Process for the preparation of secondary monomethylalkyl amines

Abstract: A process for the preparation of a highly selective amount of secondary monomethylalkyl amine, said process comprising reacting, at elevated temperature and pressure, a hexahydrotriazine compound in the liquid state with hydrogen in the presence of a catalyst material having at least one catalytically active metal, said hexahydrotriazine compound having the formula wherein R₁, R₂, and R₃ are, independently, straight or branched, saturated or unsaturated, linear or cyclic hydrocarbon groups or straight or branched, saturated or unsaturated, linear or cyclic hydrocarbon groups wherein one or more CH₂ groups are replaced by an oxygen atom or a tertiary amine group, provided that any unsaturated group is separated from nitrogen in the hexahydrotriazine ring by at least one carbon atom, any said oxygen atom is enclosed by two carbon groups, and any said oxygen atoms and any said amine groups are separated from other oxygen atoms and other amine groups and from said nitrogen in the hexahydrotriazine ring by at least two carbon atoms.

Description: The invention relates to a process for the preparation of secondary methylalkyl amines by reduction of a hexahydrotriazine compound in the presence of a metal component. Such a process is known from US 2 657 237 in which a process is given for the continuous preparation of dimethylamine by dissociation of trimethyltrimethylene triamine into monomeric methylmethylene amine, and subsequent catalytic hydrogenation of the monomer into dimethylamine. The process taught is complicated in that it requires specific engineering and equipment to enable the continuous process to be carried out, and a mixture of hydrogen and the liquid trimethyltrimethylene triamine has to be vaporized in a separate preparatory step. Thus, the process is carried out by many sequential process steps, including the separate vaporization step, reaction of the components, separation of the reaction product and feeding the reaction product to a second reaction means. In the second reaction means gaseous reactants are to be passed through a catalyst, upon which dimethylamine is formed. Another drawback of such a process is that its use is uneconomical for the production of monomethylalkyl amines having large alkyl groups, since vaporization of the precursors is rather complicated by their lower volatility. "Bequeme Darstellung von reinen N-Methylalkylaminen durch Zink/Salzsäure-Reduktion von 1,3,5-Tris(alkyl)-hexahydro-1,3,5-triazinen", M. Al Schaik and H. Oelschläger, Arch. Pharm. , 317, pp. 214-219 (1984) describes a process for preparation of N-methylalkyl amines by zinc/hydrochloric acid reduction of trialkylhexahydrotriazines. The process is carried out at -5°C using a drop-in procedure which is rather uneconomical. Futher, the use of a chemical type of reduction is generally considered a major drawback. Together with the use of highly corrosive hydrochloric acid, the method described is expensive and difficult to practice on plant scale. Also the amine is obtained as its hydrochloric acid salt, from which it must be liberated with, for example, sodium hydroxide. Another drawback of this procedure is the large amount of zinc chloride waste produced and the rather low yield of the desired product obtained. The British patent GB 1 305 258 relates to a method for the preparation of secondary or tertiary amines. In this patent specification, secondary or tertiary amines are prepared by reaction of a primary amine with formaldehyde in the presence of H 2 , an alcohol and a catalyst. By this reaction, no hexahydrotriazine as used according to the present invention is formed, nor is a highly selective process for the production of secondary monomethylalkyl amines given. The process according to the invention is characterized in that the reduction is carried out in the liquid state, at a temperature above 150°C and a pressure above 6 bar, with hydrogen in the presence of a catalyst material comprising catalytically active copper, said hexahydrotriazine compound having the formula wherein R 1 , R 2 , and R 3 are, independently, straight or branched, saturated or unsaturated, linear or cyclic hydrocarbon groups or straight or branched, saturated or unsaturated, linear or cyclic hydrocarbon groups wherein one or more CH 2 groups are replaced by an oxygen atom or a tertiary amine group, provided that any unsaturated group is separated from nitrogen in the hexahydrotriazine ring by at least one carbon atom, any