Patent GB-338150-A (GB)
Title: Improved method and apparatus for destructive hydrogenation of carbonaceous liquids
IPC: C10G1/06
Filed: 1929-08-13
Abstract: 338,150. Tate, W. R., Stephenson, H. P., and Imperial Chemical Industries, Ltd. Aug. 13, 1929. Hydrogenation, destructive.-In the destructive hydrogenation of carbonaceous liquids such as oils or of suspensions of coal in oils &c., a vertical reaction vessel and a vessel for the separation of liquid and vaporous products are housed in the same high pressure vessel, the separator being maintained at a temperature lower than the reaction vessel by using the reacting products to preheat the liquid or gaseous materials or both of these. The entering hydrogen may be divided into two streams, one passing over an electric heater and into the reaction chamber and then serving to cool the reaction products before proceeding to the heater. Alternatively, the incoming liquid may first be preheated by the outgoing liquid reaction products and then, in conjunction with part of the hydrogen, by the reaction products before their separation into liquid and vapour, the other part of the hydrogen being partly heated by the outgoing vaporous reaction products and partly by an electric heater. In the form shown in Fig. 1, a reaction vessel 1 and a separator 2 are housed within a high-pressure vessel 3, there being provided next to the high pressure wall an annular jacket 4, through which the hydrogen passes, entering at 5 and leaving at 6. The intervening space is filled with asbestos or asbestos cement. The hydrogen which leaves at is divided into two streams, one passing directly by a pipe 10, which may be valved, to a chamber 21 containing an electric heater 12 and being in communication with the packing space, and the other passing first through a valved pipe 8 to a preheater 9 formed by a pipe 17 which delivers the reaction products to the separator 2, the pipe 8 then conveving the hydrogen to the chamber 21. From the chamber 21 the hydrogen passes by a central pipe 13 to the bottom of the reaction chamber. Passage through the preheater 9 reduces the temperature of the reaction products from say 420‹ C. to 300‹ C. so that heavy oils pass away from the separator 2 by a pipe 19 and vapours of light and middle oils leave, with the gases, by a pipe 18, the heavy oils serving to preheat, at 15, fresh material entering by a pipe 14. Heat exchange may be effected between hydrogen in the pipe 10 and the products leaving by the pipe 18. The separated heavy oil after removal of solid material may be returned for further treatment mixed, if desired, with powdered coal. In the form shown in Fig. 2, the hydrogen, after passing through the annular jacket 4, is preheated at 7 by the vapourous reaction products, passing by a pipe 8 from the separator 2, and is divided into two streams, one passing bv a pipe 12 past an electric heater 9 and by a pipe 17 to the base of the reaction chamber 1, and the other by a valved pipe 13 to a tubular preheater 15 heated by the reaction products passing through a pipe 16. From the preheater the reaction products pass by a pipe 19 to the separator 2 whence the vapours and gases pass from the upper part by way of the pipe 8 and preheater 7 to the outlet pipe 20, and the liquid products pass from the lower part by a pipe 21 to a tubular preheater 22 and out by a pipe 24. Fresh material enters the preheater 22 by a pipe 23 and passes by a pipe 14 to the preheater 15 entering, together with the hydrogen, the reaction chamber by a pipe 18.