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Catalytic dehydrogenation of n-butane

Table I summarizes the results of previous investigations on catalytic dehydrogenation of n-butane. In this table 2 models were used to correlate dehydrogenation rate data by various investigators one is a power function model, and the other is a Langmuir-Hinshelwood model. The power function model can be obtained by applying the mass action law to describe rate data. Thus, the model presents the dependence of partial... Table I summarizes the results of previous investigations on catalytic dehydrogenation of n-butane. In this table 2 models were used to correlate dehydrogenation rate data by various investigators one is a power function model, and the other is a Langmuir-Hinshelwood model. The power function model can be obtained by applying the mass action law to describe rate data. Thus, the model presents the dependence of partial...
Butadiene is mainly obtained as a byproduct from the steam cracking of hydrocarbons and from catalytic cracking. These two sources account for over 90% of butadiene demand. The remainder comes from dehydrogenation of n-butane or n-butene streams (Chapter 3). The 1998 U.S. production of butadiene was approximately 4 billion pounds, and it was the 36th highest-volume chemical. Worldwide butadiene capacity was nearly 20 billion pounds. [Pg.256]

Butadiene (> 98%w/w) 20 ooo longtons Catalytic dehydrogenation of n-butenes feedstock of liquid mixed hydrocarbon stream containing 80.5 mol % n-butenes, 11.5 mol % n-butane, and 1 mol % of higher hydrocarbons. [Pg.343]

The dehydrogenation process feed can be refinery streams from the catalytic cracking processes. This mixed C4 stream typically contains less than 20 percent n-butenes. For use in dehydrogenation, however, it should be concentrated to 80-95 percent. The isobutylene generally is removed first by a selective extraction-hydration process. The n-butenes in the raffinate are then separated from the butanes by an extractive distillation. The catalytic dehydrogenation of n-butenes to 1,3-butadiene is carried out in the presence of steam at high temperature (>600°C) and... [Pg.390]

VO)2P207 is superior for the selective dehydrogenation of n-butane to butene to other crystalline V-P oxides, while few differences exist between the oxidation of butene and butadiene, which are considered reaction intermediates. The abstraction of methylene hydrogen from n-butane is the slowest step. Hence this step determines the overall catalytic activity." 2) Selectivity in forming anhydride from C4 and C5 alkanes, but not in selective oxidation of lower (C2 and C3) or higher (Ce-Cg) alkanes." 3) The number of surface layers involving the catalytic reactions is limited to 2-3 in contrast to Bi-Mo-O catalysts. [Pg.3391]

I 6 Photoelectron Spectroscopy of Catalytic Oxide Materials 63.2.2 Oxidative Dehydrogenation of n-Butane... [Pg.266]

A quantitative kinetic model, denominated TC4, for the catalytic conversion of n-butane is proposed. The model considers 56 elementary reactions, six of them were chosen to occur in heterogeneous phase. The TC4 model can be used to predict the product distribution and the heterogeneous rate constants for a wide range of conditions and on different catalyst types. The model can fit also the experimental data from the isobutane dehydrogenation reaction. A plot, that we have denominated "the graphic s performance of a catalyst", is proposed for the evaluation of the maximum yield of a catalyst with a minimum of experimental data. [Pg.517]

Milne, D., Seodigeng, T., Glasser, D., Hildebrandt, D., Hausherger, B., 2010. The oxidative dehydrogenation of n-butane in a differential side-stream catalytic membrane reactor. Catal. Today 156, 237-245. [Pg.307]

Blasco T, Nieto JML, Dejoz A, Vazaquez MI (1995) Inllucaice of the acid-base character of supported vanadium catalysts on their catalytic properties for the oxidative dehydrogenation of n-butane. J Catal 157 271-282... [Pg.299]

