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Third catalyst bed

Haldor Topspe also offers the S-250 concept and the three-bed S-300 converter. The S-250 uses the S-200 converter followed by a one-bed S-50 converter with a steam boiler or steam superheater between the two converters85. The S-50 catalyst bed inlet temperature (which is equal to the converter inlet temperature) is controlled by the amount of steam superheating that occurs upstream of the S-50. The S-300 has an internal heat exchanger installed between the second and third catalyst beds. In 2001 a total of thirteen (13) S-300 converters were in operation or under construction. A cut-away view of an S-300 converter is shown in Figure 6.9207. [Pg.179]

The gas enters the converter (a) at 295 °C and is subsequently heated in the internal heat exchanger to 390 °C before it enters the first catalyst layer. The outlet gas from the first layer then passes through the aforementioned heat exchanger and enters the second bed, after which the gas leaves the converter with 469 °C and passes a waste heat boiler generating 125 bar steam. The inlet gas of the second vessel, which accommodates the third catalyst bed, has a temperature of 401 °C and the outlet enters a further waste heat boiler generating 125 bar steam. [Pg.172]

Key features are the high reforming pressure (up to 41 bar) to save compression energy, use of Uhde s proprietary reformer design [1084] with rigid connection of the reformer tubes to the outlet header, also well proven in many installations for hydrogen and methanol service. Steam to carbon ratio is around 3 and methane slip from the secondary reformer is about 0.6 mol % (dry basis). The temperature of the mixed feed was raised to 580 °C and that of the process air to 600 °C. Shift conversion and methanation have a standard configuration, and for C02 removal BASF s aMDEA process is preferred, with the possibility of other process options, too. Synthesis is performed at about 180 bar in Uhde s proprietary converter concept with two catalyst beds in the first pressure vessel and the third catalyst bed in the second vessel. [Pg.189]

From the shell side of the first interbed heat exchanger, the gas is transferred to the second catalyst bed through the panels around the bed. The effluent from the second catalyst bed passes the shell side of the second interbed heat exchanger for cooling to the proper inlet temperature to the third catalyst bed by heat exchange with gas introduced to the tube side of the second interbed heat exchanger through the bottom inlet as described above. [Pg.27]

Both second and third catalyst beds are passed in inward direction, the gas distribution being ensured by means of appropriate perforation at the walls of the bed. [Pg.27]

The temperature inlet the third catalyst bed is controlled by means of the bypass around the loop boiler feed water preheater, adjusting the gas temperature at converter inlet. [Pg.27]

The gas leaving the third catalyst bed passes the perforated centre tube and flows to the converter outlet. [Pg.27]

Uhde uses three catalyst beds. The first two beds and an interchanger are in one vessel. A waste heat boiler generating HP steam cools the gas before it entCTS second vessel containing the third catalyst bed. The effluent of the third bed goes through a second HP steam boiler. [Pg.174]

Sulphur trioxide is absorbed in the intermediate absorber and in the final absorber. The former absorbs SO 3 from the third catalyst bed and the latter from the first bed. If water is used for absorption a fine acid mist forms which is unacceptable in practical or environmental terms. In order to prevent this the vapour pressure above the acid must be made sufficiently low. This can only be achieved if the absorption medium is greater than 97% strength sulphuric acid—in practice 98% sulphuric acid is employed. The final product is about 98.5% sulphuric acid, which is then diluted to 98% with water in the pump tanks. The heat formed in the reaction... [Pg.159]

Figure 6.2. Fractional-conversion profiles in adiabatic catalyst beds vs contact time. Curve a represents the behavior of the first catalyst bed of an ammonia converter. Curve b refers to the third catalyst bed, which operates in a range of comparatively low reaction rates, of the same converter. Figure 6.2. Fractional-conversion profiles in adiabatic catalyst beds vs contact time. Curve a represents the behavior of the first catalyst bed of an ammonia converter. Curve b refers to the third catalyst bed, which operates in a range of comparatively low reaction rates, of the same converter.
Figure 6.5. Relationship between the maldistribution factor (p and the height-to-diameter ratio of the third catalyst bed of Fig. 6.2 in the tt- and Z-configuration. Operating conditions are as... Figure 6.5. Relationship between the maldistribution factor (p and the height-to-diameter ratio of the third catalyst bed of Fig. 6.2 in the tt- and Z-configuration. Operating conditions are as...
I) departs the third catalyst bed at near-intercept conditions (98% SO2/45O °C) and proceeds to cooling and H2SO4 making (Chapter 9). [Pg.87]

