Superheater for steam

From steam tables, the outlet temperature is 160°C, which is superheated by 16°C. Again, it is desirable to have some superheat for the steam fed to the main to avoid condensation in the main. 

Decant the ethereal solution from the yellow aldimine stannichloride which has separated, rinse the solid with two 50 ml. portions of ether, and transfer the solid to a 2-5 litre flask fitted for steam distillation and immersed in an oil bath at 110-120°. Pass steam through a trap (compare Fig. 11,40, 1,6) to remove condensed water, then through a superheater heated to 260° (Fig. I, 7, 2), and finally into the mixture (2). Continue the passage of y steam until the aldehyde is completely removed (4-5 litres 8-10 hours). Filter the white soUd at the pump, and dry in the air. The resulting p-naphthaldehyde, m.p. 53-54°, weighs 12 g. It may be further purified by distillation under diminished pressure (Fig. II, 19, ) -, pour the colourless distillate, b.p. 156-158°/15 mm., while hot into a mortar and powder it when cold. The m.p. is 57- 58°, and the recovery is over 90 per cent. 

Wilhelm Schmidt Steam superheater for locomotives. and ALCO largest ever built (540 long tons). 

Section 38 of the Factories Act 1961 defines a steam boiler as a any closed vessel in which for any purpose steam is generated under pressure greater than atmospheric pressure . Economizers used to heat water being fed to such a vessel and superheater for heating steam are also included. Every boiler must be fitted with the recommended safety measures (e.g. safety valve, stop valve, water gauge, low-water alarms, pressure gages, etc.). 

Exiting steam from the roof and convection-pass cooling sections is collected in headers and typically passes through a primary superheater tube bundle, where a controlled amount of superheat is provided. In the superheater the steam discharges through an outlet header and across a spray attemperator (which provides the steam temperature control) and is then delivered to the control valves for distribution and subsequent use in a turbine or other items of process equipment. 

The flue gas tunnels are rectangular fire-brick structures at the reformer s bottom. They act as horizontal ducts for flue gas removal. The flue gas exits at 1,800°F to 1,900°F. A heat recovery unit is provided to recover heat from this gas. This unit contains a reformer feed preheat coil, steam superheat coil, steam generation coil and boiler feed water preheat coil. 

The LTSC effluent (stream 112) is utilized to superheat the steam required for the reformer and water gas shift reactions. The saturated steam sent to the superheater is supplied by the fuel cell water cooling circuit. The cooled stream (stream 113) is further cooled in a fuel gas contact... 

The most commonly used steam is 100 psig with 10-15° superheat, the latter characteristic in order to avoid the erosive effect of liquids on the throats of the ejectors. In Figure 7.31 the steam consumptions are given as lb of motive steam per lb of equivalent air to the first stage. Corrections are shown for steam pressures other than 100 psig. When some portion of the initial suction gas is condensable, downward corrections to these rates are to be made for those ejector assemblies that have intercondensers. Such corrections and also the distribution of motive steam to the individual stages are problems best passed on to ejector manufacturers who have experience and a body of test data. 

The major process units include an air compressor to provide feed air to the process, and an ammonia vaporizer and superheater for pretreatment of the feed ammonia. A reactor vessel with a fixed platinum/rhodium catalyst bed quickly oxidizes the ammonia at reaction temperatures approaching 950°C. The reaction yield is 95%. A heat exchanger train immediately following the reactor is used to recover reaction heat. Reaction heat is recovered for both gas expansion (to provide shaft power for the air compressors) and for production of medium-pressure steam (at 380°C and 4000 kPa). The high-level energy available in the process is shared approximately equally between gas expansion and steam production. About 40% of all steam production is delegated to in- house process requirements, leaving about 3200 kg/hour available for export. 

Steam Superheater This unit superheats saturated steam from 250°C (and 4000kPa) to 380°C. The product steam is of medium pressure and suitable quality for in-house application and also for export. The superheater cools the reaction gases from the reactor exit temperature of 645°C to 595°C. Design pressure on the shell side is approximately 5000 kPa. The steam superheater is constructed from mild steel. 

It is the second of these two areas that is of interest in this chapter. Heat is delivered for steam production in many separate stages. Preheat is first supplied to the low-pressure deionized water prior to deaeration. Higher pressure product (HP boiler feedwater) is further preheated to around 100°C for supply to the waste-heat boiler. The waste-heat boiler is then able to vapourize the high-pressure deionized and deaerated water for final delivery to the steam superheater. 

The vapour/liquid separator receives saturated steam at 4000 kPa (250°C) from the waste- heat boiler. Much of this steam leaves for the steam superheater. Some steam is condensed in order to heat the incoming deionized boiler-feed water (at 96°C). The equilibrium temperature of the liquid in this vessel is about 117°C. (These calculations have already been performed in Section F.2.7). 

For steam service at 10% overpressure, we use the following formula based on the empirical Napier formula for steam flow. Correction factors are included to account for the effects of superheat, backpressure and subsonic flow. An additional correction factor, Kn, is required by ASME when the relieving pressure (Pj) is higher than 1500psia (10.340kPaA). 

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