follows: PIP: 3.41% by weight, DETA: 10.57% by weight, AEEA: 2.26% by weight, AEP: 1.63% by weight, TETA: 4.33% by weight, and TEPA: 1.13% by weight. EXAMPLE 27 The reaction was conducted under the same condition as in Example 2 except that 1 g of Catalyst 24 was used and the reaction time was changed to 2 hours. The convension of MEA was 50.5%. EXAMPLES 28 to 35 The reactions were conducted under the same condition as in Example 2 except that 1 g of the catalysts as identified in Table 8 were used. The results are shown in Table 8. Catalyst Conversion of MEA (%) Example 28 Catalyst 21 14.7 Example 29 Catalyst 22 40.5 Example 30 Catalyst 25 46.4 Example 31 Catalyst 26 13.4 Example 32 Catalyst 27 33.0 Example 33 Catalyst 28 16.0 Example 34 Catalyst 29 12.5 Example 35 Catalyst 30 9.9

Claims: A process for producing non-cyclic alkylenamines, which comprises reacting ammonia and/or an alkylenamine with an alkanolamine in the presence of a mixed oxide catalyst to obtain alkylenamines having an increased number of alkylene moieties over the ammonia and/or the alkylenamine used as starting material, wherein said mixed oxide catalyst comprises niobium oxide and titania, alumina, silica or zirconia, and/or an oxide of an element of Group IIA, VA, VIA, IB, IIB, IIIB, VB, VIB, VIIB or VIII of the Periodic Table except oxides of the elements Fe, Cr and W. The process according to Claim 1, wherein the mixed oxide catalyst comprises niobium oxide and titania in a molar ratio of Nb/Ti of from 0.01 to 100. The process according to Claim 1, wherein the mixed oxide catalyst comprises niobium oxide and alumina in a molar ratio of Nb/Al of from 0.001 to 100. The process according to Claim 1, wherein the mixed oxide catalyst comprises niobium oxide and silica in a molar ratio of Nb/Si of from 0.001 to 100. The process according to Claim 1, wherein the mixed oxide catalyst comprises niobium oxide and zirconia in a molar ratio of from 0.001 to 100. The process according to any one of Claims 1 to 5, wherein the alkylenamine used as starting material is an ethylenamine. The process according to any one of Claims 1 to 6, wherein the alkanolamine is an ethanolamine.

Inventors: HARA, YASUSHI, ITO, YUKIO, SEKIZAWA, KAZUHIKO, SUZUKI, NOBUMASA
Applicants: TOSOH CORPORATION
Application year: 1988
Main classification: B01J23
IPC codes: B01J23, C07C209