Sulfur and nitric oxide (NO) are given as the products by the reaction of hydrogen sulfide and nitric oxide. For instance, Copolymer 3 achieves much greater hydrogen-methane selectivity than Cytop® and Hyflon® AD60, while its hydrogen permeance is greater than that of Cytop® and less than that of Hyflon® AD60. In this process, the molar concentration of hydrogen sulfide in the feed-gas stream 401 is reduced by a factor of 20-30 compared with the concentration of hydrogen sulfide in the third membrane-stage permeate stream 482. For example, if the composition of Monomer D is greater than about 30 mol % the resulting copolymers are completely amorphous and soluble in fluorinated solvents. In some instances a concentration greater than about 90 mol % hydrogen sulfide can be achieved. 4. The second permeate-in-series retentate stream 451, which contained about 2 mol % hydrogen sulfide, was combined with the feed-gas stream 401 to be recycled through the process. 4b (Table 6). However, this configuration required the most membrane area and compressor power of the configurations shown in FIG. Because monomer reactivity ratios are nearly equal, resulting copolymers form an ideal random structure. Using membranes in this configuration with carbon dioxide-hydrogen sulfide selectivity of at least 10 produces a second permeate-in-series permeate stream 452 that has a sufficiently low concentration of hydrogen sulfide to allow safe discharge without further treatment (other than catalytic or thermal oxidation). Nitric acid decomposition 4c; and a three-stage configuration in FIG. Membranes having the perfluoropolymers described in this specification can be designed to be used in membrane modules using conventional techniques. About 95-99% of the hydrogen sulfide in feed-gas stream 401 was concentrated in first permeate-in-series retentate stream 441, and only a few percent ends up in second permeate-in-series permeate stream 452 (Table 7). However, this configuration can still be used with an additional polishing step. Multiple membrane modules can be manifolded together in a membrane separation unit to achieve a desired membrane area. To illustrate the process of FIG. 8. TABLE 4 Pure and mixed gas permeance and selectivities for membranes having commercial perfluoro- polymers and copolymers of Monomers B and H Pure gasa Mixed gasb Permeance Selec- Permeance Selec- (gpu) tivity (gpu) tivity Membrane N2 CO2 CO2/N2 H2S CO2 CO2/H2S Hyflon ® 26 160 6.2 12.2 170 14 AD40 Hyflon ® 79 500 6.4 38 490 13 AD60 Copolymers 37 280 7.7 5.3 170 32 of Mono- mers B and H aPure feed gas at 50 psig feed pressure and 30° C. bMixed feed gas containing 33 mol % hydrogen sulfide in carbon dioxide at 50 psig and 30° C. (saturated with H2O). Furthermore, the terms “comprising,” “including,” “having,” and the like, as used with respect to embodiments of the present disclosure, are synonymous. The process of claim 2, further comprising the step of: 4. The processes illustrated in FIG. TABLE 2 Glass transition temperature (Tg) resulting from various copolymer compositions of Monomer D and Monomer H Monomer D Monomer H composition composition Tg Polymer (mol %) (mol %) (° C.) Monomer D 100 0 165 Copolymer 1 74 26 155 Copolymer 2 58 42 145 Copolymer 3 43 57 125 Copolymer 4 20 80 106 Monomer H 0 100 228a aMelting temperature (Tm). 198-202; Mikeš et al., “Characterization and properties of semi crystalline and amorphous perfluoropolymers: poly(per-fluoro-2-methylene-1,3-dioxolane),” Polym. 2. Mixed feed-gas stream 402 is fed to first retentate-in-series membrane stage 420 where it is separated using a carbon dioxide-selective membrane to obtain first retentate-in-series retentate stream 421 and first retentate-in-series permeate stream 422; the first retentate-in-series retentate stream 421 and the first retentate-in-series permeate stream 422 being enriched in hydrogen sulfide and carbon dioxide respectively.

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