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Heat Exchanger Thermal Design Tasc 23.0File name: Untitled.EDR Date: 4/26/2011 Time: 9:03:06 AM

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Heat Exchanger Specification Sheet

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6 Size 19/ 39.3701in Type BEM Hor Connected in 1 parallel 1 series

7 Surf/unit(eff.) 198.1 ft2 Shells/unit 1 Surf/shell (eff.) 198.1 ft2

8 PERFORMANCE OF ONE UNIT

9 Fluid allocation Shell Side Tube Side

10 Fluid name HOT OIL WATER

11 Fluid quantity, Total lb/h 16509 22046

12 Vapor (In/Out) lb/h 0 0 0

13 Liquid lb/h 16509 16509 22046 22046

14 Noncondensable lb/h 0 0

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16 Temperature (In/Out) F 302 248 86 107.6

17 Dew / Bubble point F

18 Density (Vap / Liq) lb/ft3 / 51.406 / 52.9 / 62.262 / 62.043

19 Viscosity cp / 0.4646 / 0.599 / 0.7998 / 0.6301

20 Molecular wt, Vap

21 Molecular wt, NC

22 Specific heat BTU/(lb*F) / 0.5433 / 0.525 / 1.0008 / 1.0001

23 Thermal conductivity BTU/(ft*h*F) / 0.071 / 0.074 / 0.351 / 0.36

24 Latent heat BTU/lb

25 Pressure psi 64.005 63.741 71.117 70.827

26 Velocity ft/s 0.08 0.28


27 Pressure drop, allow./calc. psi 3.75 0.264 7.25 0.29

28 Fouling resist. (min) ft2*h*F/BTU 0 0 0 Ao based

29 Heat exchanged 476391 BTU/h MTD corrected 176.75 F

30 Transfer rate, Service 13.61 Dirty 9.97 Clean 9.97 BTU/(h*ft2*F)

31 CONSTRUCTION OF ONE SHELL Sketch

32 Shell Side Tube Side

33 Design/Vac/Test pressure psi 80 / / 80 / /

34 Design temperature F 370 180

35 Number passes per shell 1 2

36 Corrosion allowance in 0.125 0.125

37 Connections In in1 2 / - 1 2 / -

38 Size/rating Out 1 1.5 / - 1 1.5 / -

39 Nominal Intermediate / - / -

40 Tube No. 334 OD 0.75 Tks- Avg 0.065 in Length 3.2808 ft Pitch0.9375 in

41 Tube type Plain Material Carbon Steel Tube pattern 30

42 Shell Carbon Steel ID 19.685 OD 20.435 in Shell cover -

43 Channel or bonnet Carbon Steel Channel cover -

44 Tubesheet-stationary Carbon Steel Tubesheet-floating -

45 Floating head cover - Impingement protection None

46 Baffle-crossing Carbon Steel Type Unbaffled Cut(%d) Spacing: c/c 19.685

47 Baffle-long - Seal type Inlet

48 Supports-tube U-bend Type

49 Bypass seal Tube-tubesheet joint Exp.

50 Expansion joint - Type

51 RhoV2-Inlet nozzle 753 Bundle entrance 25 Bundle exit 24 lb/(ft*s2)

52 Gaskets - Shell side Flat Metal Jacket Fibe Tube Side Flat Metal Jacket Fibe

53 Floating head -

54 Code requirements ASME Code Sec VIII Div 1 TEMA class R - refinery service

55 Weight/Shell 1517.1 Filled with water 2056 Bundle 764.4

T1

T2 S1S2


56 Remarks

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Overall Performance

Rating / Checking Shell Side

Total mass flow rate lb/h 16509

Vapor mass flow rate (In/Out) lb/h 0 0 0

Liquid mass flow rate lb/h 16509 16509 22046

Vapor mass quallity 0 0 0

Temperatures F 302 248 86

Dew point / Bubble point F

Operating Pressures psi 64.005 63.741 71.117

Film coefficient BTU/(h*ft2*F) 11.41

Fouling resistance ft2*h*F/BTU 0

Velocity (highest) ft/s 0.08

Pressure drop (allow./calc.) psi 3.75 / 0.264 7.25

Total heat exchanged BTU/h 476391 Unit BEM 2 pass

Overall clean coeff. (plain/finned) BTU/(h*ft2*F) 9.97 / Shell size 19

Overall dirty coeff. (plain/finned) BTU/(h*ft2*F) 9.97 / Tubes Plain

Effective area (plain/finned) ft2 198.1 / No. 334 OD 0.75

Effective MTD F 176.75 Pattern 30

Actual/Required area ratio (dirty/clean) 0.73 / 0.73 Baffles Unbaffled

Vibration problem (Tasc/TEMA) /

RhoV2 problem No Total cost 14726

Resistance Distribution

