R&D on Hydrogen Production by Autothermal Reforming

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Gasification rate (%) Temperature (°C) 4 Time (hr) Upper catalyst layer Middle catalyst layer Lower catalyst layer Figure 3.1.4: Catalyst Layer Temperature Distribution (650°C) in Autothermal Reforming Reaction at 1 Nm 3 /hr Gasification rate (%) C2-C4 selection rate Reaction temperature (°C) Figure 3.1.5: Impact of Reaction Temperature on Gasification Rate and C2-C4 Hydrocarbon Selection Rate C2-C4 selection rate (%) (H2 + CO) yield (%) Reaction temperature (°C) Equilibrium value Equilibrium value Figure 3.1.6: Impact of Reaction Temperature on Hydrogen Yield and Hydrogen Production Volume 3.2 Basic Design of Autothermal Reforming - Fuel Processing System 3.2.1 ATR-FPS Basic Design (1) ATR-FPS outline and design conditions ATR-FPS is a hydrogen production process that uses the autothermal reforming method. In the latest investigation, two units each of shift and selective oxidation reactor were installed so that CO shift or selective removal would be accomplished more securely. The ATR-FPS flow process is shown in Figure 3.2.1. (H2 + CO) Production Volume (Nm 3 /hr)
Figure 3.2.1: ATR-FPS Flow Diagram (2) Raw material specifications 5 Autothermal reform type hydrogen production Reactor system Flow sheet In the latest investigation, the crude oil composition ratio used was n-decane:n-butyl-cyclohexane:diethyl benzene (= 64:16:20 mol%); crude oil molecular formula was C11.3H22.3; crude oil molecular volume was 158.55; crude oil density (25°C) was 756.6 kg/m 3 , and crude oil flow volume was 380 ml/hr (= 287.6 g/hr = 1.813 gmol/hr). Steam and air supplied for reforming were each set at O2/C = 0.45 and S/C = 2.44, the conditions for attaining heat balance. In addition, as opposed to CO concentration at the shift reactor outlet, O2/CO was set to 1.5 (3 times the theoretical ratio) at the first CO selective remover and to 0.15 at the second reactor (1/10 the volume at the first reactor). (3) Substance balance Table 3.2.1 presents substance balance as calculated based on the conditions given in Section 3.2.1 (2). The following was also clarified. Hydrogen was produced at approximately 950 Nl/hr from raw material kerosene at 380 ml/hr (approx. 290 g/hr). The composition of hydrogen-rich gas product was H2 (42.83 mol%): CH4 (0.015 mol%): CO2 (20.66 mol%): N2 (36.49 mol%), with the ratios of H2, CO2 and N2 at roughly 6:3:5.
Page 1 and 2: 2002.08.sin 2.3 R&D on Hydrogen Pro
Page 3: Figure 3.1.2: O2/C Ratio vs S/C Rat
Page 7 and 8: Table 3.2.2: Heat Balance Received
Page 9 and 10: Figure 3.3.3. It was recognized tha
Page 11 and 12: 3.4.2 Reforming Reactivity of Norma
Page 13 and 14: 3.4.4 Reforming Reactivity of Each
Page 15 and 16: Table 3.5.2: List of Catalysts for
Page 17: 4.3 Development of Autothermal Refo

R&D on Hydrogen Production by Autothermal Reforming

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