Patent GB-881753-A (GB)
Title: Improvements in or relating to the manufacture of motor benzol
IPC: C10C1/20
Filed: 1958-02-06
Abstract: <PICT:0881753/III/1> A process for manufacturing motor benzol from crude benzol by catalytic hydrofining is characterized by heating the liquid crude benzol to 210 DEG -230 DEG  C. in a continuous heater at a sufficient pressure to maintain at least 90% in the liquid state; expanding the heated material in a chamber to vaporize the benzol hydrocarbons and leave a liquid residue containing higher boiling hydrocarbons and compounds formed by polymerization of polymerizable constituents of the crude benzol; condensing the benzol hydrocarbon vapours; heating the condensate to about 350 DEG  C. in a second continuous heater at a pressure high enough to maintain at least 90% in the liquid state; expanding it in an evaporator to vaporize the benzol; mixing it with preheated hydrogen gas; and introducing it into the catalyst bed of a hydrofining zone.  Alternatively the hydrogen gas may be present during the second expansion of the material.  In the Figure, the crude benzol is introduced at 1, heated to 220 DEG  C. in coil 4, expanded in chamber 7, condensed in condenser 10, heated to 350 DEG  C. in coil 13, mixed with coke oven gas at 390 DEG  C. in mixer 15, expanded in chamber 18, hydrogenated in the catalyst bed 20 of hydrofining zone 19, and condensed in condenser 23.  The hydrofined benzol is discharged through line 24 and the unused hydrogen is recycled through line 25.  A benzol fraction having a freezing point of 5.4 DEG  C. and a sulphur content of less than 1 ppm can be obtained from the product withdrawn through line 24. Specification 692,639 is referred to.ALSO:<PICT:0881753/IV (b)/1> A process for manufacturing motor benzol from crude benzol by catalytic hydrofining is characterized by heating the liquid crude benzol to 210 DEG C.-230 DEG C. in a continuous heater at a sufficient pressure to maintain at least 90% in the liquid state; expanding the heated material in a chamber to vaporize the benzol hydrocarbons and leave a liquid residue containing higher boiling hydrocarbons and compounds formed by polymerization of polymerizable constituents of the crude benzol; condensing the benzol hydrocarbon vapours; heating the condensate to about 350 DEG C. in a second continuous heater at a pressure high enough to maintain at least 90% in the liquid state; expanding it in an evaporator to vaporize the benzol; mixing it with preheated hydrogen gas; and introducing it into the catalyst bed of a hydrofining zone.  Alternatively, the hydrogen gas may be present during the second expansion of the material.  In the Figure the crude benzol is introduced at 1, heated to 220 DEG C. in coil 4, expanded in chamber 7, condensed in condenser 10, heated to 350 DEG C. in coil 13, mixed with coke oven gas at 390 DEG C. in mixer 15, expended in chamber 18, hydrogenated in the catalyst bed 20 of hydrofining zone 19, and condensed in condenser 23.  The hydrofined benzol is discharged through line 24 and the unused hydrogen is recycled through line 25.  A benzol fraction having a freezing point of 5.4 DEG C. and a sulphur content of less than 1 ppm can be obtained from the product withdrawn through line 24. Specification 692,639 is referred to.