Patent GB-359023-A (GB)
Title: An improved process and apparatus for hydrogenating hydrocarbons
IPC: C10G69/00
Filed: 1930-07-15
Abstract: Hydrocarbon oils are admitted, preheated if desired, to a vaporizer 7, an intermediate condensate is circulated with or without the heavier liquid residue through cracking and hydrogenating zones such as coils 25, 26, 27 with or without conversion chambers 30, 32, and with or without catalysts, and the products of hydrogenation are returned to the vaporizer.  Vapours withdrawn at 55 are worked up for gasoline and other light fractions.  Molybdenum and tungsten catalysts are mentioned.  The apparatus is similar to that described in Specification 359,022 (Fig. 3, Provisional, and Figs. 4 and 5, Complete), with additions and modifications required for the hydrogenation process.  The hydrocarbons are treated in the coils at temperatures between 750 DEG  and 1500 DEG  F. under pressures between 50-300 atmospheres or more, and in the conversion chambers at 750 DEG  and 850 DEG  F. and under similar pressures.  When hydrogenation is effected in coils only the temperature is between 750-1500 DEG  F. under similar pressures, while the pressure in the vaporizer 7 may be atmospheric, or 5 atmospheres or more. Hydrogenation is effected in the presence of an excess of hydrogen gas or of gases containing free hydrogen, or in the presence of gases or other substances capable of liberating free hydrogen or gaseous hydrocarbons in excess.  Substances specified are natural gas, coal gas, steam and iron, water and alkali metals or carbide, naphthenes and nickel, hexamethylene and porous porcelain.  Such materials or the catalysts or both may be spread on porous trays in the conversion chambers, or circulated with the oil in suspension or in colloidal solution, or they may be placed in the section 27 of the coil 23, this section being made of larger diameter tubing than the others. The conversion chambers 30, 32 may be provided with agitators or the contents may be recirculated by a pump 52 either through the chambers or through the coils.  The chambers 30, 32 may be operated in series or in parallel.  Hydrogenating gas may be delivered from a source 99 by pump 101 through a heating <PICT:0359023/III/1> coil 102 and line 103 to the inlet of the coil 23, or through branches 105, 104, 106 to an intermediate point of the coil, to its outlet, or direct to the conversion chambers 30, 32.  The intermediate condensate from the vaporizer 7 may be recirculated, directly or after removal of the lighter fractions by distillation, and the coil section 27 may be byepassed, as in Specification 359,022.  The heavy residue from the vaporizer may be withdrawn at 44 or recirculated by lines 45, 47, 48, or hydrogenated in a separate system, or it may be distilled at 74, 75 and the final residues returned to the hydrogenation system through lines 113, 45.  The vapour line 54 to 93 includes a separator 109 from which hydrogenating gas is returned to the supply 99 through line 112 and purifiers 114, 114<1> for absorption of hydrogen sulphide and of volatile oils.  When molybdenum, tungsten, and like catalysts are used, the hydrogen sulphide is not removed.  Gases and vapours from the line 112, and additional hydrogenating gases such as natural gas or refinery gas, may be heated to dissociation temperature in a furnace coil or in an electric are furnace, as described in Specification 359,026, before they are introduced into the hydrogenation system.