Staged epoxidation of propylene with recycle

In a process for preparing propylene oxide and tertiary butyl alcohol by reacting propylene with tertiary butyl hydroperoxide in solution in tertiary butyl alcohol in the presence of a soluble molybdenum catalyst, the improvement which comprises:

• continuously conducting said process in a reactor system comprising a first isothermal segment and a second adiabatic segment,
• preparing a tertiary butyl alcohol solution containing about 35 to about 60 wt. % of tertiary butyl hydroperoxide, correspondingly, about 65 to about 40 wt. % of tertiary butyl alcohol and about 100 to about 1,000 ppm of a soluble molybdenum catalyst,
• continuously educting a recycle stream into a flowing stream of propylene in an eductor, said recycle stream being about 25 to about 100 wt. %, of the combined weight of the propylene, and of the tertiary butyl alcohol solution,
• continuously charging to said isothermal segment a feed mixture comprising said educted recycle stream, said propylene and said tertiary butyl alcohol solution, and converting about 60 to 80 wt. % of the charged tertiary butyl hydroperoxide therein to provide an intermediate reaction mixture,
• removing said recycle stream from the intermediate reaction mixture, and
• passing the remainder of the intermediate reaction mixture through the adiabatic segment and converting therein an additional 20 to 40 wt. % of the tertiary butyl hydroperoxide charged thereto.

In a process for the preparation of tertiary butyl alcohol and propylene oxide by reacting propylene with tertiary butyl hydroperoxide in the presence of a molybdenum catalyst at an elevated temperature and a pressure sufficient to maintain the reactants in liquid phase, said reaction being conducted in a reaction zone comprising a first isothermal segment and at a second adiabatic segment, the improvement which comprises the steps of:

• a. preparing a tertiary butyl alcohol solution containing about 35 to about 60 wt. % of tertiary butyl hydroperoxide, correspondingly, about 65 to about 40 wt. % of tertiary butyl alcohol and about 100 to about 1,000 ppm of a soluble molybdenum catalyst,
• b. continuously charging to said isothermal segment a feed mixture comprising propylene, said tertiary butyl alcohol solution and a recycle stream comprising about 25 to 100 wt. % of the combined weight of said propylene and said tertiary butyl alcohol solution, said propylene being charged in an amount sufficient to provide an initial charge ratio of about 1 to about 3 moles of propylene per mole of tertiary butyl hydroperoxide,
• c. continuously passing said feed mixture through said isothermal segment under epoxidation reaction conditions of time and temperature sufficient to convert about 60 to about 80% of the tertiary butyl hydroperoxide to reaction products including propylene oxide and tertiary butyl alcohol, and to provide an isothermal segment reaction product,
• d. continuously removing said recycle stream from said isothermal segment reaction product to provide an intermediate reaction mixture comprising the remainder of said isothermal segment reaction product,
• e. continuously returning said recycle stream to said isothermal segment,
• f. continuously charging said intermediate reaction mixture to said adiabatic segment and flowing said intermediate reaction mixture therethrough under adiabatic epoxidation reaction conditions of temperature and time sufficient to convert therein an additional 20 to 40 wt. % of the tertiary butyl hydroperoxide charged thereto to reaction products, principally propylene oxide and tertiary butyl alcohol to provide a final reaction product, and
• g. continuously recovering propylene oxide and tertiary butyl alcohol from said final reaction product,
• h. said epoxidation reaction conditions in said isothermal segment and said adiabatic segment of said epoxidation reaction zone including a temperature of about 50.degree. to 180.degree. C., and a reaction time of about 0.3 to about 3 hours.

