Page 360 - Adsorbents fundamentals and applications
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DESULFURIZATION OF TRANSPORTATION FUELS  345

            Table 10.11. Comparison of various sorbents for N 2 /CH 4 separation using the standard
            five-step PSA cycle
             Run  Co-Current  Feed    CH 4 Product Purity  CH 4    CH 4 Product
             No.  Blowdown   Velocity  (%) — Average of  Product  Throughput (kg
                   Pressure   (m/s)  Co-Current Blowdown  Recovery  Product/h/kg of
                     (bar)               and Ads Step      (%)      Sorbent)
             ETS-4
             1        1       0.05         97.255         53.192      0.081
             2        1       0.12         95.244         71.281      0.172
             3        1       0.20         92.821         80.392      0.276
             4        2       0.20         92.732         79.327      0.272
             Purified clinoptilolite
             5        1       0.05         94.486         80.653      0.123
             6        1       0.12         92.050         87.812      0.212
             7        1       0.20         90.148         91.634      0.315
             8        2       0.05         95.382         73.131      0.112

             Mg-clinoptilolite
             9        1       0.05         89.057         63.151      0.114
             10       2       0.05         90.630         55.165      0.100
             11       4       0.05         93.273         41.648      0.075
            Feed = 85% CH 4 + 15% N 2 at 298 K and 7 atm. Desorption pressure = 0.4 atm. Column size:
            0.2 m diameter and 2.0 m length. Cycle step times: t press = 30 s; t ads = 60 s; t co bdn = 10 s; t cn bdn =
            30 s; t des = 60 s (Jayaraman et al., 2002).



            diesel from the current average of 500 ppmw to 15 ppmw by June 2006, and
            that in gasoline from 350 ppmw to 30 ppmw by January 2005 (Avidan et al.,
            2001). The detailed sulfur standards are complicated because different standards
            are applied to individual refinery, corporate pool, and per gallon basis (Avidan
            et al., 2001).
              Removal of sulfur-containing compounds is an important operation in
            petroleum refining, and is achieved by catalytic processes operated at elevated
                             ◦
            temperatures (∼300 C) and pressures (20–100 atm H 2 )using Co-Mo/Al 2 O 3
            or Ni-Mo/Al 2 O 3 catalyst (Gates et al., 1979). The hydrodesulfurization (HDS)
            process is highly efficient in removing thiols, sulfides, and disulfides, but
            less effective for thiophenes and thiophene derivatives. Thus, the sulfur
            compounds that remain in the transportation fuels are mainly thiophene,
            benzothiophene, dibenzothiophene, and their alkylated derivatives. The least
            reactive derivatives are the dibenzothiophenes with methyl groups at the
            4- and 6-positions, that is, positions adjacent to S. 4-methyldibenzothiophene
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