Process for the manufacture of dimethylethylamine

Claim 2

A process for the manufacture of dimethylethylamine comprising reacting gaseous ethanol with a gaseous mixture of hydrogen and dimethylamine in the presence of a hydrogenation/dehydrogenation catalyst comprising copper and chromic oxide alone or admixed with barium oxide, zinc oxide, magnesium oxide, or other oxides, at a temperature of about 180° to 240° C. and an absolute pressure of about 1 to 15 bars for a time sufficient to form dimethylethylamine, the molar ratio of dimethylamine/ethanol being about 0.2 to 0.6 and the molar ratio of hydrogen/ethanol being about 3 to 10.

Claim 3

The process of claim 1 wherein the temperature is about 200° to 210° C., the molar ratio of dimethylamine/ethanol is about 0.25 to 0.4, and the molar ratio of hydrogen/ethanol is about 4 to 7.

Claim 4

The process of claim 1 or 2 wherein the process is carried out continuously and the unreacted gases are recycled for further reaction with 0.1 to 1% by volume of the recycled gases being replaced by hydrogen.

Claim 5

The process of claim 1 or 2 in which the flow rate of ethanol is from about 10 to 50 moles/hour per liter of catalyst.

Claim 6

The process of claim 1 in which the effluent from the reaction is treated on a hydrogenation catalyst at a temperature of about 100° to 130° C. and at a pressure essentially the same as that used in said reaction.

Claim 7

The process of claim 5, in which the hydrogenation catalyst for the effluent is identical to the catalyst used in said reaction.

Claim 8

The process according to claim 5, in which the hydrogenation catalyst for the liquid effluent is foraminous Raney nickel of 2 to 10 mm size.

Claim 9

The process of claim 5, in which the hydrogenation catalyst for the liquid effluent consists of nickel deposited on a silica support, used in the form of pellets of 3 to 10 mm size.

Claim 10

The process of claims 1 or 2 in which the effluent is treated in continuous manner with hydrazine hydrate.

Claim 11

The process of claims 1, 2 or 5 in which the reaction is conducted in the presence of a catalytic mass having undergone a regeneration consisting of an oxidation by a mixture of air diluted in nitrogen, followed by a reduction by a mixture of hydrogen and steam.

Claim 12

A process for the manufacture of dimethylethylamine comprising reacting, on a continuous basis, gaseous ethanol with a gaseous mixture of hydrogen and dimethylamine in the presence of a hydrogenation/dehydrogenation catalyst comprising copper and chromic oxide alone or admixed with barium oxide, zinc oxide, magnesium oxide, or other oxides, at a temperature of about 200° to 210° C. and an absolute pressure of about 1 to 15 bars for a time sufficient to form a reaction effluent containing dimethylethylamine, separating the unreacted gases from the reaction effluent, treating said reaction effluent with a hydrogenation catalyst at a temperature of 100° to 130° C. and at a pressure essentially the same as that used in forming the reaction effluent, recycling the separated gases for further reaction with about 0.2 to 0.7% by volume of the recycled gases being replaced by hydrogen, and recovering dimethylethylamine, the molar ratio of dimethylamine/ethanol being about 0.25 to 0.4, the molar ratio of hydrogen/ethanol being about 3 to 10, and the flow rate of the ethanol is from about 20 to 25 moles/hour per liter of catalyst.

Claim 13

A process for the manufacture of dimethylethylamine comprising reacting, on a continuous basis, gaseous ethanol with a gaseous mixture of hydrogen and dimethylamine in the presence of a hydrogenation/dehydrogenation catalyst comprising copper and chromic oxide alone or admixed with barium oxide, zinc oxide, magnesium oxide, or other oxides, at a temperature of about 200° to 210° C. and an absolute pressure of about 1 to 15 bars for a time sufficient to form a reaction effluent containing dimethylethylamine, separating the unreacted gases from the reaction effluent, treating said reaction effluent with a hydrogenation catalyst at a temperature of 100° to 130° C. and at a pressure essentially the same as that used in forming the reaction effluent, recycling the separated gases for further reaction with about 0.2 to 0.7% by volume of the recycled gases being replaced by hydrogen, and recovering dimethylethylamine, the molar ratio of dimethylamine/ethanol being about 0.25 to 0.4, the molar ratio of hydrogen/ethanol being about 3 to 10, and the flow rate of the ethanol is from about 20 to 25 moles/hour per liter of catalyst.