Catalyst deactivation selectivity

In order to elucidate the effect of liquid products on the catalyst deactivation, selectivity versus conversion was investigated. As indicated above particularly interesting was the rapid decrease of conversion over 0.6 g compared to 0.4 g and 0.2 g of catalyst, however a comparison of product selectivities as a function of conversion gave no direct explanation for this rapid deactivation. Very similar... 

Conditions of hydrogenation also determine the composition of the product. The rate of reaction is increased by increases in temperature, pressure, agitation, and catalyst concentration. Selectivity is increased by increasing temperature and negatively affected by increases in pressure, agitation, and catalyst. Double-bond isomerization is enhanced by a temperature increase but decreased with increasing pressure, agitation, and catalyst. Trans isomers may also be favored by use of reused (deactivated) catalyst or sulfur-poisoned catalyst. 

Catalyst Selection. The choice of catalyst is one of the most important design decisions. Selection is usually based on activity, selectivity, stabiUty, mechanical strength, and cost (31). StabiUty and mechanical strength, which make for steady, long-term performance, are the key characteristics. The basic strategy in process design is to minimize catalyst deactivation, while optimizing pollutant destmction. 

A good catalyst is also stable. It must not deactivate at the high temperature levels (1300 to 1400°F) experienced in regenerators. It must also be resistant to contamination. While all catalysts are subject to contamination by certain metals, such as nickel, vanadium, and iron in extremely minute amounts, some are affected much more than others. While metal contaminants deactivate the catalyst slightly, this is not serious. The really important effect of the metals is that they destroy a catalyst s selectivity. The hydrogen and coke yields go up very rapidly, and the gasoline yield goes down. While Zeolite catalysts are not as sensitive to metals as 3A catalysts, they are more sensitive to the carbon level on the catalyst than 3A. Since all commercial catalysts are contaminated to some extent, it has been necessary to set up a measure that will reflect just how badly they are contaminated. 

The process is characterized by high yield (nearly complete hydrogenation of acetylenes) and high selectivity (only a small loss of butadiene by hydrogenation). The process does not lead to polymerization, which might otherwise cause catalyst deactivation, and only infrequent regeneration of catalyst is necessary. 

The selection of reactor type in the traditionally continuous bulk chemicals industry has always been dominated by considering the number and type of phases present, the relative importance of transport processes (both heat and mass transfer) and reaction kinetics plus the reaction network relating to required and undesired reactions and any aspects of catalyst deactivation. The opportunity for economic... 

The catalyst deactivates, but after four runs the conversion is still significantly higher (> 99% after 2 h) as compared with the uncatalyzed reaction. Moreover, the Z-selectivity in all four runs is higher than 80%, whereas in the uncatalyzed reaction, it is typically only 30% (Z). The fact that the solid powder can be used several times furthermore supports the fact that the reaction mechanism is heterogeneous. The reason for the deactivation is unknown. A disadvantage of the nanoparticles is the difficulty of separation. Thus, in some cases the particles form col-... 

Figure 1 shows tire relationship betweai CHO conversion, CL selectivity and process time (time on str m) over TS-ls with different Si/11 ratio and SSZ-41, The result over ZSM-5 (Si/Al ratio=90) is also represented in Figure 1. The CHO conversion decreases with process time, whereas the CL selectivity is almost constant during the process time. The deactivation of SSZ-31 is largest among toe zeolites. The CL selectivity over SSZ-31 is lowest among the zeolites. The catalyst dractivation of TS-1(45) is larpr than fliat of TS-1(200). These results suggest that the acidity and micro pesre size of the zeolite siraultaiKously affected the catalyst deactivation.

One of the most studied applications of Catalytic Membrane Reactors (CMRs) is the dehydrogenation of alkanes. For this reaction, in conventional reactors and under classical conditions, the conversion is controlled by thermodynamics and high temperatures are required leading to a rapid catalyst deactivation and expensive operative costs In a CMR, the selective removal of hydrogen from the reaction zone through a permselective membrane will favour the conversion and then allow higher olefin yields when compared to conventional (nonmembrane) reactors [1-3]... 

According to the classical definition of catalysis a catalyst does not cheinge during reaction. In practice this is not true during operation the catalyst loses activity, and often also selectivity and mechanical strength. Catalyst deactivation is a common phenomenon rather than exception. 

The selectivity in a system of parallel reactions does not depend much on the catalyst size if effective diffusivities of reactants, intermediates, and products are similar. The same applies to consecutive reactions with the product desired being the final product in the series. In contrast with this, for consecutive reactions in which the intermediate is the desired product, the selectivity much depends on the catalyst size. This was proven by Edvinsson and Cybulski (1994, 1995) for. selective hydrogenations and also by Colen et al. (1988) for the hydrogenation of unsaturated fats. Diffusion limitations can also affect catalyst deactivation. Poisoning by deposition of impurities in the feed is usually slower for larger particles. However, if carbonaceous depositions are formed on the catalyst internal surface, ageing might not depend very much on the catalyst size. 

By decreasing the GHSV values, the selectivity dramatically decreased due to the presence of the side-reaction of C-alkylation on the aromatic ring, giving rise to relevant amounts of 3-MC and a not-fully-identified methyl-MDB derivative (however, the 3-methyl isomer is the most probable candidate). Lastly, the lowest GHSV value was conducive to the condensation of PYC, with a formation of heavy by-products, a dramatic decrease of C-balance, and resulting catalyst deactivation. 

What does the longitudinal temperature profile look like for given inlet temperatures and/or wall temperature profiles Are the hot spots excessive for reasons of selectivity, catalyst deactivation, etc ... 

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