Patent GB-873832-A (GB)
Title: Method of and apparatus for carrying out reactions between gases and liquids or fusible solids in fluidised beds
Inventor: DENT FREDERICK JAMES
IPC: B01J8/24
Filed: 1956-08-15
Abstract: 873,832. Gas manufacture. GAS COUNCIL. Aug. 15, 1957 [Aug. 15, 1956], No. 25001/56. Class 55 (2). Apparatus for carrying out reactions in a fluidized bed between gases and liquid or fusible materials which are liable under the action of heat to produce deposits or cause the agglomeration of particles in the fluidized bed, comprises a reaction vessel 10, Fig. 1, having a frustoconical lower portion 11 tapering downwardly from the full width of the vessel to the outer edge of a perforated wall 12, there being a gas inlet 13 in the perforated wall, with an atomizing nozzle 15, situated at or near the opening of the inlet 13 for directing atomized liquid upwardly into the incoming gas, and a chamber 18, surrounding the inlet 13, for introducing gas through the perforated wall 12 into the reaction vessel. The apparatus may be used in a process for the gasification of hydrocarbon-containing oils, such as petroleum oil or an oil or tar obtained by the distillation of coal, as in Specification 830,960 wherein the oil is subjected to interaction with hydrogen to produce a gas containing gaseous hydrocarbons. Particulate material from the fluidized bed 21 flows through the conduit 22 and is carried upwardly by the hydrogenating gas through conduit 14 back into the bed 21. A small amount of the hydrogenating gas is supplied through a pipe 17 for atomizing the oil which enters through pipe 16. About 75 to 90% of the gas is introduced at a velocity of 25 to 30 feet per second through the inlet 13. The remainder of the gas passes through pipe 19, chamber 18, and perforated wall 12, to enter the vessel 10 at a velocity of about 6 inches per second. In a modification, Fig. 2, an annular frusto-conical portion 31 forming the lower end of vessel 30, is bounded at its base by an annular perforated wall 32. The frusto-conical portion 31 surrounds the central vertical conduit 33 through which particulate material flows from the bed 55 to be returned through a plurality of gas supply conduits 40. A perforated baffle 53 separates the upper portion 54 of the fluidized bed from the main portion 55. The hydrogenating gas passes through pipe 36 and coil 37, to be heated by the portion 54 of the fluidized bed, and passes through pipe 38 to an annular header 39 which supplies the conduits 40. A plurality of gas inlets 34 are arranged in an annulus around the conduit 33, each inlet being supplied through a conduit 40. Nozzles 35 in the inlets 34 are supplied with oil through a pipe 45, annular header 46 and pipes 47, a small amount of gas entering from pipe 38 through pipe 43 and header 44. A branch pipe 41 and annular header 42 supply the gas through the perforated wall 32. In an example Kuwait crude petroleum oil was preheated to 300‹ C. and atomized by means of part of the hydrogenating gas preheated to 350‹ C. 90% of the gas was supplied at a velocity of approximately 25 feet per second through the main inlet and the remaining 10% at a velocity of 0.35 feet per second through the perforated wall, the hydrogenating gas being preheated to 505‹ C. and the temperature range in the fluidized bed, consisting of coke particles, being 780‹ C. to 820‹ C. The gas produced has the following average percentage by volume, carbon dioxide 0.3, unsaturated hydrocarbons 0.15, hydrogen 57.45, carbon monoxide 1.15, saturated hydrocarbons 39.2, nitrogen 1.75. A single reaction vessel having a plurality of oil and gas inlets may be divided into two or more separate compartments by vertical partitions so that different oils may be treated in different compartments. When two compartments are provided oil may be treated in one compartment and the tar condensed from the gas produced may be treated in the other compartment. Or three compartments may be used, the third being supplied with particulate material containing deposited carbon which is gasified. The higher temperatures required for hydrogenation of the tar and deposited carbon may be produced by admitting air or oxygen with the hydrogenating gas.