Crude benzene catalytically refined with hydrogen containing carbon monoxide under such conditions that during the refining such an amount of carbon monoxide reacts with hydrogen that a temperature rise of 10-50 DEG C. occurs in the reaction zone. The process is carried out using 0.2-2.5 cu. metres of hydrogen containing carbon monoxide at a hydrogen partial pressure of 10-60 atm., a throughput of 0.3-2.5 kg. of feedstock per litre of catalyst per hour, and an initial temperature of 280-450 DEG C. in the reaction zone. The treatment may remove sulphur, oxygen and nitrogen compounds. Catalysts referred to are active catalysts such as the compounds of metals of Groups 5, 6 and 8, e.g. oxides, sulphides, silicates, halides, chromates, phosphates, borates, carbonates and salts of organic acids of Na, Mo, W, U, Cr, Fe, Ni, Co, Pt, Pd and Ru; these may be supported on synthetic active carriers, e.g. activated alumina or synthetic silicates, such as those of the metals of Groups 6-8 and of Al, Mg, Zn, Zr and the rare earths, catalysts of medium activity such as the compounds, such as the oxides, sulphides or silicates, of metals of Groups 5, 6 or 8, on natural carriers, e.g. bauxite, bleaching earths or pumice; and less-active catalysts such as the compounds of Groups 1-4 and 7, e.g. oxides of Cu, Ag, Au, Mg, Zn, Cd, Al, Ti, Be, Zr and Mn. The hydrogen may contain 4-20 per cent of carbon monoxide, e.g. coke oven gas, illuminating gas or water gas may be used. The gases may first be freed from unsaturated compounds, carbon dioxide and nitrogen oxide; the gas may be washed under pressure with the initial feedstock to be refined, dissolved gases separated therefrom, and the initial material refined with the purified gases. The crude material may be heated before the hydrogenation step to allow polymers to form. In an example, the refining of crude benzene is described, using coke oven gas containing 54 per cent of hydrogen, an initial temperature of 350 DEG C., a pressure of 50 atm., a hydrogen partial pressure of 18 atm., a feed rate of crude benzene of 1.5 kg./1./hr., a gas rate of 1.8 cu.m./kg. crude benzene, and a catalyst consisting of activated alumina impregnated with 10 per cent of molybdic acid.ALSO:Crude gasoline, crude kerosene and crude gas oil are catalytically refined with hydrogen containing carbon monoxide under such conditions that during the refining such an amount of carbon monoxide reacts with hydrogen that a temperature rise of 10-50 DEG C. occurs in the reaction zone. The process is carried out using 0.2-2.5 cu. metres of hydrogen containing carbon monoxide at a hydrogen partial pressure of 10-60 atm., a throughput of 0.3-2.5 kg. of feedstock per litre of catalyst per hour, and an initial temperature of 280-450 DEG C. in the reaction zone. The treatment may remove sulphur, oxygen and nitrogen compounds. Catalysts referred to are active catalysts such as the compounds of metals of Groups 5, 6 and 8, e.g. oxides, sulphides, silicates, halides, chromates, phosphates, borates, carbonates and salts of organic acids of Na, Mo, W, U, Cr, Fe, Ni, Co, Pt, Pd and Ru; these may be supported on synthetic active carriers, e.g. activated alumina or synthetic silicates, such as those of the metals of Groups 6-8 and of Al, Mg, Zn, Zr and the rare earths; catalysts of medium activity such as the compounds, such as the oxides, sulphides or silicates, of metals of Groups 5, 6 or 8, on natural carriers, e.g. bauxite, bleaching earths or pumice; and lessactive catalysts such as the compounds of Groups 1-4 and 7, e.g. oxides of Cu, Ag, Au, Mg, Zn, Cd, Al, Ti, Be, Zr and Mn. The hydrogen may contain 4-20 per cent of carbon monoxide, e.g. coke oven gas, illuminating gas, or water gas may be used. The gases may first be freed from unsaturated compounds, carbon dioxide and nitrogen oxide; the gas may be washed under pressure with the initial feedstock to be refined, dissolved gases separated therefrom, and the initial material refined with the purified gases. The crude material may be heated before the hydrogenation step to allow polymers to form. In examples, the refining of crude kerosene using town gas, an initial temperature of 335 DEG C. and a catalyst consisting of activated alumina and 10 per cent of molybdenum and cobalt sulphides, and of gasoline with coke oven gas using an initial temperature of 310 DEG C. and a catalyst consistng of tungsten and nickel sulphides, is described.
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