section a1
purpose and organization
a1 purpose and organization
a1.1 general description
a1.2 suggested uses
a1.3 organization
section a2
units conversion
a2 units conversion
a2.1 definitions
a2.2 conventions
a2.3 conversion factors
table a2-1 basic si units
table a2-2 frequently used derived si units
table a2-3 prefixes indicating decimal multipilers
table a2-4 conversion factors for common measurements
section b1
principles of heat transfer
b1.1 principles of heat transfer processes
references
b1.2 overall heat transfer coefficient and supporting calculations
b1.2.1 fourier’s law concepts
b1.2.2 driving force and resistance concept
b1.2.3 derivation of the overall heat transfer coefficient, u
b1.2.3.1 basic relationships, flat plates
b1.2.3.2 circular cross sections
b1.2.3.3 estimating individual heat transfer coefficients
b1.2.4 derivation of the tube wall temperature, Tw
b1.2.5 average bulk temperature
b1.2.5.1 arithmetic average bulk temperature
b1.2.5.2 colburn caloric bulk temperature
references
b1.3 mean temperature difference
b1.3.1 exact and integrated solution
b1.3.2 flow arrangements
b1.3.2.1 f-correction-factor method
b1.3.2.2 number-of-transfer-units(NTU)method
b1.3.2.3 θ-p-ntu method
b1.3.2.4 effectiveness method
b1.3.3 graphical solutions
b1.3.4 mean temperature difference graphs for shell-and-tube exchangers
b1.3.4.1 countercurrent flow exchangers
b1.3.4.2 cocurrent flow exchangers
b1.3.4.3 tema e shell with even number of tubepasses, shell fluid mixed
b1.3.4.4 tema e shells, two to six units in series, even number of tubepasses
b1.3.4.8 tema h shell (double divided flow), even number of tubepasses
b1.3.4.9 tema f shell
b1.3.5 mean temperature difference graphs for crossflow arrangements
b1.3.5.1 unmixed-unmixed cross flow
b1.3.5.2 one pass and one, two, three, and four tuberows
b1.3.5.3 n tuberows in n passes, n = 2,3, and 4, countercurrent cross flow (u-bend sections)
b1.3.5.4 two passes, four tuberows, mixed between passes, counter flow (u-bend sections)
b1.3.5.5 n tuberows in n passes, n = 2 and 4, cocurrent cross flow (u-bend sections)
b1.3.5.6 two passes, four tuberows, mixed between passes, cocurrent cross flow
acknowledgements
references
nomenclature
figures
figure b1.2-1 heat transfer through a composite wall with fouling layers
figure b1.2-2 heat transfer through circular tubes
figure b1.2-3 wall resistance as a function of wall thickness and thermal conductivity
figure b1.3-1 diagram of temperature profiles
figure b1.3-2 graphical intergration of heat transfer equation
figure b1.3-3 tema e shell effectiveness, ξ versus NTUmin with Cmin/Cmax in parameter
figure b1.3-4 schematic relation of the f-p and θ-p-NTU2 charts
figure b1.3-5 countercurrent flow
figure b1.3-6 cocurrent flow
figure b1.3-7 one tema e shell with any even number of tubepasses(shell fluid mixed)
figure b1.3-8 schematic temperature profiles in two-tubepass tema e shell exchangers
figure b1.3-9 estimation of units in series from terminal temperatures
figure b1.3-10 two tema e shells in series with any even number of tubepasses
figure b1.3-11 three tema e shell in series with any even number of tubepasses
figure b1.3-12 four tema e shells in series with any even number of tubepasses
figure b1.3-13 five tema e shells in series with any even number of tubepasses
figure b1.3-14 six tema e shells in series with any even number of tubepasses
figure b1.3-15 tema j shell with one tubepasses
figure b1.3-16 tema j shell with any even number of tubepasses(also mixed-mixed cross flow)
figure b1.3-17 tema g shell with any even number of tubepasses(also mixed-mixed cross flow)
