A regeneration device, a device for preparing low-carbon olefins, and a use thereof are provided. The regeneration device includes a first regenerator and a second regenerator; a first activation zone of the first regenerator is connected to the second regenerator through a pipeline, such that a catalyst in the first activation zone is able to be delivered to the second regenerator; and the second regenerator is connected to a gas-solid separation zone of the first regenerator through a pipeline, such that a catalyst in the second regenerator is able to be delivered to the gas-solid separation zone. The regeneration device can adjust the coke content, coke content distribution, and coke species in a dimethyl ether/methanol to olefins (DMTO) catalyst to control an operation window of the DMTO catalyst, which improves the selectivity for low-carbon olefins and the atomic economy of a methanol-to-olefins (MTO) technology.

A regeneration device, a device for preparing low-carbon olefins, and a use thereof are provided. The regeneration device includes a first regenerator and a second regenerator; a first activation zone of the first regenerator is connected to the second regenerator through a pipeline, such that a catalyst in the first activation zone is able to be delivered to the second regenerator; and the second regenerator is connected to a gas-solid separation zone of the first regenerator through a pipeline, such that a catalyst in the second regenerator is able to be delivered to the gas-solid separation zone. The regeneration device can adjust the coke content, coke content distribution, and coke species in a dimethyl ether/methanol to olefins (DMTO) catalyst to control an operation window of the DMTO catalyst, which improves the selectivity for low-carbon olefins and the atomic economy of a methanol-to-olefins (MTO) technology.

The invention relates to a process of converting methanol in a fluidized bed reactor comprising feeding a methanol-containing feedstock into a fluidized bed reactor, contacting the feedstock with a catalyst, to produce a product comprising ethylene and propylene under effective conditions; the fluidized bed reactor comprises a diluent-phase zone and a dense-phase zone, wherein the diluent-phase temperature difference between any regions of the diluent-phase zone having a methanol concentration of more than 0.1 wt % (preferably more than 0.01 wt %) in the fluidized bed reactor is controlled to be less than 20° C., and the dense-phase temperature difference between any regions in the dense-phase zone having a methanol concentration of more than 0.1 wt % (preferably more than 0.01 wt %) in the fluidized bed reactor is controlled to be less than 10° C.

The invention relates to a process of converting methanol in a fluidized bed reactor comprising feeding a methanol-containing feedstock into a fluidized bed reactor, contacting the feedstock with a catalyst, to produce a product comprising ethylene and propylene under effective conditions; the fluidized bed reactor comprises a diluent-phase zone and a dense-phase zone, wherein the diluent-phase temperature difference between any regions of the diluent-phase zone having a methanol concentration of more than 0.1 wt % (preferably more than 0.01 wt %) in the fluidized bed reactor is controlled to be less than 20° C., and the dense-phase temperature difference between any regions in the dense-phase zone having a methanol concentration of more than 0.1 wt % (preferably more than 0.01 wt %) in the fluidized bed reactor is controlled to be less than 10° C.

The invention relates to a process of converting methanol in a fluidized bed reactor comprising feeding a methanol-containing feedstock into a fluidized bed reactor, contacting the feedstock with a catalyst, to produce a product comprising ethylene and propylene under effective conditions; the fluidized bed reactor comprises a diluent-phase zone and a dense-phase zone, wherein the diluent-phase temperature difference between any regions of the diluent-phase zone having a methanol concentration of more than 0.1 wt % (preferably more than 0.01 wt %) in the fluidized bed reactor is controlled to be less than 20° C., and the dense-phase temperature difference between any regions in the dense-phase zone having a methanol concentration of more than 0.1 wt % (preferably more than 0.01 wt %) in the fluidized bed reactor is controlled to be less than 10° C.

A process for producing lower olefins from oxygenates includes the steps of contacting a feedstock comprising oxygenates with molecular sieve catalyst in fluidized bed reaction zone under effective conditions, to produce product including ethylene and/or propylene;

the effective conditions include that in the fluidized bed reaction zone, the weights of catalysts having various carbon deposition amounts are controlled, calculated as the weight of the molecular sieve in the catalysts, to have the following proportions based on the total weight of the catalysts in the fluidized bed reaction zone:

the proportion of the weight of the catalyst having a coke deposition amount of less than 3 wt % is 1-20 wt %;

the catalyst having a coke deposition amount of from 3 wt % to less than 5 wt % represents 10 to 70 wt %;

the catalyst having a coke deposition amount from 5 wt % to 10 wt % represents 10 to 88 wt %.

A process for producing lower olefins from oxygenates includes the steps of contacting a feedstock comprising oxygenates with molecular sieve catalyst in fluidized bed reaction zone under effective conditions, to produce product including ethylene and/or propylene;

the effective conditions include that in the fluidized bed reaction zone, the weights of catalysts having various carbon deposition amounts are controlled, calculated as the weight of the molecular sieve in the catalysts, to have the following proportions based on the total weight of the catalysts in the fluidized bed reaction zone:

the proportion of the weight of the catalyst having a coke deposition amount of less than 3 wt % is 1-20 wt %;

the catalyst having a coke deposition amount of from 3 wt % to less than 5 wt % represents 10 to 70 wt %;

the catalyst having a coke deposition amount from 5 wt % to 10 wt % represents 10 to 88 wt %.

Processes for converting one or more C.sub.1-C.sub.5 linear or branched alcohols to one or more C.sub.2-C.sub.5 olefins are provided. In one exemplary embodiment, the process can be a single stage process for the direct conversion of C.sub.1-C.sub.5 alcohols to olefinic mixtures (e.g., C.sub.2-C.sub.5) carried out in a reactor using a catalyst that includes zeolite doped with boron and phosphor. Systems for carrying out these processes are also provided.

Processes for converting one or more C.sub.1-C.sub.5 linear or branched alcohols to one or more C.sub.2-C.sub.5 olefins are provided. In one exemplary embodiment, the process can be a single stage process for the direct conversion of C.sub.1-C.sub.5 alcohols to olefinic mixtures (e.g., C.sub.2-C.sub.5) carried out in a reactor using a catalyst that includes zeolite doped with boron and phosphor. Systems for carrying out these processes are also provided.

A bifunctional catalyst for example for conversion of oxygenates, the bifunctional catalyst comprising zeolite, alumina binder, Zn and P, wherein Zn is present at least partly as ZnAl.sub.2O.sub.4.