457--Introduction

doi:10.1615/hedhme.a.000457

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Hagen-Poiseuille law Hagen-Rubens relation, between electrical and optical constants, Hall Taylor, N S, Halogenated hydrocarbons: Handley and Heggs equation for fixed bed pressure drop, Hankinson and Thomson method, for liquid density: Hardening (precipative) of stainless steels, Hardwick, R, Harris, D, Hausen equation for developing laminar flow, Hays, G F Headers in shell-and-tube heat exchangers, Heads, in heat exchangers: Heat and mass transfer: Heat exchanger design, introduction, Heat exchangers: Heat of vaporisation (see Enthalpy of vaporisation), of pure substances Heat pipes: Heat pumping, relation to heat exchanger network design, Heat storage (see Regenerators and thermal energy storage) entropy generation in, Heat transfer: Heat transfer coefficient: Heat transfer media, Heat transfer salt, Heat transfer regimes: Heat of vaporization, Heated cavity reflectometer, Heating media, for reboilers, Heavy water, physical properties of, Heggs, P J, Helical coils of circular cross section: Helical coils of rectangular cross section, Helical inserts, for enhancement of heat transfer in boiling, Helium: Helmholtz reciprocity principle, in radiative heat transfer, Henry, J A R, Henry-Fauske model, for critical two-phase flow, Henry's law, for partial pressure, Heptadecane: Heptadecene: Heptane: 1-Heptanol: 1-Heptene: Herman, K W, Hermes, C L L, Heterogeneous conveyance in horizontal pipes, Heterogeneous nucleation in boiling, Hewitt, G F

Introduction and Fundamentals Boiling within Vertical Tubes Conective Boiling Inside Horizontal Tubes Introduction Introduction

Hexachloroethane (Refrigerant 116): Hexacyclopentane, superheated vapor properties, Hexadecane: Hexadecene: 1,5-Hexadiene: Hexagonal cells, in free convection, Hexamethylbenzene: Hexane: Hexanoic acid: 1-Hexanol: 1-Hexene: Hexylbenzene: Hexylcyclohexane: Hexylcyclopentane, Hicks equation, for fixed-bed pressure drop, High pressure closures, ASME VIII code guidance for, High-chrome steels, thermal and mechanical properties, High-finned tubes, correlations for single-phase heat transfer in flow over, Hills, P D Hohlraum cavity, Holdup, in liquid-liquid flow, Holland, guide to national practice for mechanical design of heat exchangers, Homogeneous condensation (fog formation), Homogeneous model: Homogeneous nucleation: Honeycombs: Hopkins, D, Horizontal condensers: Horizontal cylinders: Horizontal layers, of fluid, free convection heat transfer in, Horizontal pipes: Horizontal shell-side evaporator, Horizontal surfaces: Horizontal thermosiphon reboilers: Horizontal tube-side evaporator, Horizontal tubes: Hottel's rule, in absorption of radiation by gases, Hsu criterion, for onset of nucleate boiling, Hybrid cooling towers, Hydraulic conveyance: Hydraulic expansion, of tubes into tube sheets in shell-and-tube heat exchangers, Hydraulic turbine, lost work in, Hydraulic resistance, in flow of supercritical fluids, Hydraulically smooth surface, Hydrazine: Hydrocarbons: Hydrodynamic entrance length, in single-phase flow in ducts, Hydrogen: Hydrogen bromide: Hydrogen chloride: Hydrogen cyanide: Hydrogen fluoride: Hydrogen iodide: Hydrogen peroxide: Hydrogen sulfide: Hydrostatic testing of shell-and-tube heat exchangers, Hysteresis:

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HEDH

A B C D E F G H

Hagen-Poiseuille law Hagen-Rubens relation, between electrical and optical constants, Hall Taylor, N S, Halogenated hydrocarbons: Handley and Heggs equation for fixed bed pressure drop, Hankinson and Thomson method, for liquid density: Hardening (precipative) of stainless steels, Hardwick, R, Harris, D, Hausen equation for developing laminar flow, Hays, G F Headers in shell-and-tube heat exchangers, Heads, in heat exchangers: Heat and mass transfer: Heat exchanger design, introduction, Heat exchangers: Heat of vaporisation (see Enthalpy of vaporisation), of pure substances Heat pipes: Heat pumping, relation to heat exchanger network design, Heat storage (see Regenerators and thermal energy storage) entropy generation in, Heat transfer: Heat transfer coefficient: Heat transfer media, Heat transfer salt, Heat transfer regimes: Heat of vaporization, Heated cavity reflectometer, Heating media, for reboilers, Heavy water, physical properties of, Heggs, P J, Helical coils of circular cross section: Helical coils of rectangular cross section, Helical inserts, for enhancement of heat transfer in boiling, Helium: Helmholtz reciprocity principle, in radiative heat transfer, Henry, J A R, Henry-Fauske model, for critical two-phase flow, Henry's law, for partial pressure, Heptadecane: Heptadecene: Heptane: 1-Heptanol: 1-Heptene: Herman, K W, Hermes, C L L, Heterogeneous conveyance in horizontal pipes, Heterogeneous nucleation in boiling, Hewitt, G F

Introduction and Fundamentals Boiling within Vertical Tubes Conective Boiling Inside Horizontal Tubes Introduction Introduction