figure b1.3-18 tema h shell with any even number of tubepasses
figure b1.3-19 correction factor Fb for thermal leakage through longitudinal baffles in tema f shell exchangers
figure b1.3-20 basic flow combinations for a single-pass crossflow exchanger
figure b1.3-21 cross flow with both fluids unmixed
figure b1.3-22 crossflow unit with one tuberow, fluids unmixed
figure b1.3-23 crossflow unit with two tuberows and one pass, fluids unmixed
figure b1.3-24 crossflow unit with three tuberows and one pass, fluids unmixed
figure b1.3-25 crossflow unit with four tuberows and one pass, fluids unmixed
figure b1.3-26 crossflow unit with two tuberows and two passes, fluids unmixed between passes
figure b1.3-27 crossflow unit with three tuberows and three passes, fluids unmixed between passes
figure b1.3-28 crossflow unit with four tuberows and three passes, fluids unmixed between passes
figure b1.3-29 crossflow unit with four tuberows in two passes, two tuberows per pass, fluids mixed as the header
figure b1.3-30 crossflow unit with four tuberows and four passes, fluids unmixed between passes(cocurent)
figure b1.3-31 crossflow unit with four tuberows and two passes, fluids unmixed between passes (cocurrent)
figure b1.3-32 crossflow unit four tuberows in two passes, two tuberows per pass, fluids mixed at the header(cocurrent)
table b1.2-1 approximate ranges of heat transfer coefficients under clean conditions
section b2
single-phase pressure drop
b2.1 pressure drop inside conduits of constant cross section
b2.1.1 flow inside tubes
b2.1.1.1 isothermal flow
b2.1.1.2 nonisothermal flow
b2.1.1.3 calculated example
b2.1.2 flow inside tubes with twisted tape inserts
b2.1.2.1 turbulent flow
b2.1.2.2 laminar flow
b2.1.2.3 calculated example
b2.1.3 flow inside tubes with internal fins
b2.1.3.1 turbulent flow
b2.1.3.2 laminar flow
b2.1.4 in annuli
b2.1.5 axial flow in tube bundles with rod-type tube supports
b2.1.5.1 plain tubes
b2.1.5.2 finned tubes(annular low fins)
b2.1.5.3 calculated example, plain tubes
b2.1.5.4 calculated example, finned tubes
references
b2.2 pressure drop across plain tube banks
b2.2.1 basic geometry
b2.2.1.1 tube spacing terms
b2.2.1.2 cross-sectional flow area, Sx
b2.2.1.3 number of tuberows crossed in cross flow, Nrx
b2.2.2 isothermal flow
b2.2.3 nonisothermal flow
b2.2.3.1 nonisothermal correction, liquids
b2.2.3.2 nonisothermal correction, gases
b2.2.4 calculated example, plain tubes
references
b2.3 pressure drop across low-finned tube banks
b2.3.1 basic geometry
b2.3.2 friction factor correction
b2.3.3 nonisothermal correction
b2.3.4 pressure drop
b2.3.5 calculated example, low-finned tubes, 19 fins/in
references
b2.4 pressure drop across high-finned tube banks
b2.4.1 definitions and limitations
b2.4.1.1 air-cooler and limitations
b2.4.1.2 heat recovery tubes
b2.4.1.3 furnace convection sections
b2.4.1.4 HTRI corrections
b2.4.2 friction factor definition
b2.4.3 general correlation
b2.4.3.1 isothermal friction factor
b2.4.3.2 row correction factor
b2.4.3.3 physical property correction factor
b2.4.4 nonequilateral staggered layouts
b2.4.5 nonsquare inline layouts
b2.4.6 special finned tubes
b2.4.6.1 case1:small diameter tubes
b2.4.6.2 case2:serrated-finned tubes
b2.4.6.3 case3:large diameter smooth-finned tubes
b2.4.6.4 case4:large diameter stud-finned tubes
references
b2.5 pressure drop in plate-and-frame exchangers
b2.5.1 typical plate-and-frame configuration
b2.5.2 pressure drop estimation method
b2.5.2.1 channel flow pressure drop
b2.5.2.2 port pressure drop
references
b2.6 pressure drop in spiral plate heat exchangers
b2.6.1 pressure drop estimation method
