Read e-book online Mechanical Design of Process Systems Vol. 2 : Shell and Tube PDF

By Escoe A. Keith

Chapters hide: the engineering mechanics of packing containers, silos, and stacks; rotating gear; the mechanical layout of shell-and-tube warmth exchangers; exterior loadings on shell buildings; partial volumes and strain vessel calculations; nationwide wind layout criteria; homes of pipe; conversion elements; index.

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Read or Download Mechanical Design of Process Systems Vol. 2 : Shell and Tube Heat Exchangers, Rotating Equipment, Bins, Silos, Stacks PDF

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Mechanical Design of Process Systems Vol. 2 : Shell and Tube by Escoe A. Keith PDF

Chapters hide: the engineering mechanics of containers, silos, and stacks; rotating apparatus; the mechanical layout of shell-and-tube warmth exchangers; exterior loadings on shell constructions; partial volumes and strain vessel calculations; nationwide wind layout criteria; homes of pipe; conversion components; index.

Additional resources for Mechanical Design of Process Systems Vol. 2 : Shell and Tube Heat Exchangers, Rotating Equipment, Bins, Silos, Stacks

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V: z: R: R: P absolute pressure, psra volume of gas, ft3 : compressibility factor for real gases (z 1 for a perfect gas) R/mw gas constant of the particular gas universal gas constant 1,545 ft-lbr/lb. 7 molecular weight of gas number of moles of gas m/mw specific volume of gas, ft3llb. : Mo A very important gas property is the specific heat ratio, k. -mole-"F for most diatomic gases Reverslble Adiabatlc (lsentropic) Compression a The reversible adiabatic (isentropic) compression of o an ideal gas is obtained when no heat is added to, or removed from, the gas during compression.

To correct for the pumped liquid's viscosity, Figures 6-7 and 6-8 are used to approximate the equivalent water performance. The figures, developed by the Hydrauiic Institute, are used by entering the bottom with the viscous flow rate (gpm), moving vertically upward to the desired viscous head (head per stage for multistage pumps), then moving horizontally to the left or right to the viscosity line, and proceeding vertically upward to the correction-factor curves for the head and capacity. The equivalent water-performance values are then obtained by dividing the viscousperformance values by the correction values.

If low rates carmot be avoided, a by-pass may be required to prevent vaporization and subsequent pump damage. Thus, vaporization of the pumped liquid can occur two ways: (1) the NPSH required is not being met and cavitation occurs in the liquid causing vapor bubbles that can severely damage the impeller or (2) the pump horsepower overheats the pumped liquid, forming vapor bubbles that can (and normally will) damage the pump. Excess heat resulting in pumping a fluid can be avoided by determining t}re minimum flow required to allow proper heat dissipation.

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Mechanical Design of Process Systems Vol. 2 : Shell and Tube Heat Exchangers, Rotating Equipment, Bins, Silos, Stacks by Escoe A. Keith


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