Abstract
Many industrial scale trickle bed reactors (TBR) operate at lower liquid superficial velocities (<0.5 cm/s) at which the catalyst particle are not completely wetted. This phenomenon of incomplete wetting has therefore received significant attention and numerous studies have addressed the influence of wetting on the overall rate, conversion/selectivity behavior, and heat effects in TBR. The incomplete wetting conditions correspond to stagnant liquid pockets due to lower liquid superficial velocity which could cause significant influence on reactor performances. In this paper, several models for wetting efficiency in TBR on industrial level are examined and influence on reaction rate and reactor performance is discussed.
Highlights
Najbolje slaganje sa eksperimentalnom tačkom sa industrijskog testa dali su modeli koji predvidjaju potpuno isparavanje tečne faze, Dudukovic [6], Burdhard [7], i Ring [10], dok je najveća odstupanja za posmatrani sistem dao model Herkowitz [9]
Several models for wetting efficiency in trickle bed reactors (TBR) on industrial level are examined and influence on reaction rate and reactor performance is discussed
Summary
Industrijski reaktor za katalitičku hidroobradu je punjen konvencionalnim katalizatorom (Co-Mo/γAl2O3) čije su čestice oblika trilobe, poroznosti 0,52 cm3/g. Ulazna smeša u reaktor je gasno ulje kome je tokom rada periodično dodavano lako ciklično ulje i krekovana nafta. U ulaznoj smeši prisutno je više različitih klasa sumpornih jedinjenja: supstituisani benzotiofeni (C1-C4-BT), dibenzotiofeni i naftotiofeni (DBT i NT), i supstituisani dibenzotiofeni i naftotiofeni (C1-C3-DBT i C1-C3-NT). Raspodela sumpornih jedinjenja u ulaznoj smeši je utvrđena pomoću GC-MS analize [4]. Pritisak u reaktoru je 40 bar, ulazna temperatura je 602 K a ukupna masa katalizatora je 18000 kg. Detaljniji opis industrijskog reaktora, katalizatora i celokupnog procesa je prethodno dat u literaturi [4]. Materijalni i energetski bilansi su izvedeni za sve pseudokomponente u parnoj i tečnoj fazi, a detaljan opis matematičkog modela je prethodno objavljen [5], zajedno sa kinetičkim izrazima i parametrima za reakcije HDS i HDA. Izrazi preuzeti iz literature [6-11], dobijeni su različitim metodama
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