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G-type shells in shell-and-tube heat exchangers: Gaddis, E S,
Introduction
Galerkin method, for heat conduction finite-element calculations, Galileo number, Gas-liquid flows: Gas-liquid-solid interfaces, fouling at, Gas-solid interfaces, fouling at, Gas tungsten arc welding, Gaseous fuels, properties of, Gases: Gaskets: Gauss-Seidel method, for solution of implicit equations, Geometric optics models for radiative heat transfer from surfaces, geothermal brines, fouling of heat exchangers by, Germany, Federal Republic of, mechanical design of heat exchangers in: Gersten, K, Girth flanges, in shell-and-tube heat exchangers, Glass production, furnaces and kilns for, Glycerol (glycerine): Gn (heat generation number), Gnielinski, V Gnielinski correlation, for heat transfer in tube banks, Gomez-Thodas method, for vapour pressure, Goodness factor, as a basis for comparison of plate fin heat exchanger surfaces, Goody narrow band model for gas radiation properties, Gorenflo correlation, for nucleate boiling, Gowenlock, R, Graetz number: Granular products, moving, heat transfer to, Graphite, density of, Grashof number Gravitational acceleration, effect in pool boiling, Gravity conveyor: Gregorig effect in enhancement of condensation, Grid baffles: Grid selection, for finite difference method, Griffin, J M, Groeneveld correlation for postdryout heat transfer, Groeneveld and Delorme correlation for postdryout heat transfer, Gross plastic deformation Group contribution parameters tables, Guerrieri and Talty correlations for forced convective heat transfer in two-phase flow, Gungor and Winterton correlation, for forced convective boiling, Gylys, J,

Index

HEDH
A B C D E F G
G-type shells in shell-and-tube heat exchangers: Gaddis, E S,
Introduction
Galerkin method, for heat conduction finite-element calculations, Galileo number, Gas-liquid flows: Gas-liquid-solid interfaces, fouling at, Gas-solid interfaces, fouling at, Gas tungsten arc welding, Gaseous fuels, properties of, Gases: Gaskets: Gauss-Seidel method, for solution of implicit equations, Geometric optics models for radiative heat transfer from surfaces, geothermal brines, fouling of heat exchangers by, Germany, Federal Republic of, mechanical design of heat exchangers in: Gersten, K, Girth flanges, in shell-and-tube heat exchangers, Glass production, furnaces and kilns for, Glycerol (glycerine): Gn (heat generation number), Gnielinski, V Gnielinski correlation, for heat transfer in tube banks, Gomez-Thodas method, for vapour pressure, Goodness factor, as a basis for comparison of plate fin heat exchanger surfaces, Goody narrow band model for gas radiation properties, Gorenflo correlation, for nucleate boiling, Gowenlock, R, Graetz number: Granular products, moving, heat transfer to, Graphite, density of, Grashof number Gravitational acceleration, effect in pool boiling, Gravity conveyor: Gregorig effect in enhancement of condensation, Grid baffles: Grid selection, for finite difference method, Griffin, J M, Groeneveld correlation for postdryout heat transfer, Groeneveld and Delorme correlation for postdryout heat transfer, Gross plastic deformation Group contribution parameters tables, Guerrieri and Talty correlations for forced convective heat transfer in two-phase flow, Gungor and Winterton correlation, for forced convective boiling, Gylys, J,
H I J K L M N O P Q R S T U V W X Y Z
G Gaddis, E S,
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Introduction

DOI 10.1615/hedhme.a.000108

1.6 SHELL-AND-TUBE HEAT EXCHANGERS (CELL METHOD)
1.6.1 Introduction

E.S. Gaddis

Single-phase multipass shell-and-tube heat exchangers provided with segmental baffles have a more or less cross flow through the tube bundle. Baffle-induced shell-side flow might influence the effective mean temperature difference and hence the effectiveness of the heat exchanger. The influence of the baffles on the heat exchanger effectiveness and on the mean temperature difference is ignored in most present thermal design calculations (see Section 106). In general, this can be justified in the following cases:

  • Large number of baffles or large number of tube-side passes.
  • Heat capacity rates Ċ1 and Ċ2 (Ċ = Ṁ c) of the two streams differ greatly from one another.
  • Number of transfer units (NTU) is small.

More details are given in Section 118.

If neither of the above conditions is fulfilled, the error in computing the effectiveness of the heat exchanger due to ignoring the influence of the baffle-induced shell-side flow may not be small. To evaluate the thermal performance of the apparatus in such cases, the heat exchanger (Figure 1a) can be divided into a number of cells (sub-exchangers) coupled together as shown in Figure 1b. The background development of this method is described in References Gaddis and Schlünder (1975), Gaddis (1978), Gaddis and Vogelpohl (1984) and Gaddis and Schlünder (1976). The purpose of Section 1.6 is to illustrate with numerical examples the calculation procedure and to present rules that enable the designer to choose the flow configuration with the highest heat exchanger effectiveness.

Figure 1 (a) Multipass shell-and-tube heat exchanger with segmental baffles. (b) Idealized heat exchanger composed of cells (sub-exchangers) coupled together

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