Overall Coefficient / Resistance Summary Clean Dirty

Area required ft2 270.5 270.5

Area ratio: actual/required 0.73 0.73


Overall coefficient BTU/(h*ft2*F) 9.97 9.97

Overall resistance ft2*h*F/BTU 0.1003 0.1003

Shell side fouling ft2*h*F/BTU 0.0 0

Tube side fouling 0.0 0

Resistance Distribution BTU/(h*ft2*F) ft2*h*F/BTU % %

Shell side film 5028.21 0.0876 87.31 87.31

Shell side fouling 0 0

Tube wall 5028.21 0.0002 0.2 0.2

Tube side fouling * 0 0

Tube side film * 79.77 0.0125 12.49 12.49

* Based on outside surface - Area ratio: Ao/Ai = 1.21

Heat Transfer Coefficients

Film coefficients BTU/(h*ft2*F) Shell Side

Bare area (OD) / Finned area

Overall film coefficients 11.41 / 79.77

Vapor sensible 0 /

Two phase 0 /

Liquid sensible 11.41 / 79.77

Heat Transfer Parameters In Out In

Prandtl numbers Vapor

Liquid 8.63 10.33

Reynolds numbers Vapor Nominal

Liquid Nominal 843.28 654.57 1681.44

MTD and Flux

Temperature Difference F Heat Flux (based on tube O.D)

Overall effective MTD 176.75 Overall actual flux


One pass counterflow MTD 177.86 Critical flux

LMTD based on end points 177.71 Highest actual flux

Effective MTD correction factor 0.99 Highest actual/critical flux

Wall Temperatures F

Shell mean metal temperature 273.96

Tube mean metal temperature 119.24

Tube wall temperatures (highest/lowest) 125.59 / 107.65

Duty Distribution

Heat Load Summary Shell Side

BTU/h % total

Vapor only 0 0

2-Phase vapor 0 0

Latent heat 0 0

2-Phase liquid 0 0

Liquid only 476391 100

Total 476391 100

Pressure Drop

Pressure Drop psi Shell Side

Maximum allowed 3.75

Total calculated 0.264

Gravitational 0

Frictional 0.264

Momentum change 0

Pressure drop distribution ft/s psi %dp ft/s

Inlet nozzle 3.83 0.096 36.46 4.22


Entering bundle 0.7 0.28

Inside tubes 0.28 0.28

Inlet space Xflow 0 0

Baffle Xflow 0 0

Baffle windows 0.08 0.08 0 0.13

Outlet space Xflow 0 0

Exiting bundle 0.68 0.28

Outlet nozzle 6.13 0.167 63.41 6.98

Intermediate nozzles

Thermosiphon Piping

Piping reference points ft Pressure points psi F

Height of liquid in column Liquid level in column

Height of heat transfer region inlet Inlet to heated section

Height of heat transfer region outlet Boiling boundary position

Height of column return line Outlet of heated section 107.6

Exit of outlet piping

Pressure changes (-loss/+gain) psi Inlet circuit Exchanger

Frictional

Gravitational

Momentum

Flashing

Nozzles

Total

Inlet Circuit Piping

Inlet circuit element

Frictional pressure drop at entry psi

Frictional pressure drop at element psi


Outlet Circuit Piping

Outlet circuit element

Frictional pressure drop at entry psi

Frictional pressure drop at element psi

Void fraction

Two phase flow pattern

Flow Analysis

Shell Side Flow Fractions Inlet Middle Outlet

Crossflow 0 0 0

Window 0.93 0.93 0.93

Baffle hole - tube OD 0 0 0

Baffle OD - shell ID 0 0 0

Shell ID - bundle OTL 0.07 0.07 0.07

Pass lanes 0 0 0

Rho*V2 Analysis Flow area Velocity Density

in2 ft/s lb/ft3

Shell inlet nozzle 3.356 3.83 51.406

Shell entrance 7.85 1.64 51.406

Bundle entrance 18.431 0.7 51.406

Bundle exit 18.431 0.68 52.9

Shell exit 6.053 2.06 52.9

Shell outlet nozzle 2.036 6.13 52.9

in2 ft/s lb/ft3

Tube inlet nozzle 3.356 4.22 62.262

Tube inlet 50.418 0.28 62.262

Tube outlet 50.418 0.28 62.043

Tube outlet nozzle 2.036 6.98 62.043


Thermosiphons and Kettles

Thermosiphons

Thermosiphon stability

Vertical tube side thermosiphons

Flow reversal criterion - top of the tubes (should be >0.5)

Flooding criterion - top of the tubes (should be >1.0)