b2.6.2 range of data and accuracy
references
b2.6 pressure drop in spiral plate heat exchangers
b2.6.1 pressure drop estimation method
b2.6.2 range of data and accuracy
references
b2.7 pressure drop in bends
b2.7.1 secondary flow
b2.7.2 bend classification
b2.7.3 loss coefficient method
b2.8 nomenclature
figures
figure b2.1-1 isothermal tubeside friction factor
figure b2.1-2 viscosity gradient correction factor
figure b2.1-3 natural convection correction factor
figure b2.1-4 RODbaffles with plate- and rode-type baffles rings
figure b2.2-1 tube layout angle = 30
figure b2.2-2 tube layout angle =45
figure b2.2-3 tube layout angle =60
figure b2.2-4 tube layout angle =90
figure b2.3-1 typical cross section and geometry of an integral fin tube
figure b2.4-1 transverse pitch correction factor for smooth-finned tubes in staggered layouts
figure b2.4-2 correlation exponent b* for smooth-finned tubes in staggered lay outs
figure b2.4-3 row correction factors for staggered layouts
figure b2.4-4 longitudinal pitch correction factor for staggered layouts
figure b2.4-5 longitudinal pitch correction factor for smooth-finned tubes,inline layouts
figure b2.4-6 longitudinal pitch correction for segmented-finned tubes,inline layouts
figure 2.5-1 plate heat exchanger f- and j-factors
figure 2.5-2 relationship between corrugated plate depth(Pp),plate spacing(Bp),and plate wall thickness(Tp)
figure 2.5-3 port pressure and channel pressure drop distributions for U arrangement
figure 2.5-4 port pressure and channel pressure drop distributions for Z arrangement
figure 2.5-5 relationship of Hp and △Pp,max/△Pt for U and Z arrangements
figure 2.6-1 SPHE with spiral/spiral flow (courtesy of Alfa Laval inc.)
figure 2.6-2 SPHE with spiral/axial flow (courtesy of alfa laval inc.)
figure 2.6-3 SPHE with spiral-spiral/axial flow(courtesy of alfa laval inc.)
figure 2.7-1 primary and secondary flow patterns through pipe bend
figure 2.7-2 turbulent eddies produced in sharp bend
tables
table b2.2-1 tube layout dimensions
table b2.2-2 constants for isothermal friction factor correlations
table b2.3-1 selected geometry for two low-finned tube types
table b2.3-2 physical property correction constants
table 2.4-1 data bank parameter ranges
table 2.4-2 constants for correlation equations
table 2.4-3 special finned-tube geometry and layout
table b2.6-1 statistically screened data used for SPHE pressure drop method evaluation
table b2.7-1 resistance coefficients for sharp bends(–)and large reynolds number (–)
section b3
single-phase heat transfer
b3.1 heat transfer inside conduits of constant cross section
b3.1.1 inside plain tubes
b3.1.1.1 turbulent flow:re > 10000
b3.1.1.2 laminar flow:re < 2000
b3.1.1.3 transitional flow:2000 < re < 10000
b3.1.1.4 stepwise determination of convective heat transfer coefficients
b3.1.1.5 calculated examples
b3.1.3 inside tubes with internal fins
b3.1.4 in annuli
b3.1.5 axial flow in tube bundles with rod-type tube supports
b3.1.5.1 plain tubes
b3.1.5.2 finned tubes(annular low fins)
b3.1.5.3 calculated examples
references
b3.2 heat transfer, plain tube banks
b3.2.1 basic correction
b3.2.2 curve-fit equation for(Ji)10
b3.2.2.1 liquids
b3.2.2.2 gases
b3.2.3 tuberow correction
b3.2.4 alternative form for turbulent flow
b3.2.5 baffled heat exchanger window heat transfer
b3.2.6 calculated example, plain tubes
references
b3.3 heat transfer, low-finned tube banks
b3.3.1 basic geometry, low-finned tubes
b3.3.2 heat transfer, j-factor correlation
b3.3.2.1 turbulent flow
b3.3.2.2 low reynolds numbers: RExr < 200(liquids) or RExr < 800(gases)
b3.3.2.3 gases with 800