Method for the preparation of 1,2-propanediol
1,2-propanediol is prepared by a method involving reacting propene with hydrogen peroxide at 50 to 110° C. in the presence of a catalyst mixture, containing a phase transfer catalyst and a polytungstophosphate, in a liquid reaction mixture containing an aqueous phase with a maximum apparent pH of 6 and an organic phase. The method then involves separating the reaction mixture into an aqueous phase containing 1,2-propanediol and an organic phase; recycling at least part of the separated organic phase to the reaction; and recovering 1,2 propanediol from the aqueous phase. The method further involves reacting a tungstate with hydrogen peroxide and phosphoric acid at 5 to 40° C., in the presence of the phase transfer catalyst, in a liquid mixture containing an aqueous and an organic phase, followed by passing at least a part of the resulting organic phase containing the polytungstophosphate and phase transfer catalyst to the initial reaction.
1 . A method for the preparation of 1,2-propanediol, comprising:
a) reacting propene with hydrogen peroxide at a temperature of from 50 to 110° C. in the presence of a catalyst mixture, comprising a phase transfer catalyst and a polytungstophosphate, in a liquid reaction mixture comprising an aqueous phase with a maximum apparent pH of 6 and an organic phase, wherein apparent pH refers to a value determined by measurement with a glass electrode employing a commercial pH meter calibrated with aqueous buffer solution of known pH for measuring dilute aqueous solutions;
b) separating the liquid reaction mixture into an aqueous phase (P a ) comprising 1,2-propanediol and an organic phase (P o );
c) recycling at least a part of the organic phase (P o ) to a); and
d) recovering the 1,2-propanediol from the aqueous phase (P a );
wherein the method further comprises at least one of
e) reacting a tungstate with hydrogen peroxide and phosphoric acid at a temperature of from 5 to 40° C., in the presence of the phase transfer catalyst, in a liquid mixture comprising an aqueous phase and an organic phase, followed by passing at least a part of a resulting organic phase (P oc ) comprising polytungstophosphate and the phase transfer catalyst to a).
2 . The method of claim 1 , wherein in e), the tungstate is reacted with the hydrogen peroxide and the phosphoric acid in the presence of an organic solvent having a boiling point of more than 100° C. at atmospheric pressure and a solubility in water at 20° C. of less than 250 mg/kg.
3 . The method of claim 1 , wherein at least a part of the organic phase (P o ) separated in b) is used as a tungstate source for e), followed by passing the resulting organic phase (P oc ) to a) to provide for the recycling of c).
4 . The method of claim 3 , wherein a volume ratio of organic phase to aqueous phase in e) is from 50:1 to 1:1.
5 . The method of claim 3 , wherein a volume ratio of organic phase to aqueous phase is less than 10:1, and
wherein a resulting aqueous phase (P ac ) and the resulting organic phase (P oc ) are separated, and a part of the resulting aqueous phase (P ac ) is reused as a phosphoric acid source for e).
6 . The method of claim 1 , wherein at least part of a resulting aqueous phase (P ac ) resulting in e) is passed to a).
7 . The method of claim 1 , wherein the hydrogen peroxide is used in e) in an amount providing at least 2 mol hydrogen peroxide per mol tungsten.
8 . The method of claim 1 , wherein in e), the aqueous phase of said liquid mixture comprises from 10 to 40% by weight of the phosphoric acid.
9 . The method of claim 1 , wherein no propene is added in e).
10 . The method of claim 1 , wherein in d), the aqueous phase (P a ) is subjected to a catalytic hydrogenation prior to recovering the 1,2-propanediol by distillation.
11 . The method of claim 1 , wherein a) is conducted continuously and a concentration of the hydrogen peroxide in the aqueous phase of a) is from 0.1 to 5% by weight.
12 . The method of claim 1 , wherein a) is conducted continuously in a loop reactor comprising fixed internals in a tubular section, and the liquid reaction mixture is passed through the loop reactor at a flow rate sufficient to provide turbulent flow at said fixed internals.
13 . The method of claim 1 , wherein the organic phase in a) comprises an organic solvent having a boiling point of more than 100° C. at atmospheric pressure and a solubility in water at 20° C. of less than 250 mg/kg.
14 . The method of claim 1 , wherein the phase transfer catalyst comprises at least one selected from the group consisting of a tertiary amine, a tertiary ammonium salt, and a quaternary ammonium salt, and
wherein the tertiary amine, the tertiary ammonium salt, and the quaternary ammonium salt each comprises in total at least 12 carbon atoms.
15 . The method of claim 14 , wherein the phase transfer catalyst comprises a tertiary or quaternary ammonium ion having the structure R 1 R 2 R 3 NR 4+ ,
wherein
R 1 , R 2 , and R 3 are the same or different and are each an alkyl group having from 8 to 10 carbon atoms, and
R 4 is hydrogen or methyl.
16 . The method of claim 2 , wherein the organic solvent comprises more than 50% by weight of at least one alkylated aromatic hydrocarbon having from 8 to 12 carbon atoms.
17 . The method of claim 4 , wherein the volume ratio of organic phase to aqueous phase in e) is from 14:1 to 8:1.
18 . The method of claim 5 , wherein the volume ratio of organic phase to aqueous phase is from 7:1 to 0.1:1.
19 . The method of claim 8 , wherein in e), the aqueous phase of the liquid mixture comprises from 18 to 35% by weight of the phosphoric acid.
20 . The method of claim 13 , wherein the organic solvent is a mixture of alkylated aromatic hydrocarbons having 8 to 12 carbon atoms.