Process for converting LPG to higher hydrocarbon(s)
AssigneeSabic Global Technologies B.V.
InventorChristoph Dittrich
Life of this patent
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Abstract
A process for converting a feed comprising C2-C4 alkanes to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (n-m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said a feed comprising C2-C4 alkanes to an effluent having said higher hydrocarbon(s). An object of the present invention is to provide a process for converting LPG to higher hydrocarbon(s) including aromatic hydrocarbon(s) wherein a high reactant, i.e. ethane, propane and/or butane, conversion can be achieved.
Claims21
A process for converting LPG to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (n-m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said LPG to an effluent having said higher hydrocarbon(s), wherein each reaction zone is initially numbered serially with a designator from 1 to n, wherein said total number of reaction zones, n, is at least 3, said total number of reaction zones not participating in the conversion process, m, is at least 1, and (n-m) is at least 2, the process comprising:
- (a) providing a quantity of catalytic material within each reaction zone;
- (b) providing to the reaction zone designated as 1 a hydrocarbon feedstock containing LPG;
- (c) heating at least a portion of the effluent of each reaction zone with a designator equal to or smaller than (n-m-1) to the inlet temperature of the reaction zone with a designator larger by one than that of the reaction zone from which said effluent originates;
- (d) transferring said at least a portion of said effluent of each reaction zone with a designator equal to or smaller than (n-m-1) to the reaction zone with a designator larger by one than that of the reaction zone from which said at least a portion of said effluent originates;
- (e) maintaining each reaction zone with a designator equal to or smaller than (n-m) at an average bed temperature higher than or equal to an average temperature in the reaction zone with a designator smaller by one than that of said reaction zone, feeding the effluent from the reaction zone with the designator (n-m) to another process unit, and regenerating the reaction zones with a designator larger than (n-m), followed by
- (f) terminating transferring effluent from the reaction zone with the designator (n-m-1) to the reaction zone with the designator (n-m);
- (g) starting regenerating said reaction zone with the designator (n-m) containing deactivated catalytic material;
- (h) raising the inlet temperature of each reaction zone with a designator equal to or smaller than (n-m-1) to the former inlet temperature of the reaction zones with a designator larger by one than that of said reaction zone, respectively;
- (i) changing the value of each designator equal to or smaller than (n-1) to a number larger by one than its initial value, and changing the value of the designator with a value of n to 1,
- (j) repeating steps (b) to (i).
A process for converting LPG to higher hydrocarbon(s) including aromatic hydrocarbon(s) in n reaction zones operated in series, wherein m reaction zones are not participating in the conversion process and only (n-m) reaction zones are operated under reaction conditions sufficient to convert at least a portion of said LPG to an effluent having said higher hydrocarbon(s), wherein each reaction zone is initially numbered serially with a designator from 1 to n, wherein said total number of reaction zones, n, is at least 3, said total number of reaction zones not participating in the conversion process, m, is at least 1, and (n-m) is at least 2, the process comprising:
- (a) providing a quantity of catalytic material within each reaction zone;
- (b) providing to the reaction zone designated as 1 a hydrocarbon feedstock containing LPG;
- (c) heating at least a portion of the effluent of each reaction zone with a designator equal to or smaller than (n-m-1) to the inlet temperature of the reaction zone with a designator larger by one than that of the reaction zone from which said effluent originates;
- (d) transferring said at least a portion of effluent of each said reaction zone with a designator equal to or smaller than (n-m-1) to the reaction zone with a designator larger by one than that of the reaction zone from which said at least a portion of said effluent originates;
- (e) maintaining each reaction zone with a designator equal to or smaller than (n-m) at an average bed temperature higher than or equal to an average temperature in the reaction zone with a designator smaller by one than that of said reaction zone, feeding the effluent from the reaction zone with the designator (n-m) to another process unit, and regenerating the reaction zones with a designator larger than (n-m), followed by
- (f) terminating transferring effluent from the reaction zone designated as 1 to the reaction zone designated as 2;
- (g) starting regenerating the reaction zone designated as 1 containing deactivated catalytic material;
- (h) decreasing the inlet temperature of each reaction zone with a designator larger than 1 and equal to or smaller than (n-m) to the former inlet temperature of the reaction zones with a designator smaller by one than that of said reaction zone, respectively;
- (i) changing the value of each designator equal to and larger than 2 to a number smaller by one than its initial value, and changing the value of the designator with value 1 to n,
- (j) repeating steps (b) to (i).
Dependencies are inferred from the claim text.