Hexachloroethane (Refrigerant 116): Hexacyclopentane, superheated vapor properties, Hexadecane: Hexadecene: 1,5-Hexadiene: Hexagonal cells, in free convection, Hexamethylbenzene: Hexane: Hexanoic acid: 1-Hexanol: 1-Hexene: Hexylbenzene: Hexylcyclohexane: Hexylcyclopentane, Hicks equation, for fixed-bed pressure drop, High pressure closures, ASME VIII code guidance for, High-chrome steels, thermal and mechanical properties, High-finned tubes, correlations for single-phase heat transfer in flow over, Hills, P D Hohlraum cavity, Holdup, in liquid-liquid flow, Holland, guide to national practice for mechanical design of heat exchangers, Homogeneous condensation (fog formation), Homogeneous model: Homogeneous nucleation: Honeycombs: Hopkins, D, Horizontal condensers: Horizontal cylinders: Horizontal layers, of fluid, free convection heat transfer in, Horizontal pipes: Horizontal shell-side evaporator, Horizontal surfaces: Horizontal thermosiphon reboilers: Horizontal tube-side evaporator, Horizontal tubes: Hottel's rule, in absorption of radiation by gases, Hsu criterion, for onset of nucleate boiling, Hybrid cooling towers, Hydraulic conveyance: Hydraulic expansion, of tubes into tube sheets in shell-and-tube heat exchangers, Hydraulic turbine, lost work in, Hydraulic resistance, in flow of supercritical fluids, Hydraulically smooth surface, Hydrazine: Hydrocarbons: Hydrodynamic entrance length, in single-phase flow in ducts, Hydrogen: Hydrogen bromide: Hydrogen chloride: Hydrogen cyanide: Hydrogen fluoride: Hydrogen iodide: Hydrogen peroxide: Hydrogen sulfide: Hydrostatic testing of shell-and-tube heat exchangers, Hysteresis:

I J K L M N O P Q R S T U V W X Y Z

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Introduction

DOI 10.1615/hedhme.a.000457

4.8 COSTING OF HEAT EXCHANGERS
4.8.1 Introduction

G. F. Hewitt

A. Background

Perhaps the most important step in the application of heat exchangers to industrial processes is that which occurs at the process design stage. Here, the process designer makes a selection (which often turns out to be the final selection) of the type of heat exchanger which is to be used. In practice, many types can be eliminated at this stage on the grounds of unsuitability for the process; thus, for example, the process pressure may be greater than the maximum operating pressure of some exchanger types. Similarly, the toxicity of the process fluids may be such as to eliminate exchangers where the possibility of leakage occurs (for example through the gaskets of plate-and-frame heat exchangers). However, in most situations, there are several feasible types of heat exchanger available for a given application. Often, the selection is made on the basis of previous practice; thus, if shell-and-tube exchangers have always been used for a particular process application, then a safe option is to use them in any new process plant for the same application. It would be more logical to make a choice on the grounds of capital (and perhaps also operating) cost, but this depends on having sufficiently accurate costing methods at the process design stage. The object of this Section of HEDH is to provide a platform for the presentation of such methods.

Since perhaps the majority of heat exchangers are custom-built (or at least built by integrating mass produced parts) for each application, accurate costing is quite difficult to achieve and is usually done using proprietary computer codes developed and held by the manufacturers. These codes depend on estimation of materials, labour, overheads and shipping costs which are specific to a given manufacturer. However, the dictates of competition generally lead to costs from different manufacturers which are surprisingly similar. Here, one should make a clear distinction between cost and price, the latter being the result of a market judgement by the manufacturer’s sales team. If rapid delivery is required, the price may be much higher than the cost. If, on the other hand, the manufacturer wishes to maintain loading on his plant, they may actually sometimes quote a price which is lower than the cost as a short term measure (often called “buying the job” in the industry). Clearly, such a marketing policy could not be pursued in the longer term! Thus, it is assumed here that, on average over time, the price will be a reasonable reflection of the cost.

There are a number of techniques for carrying out rapid costing of heat exchangers. These include:

Using thermal design data, carry out a costing approximating to the full costing methodology. This could include, for instance, correction factors allowing adjustment of costs for a given design relative to a standard design. This is essentially the methodology given in Section 458, Section 459 and Section 460 for shell-and-tube, air-cooled and plate and frame exchangers respectively.
Base the cost on a predicted heat exchanger area. Here, the prediction is achieved normally by using estimated overall heat transfer coefficient (U) values and determining the surface area A from the relationship.

\[\label{eq1} A=\dfrac{\dot{Q}}{U\varDelta T_m} \tag{1}\]

where Q̇ is the total rate of heat transfer (W) and ΔT_m the mean temperature difference.
Base the cost on a predicted heat exchanger volume. Here, the volume (V) can be determined from the following relationship:

\[\label{eq2} V=\dfrac{\dot{Q}}{B\varDelta T_m} \tag{2}\]

where B is a volumetric overall heat transfer coefficient (W/m³K).
Base the estimate of cost on cost (C) per unit Q̇ /ΔT_m. This approach avoids problems in definition of heat exchanger area and allows direct comparison of various heat exchangers for a given duty. The method was originally devised by Hewitt, Guy and Marsland (Hewitt et al., 1982) but has been extensively adopted in later work by the Engineering Sciences Data Unit (ESDU, 1986; ESDU, 1994; ESDU, 1995; ESDU, 1997; ESDU, 1994).

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