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Converter heat exchanger system

Adl b tic Converters. The adiabatic converter system employs heat exchangers rather than quench gas for interbed cooling (Fig. 7b). Because the beds are adiabatic, the temperature profile stiU exhibits the same sawtooth approach to the maximum reaction rate, but catalyst productivity is somewhat improved because all of the gas passes through the entire catalyst volume. Costs for vessels and exchangers are generally higher than for quench converter systems. [Pg.279]

Converting Heat to Work. There has been a historic bias in the chemical industry to think of energy use in terms of fuel and steam (qv) systems. A more fundamental approach is to minimise the input of work potential embedded in the fuel and feedstock, as well as work purchased direcdy as electricity. Steam is really just a medium of exchange, like money in an economy. [Pg.223]

Fig. 5. Catalytic system designs (11) of (a) basic VOC catalytic converter containing a preheater section, a reactor housing the catalyst, and essential controls, ducting, instmmentation, and other elements (b) a heat exchanger using the cleaned air exiting the reactor to raise the temperature of the incoming process exhaust and (c) extracting additional heat from the exit gases by a secondary heat exchanger. Fig. 5. Catalytic system designs (11) of (a) basic VOC catalytic converter containing a preheater section, a reactor housing the catalyst, and essential controls, ducting, instmmentation, and other elements (b) a heat exchanger using the cleaned air exiting the reactor to raise the temperature of the incoming process exhaust and (c) extracting additional heat from the exit gases by a secondary heat exchanger.
Pressure loss in a piping system (not including the tanks, heat exchangers, distillation columns, etc.) is usually expressed in units oi feet of flowing fluid, or the equivalent converted to pounds per square inch. Some published pressure loss data is expressed as per 100 equivalent feet of the size pipe being used or estimated. [Pg.86]

The reactor volume is taken as the volume of the reactor physically occupied by the reacting fluids. It does not include the volume occupied by agitation devices, heat exchange equipment, or head-room above liquids. One may arbitrarily select the temperature, pressure, and even the state of aggregation (gas or liquid) at which the volumetric flow rate to the reactor will be measured. For design calculations it is usually convenient to choose the reference conditions as those that prevail at the the inlet to the reactor. However, it is easy to convert to any other basis if the pressure-volume-temperature behavior of the system is known. Since the reference volumetric flow rate is arbitrary, care must be taken to specify precisely the reference conditions in order to allow for proper interpretation of the resultant space time. Unless an explicit statement is made to the contrary, we will choose our reference state as that prevailing at the reactor inlet and emphasize this choice by the use of the subscript zero. Henceforth,... [Pg.255]

W-Methyl-A/ -nitroso-p-toluenesulfonamide (MNTS) is an important precursor for the production of diazomethane. Diazomethane is then further converted to a range of useful molecules in the pharmaceutical and fine chemical industry [69]. Production of MNTS is a highly exothermic process and includes the presence of the extremely toxic materials. Stark et al. [70] have explored the application of microreactor technology for the production of this industrially valuable material, assuming that due to the efficient heat exchange and the closed system, microflow conditions provide a safer environment for these hazards. [Pg.186]


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