DEM Analysis of Particle Trajectory in Circumferential Direction at Bell-less Top

Abstract

Uneven charging of burden in circumferential direction has a negative impact to stable operation of ironmaking blast furnaces. To visualize and prevent uneven charging, particle flow in bell-less top with parallel hoppers was simulated with different tilting angles of rotating chute by Discrete Element Method (DEM). The simulation revealed that the particles flowed decentering in the vertical chute, which led to circumferential imbalance in the trajectory from the rotating chute. The tendency of imbalance against the circumferential direction also differed by the chute titling angle. This tendency was also confirmed in the scaled down experimental work. As a counter measure, DEM simulations showed that after tapered vertical chute installed was improved the circumferential imbalance significantly.

Causes of Particle Trajectory Fluctuation on the Rotating Chute in Circumferential Direction at Bell-less Top with Parallel Type Hoppers

“…cross-section of the chute, but such a trajectory fluctuation against the circumferential direction is not clearly demonstrated. On the contrary, Narita et al 13) attributed the change in the particle trajectory to the interaction between the centrifugal force and the named curvature force. Therefore, it is essential to elucidate the reasons for the particle trajectory fluctuation in the circumferential direction at the bell-less top with parallel type hoppers.…”

“…The DEM and theoretical models are firstly validated against the results from the reference. 13) Three chute rotating angles are defined in the Fig. 4 to distinguish the quantitative results.…”

Detailed Modeling of Melt Dripping in Coke Bed by DEM – SPH

“…Shungo NATSUI, 1) * Ko-ichiro OHNO, 2) Sohei SUKENAGA, 3) Tatsuya KIKUCHI 1) and Ryosuke O. SUZUKI 1) dimensionless correlation between hs and parameters from Buckingham's π theorem, 13) it is determined by the force balance of gravity and surface tension, and a modified capillary number Cp m is widely used. Although various forms of Cp m have been proposed, for liquids, it is generally defined as (gravitational force)/(capillary force), e.g., Cp m = ρg(ϕd p ) 2 / σ(1+cosθ)(1−ε) 2 for adhesion wetting mode 14) and Cp m = ρg(d p ϕε) 2 /|σcosθ|(1−ε) 2 for immersion wetting mode.…”

“…Recently, a detailed numerical model of the ironmaking blast furnace has been developed for gaining a better understanding of in-furnace phenomena 1) such as burden distribution, 2,3) gas-solid motion, 4) heat and mass transfer, 5,6) gas injection behavior, 7,8) fines clogging, 9) liquid flow in the tapping process, 10) and melt dripping in a coke-packed bed. 11) Nevertheless, the dripping behavior of the melt in the lower part of the blast furnace is still difficult to control; this remains one of the most important issues from the viewpoint of operational stability because it significantly decreases the permeability of the packed bed.…”

Experimental Study of the Effects of Operation Conditions on Burden Distribution in the COREX Melter Gasifier

“…and shaft furnace including falling trajectory, [7][8][9][10][11][12] burden profile, [13][14][15] burden pile structure [16][17][18][19] and the descent of burden layer, 20,21) only a few studies were dedicated to the burden distribution in the MG to achieve reasonable gas flow, mainly due to the short history of the process and limited experimental techniques. [22][23][24][25][26][27][28][29] Several numerical studies on the COREX MG were conducted.…”