Conversion of oxygenates to lower olefins in a turbulent fluidized catalyst bed

Claim 2

A fluidized bed catalytic process for substantially complete conversion of feedstock consisting essentially of methanol and/or dimethylether to hydrocarbons rich in light olefins, comprising the steps of maintaining a fluidized bed of zeolite catalyst particles in a turbulent reactor bed at a temperature of at least 475° C., said catalyst having an apparent particle density of about 0.9 to 1.6 g/cm 3 and a size range of about 1 to 150 microns, and average catalyst particle size of about 20 to 100 microns containing about 10 to 25 weight percent of fine particles having a particle size less than 32 microns; passing hot feedstock vapor upwardly through the fluidized catalyst bed under turbulent flow conditions; maintaining turbulent fluidized bed conditions through the reactor bed between transition velocity and transport velocity at a superficial fluid velocity of about 0.3 to 2 meters per second; and recovering hydrocarbon product containing a major amount of olefins and having a molar ratio of C 3 + olefins to ethene of at least 12:1.

Claim 3

A fluidized bed process according to claim 1 wherein the fluidized bed density is about 100 to 300 kg/m 3 , measured at the bottom of the bed, and wherein the catalyst comprises ZSM-5 type zeolite.

Claim 4

The process of claim 1 wherein the feedstock comprises crude methanol which is converted at least 98 weight percent in the turbulent reactor bed, which has a bed height of at least 9 meters.

Claim 5

In the process for continuous conversion of methanol and/or dimethylether feedstock to hydrocarbon products consisting predominately of lower olefins wherein the feedstock is contacted at elevated temperature of at least 475° C. with a fluidized bed of zeolite catalyst under conversion conditions, the improvement which comprises maintaining the fluidized catalyst bed in a vertical reactor column having a turbulent reaction zone by passing feedstock vapor upwardly through the reaction zone at a velocity greater than dense bed transition velocity to a turbulent regime and less than transport velocity for the average catalyst particle; maintaining superficial feedstock vaper velocity at about 0.3-2 m/sec and weight hourly feedstock space velocity (based on methanol equivalent and total reactor catalyst inventory) at about 1 to 3; wherein the average fluidized bed density measured at the reaction zone bottom is about 100 to 300 kg/m 3 for zeolite having apparent crystal density of about 0.9 to 1.6 gm/cm 3 ; withdrawing a portion of coked catalyst from the reaction zone, oxidatively regenerating the withdrawn catalyst and returning regenerated catalyst to the reaction zone at a rate to control catalyst activity whereby propane:propene molar ratio in the hydrocarbon product is maintained at about 0.04:1 to 0.1:1 under conditions of substantially complete feedstock conversion, thereby producing C 3 + olefins at an ethene molar ratio greater than about 12:1.

Claim 6

In the process for continuous conversion of methanol and/or dimethylether feedstock to hydrocarbon products consisting predominately of lower olefins wherein the feedstock is contacted at elevated temperature of at least 475° C. with a fluidized bed of zeolite catalyst under conversion conditions, the improvement which comprises maintaining the fluidized catalyst bed in a vertical reactor column having a turbulent reaction zone by passing feedstock vapor upwardly through the reaction zone at a velocity greater than dense bed transition velocity to a turbulent regime and less than transport velocity for the average catalyst particle; maintaining superficial feedstock vaper velocity at about 0.3-2 m/sec and weight hourly feedstock space velocity (based on methanol equivalent and total reactor catalyst inventory) at about 1 to 3; wherein the average fluidized bed density measured at the reaction zone bottom is about 100 to 300 kg/m 3 for zeolite having apparent crystal density of about 0.9 to 1.6 gm/cm 3 ; withdrawing a portion of coked catalyst from the reaction zone, oxidatively regenerating the withdrawn catalyst and returning regenerated catalyst to the reaction zone at a rate to control catalyst activity whereby propane:propene molar ratio in the hydrocarbon product is maintained at about 0.04:1 to 0.1:1 under conditions of substantially complete feedstock conversion, thereby producing C 3 + olefins at an ethene molar ratio greater than about 12:1.

Claim 7

The process of claim 4 wherein the catalyst consists essentially of a medium pore pentasil zeolite having an apparent alpha value of about 3 to 50, and average particle size of about 20 to 100 microns, the reactor catalyst inventory including at least 10 weight percent fine particles having a particle size less than 32 microns.

Claim 8

The process of claim 5 wherein the catalyst particles comprise about 5 to 90 weight percent ZSM-5 zeolite having a crystal size of about 1-2 microns.

Claim 9

The process of claim 4 wherein the hydrocarbon product contains at least 70 weight percent total olefins, including at least 50 weight percent C 2 -C 4 olefins and not more than 10 weight percent aromatic hydrocarbons.

Claim 10

The process of claim 1 wherein the feedstock comprises a major amount of methanol and 0 to 50 mole percent of a diluent gas, and wherein the partial pressure of methanol is about 35 to 240 kPa.

Claim 11

The process of claim 8 wherein the product mole ratio of C 3 + olefin to ethene is at least 12:1.