MTBE is produced by reacting methanol with isobutene. Isobutene is contained in the C4 stream from steam crackers and from fluid catalytic cracking m the crude oil-refining process. However, isobutene has been in short supply in many locations. The use of raw materials other than isobutene for MTBE production has been actively sought. Figure 2 describes the reaction network for MTBE production. Isobutene can be made by dehydration of i-butyl alcohol, isomerization of -butenes [73], and isomerization and dehydrogenation of n-butane [74, 75]. t-Butanol can also react with methanol to form MTBE over acid alumina, silica, clay, or zeolite in one step [7678]. t-Butanol is readily available by oxidation of isobutane or, in the future, from syngas. The C4 fraction from the methanol-to-olefins process may be used for MTBE production, and the C5 fraction may be used to make TAME. It is also conceivable that these... [Pg.16]

The chief sources of olefins are cracking operations, especially catalytic cracking. However, olefins can be produced by the dehydrogenation of paraffins butanes are dehydrogenated commercially to provide feeds to alkylation. Isobutane is obtained from crude oils, cracking operations, catalytic reformers, and natural gas. To supplement these sources, n-butane is sometimes isomer-ized. Only small concentrations of diolefins are permissible in feeds to alkylation, particularly for sulfuric add catalyst. Diolefins increase the consumption of acid. [Pg.2565]

Wang et al. [5] reported the dehydrogenation and isomerization of -butane on Cr-supported W03-Zr02 and, in his case, the catalytic activity decreased with reaction time by deposition of carbon. In our study, the catalyst performance for -butane conversion and the C4 products selectivity over Cr/H-SSZ-35 catalyst (Si/Al2=500) remained unchanged at 500°C for 6 h. From these findings on the catalytic activity and lifetime, H-SSZ-35 was expected to be one of the promising supports for the production of isobutene by hydrogenation and isomerization of n-butane. [Pg.644]

To promote both the conversion of reactants and the selectivity to partial oxidation products, many kinds of metal compounds are used to create catalytically active sites in different oxidation reaction processes [4]. The most well-known oxidation of lower alkanes is the selective oxidation of n-butane to maleic anhydride, which has been successfully demonstrated using crystalline V-P-O complex oxide catalysts [5] and the process has been commercialized. The selective conversions of methane to methanol, formaldehyde, and higher hydrocarbons (by oxidative coupling of methane [OCM]) are also widely investigated [6-8]. The oxidative dehydrogenation of ethane has also received attention [9,10],... [Pg.433]

Supported vanadium oxides have been proposed as selective catalysts in partial oxidation reactions [1] and more specifically in the oxidative dehydrogenation (ODH) of short chain alkanes [2, 3]. However, it has been observed that the catalytic behavior of these catalysts during the oxidation of alkanes depends on the vanadium loading and the acid-base character of metal oxide support. In this way, alumina-supported vanadia catalysts with low V-loading are highly active and selective during the ODH of ethane [4-7] and propane [8] but they show a low selectivity in the ODH of n-butane [4, 5, 9, 10]. [Pg.443]

With respect to the catalytic reactions, there are well-established industrial reactions (as occurs in the case of n-butane to maleic anhydride), reactions in the preindustrial stage (such as the transformation of propane to acrylonitrile), very promising reactions (such as ethane oxidative dehydrogenation to ethylene), and potential reactions whose economical viability will depend on the prices of crude and natural gas in the future (such as propane selective oxidation to acrylic acid or methane transformation). [Pg.815]

ExxonMobil produces MEK from catalytic dehydrogenation of sec-butanol feedstock. On the other hand, Celanese produces MEK as a byproduct from their acetic acid production from the controlled oxidation of n-butane feedstock. [Pg.467]

Major methods for isobutene production are from a C4 stream of a steam cracker, from a catalytic cracker butene-butane stream, through dehydration of tert-butanol (which is obtained from a propene oxide process) and through isomerisation of n-butane to isobutene and subsequent dehydrogenation to isobutene (Obenaus et al. 2000 van Leeuwen et al. 2012 Romanow-Garcia et al. 2007). [Pg.112]


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Catalytic dehydrogenation

Catalytic dehydrogenation of butane

Dehydrogenation butan

Dehydrogenation of butan

Dehydrogenation of butane

Dehydrogenation of n-butane

N Butane

N-Butane dehydrogenation

N-butanal

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