First (feed gas) catalyst bed Second catalyst bed Third catalyst bed... [Pg.97]

Figure 8.4 Industrial first, second, and third catalyst bed thicknesses. They are from Tables 7.2 to 7.6. They increase from bed 1 through bed 3. Figure 8.4 Industrial first, second, and third catalyst bed thicknesses. They are from Tables 7.2 to 7.6. They increase from bed 1 through bed 3.
Figure 8.6 Industrial first, second, and third catalyst bed gas nominal residence times. They increase with increasing bed number. This is due to the increase in bed thickness with increasing bed number (Fig. 8.4). The points have been calculated from Tables 7.2 to 7.6 industrial catalyst bed thicknesses, converter diameters, and converter input gas flow rates. Figure 8.6 Industrial first, second, and third catalyst bed gas nominal residence times. They increase with increasing bed number. This is due to the increase in bed thickness with increasing bed number (Fig. 8.4). The points have been calculated from Tables 7.2 to 7.6 industrial catalyst bed thicknesses, converter diameters, and converter input gas flow rates.
Second bed intercept gas quantities are needed for Chapter 16 s third catalyst bed calculations. They are obtained from the intercept results in Table M.2. They are ... [Pg.180]

H2SO4 making by contact of cooled third catalyst bed exit gas with strong sulfuric acid (Fig. 16.1). [Pg.183]

This chapter describes cooling of second catalyst bed exit gas and oxidation of the cooled gas SO2 in a third catalyst bed. Its objectives are to ... [Pg.183]

Figure 16.1 Schematic of single contact, third catalyst bed sulfuric acid plant. It is a single contact plant because it has only one H2SO4 making step. Note gas cooling between catalyst beds. It permits further SO2 oxidation in the next catalyst bed. Figure 16.1 Schematic of single contact, third catalyst bed sulfuric acid plant. It is a single contact plant because it has only one H2SO4 making step. Note gas cooling between catalyst beds. It permits further SO2 oxidation in the next catalyst bed.
This chapter s third catalyst bed heatup path is calculated much like Chapter 14 s second catalyst bed heatup path. Differences are ... [Pg.184]

Figure 16.2 Specifications for (i) 2-3 cooldown and (ii) third catalyst bed heatup path and intercept calculations. The first and second catalyst bed exit gas quantities are equivalent to ... Figure 16.2 Specifications for (i) 2-3 cooldown and (ii) third catalyst bed heatup path and intercept calculations. The first and second catalyst bed exit gas quantities are equivalent to ...
Figure 16.3 Third catalyst bed SO2 oxidation with gas cooling between beds. The equiUbrium curve is the same for all beds (Section 15.1.1) because ... Figure 16.3 Third catalyst bed SO2 oxidation with gas cooling between beds. The equiUbrium curve is the same for all beds (Section 15.1.1) because ...
Appendix N shows a third catalyst bed heatup path matrix with these equations. It also shows several heatup path points. Figures 16.3 and 16.4 show the entire heatup path. [Pg.186]

Appendix O describes a third catalyst bed intercept calculation—with Fig. 16.2 specifications. The third bed intercept with these specifications is ... [Pg.187]

Third catalyst bed SO2 oxidation efficiency is about 98%. Beds 1,2, and 3 contribute... [Pg.187]


See other pages where Third catalyst bed is mentioned: [Pg.190]    [Pg.128]    [Pg.135]    [Pg.234]    [Pg.234]    [Pg.240]    [Pg.242]    [Pg.87]    [Pg.181]    [Pg.183]    [Pg.183]    [Pg.184]    [Pg.184]    [Pg.185]    [Pg.187]    [Pg.187]    [Pg.188]    [Pg.188]    [Pg.188]    [Pg.188]    [Pg.199]    [Pg.199]    [Pg.199]    [Pg.199]   
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