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, the process comprising: (a) providing a quantity of catalytic material within each reaction zone in an adiabatic catalytic fixed bed reactor; (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 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, such as heating at least a portion of the effluent of the said reaction zone designated as 1 to the inlet temperature of the reaction zone designated as 2; (d) transferring said at least portion of said effluent of said reaction zone with a designator equal 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 portion of said effluent originates, such as transferring said at least portion of said effluent of the said reaction zone designated as 1 to said reaction zone designated as 2; (e) maintaining each reaction zone with a designator equal or smaller than (n-m) at an average temperature higher or equal as in the reaction zone with designator smaller by one than that of said reaction zone, such as maintaining said reaction zone designated as 2 at an average temperature higher than or equal as in reaction zone designated as 1, 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 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 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) providing a quantity of catalytic material within each reaction zone in an adiabatic catalytic fixed bed reactor; (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 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, such as heating at least a portion of the effluent of the said reaction zone designated as 1 to the inlet temperature of the reaction zone designated as 2; (d) transferring said at least portion of said effluent of said reaction zone with a designator equal 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 portion of said effluent originates, such as transferring said at least portion of said effluent of the said reaction zone designated as 1 to said reaction zone designated as 2; (e) maintaining each reaction zone with a designator equal or smaller than (n-m) at an average temperature higher or equal as in the reaction zone with designator smaller by one than that of said reaction zone, such as maintaining said reaction zone designated as 2 at an average temperature higher than or equal as in reaction zone designated as 1, 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 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 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).