Weight catalyst

These design fundamentals result in the requirement that space velocity, effective space—time, fraction of bubble gas exchanged with the emulsion gas, bubble residence time, bed expansion relative to settled bed height, and length-to-diameter ratio be held constant. Effective space—time, the product of bubble residence time and fraction of bubble gas exchanged, accounts for the reduction in gas residence time because of the rapid ascent of bubbles, and thereby for the lower conversions compared with a fixed bed with equal gas flow rates and catalyst weights. 

Fig. 6. Influence of catalyst weight and residence time on phenol conversion (CONV), and formation of catechol (CAT), hydroquinone (HQ) and para-benzoquinone (PBQ) over CuCl Pc-Na-Y (0.26) at 353 K see Table 6 for reaction conditions.

Catalyst weight = 0.3 g. Reaction temperature = 473 K. Total flow rate = 18 cm. min i. 5% nC4 in H2. Pretreatment 2 h at 473K imder flowing nitrogen. 

Figure 1. CH reactions with different oxidizing compounds over CoZSM-5 catalyst conversion of NO into (A) and of CH into COj (B) as a function of temperature. Catalyst weight was 100 mg, feed contained 0.28% CH4, 0.21% NO or NOj (when used), and 2.6% Oj (when used) in He at a flow rate of 75 ml/min (GHSV = 22,500 h- ).

Slurry inlet flow channels width 400 pm Catalyst weight 40 mg... 

The reaction rate was calculated from hydrogen consumption, from pressure drop. As the hydrogen consumption rate was dependent on amount and purity of substrate, catalyst weight and metal content, conversion rate was given (%/min mg Pd), the measured total hydrogen consumption was taken equivalent with 100% conversion. 

Figure 5.7. TPD and TPSR over y-Al203 alone (a) TPD of NO pre-adsorbed at RT, in the presence of oxygen (function 3 alone), (b) DeNOx activity of y-A Oj in the presence of CH3OH (total flow rate 250cm3 min catalyst weight 0.2g, VVH 50000h 1, 200ppm NO/9vol.% 02/1000ppm CH.OI I) [26],...

Figure 5.12. Catalytic oxidation of NO to N02 over 0.5, 1, 2wt.% Co/A1203. Successive isotherms. 200ppm NO/9vol.% 02/Ar total flow rate 250 cm3 min catalyst weight 0.2 g VVH 50 000 IT1 [26],...

Figure 6.1. Subsequent NO storage runs in NO (1000 ppm) + 02 (3%, v/v), He balance (total flow 200 Ncc/min, catalyst weight 120 mg) at 350°C on a fresh sample of Pt—Ba/Al203 (1/20/100 w/w). NO, H20 and C02 are outlet concentrations, and NO is inlet concentration.

Figure 6.3. Storage run in N02 (1000 ppm), He balance (total flow 200Ncc/min, catalyst weight 120mg) at 350°C over Pt—Ba/Al203 (1/20/100w/w) catalyst. NO and N02 are outlet concentrations, and N02 is inlet concentration, (b) Results of N02 adsorption using FTIR experiments spectra are reported after 1 and 10 min of exposure to 5mbar of N02 at 350°C. Each spectrum is reported as difference from the spectrum before N02 admission.

Figure 6.10. Reduction of stored N( ), with H2 (2000 ppm) balance He (total flow lOONcc/min, catalyst weight 60 mg) at 350°C over Pt—Ba/Al203 (1/20/100 w/w) catalyst after storage at saturation at the same temperature. N2, NH3, NO and H2 are outlet concentrations, and H2 is inlet concentration.

Weighing of module and repetition of coating procedure until 180-200 mgcat/mlsubstlate are reached (in case of a pore building agent +10% catalyst weight)... 

Assuming zero order kinetics, the reaction rate constants can be calculated from the slope of the hydrogen uptake curve. Table 1 shows that the first three catalysts have similar rate constants on catalyst weight basis, from 5.6xl0"3 to... 

The new DeLink 3%Pd/CPS4 catalyst has been tested for debenzylation of N-phenylbenzylamine also. Under the same reaction conditions, 3%Pd/CPS4 has approximately the same activity as the current commercially produced 5%Pd/CPS2 in this N-debenzylation reaction on catalyst weight basis. 

For their runs at approximately 150 °C, the unreduced catalyst weight was 0.7961 g and the following data were obtained. 

The effect of mass velocity on the conversion rate was studied by using a tube of fixed diameter that was filled with a sample of a given catalyst diameter to give beds with volumes of either 10 or 20 cm3. At a constant ratio of catalyst weight to reactant feed, this method of varying the bed volume has the effect of varying the mass velocity through the bed. 

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