said oxygen atom is enclosed by two carbon groups, and any said oxygen atoms and any said amine groups are separated from other oxygen atoms and other amine groups and from said nitrogen in the hexahydrotriazine ring by at least two carbon atoms. By a hexahydrotriazine compound in the liquid state is meant that a hexahydrotriazine of the above formula is contacted with hydrogen and the catalyst without a separate preparatory vaporization step for the hexahydrotriazine. By cyclic hydrocarbon groups are meant, e.g., alicyclic, aromatic, or heterocyclic hydrocarbon groups. The process is carried out at an elevated temperature above 150°C and an elevated pressure above 6 bar Preferably, the process is carried out at a temperature between 170°C and 250°C, preferably between 200°C and 250°C, at a pressure of 10 to 105 bar. Contacting the hydrogen, the hexahydrotriazine compound and the catalyst for at least 0,5 hour, and preferably more than one hour, has provided favorable yields of secondary monomethylalkyl amines. More preferably, the process is carried out at a temperature between 200°C and 250°C and at a pressure of 25 to 70 bar for at least one hour. In a highly economical embodiment of the present process, hexahydrotriazine compounds having large R 1 , R 2 , or R 3 groups, are reacted at 220°C to 230°C and 27,5 bar for a period of between 1 to 3 hours. The hexahydrotriazine can of course be in solid or liquid state at room temperature. At reaction conditions, however, the hexahydrotriazine reacting in the process of the current invention will be substantially in the liquid state. The current process is particularly suitable for hexahydrotriazine compounds having at least one large R 1 , R 2 , or R 3 group. For the current process, a "large" group is one having about 4-40 carbon atoms. The process has shown to provide very useful products when R 1 , R 2 , and R 3 , independently, have 8 to 30, preferably 12-22 carbon atoms. Examples of suitable groups for R 1 , R 2 , and/or R 3 are t-butyl, n-butyl, amyl, hexyl, benzyl, octyl, 2-ethylhexyl , 2-dodecyl-dodecyl, 1-heptadecyl-octadecyl, and the chains occuring in natural fatty compounds (e.g. coco, palm and tallow compounds). The process of the present invention results in highly selective production of the monomethylalkyl amine, in which the alkyl group can be any of the groups within the range discussed above. Products to be formed by the method of the present invention are, for example, N-methyl-t-butyl amine, N-methyl-benzyl amine, N-methyl-dodecyl amine, N-methyl-tallow amine, N-methyl-hydrogenated-tallow amine, and N-methyl-oleyl amine. The catalyst material has copper as the catalytically active metal. Alternatively, another metal compound can be present with the copper as a promoter. For example, other metal oxides like potassium oxide, zinc oxide, magnesium oxide and/or barium oxide can be added to the catalyst. Other materials, like chromite, alumina or silica can be applied with the metal component. Very good results were obtained by use of a catalyst having copper and chromium in the form of copper chromite, on which, additionally, barium can be present in minor amounts. Also a catalyst containing copper and zinc can be applied favorably. The metal catalyst can be applied as such, but can also be distributed on and/or in a carrier material, such as, for example, silica and/or alumina via methods such as impregnation or coprecipitation. Nickel-containing catalysts have been found not to be useful in the process of the present invention, since the use of such a catalytic material results in various by-products being formed. Therefore, the process is preferably carried out in the presence of a catalyst wherein the catalytically active material is substantially free of nickel. It has been found that a very economical process is obtained if use is made of 0,5 wt% copper catalyst based on the weight of hexahydrotriazine present at initiation of the reaction. Favorably, use can be made of a copper chromite catalyst at a level of 0,5-2%, based on the weight of hexahydrotriazine. Additives can be used to influence the yield and speed of the reaction or to ease filtration after reaction. The hexahydrotriazine applied in the process of the present invention can be prepared by any process known in the art. Such are commonly prepared by reaction of formaldehyde and a primary amine and removal of the water being formed. A useful method is described in, e.g., "Polymorphic behavior of 1,3,5-tridodecyl- and 1,3,5-trioctadecylhexahydro-sym-triazines", by C.W. Hoerr et al., J. Am. Chem. Soc. , Vol. . 