Patent GB-451788-A (GB)
Title: Method for converting hydrocarbon gases into high anti-knock rating gasoline
IPC: C10G50/00
Filed: 1935-02-15
Abstract: A process of polymerizing olefine-containing gases comprises the steps of treating the said gases with a solvent which is a poor solvent for hydrogen and methane, separating the dissolved gases therefrom, polymerizing them under superatmospheric pressure, suddenly chilling the polymerization products while under high pressure by means of part of the liquid product previously produced to cool it below conversion temperature, fractionating the resulting mixture into uncondensed gas and condensed liquid, separating dissolved gases and recycling them to the polymerization zone.  A plant for carrying out the process comprises a coil 2 for heating hydrocarbon gases to 1300 to 1600 DEG  F., a condenser 22 and gas separator 24 from which liquid hydrocarbons may be withdrawn part to act as reflux liquid in the tar separator and part to act as shock-chilling material for the heated gases.  Gases pass from the separator 24 to a collecting tank 32 and thence to an absorber 56 wherein they are sprayed with light gas oil under pressure.  The oil and absorbed gases are passed to a stripping tower 76 where they are heated to 300--400 DEG  F., the evolved <PICT:0451788/IV/1> <PICT:0451788/IV/2> gases, which are rich in olefines, passing to a cooling coil 92, where heavier gases such as propylene and butylene are condensed, and then into a gas separator 94 whence the uncondensed gases are returned to the tank 32 and the condensed gases are forced into a polymerizing coil 104 and heated to 600 to 1300 DEG F. at pressures of 100 to 1500 pounds per square inch.  Byepass lines 128, 130, 132 are provided in the heating coil by which olefines may be fed into various portions thereof for control of temperature. From the coil the gases pass to an unheated reaction chamber 106 which may be byepassed by line 140 if desired.  The products then proceed by way of a tar separator 146 and condensing coil 150 to a gas separator 157.  Heavy polymers are withdrawn from the bottom of separator 146 and part thereof may be recycled through the polymerizing coil.  Gas from the separator 157 is returned to the coil 2; liquid is in part returned to the separator 146, and is in part returned through lines 170, 172 to the line 144 suddenly to chill the products below polymerizing temperature.  The remaining liquid from 157 is passed together with liquid from separators 24 and 56 to a tower still 191 where higher fractions such as butane, butylene, propane and propylene are separated and pass into a gas separator 195, the lighter for return to the absorber 56, the heavier to separator 94.  The liquid from the tower 191 passes to a storage tank 204.  Naphtha may be introduced into the system prior to the polymerizing stage through a line 210 and assists in controlling the temperature.  Clay or other polymerizing catalyst may be introduced through line 214.ALSO:<PICT:0451788/III/1> <PICT:0451788/III/2> A process of polymerizing olefine-containing gases comprises the steps of treating the said gases with a solvent which is a poor solvent for hydrogen and methane, separating the dissolved gases therefrom, polymerizing them under superatmospheric pressure, suddenly chilling the polymerization products while under high pressure by means part of the liquid product previously produced to cool it below conversion temperature, fractionating the resulting mixture into uncondensed gas and condensed liquid, separating dissolved gases and recycling them to the polymerization zone.  A plant for carrying out the process comprises a coil 2 for heating hydrocarbon gases to 1300 to 1600 DEG F., a condenser 22 and gas separator 24 from which liquid hydrocarbons may be withdrawn part to act as reflux liquid in the tar separator and part to act as shock-chilling material for the heated gases.  Gases pass from the separator 24 to a collecting tank 32 and thence to an absorber 56 wherein they are sprayed with light gas oil under pressure.  The oil and absorbed gases are passed to a stripping tower 76 where they are heated to 300--400 DEG  F, the evolved gases which are rich in olefines passing to a cooling coil 92 where heavier gases such as propylene and butylene are condensed, and then into a gas separator 94 whence the uncondensed gases are returned to the tank 32 and the condensed gases are forced into a polymerizing coil 104 and heated to 600 to 1300 DEG  F., at pressures of 100 to 1500 pounds per square inch. Byepass lines 128, 130, 132 are provided in the heating coil by which olefines may be fed into various portions thereof for control of temperature.  From the coil the gases pass to an unheated reaction chamber 106 which may be byepassed by line 140 if desired.  The products then proceed by way of a tar separator 146 and condensing coil 150 to a gas separator 157.  Heavy polymers are withdrawn from the bottom of separator 146 and part thereof may be recycled through the polymerizing coil.  Gas from the separator 157 is returned to the coil 2; liquid is in part returned to the separator 146, and is in part returned through lines 170, 172 to the line 144 suddenly to chill the products below polymerizing temperature.  The remaining liquid from 157 is passed together with liquid from separators 24 and 56 to a tower still 191 where higher fractions such as butane, butylene, propane and propylene are separated and pass into a gas separator 195, the lighter for return to the absorber 56, the heavier to separator 94.  The liquid from the tower 191 passes to a storage tank 204. Naphtha may be introduced into the system prior to the polymerizing stage through a line 210 and assists in controlling the temperature.  Clay or other polymerizing catalyst may be introduced through line 214.