In a process for the preparation of tertiary butyl alcohol and propylene oxide by reacting propylene with tertiary butyl hydroperoxide in the presence of a molybdenum catalyst at an elevated temperature and at a pressure sufficient to maintain the reactants in liquid phase, said reaction being conducted in a reaction zone comprising a first isothermal segment and at a second adiabatic segment, the improvement which comprises the steps of:

• a. preparing a tertiary butyl alcohol solution containing about 35 to about 60 wt. % of tertiary butyl hydroperoxide, correspondingly, about 65 to about 40 wt. % of tertiary butyl alcohol and about 100 to about 1,000 ppm of a soluble molybdenum catalyst,
• b. continuously educting a recycle stream into a stream of propylene, said recycle stream comprising about 25 to about 100 wt. % of the combined weight of said propylene, and tertiary butyl alcohol solution,
• c. continuously charging to said isothermal segment a feed mixture comprising said recycle stream, and propylene and said tertiary butyl alcohol solution, said propylene being charged in an amount sufficient to provide an initial charge reaction mixture having a charge ratio of about 1 to about 3 moles of propylene per mole of tertiary butyl hydroperoxide,
• d. condinuously passing said initial charge reaction mixture through said isothermal segment under reaction conditions of time and temperature sufficient to convert about 60% to about 80% of the tertiary butyl hydroperoxide to reaction products including propylene oxide and tertiary butyl alcohol, and to provide an isothermal segment reaction product,
• e. continuously removing said recycle stream from said isothermal segment reaction product to provide an intermediate reaction mixture comprising the remainder of said isothermal segment reaction product,
• f. continuously charging said intermediate reaction mixture to said adiabatic segment and flowing said intermediate reaction mixture therethrough under adiabatic reaction conditions of temperature and pressure sufficient to convert therein an additional 20 to 40 wt. % of the tertiary butyl hydroperoxide charged thereto to reaction products, principally propylene oxide and tertiary butyl alcohol to provide a final reaction product, and
• g. continuously recovering propylene oxide and tertiary butyl alcohol from said final reaction product,
• h. said epoxidation reaction conditions in said isothermal segment and said adiabatic segment of said epoxidation reaction zone including a temperature of about 50.degree. to 180.degree. C., a pressure sufficient to maintain the reactants and the reaction products in liquid phase and a reaction time of about 0.3 to about 5 hours.

In a continuous process for preparing propylene oxide and tertiary butyl alcohol wherein propylene and tertiary butyl hydroperoxide are reacted in an epoxidation reaction zone under predetermined reaction conditions, said epoxidation reaction zone comprising an isothermal segment and an adiabatic segment, said propylene being reacted with said tertiary butyl hydroperoxide in solution in tertiary butyl alcohol in the presence of a catalytic amount of a soluble complex of molybdenum with ethylene glycol the improvement which comprises the steps of:

• a. preparing a tertiary butyl alcohol solution containing about 35 to about 60 wt. % of tertiary butyl hydroperoxide, correspondingly, about 65 to about 40 wt. % of tertiary butyl alcohol and about 100 to about 1,000 ppm of a soluble molybdenum catalyst,
• b. continuously educting a recycle stream into a propylene stream, said recycle stream comprising at 25 to about 100 wt. % of the combined weight of the propylene and the tertiary butyl alcohol solution,
• c. charging to said isothermal segment a feed mixture comprising said recycle stream, and propylene stream and said tertiary butyl alcohol solution, said propylene being charged in an amount sufficient to provide an initial charge ratio of about 1 to about 3 moles of propylene per mole of tertiary butyl hydroperoxide,
• d. continuously passing said feed mixture through said isothermal segment under reaction conditions of time and temperature sufficient to convert about 60% to about 80% of the tertiary butyl hydroperoxide to reaction products including propylene oxide and tertiary butyl alcohol, and to provide an isothermal segment reaction product,
• e. continuously removing said recycle stream from said isothermal segment reaction product to provide an intermediate reaction mixture comprising the remainder of said isothermal segment reaction product,
• f. continuously charging said intermediate reaction mixture to said adiabatic segment and flowing said intermediate reaction mixture therethrough under adiabatic reaction conditions of temperature and pressure sufficient to convert therein an additional 20 to 40 wt. % of the tertiary butyl hydroperoxide charged thereto to reaction products to provide a final epoxidation reaction product comprising unreacted propylene, unreacted tertiary butyl hydroperoxide, propylene oxide, tertiary butyl alcohol, dissolved molybdenum-ethylene glycol catalyst complex, and oxygen-containing impurities, and
• g. continuously charging said final epoxidation reaction product to a distillation zone and resolving it therein into distillation fractions, including a distillate propylene fraction, a distillate propylene oxide fraction, a distillate tertiary butyl alcohol fraction and a bottoms fraction composed primarily of tertiary butyl hydroperoxide, tertiary butyl alcohol, oxygen-containing impurities and dissolved molybdenum-ethylene glycol catalyst complex,
• h. said epoxidation reaction conditions in said isothermal segment and said adiabatic segment of said epoxidation reaction zone including a temperature of about 50.degree. to 180.degree. C., a pressure sufficient to maintain the reactants and the reaction products in liquid phase and a reaction time of about 0.3 to about 5 hours.

