| 摘要 |
1,171,103. Hydrogen separation. GAS COUNCIL. 14 March, 1967 [24 March, 1966], No. 13123/66. Heading B1L. [Also in Division C5] In a process for hydrogenating a hydrocarbon feedstock to produce combustible gas containing substantial proportions of methane and ethane, the gas leaving the hydrogenator is contacted with an absorbent for the methane and ethane, and unabsorbed hydrogen is recovered and recycled to the hydrogenator. In the apparatus shown, vaporized light distillate feedstock at 1 divides into a main stream 2 and a minor stream 3. The minor stream is reformed into a hydrogenating gas in a catalytic steam reformer 4. After passage through a CO shift-reactor 5 and CO 2 remover 6, this gas is mixed with the recycled hydrogen-rich stream 7 and the stream of distillate 2, and the mixture is heated to 430‹C in heat exchanger 8 and passed to a gas recycle hydrogenator 9 e.g. as described in Specification 1,031,717. The product gas passes via the heat exchanger to a waste heat boiler 10, quench 11 and benzole removal system 12 and is then introduced into pressure absorber 14 at a temperature of 30‹C. The liquid absorbent may be e.g. pentane, hexane or octane, or a light petroleum distillate consisting predominantly of aliphatic hydrocarbons, or it may be a predominantly aromatic oil. It may have a 95% by volume b.p. of not more than 170‹C. Hydrogen-rich gas leaves the top of the absorber to be recycled and the absorbent with dissolved methane, ethane and other constituents is passed via heat exchanger 18 to a stripping column 16 in which the absorbed gases are recovered and pass via absorbent condenser 21 to line 23. The absorbent is regenerated and returned to the absorber via line 24 and cooler 25. If the absorbent is the same as the feedstock at 1, some of the regenerated absorbent can be fed back via line 27 and vaporizer 28; further, the feedstock, instead of being supplied at 1, may be fed in at 26 to the top of the absorber. |