78, pp. 4667-4670, (1956). By another method, the reaction is carried out by contacting the primary amine and formaldehyde at a temperature between 60°C-85°C, and simultaneously stripping off the water being formed. By doing so, the product obtained is immediately cyclized to the triazine derivative. The reaction is completed by stripping off the volatiles. Another method especially useful for the formation of the hexahydrotriazine from lower amines is the reaction of an alkyl or alcyl amine with an aqueous formalin solution at a temperature in the range of 0°C-5°C. The aqueous layer formed is separated. The desired hexahydrotriazine product can be dried by the addition of, e.g., calcium oxide. Secondary monomethylalkyl amines produced by the process of the current invention are useful starting materials for further syntheses, such as, 1. alkoxylation, 2. alkoxylation and subsequent esterification and/or quaternization, 3. reaction with acrylonitrile and subsequent hydrogenation to the corresponding monomethyl diamine, 4. conversion with carbon disulfide to a dithiocarbamate, and 5. conversion with carbon disulfide to a dithiocarbamate, followed by oxidation to a thiuram. The invention is further illustrated by the following examples which are not to be construed as limiting the invention in any way. The scope of the invention is to be determined from the claims appended hereto. EXAMPLES 1-29 The following examples were carried out by addition of a hexahydrotriazine (2047 grams) in the liquid state and a catalyst in a 7,6 liter reaction vessel. The system was purged four times with 7 bar nitrogen, venting to atmospheric pressure each time. The reactants were heated under nitrogen (vent open) to reaction temperature, unless indicated differently. Hydrogen gas was added and the pressure as indicated was maintained during the reaction. After the time indicated, the reaction vessel was cooled, and the product was removed. The results are listed in Tables 1 and 2. Catalysts used in the Examples The concentrations of catalytically active metal are in percentage by weight. Between brackets the tradenames of the catalysts are mentioned. Engelhard catalysts are also known under the name Harshaw. i is a copper chromite-containing catalyst (42% CuO, 44% Cr 2 O 3 and 8% of BaO) having a surface area of 110 m 2 /g [Engelhard Cu-1182P]. ii is a copper chromite-containing catalyst (51% CuO, 49% Cr 2 O 3 ) having a surface area of 45 m 2 /g [Calsicat E123P]. iii is a copper chromite-containing catalyst (comprised of CuO and Cr 2 O 3 ) known by the trade name Cu-1950P (available from Engelhard Corp.) having a surface area of 35 m 2 /g. iv is a copper chromite-containing catalyst (53% CuO, 47% Cr 2 O 3 ) having a surface area of 34 m 2 /g [Engelhard Cu1850P]. v is a copper chromite-containing catalyst (53% CuO, 47% Cr 2 O 3 ) having a surface area of 88 m 2 /g [Engelhard Cu1850PRP]. vi is a copper chromite-containing catalyst (45% CuO, 45% Cr 2 O 3 and 8% BaO) having a surface area of 45 m 2 /g [Calsicat E108P]. vii is a copper chromite-containing catalyst (49% CuO, 47% Cr 2 O 3 and 4% of MnO 2 ) having a surface area of 25 m 2 /g [Calsicat E124P]. viii is a copper-containing catalyst (45% CuO, 45% ZnO) having a surface area of 12 m 2 /g [Calsicat E320P]. ix is a copper-containing catalyst (91% CuO and 9% Al 2 O 3 ) having a surface area of 100 m 2 /g [Calsicat E408P]. Hexahydrotriazine Reactant Used in the Examples Reactant I is tallowalkyl hexahydrotriazine. Reactant II is octadecyl hexahydrotriazine. Reactant III is hydrogenated tallow hexahydrotriazine. Products Obtained Product A is tallow amine. Product B is methyltallow amine. Product C is dimethyltallow amine. Product D is ditallow amine. Product E is octadecyl amine. Product F is octadecylmethyl amine. Product G is dimethyloctadecyl amine. Product H is dioctadecyl amine. Product K is unreacted hexahydrotriazine. Product P is hydrogenated tallow amine. Product Q is hydrogenated methyl tallow amine. Product R is hydrogenated dimethyl tallow amine. Product S is hydrogenated ditallow amine. Examples having Variations from Standard Reaction Conditions Example 12: Hydrogen was added at 100°C, up to a pressure of 20 bar. The temperature was raised to 220°C, pressure 27,5 bar. Example 13: As example 12, but hydrogen was added at 130°C and 20 bar. Example 14: As example 12, but hydrogen was added at 170°C and 20 bar. Example 15: Hydrogen was added at 170°C and 20 bar. The temperature and