Start-up and wrong-way behavior in a tubular reactor: dilution effect of the catalytic bed

TLDR: In this paper, the start-up and wrong-way behavior of a fixed-bed reactor were analyzed through one-dimensional heterogeneous and pseudo-homogeneous models, based on methanol oxidation to formaldehyde.

About: This article is published in Chemical Engineering Science.The article was published on 2000-09-15 and is currently open access. It has received 25 citations till now. The article focuses on the topics: Packed bed & Steady state.

Figures

Fig. 2. Transient axial temperature pro"les for di!erent tH values: A-0; B-10; C-50; D-100; E-200; F-300; G-400; H-500; I-1000, obtained with the PH1DT model for a "xed bed packed with pure catalyst, by changing the feed temperature: (a) #5% (¹ o "530P557 K); (b) !5% (¹ o "557P530 K).

Fig. 3. Transient axial temperature pro"les for di!erent tH values: A-0; B-50; C-100; D-200; E-300; F-400; G-500; H-700; I-1000, obtained with PH1DT model for a "xed bed with two di!erent catalytic zones, by changing the feed temperature: (a) #5% (¹ o "530P557 K); (b) !5% (¹ o "557P530 K).

Fig. 10. Dynamic response to a negative ramp in feed and wall temperatures during 0)tH)800, followed by a positive ramp during 800)tH)1600, for the PH1DT model: (a) 3-D plot; (b) Temperature versus dimensionless time for di!erent axial positions.

Fig. 9. Dynamic response to a positive ramp in feed and wall temperatures during 0)tH)800, followed by a negative ramp during 800)tH)1600, for the PH1DT model: (a) 3-D plot; (b) Temperature versus dimensionless time for di!erent axial positions.

Fig. 4. Dynamic response to a step down in feed temperature (583P530 K). Axial temperature pro"les for di!erent dimensionless times, tH": A-0; B-10; C-50; D-100; E-200; F-300; G-500; H-1000: (a)- PH1DT model; (b) HT1DT d model.

Fig. 5. Dynamic response to a step down in feed temperature (583P530 K), for the PH1DT model.