In a continuous process for preparing propylene oxide and tertiary butyl alcohol wherein propylene and tertiary butyl hydroperoxide are reacted in an epoxidation reaction zone under predetermined reaction conditions, said epoxidation reaction zone comprising an isothermal segment and an adiabatic segment, said propylene being reacted with said tertiary butyl hydroperoxide in solution in tertiary butyl alcohol in the presence of a catalytic amount of a soluble complex of molybdenum with ethylene glycol the improvement which comprises the steps of:

• a. preparing a tertiary butyl alcohol solution containing about 35 to about 60 wt. % of tertiary butyl hydroperoxide, correspondingly, about 65 to about 40 wt. % of tertiary butyl alcohol and about 100 to about 1,000 ppm of a soluble molybdenum catalyst,
• b. continuously educting a recycle stream into a propylene stream in said eductor, said recycle stream comprising about 25 to about 100 wt. % of the combined weight of the propylene and the tertiary butyl alcohol solution,
• c. charging a feed mixture to said isothermal segment in admixture, said feed mixture comprising said recycle stream, said propylene stream and said tertiary butyl alcohol solution, said propylene being charged in an amount sufficient to provide an initial charge reaction mixture having a ratio of about 1 to about 3 moles of propylene per mole of tertiary butyl hydroperoxide,
• d. continuously passing said feed mixture through said isothermal segment under reaction conditions of time and temperature sufficient to convert about 60% to about 80% of the tertiary butyl hydroperoxide and to provide an isothermal segment reaction product,
• e. continuously charging said intermediate reaction mixture to said adiabatic segment and flowing said intermediate reaction mixture therethrough under adiabatic reaction conditions of temperature and pressure sufficient to convert therein an additional 20 to 40 wt. % of the tertiary butyl hydroperoxide charged thereto to reaction products to provide a final epoxidation reaction product comprising unreacted propylene, unreacted tertiary butyl hydroperoxide, propylene oxide, tertiary butyl alcohol, dissolved molybdenum-ethylene glycol catalyst complex, and oxygen-containing impurities, and
• f. continuously charging said final epoxidation reaction product to a distillation zone and resolving it therein into distillation fractions, including a distillate propylene fraction, a distillate propylene oxide fraction, a distillate tertiary butyl alcohol fraction and a bottoms fraction composed primarily of tertiary butyl hydroperoxide, tertiary butyl alcohol, oxygen-containing impurities and dissolved molybdenum-ethylene glycol catalyst complex,
• g. said epoxidation reaction conditions in said isothermal segment and said adiabatic segment of said epoxidation reaction zone including a temperature of about 50.degree. to 180.degree. C., a pressure sufficient to maintain the reactants and the reaction products in liquid phase and a reaction time of about 0.3 to about 5 hours.