Fraction of the tube length flooded

Kutateladze Number in axial nozzle

Kettles

Recirculation ratio

Quality at top of bundle

Entrainment fraction

Methods Summary

Hot side

Heat Transfer Coefficient multiplier No

Heat Transfer Coefficient specified No

Pressure drop multiplier No

Pressure drop calculation option friction+acceleration

Calculation method Standard method

Desuperheating heat transfer method Wet wall

Multicomponent condensing heat transfer method HTFS - Silver-Bell

Vapor shear enhanced condensation Yes

Liquid subcooling heat transfer (vertical shell) Not Used


Subcooled boiling accounted for in Set default

Post dryout heat transfer accounted for in No

Correction to user-supplied boiling curve Boiling curve not used

Falling film evaporation method HTFS recommended method

Single phase tube side heat transfer method HTFS recommended method

Lowfin Calculation method HTFS / ESDU


Basic Geometry

Unit Configuration

Exchanger type Tube number

Position BEM Tube length actual ft

Arrangement 1 parallel 1 series Tube passes

Baffle type Unbaffled Tube type

Baffle number 0 Tube O.D. in

Spacing (cen-cen) in 19.685 Tube pitch in

Spacing at inlet in Tube pattern

Shell Kettle Front head Rear Head

Outside diameter in 20.435 20.435 20.435

Inside diameter in 19.685 19.685 19.685

Shell Side Shell Side Shell Side Tube Side Tube Side

Nozzle type Inlet Outlet Inlet Outlet

Number of nozzles 1 1 1 1

Actual outside diameter in 2.375 1.9 2.375 1.9

Inside diameter in 2.067 1.61 2.067 1.61

Height under nozzle in 0.7577 0.7577

Dome inside diameter in

Vapor belt inside diameter in

Vapor belt inside width in

Vapor belt slot area in2

Impingement protection No impingement No impingement

Distance to tubesheet in 34.25 4.25


Tubes

Tubes

Type Plain Total number of tubes

Outside diameter in 0.75 Number of tubes plugged

Inside diameter in 0.62 Tube length actual ft

Wall thickness in 0.065 Tube length effective ft

Area Ratio Ao/Ai 1.21 Tube sheet thickness in

Pitch in 0.9375 Material

Pattern 30 Thermal conductivity BTU/(ft*h*F)

External enhancement Internal enhancement

Low circumferential fins Low longitudinal fins

Fin density #/in Fin number

Fin height in Fin thickness in

Fin thickness in Fin height in

Tube root diameter in Fin spacing in

Tube wall thickness under

fin in Cut and twist length in

Baffles

Baffles

Type Unbaffled Baffle cut: inner/outer/interm

Tubes in window Yes Actual (% diameter) /

Number 0 Nominal (% diameter) /

Spacing (center-center) in 19.685 Actual (% area) /

Spacing at inlet in Cut orientation


Spacing at outlet in Thickness in

Spacing at center in/out for G,H,I,J in Tube rows in baffle overlap

Spacing at center for H shell in Tube rows in baffle window

End length of the front head in Baffle hole - tube od diam clearance in

End length of the rear head in Shell id - tube od diam clearance in

Variable Baffle Spacings

Baffle spacing in

Baffle cut percent, outer

Baffle cut percent, inner

Number of baffle spaces

Baffle region length in

Baffle cut area percent, outer

Baffle cut area percent, inner

Supports - Misc. Baffles

Supports - tubes Longitudinal baffle

Supports under inlet nozzle Thickness in

Supports under outlet nozzle Window length at front end in

Supports between baffles 0 Window length at center in

Supports blanking baffles No Window length at rear end in

Supports at u-bend 0

Supports at in/out of G,H,I,J shell 0

Supports at center of H shell 0

Supports for K,X shells 0


Bundle

Shell ID to center 1st tube row Tube passes

From top in 0.7577 Tube pass layout Ribbon (single band)

From bottom in 0.5643 Tube pass orientation Horizontal

From right in 0.5613 U-bend orientation undefined

From left in 0.5613 Horizontal pass lane width in

Vertical pass lane width in

Impingement protection None Interpass tube alignment

Impingement distance in Deviation in tubes/pass

Impingement plate diameter in Outer tube limit in

Impingement plate width in Shell id - bundle otl diam clearance in

Impingement plate length in Tie rod number

Gross surface area per shell ft2 215.2 Tie rod diameter in

Effective surface area per shell ft2 198.1 Sealing strips (pairs)

Bare tube area per shell ft2 198.1 Tube to Tubesheet joint

Finned area per shell ft2 0 Tube projection from front tsht in

U-bend area per shell ft2 0 Tube projection from rear tsht in

Enhancements

Internal enhancements

Tube insert type NoneTwisted tape

thickness in

Twist tape 360 deg twist pitch in


Thermosiphon Piping

Inlet circuit


Inside diameter in

Length or radius in

Number in parallel

Number in series

Outlet circuit


Inside diameter in

Length or radius in

Number in parallel

Number in series

Cost/Weights

Weights lb Cost data

Shell 415.9 Labor cost

Front head 150.2 Tube material cost

Rear head 186.6 Material cost (except tubes)

Shell cover

Bundle 764.4

Total weight - empty 1517.1 Total cost (1 shell)

Total weight - filled with water 2056 Total cost (all shells)


Tube Layout

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Documents

total cost

radius number

htfs recommende

shell supports

parallel number

psi btu

edr date

diameter