Method for producing a product containing C

1. A process for producing a product containing propylene and ethylene by simultaneous conversion of methanol and ethanol through a reaction in an adiabatic sequentially operated reactor containing a plurality of reaction stages, the process comprising:

providing each of the plurality of reaction stages of the reactor with a fixed bed of a form-selective catalyst;

charging a gaseous feed stream comprising methanol, dimethyl ether, and H 2 O to at least a first of the reaction stages of the reactor with a temperature in a range of 300 to 600° C. at a pressure in a range of 0.1 to 5 bar[a];

feeding ethanol into more than one of the reaction stages of the reactor; and

directing an effluent from a first reaction stage of the reaction stages to a next reaction stage of the reaction stages,

wherein the more than one reaction stages comprise the final reaction stage.

2. The process recited in claim 1 , wherein the gaseous feed stream further comprises a C 2 -olefin, a C 2 -paraffin, a C 3 -olefin, a C 3 -paraffin, a C 4 -olefin, a C 4 -paraffin, a C 5 -olefin, a C 5 -paraffin, a C 6 -olefin, a C 6 -paraffin, a C 7 -olefin, a C 7 -paraffin, a C 8 -olefin, a C 8 -paraffin, or a mixture of two or more of any of these.

3. The process recited in claim 1 , wherein the fixed-bed catalyst includes zeolite of the pentasile type.

4. The process recited in claim 3 , wherein the zeolite is of the type ZSM-5.

5. The process recited in claim 1 , wherein the reaction is carried out at a temperature in a range of 360 to 550° C.

6. The process recited in claim 5 , wherein the reaction is carried out at a temperature in a range of 400 to 500° C.

7. The process recited in claim 3 , wherein the reaction is carried out at a temperature in a range of 360 to 550° C.

8. The process recited in claim 1 , wherein the reaction is carried out at a pressure in a range 0.5 to 5.0 bar[a].

9. The process recited in claim 8 , wherein the reaction is carried out at a pressure in a range of 1.0 to 3.0 bar[a].

10. The process recited in claim 3 , wherein the reaction is carried out at a pressure in a range 0.5 to 5.0 bar[a].

11. The process recited in claim 5 , wherein the reaction is carried out at a pressure in a range 0.5 to 5.0 bar[a].

12. The process recited in claim 1 , wherein the methanol is charged to the reactor at a rate of 0.1 to 5.0 kg per kg of fixed-bed catalyst per hour and the total mass ratio of fed ethanol to charged methanol is 0.01 to 1.0 kg/kg.

13. The process recited in claim 12 , wherein the methanol is charged to the reactor at a rate of 0.3 to 3.0 kg per kg of fixed-bed catalyst per hour.

14. The process recited in claim 13 , wherein the methanol is charged to the reactor at a rate of 0.2 to 2.0 kg per kg of fixed-bed catalyst per hour.

15. The process recited in claim 12 , wherein the ratio of the fed ethanol to the charged methanol is 0.02 to 0.8 kg/kg.

16. The process recited in claim 15 , wherein the ratio of the fed ethanol to the charged methanol is 0.005 to 0.5 kg/kg.

17. The process recited in claim 3 , wherein the methanol is charged to the reactor at a rate of 0.1 to 5.0 kg per kg of fixed-bed catalyst per hour and the total mass ratio of fed ethanol to charged methanol is 0.01 to 1.0 kg/kg.

18. The process recited in claim 5 , wherein the methanol is charged to the reactor at a rate of 0.1 to 5.0 kg per kg of fixed-bed catalyst per hour and the total mass ratio of fed ethanol to charged methanol is 0.01 to 1.0 kg/kg.

19. The process recited in claim 8 , wherein the methanol is charged to the reactor at a rate of 0.1 to 5.0 kg per kg of fixed-bed catalyst per hour and the total mass ratio of fed ethanol to charged methanol is 0.01 to 1.0 kg/kg.

20. The process recited in claim 1 , wherein the ethanol in the feeding is added at each reaction stage of the reactor.