Other Mass Transfer Operations in .NET framework

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rates augment heat lossc~s as well as affecting the rate of drying, gas rabe ought to vary with load, to minimize losses at low rates. In a directfired system, gnu rate and heat input are not independent, since the gas is comprised of products of combustion of the fuel.
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Regulation of the Driving Force
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Lacking an on-line measurement of product moisture or any function thereof, the next step would be to look for feedforward signals to provide regulation. The principal load components affecting drying arc the flow and moisture content of the feed. The former is difficult to measure and the latter virtually impossible. Lit tle remains bul, to set the principal variables affecting the rate of dryin g on the basis of laboratory analyses of product quality. It is therefore important, to rcgulale these variables as carefully as possible in order to minimize drift, between analyses. Positioning a valve in a steam or fuel line is hardly accurate enough. Even flow control of steam or fuel is insufficient, because variations in humidit y and barometric pressure affect the rate of drying. The terminal driving forces are gas temperature at) the hot end of the dryer and dry-bulb minus wet-bulb tcmpcrature at the cold end. Both these forces should bc regulated if uniform dryness is to be achieved. Hot-end temperature is the heat input divided by the gas rate-these variables must bc manipulated together to provide control. The cold-end wet-bulb temperature varies with rate of evaporation divided by gas rate---the former is t,he load, while Ihe lat,tcr must be manipulated for control; cold-end dry-bulb t,emperature is affected by hot-end temperature and gas rate. Figure 12.14 shows how bot,h terntittal driving forces may be controlled by ntnnipulalittg heat input and gas rate. Although the two loops are coupled, decoupling is hardly necessary because hot -end temperature is a very fast-responding loop. Wit h increasing load, gas-exit dry-bulb t,etnperat,ure will tend to fall and net-bulb temperature will rise, bccausc more moisture mill have been evaporated. Increasing air flow will lower the wet-bulb temperature, restoring the exit driving force to its desired value. As air flow is increased, t h e hot-end temperature c o n t r o l l e r increments heat f l o w commensurately. The t ransport time of t,he gas stream may be only a fern seconds, while l lte solids ordinarily take an hour or more t,o t raverse the dryer. Using measurentettts of the gas st,renm for control is t,herefore dynamically advantageous, for they arc much easier to cottt,rol and respond rapidly to changes in load. The set, point, of the T - ,, controller should be rcpositioncd as necessary to obtain the desired product dryness.
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FIG 12.14. Heat and air flows entering a cocurrent dryer can be manipulated to regulate the driving forces at both ends.
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With countercurrent dryers, the product leaves the hot end. The same configuration of the control loops may be used as with a recurrent dryer, but hot-end temperature must he adjust ed for control of product quality. In either type of dryer, the driving force at the feed end has less effect In reality, on product dryness than on the economics of the operation. there is but one cont rolled variable, while bot h air flow and heat input may be msnipulskd. Any number of combinat ions of air flow and heat input could be found to deliver the required product quality, but each Exccssivc combination may result in a different cost of operat ion. gas flow increases heat losses, but limitations also exist in feed-end temperature. In a fired clryer, manipulation of fuel rate is equivalent to heat input, while air in excess of combustion requirements largely determines gas
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