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5 Validation of the mathematical model 70 Tab. 5.3.2-1 PSA performance at different N2-receiver volumes at product purity of 1000 ppm O2 5 92.80 90.30 2.694 3.27 3.239 0.948 12 97.35 97.60 -0.257 3.18 3.147 1.038 Tab. 5.3.2-2 PSA performance at different N2-receiver volumes at product purity of 10 ppm O2 5 22.82 11.00 51.797 9.65 18.282 -89.451 12 29.64 26.14 11.795 7.78 8.601 -10.553 N2-receiver volume [L] Productivity [m3n/h N2 / m3 CMS] Air demand [m3n/h air / m3n/h N2] EXP SIM Φ [%] EXP SIM Φ [%] 7 95.00 93.90 1.158 3.22 3.187 1.025 N2-receiver volume [L] Productivity [m3n/h N2 / m3 CMS] Air demand [m3n/h air / m3n/h N2] EXP SIM Φ [%] EXP SIM Φ [%] 7 25.47 17.20 32.470 8.84 12.273 -38.835 Fig. 5.3.2-2 Experimental pressure profiles of adsorber columns and N2-receiver tank at different N2- receiver volumes: (a) 12 L, (b) 7 L, (c) 5 L Tab. 5.3.2-1 shows that the model predicts the influence of the N2-receiver volume sufficiently at the lower product purity level of 1000 ppm O2. However, as the product purity requirement increases, the PSA simulation exhibits a significant relative error with the reduction of N2- receiver volume. As presented in Fig. 5.3.2-3, the quantitative representation of experimental pressure profiles becomes more challenging the smaller the tank volume. Dynamic process simulation exhibits a bigger slope of the N2-receiver pressure profile during the pressurisation and back-flow steps, respectively. Therefore, the superficial velocity of the gas in the packed bed is overestimated, especially in the initial phase of the production step, so the contact time between phases is reduced and the premature column breakthrough occurs consequently. Since the efficient production of high-purity nitrogen (10 ppm O2) is promoted at prolonged cycle times, as already proofed in Chapter 5.2.1, the productivity is underestimated to maintain the target purity level. Hence, the air demand is overestimated accordingly.PDF Image | Modelling and Simulation of Twin-Bed Pressure Swing Adsorption Plants
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