| 摘要 |
<PICT:0832009/IV (b)/1> A hydrocarbon monomer is recovered from a liquid polymerization reaction mixture obtained from the copolymerization of an aliphatic conjugated diene and a vinylidene hydrocarbon by introducing the liquid into a first separation zone wherein a substantial portion of the hydrocarbon is recovered as a vapour, passing the liquid effluent into a second separation zone, operated under reduced pressure, from which is recovered the remainder of the hydrocarbon as a vaporous stream containing atmospheric gases as impurity, contacting the vapour stream with a selective absorbent liquid to dissolve the hydrocarbon, the atmospheric gases being removed, and recovering the hydrocarbon from the absorbent. The invention is particularly applicable to the recovery of unreacted diolefine monomers from synthetic rubber latices produced, for example, by the hot or cold rubber copolymerization of butadiene, pentadiene, isoprene, piperylene, methylpentadiene or 2,3-dimethylbutadiene with styrene. The recovery of the monomers by a vacuum recovery introduces undesirable small quantities of atmospheric oxygen in the vapour phase. A latex from a butadiene-styrene copolymer plant enters separator 12 by line 11; the separator is operated at 80-120 DEG F. and 15-25 p.s.i.a. Butadiene vapours with a little styrene pass by line 13, foam trap 14, are compressed and cooled and collected as liquid in collector 19. Vapours leave by line 20 through a pressurereducing valve and is further treated as described below. Liquid leaving by line 22 is divided into two streams, one passing to vessel 37, the other passing by line 23, a polymerization inhibitor being added, to fractionator 24 where butadiene, removed by line 29 to a purification recovery stage, and styrene, removed by line 31, are separated; the styrene passes to vacuum flash evaporator 33 where traces of butadiene are p removed as vapour by line 34 to be treated as described below. Liquid latex effluent from separator 12 passes to flash evaporator 42, operated at 80-120 DEG F. and 100-250 mm. mercury, from which residual butadiene is recovered as vapour-containing oxygen and nitrogen by line 43, foam trap 44 and line 47 where it is joined by vapours from line 34. The combined vapours pass through steam ejector 48, are cooled and water separated. The vapours are joined by vapours from lines 20 and 92 and 98 described below, compressed and passed to packed tower 57. Bottoms are passed by line 96 to flash evaporator 97 from which liquid is recycled to separator 12 and vapours leave by line 98. Vapours from tower 57 are cooled and the liquid obtained passed to absorber tower 63 to the top of which is supplied an absorbent liquid which is preferably a narrow-boiling hydrocarbon fraction between the hexane and gas oil ranges such as a heavy naphtha oil, mineral seal oil, kerosene or light gas oil or furfural. Conditions in the tower may be 80-120 DEG F. at the top, 100-140 DEG F. at the bottom and 100-125 p.s.i.a. Oxygen and nitrogen are removed at the top. Absorbent containing butadiene is passed to the stripper 68 operated at 25-90 DEG F. at the top, 150-350 DEG F. at the bottom and 15-50 p.s.i.a. Stripped absorbent is withdrawn at the bottom and recycled to the absorber tower. Vapours are compressed, cooled and passed to accumulator 84 from which liquid butadiene is passed to flash zone 89. Liquid from zone 89 is passed to vessel 37 from which butadiene may be recycled to the copolymer plant. Vapours from accumulator 84 and flash zone 89 are recycled by line 92.
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