Catalyst carriers surface area

XFS and HDS activity data obtained for both fresh and spent catalysts are summarized in Table S. As explained in the experimental section, the signal intensity ratios and the catalyst properties (surface area and loadings) are used to calculate the thickness (t) and the coverage [8) of layers. For the coke-containing catalysts an assumption on the relative distribution of coke and active components has eo be made. It is emphasized that in all Calculations we have ja snin d that the coke is randomly distributed over the carrier and the active component (a). Below we. will address Che validity of this premise. The results obtained with the three catalysts will now be discussed In detail,... 

In a former study, we have prepared very highly loaded nickel catalysts, efficient for the hydrogenation of edible oil, by a (DP) method and examined the influence of the carrier surface area on the metallic dispersion and on the metal interaction with the silica. The best activity in soybean oil hydrogenation was obtained using a macroporous support with an intermediate surface area, the FC Celite (Manville) (16). We also observed that precipitate aging, at the end of the (DP) method, induced important modifications in the textural properties of the catalysts. 

Stabilization of titania and of catalysts with vanadia contents less than 10 wt % is achieved by adding sulfuric acid to the solutions. Evaporation and calcination at 350 C forms Ti02 (anatase), vanadium and vanadium-tungsten containing catalysts with lower BET surface area (40 - 65 m /g) than the values reported above. However, the calcination at 450 °C, originally proposed as a test for thermal stability and normally accompanied by loss of surface area due to the sintering of the anatase carrier, now increases the surface area and forms stable carriers and catalysts with surface areas in the range of 80 to 90 m /g. 

A few industrial catalysts have simple compositions, but the typical catalyst is a complex composite made up of several components, illustrated schematically in Figure 9 by a catalyst for ethylene oxidation. Often it consists largely of a porous support or carrier, with the catalyticaHy active components dispersed on the support surface. For example, petroleum refining catalysts used for reforming of naphtha have about 1 wt% Pt and Re on the surface of a transition alumina such as y-Al203 that has a surface area of several hundred square meters per gram. The expensive metal is dispersed as minute particles or clusters so that a large fraction of the atoms are exposed at the surface and accessible to reactants (see Catalysts, supported). 

Catalysts vary both in terms of compositional material and physical stmcture (18). The catalyst basically consists of the catalyst itself, which is a finely divided metal (14,17,19) a high surface area carrier and a support stmcture (see Catalysts, supported). Three types of conventional metal catalysts are used for oxidation reactions single- or mixed-metal oxides, noble (precious) metals, or a combination of the two (19). 

The precious metal or metal oxide imparts high intrinsic activity, the carrier provides a stable, high surface area for catalyst dispersion, and the mechanical support gives a high geometric surface area for physical support and engineering design features (20). Only the correct combination of these... 

Carrier. The metal catalyst is generally dispersed on a high surface area carrier, ie, the carrier is given a washcoat of catalyst, such that very small (2—3 nm dia) precious metal crystaUites ate widely dispersed over the surface area, serving two basic functions. It maximizes the use of the cosdy precious metal, and provides a large surface area thereby increasing gas contact and associated catalytic reactions (18). 

Only by using the carrier can the catalyst be sufficiently active because the majority of appHcations require 10 to 100 m /g of surface area (20). Surface areas for a typical monolith support stmcture and a carrier are given (20). 

Consequently the absolute potential is a material property which can be used to characterize solid electrolyte materials, several of which, as discussed in Chapter 11, are used increasingly in recent years as high surface area catalyst supports. This in turn implies that the Fermi level of dispersed metal catalysts supported on such carriers will be pinned to the Fermi level (or absolute potential) of the carrier (support). As discussed in Chapter 11 this is intimately related to the effect of metal-support interactions, which is of central importance in heterogeneous catalysis. 

Figure 4.1. Supported catalyst, consisting of small particles on a high surface area carrier such as silica or alumina, along with two simplified model systems, which in general offer much better opportunities for characterization at the molecular level.

Catalysts and their carriers are provided in micro channels by various means and in various geometric forms. In a simple variant, the catalyst itself constitutes the micro-reactor construction material without need for any carrier [2-A], In this case, however, the catalyst surface area equals that of the reactor wall and hence is comparatively low. Accordingly, applications are typically restricted to either fast reactions or processing at low flow rates for slow reactions (to enhance the residence time). 

The platinum concentrations in the platinized carbon blacks are reported to be between 10 and 40% (by mass), sometimes even higher. At low concentrations the specific surface area of the platinum on carbon is as high as lOOm /g, whereas unsupported disperse platinum has surface areas not higher than 10 to 15m /g. However, at low platinum concentrations, thicker catalyst layers must be applied, which makes reactant transport to reaction sites more difficult. The degree of dispersion and catalytic activity of the platinum depend not only on its concentration on the carrier but also on the chemical or electrochemical method used to deposit it. 

Most industrial catalysts are heterogeneous catalysts consisting of solid active components dispersed on the internal surface of an inorganic porous support. The active phases may consist of metals or oxides, and the support (also denoted the carrier) is typically composed of small oxidic structures with a surface area ranging from a few to several hundred m2/g. Catalysts for fixed bed reactors are typically produced as shaped pellets of mm to cm size or as monoliths with mm large gas channels. A catalyst may be useful for its activity referring to the rate at which it causes the reaction to approach chemical equilibrium, and for its selectivity which is a measure of the extent to which it accelerates the reaction to form the desired product when multiple products are possible [1],... 

The silica carrier of a sulphuric acid catalyst, which has a relatively low surface area, serves as an inert support for the melt. It must be chemically resistant to the very corrosive pyrosulphate melt and the pore structure of the carrier should be designed for optimum melt distribution and minimum pore diffusion restriction. Diatomaceous earth or synthetic silica may be used as the silica raw material for carrier production. The diatomaceous earth, which is also referred to as diatomite or kieselguhr, is a siliceous, sedimentary rock consisting principally of the fossilised skeletal remains of the diatom, which is a unicellular aquatic plant related to the algae. The supports made from diatomaceous earth, which may be pretreated by calcination or flux-calcination, exhibit bimodal pore size distributions due to the microstructure of the skeletons, cf. Fig. 5. 

In this part, we prepared and studied the Ag/Si02 catalyst by one-step and two-step sol-gel methods. The results show that the Ag/Si02 catalyst prepared here is one kind of bulk material which has a high surface area. The Ag/Si02 catalyst is made up with functional component of Ag or silver oxide in 20 to 30 nm and carrier Si02. Moreover, we found that the different preparation methods have great effect on crystal structure of the samples. The structure of the sample prepared by the one-step method is always a single crystal structure. And the structure of the sample prepared by the two-step method is always a mixed crystal structure. 

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