pressure were raised to 220°C and 27,5 bar in 30 minutes. The reaction of the hexahydrotriazine is measured at 30-minute sample intervals. Example 21: Hydrogen was added at 140°C and 2,5 bar. The reaction employed a pressure increase (about 0,4 bar/min) and a gradient temperature increase (about 1°C/min). The final temperature was 180°C, and the final pressure was 27,5 bar. Example 22: In this example, tallow amine was produced by starting at 80°C and 20 bar, and the reaction was carried out at 220°C and 27,5 bar. Example 23: As example 22, but the initial reaction conditions were 100°C and 20 bar. Example 30: 1022 g (4 moles) of 1,3,5-tri(t-butyl) hexahydro-1,3,5-triazine, prepared from formaldehyde and t-butyl amine, and 10.2 g of a copper chromite catalyst, containing 53% CuO, and 47% Cr 2 O 3 and having a surface area of 34 m 2 /g, were charged to a 2.5 l stainless steel autoclave with a turbine stirrer and a hydrogen inlet pipe extending into the liquid. While stirring slowly the system was purged four times with 10 bar nitrogen, then four times with 10 bar hydrogen. The stirrer speed was increased to 1000 rpm and the reactor contents were heated to 140°C, while increasing the pressure to 15 bar. After two hours the temperature was increased gradually, over a period of two hours, to 200°C while the pressure was increased to 58 bar. After three hours at 200°C, hydrogen consumption ceased. The reactor was cooled and emptied. The contents were filtrated and shown to contain 87 wt% t-butyl methyl amine. Comparative Examples The process described for Examples 1-29 was used for Comparative Examples C1-C3 except the catalysts used in the Comparative Examples contained nickel compounds. Reactant used was tallowalkyl hexahydrotriazine. The results are listed in Table 3. Catalysts Used x is a copper chromite-containing catalyst (46% CuO, 44% Cr 2 O 3 and 10% NiO) having a surface area of 45 m 2 /g [Calsicat E123P (10% nickel)]. xx is a nickel-containing catalyst, having a surface area of 175 m 2 /g, the catalyst comprised 60 wt% nickel on a silica and alumina-containing carrier material [Engelhard Ni-5132P]. xxx is a Raney nickel catalyst having a surface area of 175 m 2 /g [S&A Blackwell J10S]. From Comparative Examples C1-C3 it is seen that no selectivity was obtained for the catalysts containing nickel. While it is clear from Examples 1-30 that the use of copper at various reaction conditions provides favorable results.

Claims: A process for the preparation of a highly selective amount of secondary monomethylalkyl amines by reduction of a hexahydrotriazine compound in the presence of a metal component, characterised in that the reduction is carried out in the liquid state, at a temperature above 150°C and a pressure above 6 bar, with hydrogen in the presence of a catalyst material comprising catalytically active copper, said hexahydrotriazine compound having the formula wherein R 1 , R 2 , and R 3 are, independently, straight or branched, saturated or unsaturated, linear or cyclic hydrocarbon groups or straight or branched, saturated or unsaturated, linear or cyclic hydrocarbon groups wherein one or more CH 2 groups are replaced by an oxygen atom or a tertiary amine group, provided that any unsaturated group is separated from nitrogen in the hexahydrotriazine ring by at least one carbon atom, any said oxygen atom is enclosed by two carbon groups, and any said oxygen atoms and any said amine groups are separated from other oxygen atoms and other amine groups and from said nitrogen in the hexahydrotriazine ring by at least two carbon atoms. A process according to claim 1 wherein the catalyst material is substantially free of nickel. A process according to claim 1 or 2 wherein said catalyst material contains copper chromite. A process according to anyone of the preceding claims wherein R 1 , R 2 , and R 3 each have at least 4-40 carbon atoms. A process according to anyone of the preceding claims wherein the hexahydrotriazine compound is selected from the group consisting of hexahydrotriazine compounds wherein at least one of R 1 , R 2 , and R 3 is a straight or branched alkyl group having 12 to 22 car bon atoms. A process according to claim 1 wherein the reaction is carried out at a temperature in the range of 200°C to 250°C, at a pressure in the range of 10 to 105 bar for a period of at least one hour.

Inventors: CARR EUGENE ROBERT, CARR, EUGENE ROBERT
Applicants: AKZO NOBEL NV, AKZO NOBEL N.V.
Application year: 1992
Main classification: C07C209
IPC codes: B01J23, C07C211, C07B61, C07C209