| 摘要 |
1,160,374. Purifying combustible gases. METALLGESELLSCHAFT A.G. and LINDE A.G. 15 Nov., 1966 [15 Nov., 1965], No. 51207/66. Heading C5E. Gases rich in CO 2 , at a pressure of at least 40 atmos., e.g. converted fuel gases, have their CO 2 removed by a three stage process. The gases entering at 10 are precooled at 1, e.g. by indirect heat exchange, until CO 2 begins to condense; they are then scrubbed at 3 at subzero temperature with an organic polar absorbent, e.g. acetone or methanol, which is regenerated by decompression in stages 6 . . . 8 and by stripping, e.g. with nitrogen, at 9; and they are then cooled to below the dew point of CO 2 in a tower 2 (at 4) by regenerated absorbent. Condensate from the precooler 1 is delivered at 39 to the base of the tower 2, from where used absorbent follows one of two paths; one is via heat exchangers 17, 14, 18, 19, in all of which it is cooled, one portion being returned to the scrubber 3 and another to the precooler 1 to prevent icing therein; the other path is through the regenerator 6 . . . 9 for recycling to the top of tower 2. Gases leave the regenerator at 23 and 30: at 23 they comprise mainly H 2 and CO, and may be recycled to the crude gas; at 30 (from stages 7, 8) they are mainly CO 2 , and are passed out of the apparatus by 31, 1. In a modification. Fig. 2 (not shown) intended for crude gases containing sulphur, absorbent only partly regenerated with respect to H 2 S is taken from a point in the stripper 9 and recycled to an intermediate point in the section 4, the rest of the apparatus being unchanged. In a specific example, in which the crude gas was obtained by steam-reforming a desulphurized light petrol, the converted gas at 110 atmos. pressure was cooled to -3‹ C. at 1, being contacted in the tower 2 with methanol which is at -60‹ C. at the top and -10‹ C. at the bottom. 17 is an ammonia-evaporator to make up cold losses. |
