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344 main both in the gas phase and adsorbed. However, the top of the column is well 345 cleaned, with qCO2 → 0. In the following steps, pressure equalisations (without 346 CO2, as explained above) and repressurisation with H2 product leave the top of 347 the column free from CO2 while building up the pressure in the column. CO2 that 348 was still adsorbed at the end of the purge step remains adsorbed. The gas phase 349 concentration and solid loading at the start of the adsorption step show that the 350 increasing pressure causes readsorption of the CO2 from the gas phase. The top 351 of the column remains CO2 lean, and H2 can be produced again in the adsorption 352 step at a high carbon capture ratio. So, the purge steam effectively functions to free 353 the top part of the column from CO2, allowing to maintain a high carbon capture 354 ratio. Except for the depressurisation and the start of the purge step, there is no 355 significant pressure drop over the column (Figure 6). 356 3.1.2. Cycle performance 357 The single column performance, discussed in the previous section, forms the 358 basis for the performance of the 9 column SEWGS train. In terms of feed and prod- 359 uct streams, a single column operates in transient mode. Nine columns in parallel, 360 however, always have 2 columns in adsorption and in purge (Figure 3). Contin- 361 uous streams of H2 and CO2 are being produced. Nevertheless, transients remain 362 because of the depressurisation and repressurisation steps. These transients need to 363 be resolved for downstream processes (specifically the gas turbine section), which 364 can be done by buffering (using gas storage tanks or ‘surge tanks’ (Tondeur and 365 Wankat, 1985; Yang, 1987; Sircar, 1988)). Note that volumes in externals, piping, 366 etc. (that would cause back-mixing and buffering to some extent) are not accounted 367 for in the simulations. The performance of the SEWGS cycle is expressed in terms 368 of the time average CO2 capture rate, CO2 purity, and productivity required for 369 achieving 95% carbon capture ratio and 99% CO2 purity. The cycle performance 370 data are further discussed in § 3.2. 371 3.1.3. Implications of an adsorptive rinse 372 In the simulation of the SEWGS process, the underlying isotherm model is of 373 critical importance. The current work uses a newly developed binary adsorption 374 isotherm for the competitive adsorption of CO2 and H2O on K-HTC, measured up 375 to 24 bar partial pressure. Two aspects are new, therefore, the high pressure part 376 of the isotherm and the effect of competitive adsorption (cf. Boon et al. (2014)). 377 Indeed, as shown in Figure 5, both CO2 and H2O adsorb and desorb throughout 378 the SEWGS cycle. Especially during the rinse, a very high solid loading of H2O 379 prevails near the column entrance. At the same time, CO2 is partially desorbed and 380 displaced, exhibiting a small roll-up effect as discussed in § 3.1.1. 16PDF Image | High-temperature pressure swing adsorption cycle design for sorption
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