c08.1 - Thermal Equipment (Charts)

© 2009 IFP Training

EN ECH - 20243_a_A_pla_00 11/02/2009

Exploration & Production – Filed Operations ———

THERMAL EQUIPMENT

— Charts —

CHART 1: Units

CHART 2: Convection Heat Transfer Coefficients

CHART 3: Estimation of the Overall Heat Transfer Coefficient

CHART 4: Estimation of the Overall Heat Transfer Coefficient – Water-Hydrocarbons

CHART 5: LMTDCC Correction Factor F


00647_A_A

— Chart 1 —

UNITS

Unit systems

I.S. METRIC BRITISH

Q

units W kcalh BTU

h

Heat flowrate

W 1 0.8601 3.4118

or

kcalh 1.1626 1 3.9683

Duty

BTUh 0.2931 0.2520 1

A Units m2 m2 ft2

Heat exchange area m2 1 1 10.7639

ft2 0.0929 0.0929 1

Units W/m2 kcal

h• m2 BTUh • ft2

Φ Wm2 1 0.8601 0.3170

Thermal flux kcalh.m2 1.1626 1 0.3687

BTUh.ft2

3.1549 2.7122 1

∆θ Units K °C °F

Temperature difference K or °C 1 1 1,8

°F 0.5555 0.5555 1

units m2.KW h.m2.°C

kcal h.ft2.°FBTU

R m2.KW 1 1.1626 5.6782

Heat transfer h.m2.°Ckcal 0.8601 1 4.8824

resistance h.ft2.°FBTU 0.1761 0.2048 1

Units W

m2K kcal

h.m2.°C BTU

h.ft2.°F

U Wm2K

1 0.8601 0.1761

Heat transfer kcalh.m2.°C

1.126 1 0.2048

coefficient BTUh.ft2.°F

5,6782 4,8824 1


00647_A_A

— Chart 2 —

CONVECTION HEAT TRANSFER COEFFICIENTS

⎝⎜⎛

⎠⎟⎞ Heat transfer coefficients are expressed in kcal

h..m2 .°C • Natural convection Still air 40 km/h wind Furnace exhaust gases Gaseous hydrocarbons (reheated in storage) (* multiply these values by 2 if a stirrer is used) Water • Forced convection Laminar flow Hydrocarbons Water Turbulent flow Gaseous hydrocarbons (MW = 60) Gaseous hydrocarbons (MW = 60) + 80% + H Gasoline Water (40°C and 1 m/s) • Condensation Hydrocarbons Water Steam (∆θ = 10°C) Steam + 1% air + 2% air Vaporization Hydrocarbons Water

10 40 50 30* (µ = 1000 cP) 50* (µ = 100 cP) 50 - 250 (depending on speed and temperature) 50 - 80 (µ > 10 cP) 200 (µ = 3 cP) 150-400 1,700 (at 35 bar for ∆P = 0.5 bar) 500 (at 10 bar for ∆P = 0.2 bar) 200 (at 2 bar for ∆P = 0.06 bar) 1,700 ∅ 2,500 500 ∅ 1,000 200 ∅ 300 1,000 - 1,500 5,000 1,200 - 1,700 5,000 - 10,000 10,000 5,000 3,850 1,500 - 2,500 5,000 - 10,000

Conclusion: Generally: Natural convection < forced Laminar flow < turbulent Gas < liquid and HC < water


00647_A_A

— Chart 3 —

ESTIMATION OF THE OVERALL HEAT TRANSFER COEFFICIENT

FLUID U FLUID U

Tubes side Shell side (kcal/h.m2.°C) Tube side Shell side (kcal/h.m2.°C) 1. Coolers 2. Condensers Butadiene Steam 60 Butadiene Propylene (cooling) 330-390 Olefinic C4 Propylene (vaporization) 65-90 Olefinic C4 Propylene 290-330 Condensate ethylene Condensate and steam 450-600 Ethylene Propylene 300-450 Gaseous ethylene

Cold water 250-400 Light olefinic hydrocarbons

Propylene 250-300

Liquid ethylene Gaseous ethylene 50-100 HCl Propylene 300-550 Gaseous propane Liquid propane 30-75 Light ends and

chloroethanes Propylene 75-125

Light olefinic hydrocarbons CO, CO2, H2

Steam 50-100 Olefinic, chlorinated hydrocarbons

Water 450-600

Light, chlorinated hydrocarbons

Steam 60-150 Chlorinated hydrocarbons Water 100-150

Ethanol amine Steam 75-125 Solvent & non-condens. Water 125-75 Solvent Propylene (vaporization) 150-200 Water Gaseous propylene 650-750 Solvent Solvent 170-200 Water Propylene 300-500 Solvent Cold water 170-350 Water Steam 600-1 100 Oil Oil 300-400 Feed water Steam 100-150 Condensate Propylene 300-600 Oil Steam 350-550 25% calcium chloride Chlorinated C1 200-300 Cold water Air-Cl2 (partial condensation) 40-75 Steam Air (mixture) 50-100 Water Propylene (refrigeration and

condensation)(1)

Steam Styrene and tar 250-300 Water Light hydrocarbons (refrigeration and condensation)(1)

200-450

Cold water Freon 12 500-600 Water Ammoniac 700-800 Cold water Transformation oil 200-350 Air-steam Freon 50-250 Water Feed water (35-45°C) 500-600 3. Reboilers Water Feed water (100-35°C) 800-1 100 Olefinic C4 Steam 450-550 Water Light, chlorinated C2

hydrocarbons 30-50 Chlorinated hydrocarbons Steam 170-220

Water Heavy chlorinated C2 hydrocarbons

220-150 Olefinic chlorinated hydrocarbons

Steam 500-700

Water Perchlorethylene 270-170 Dichlorethane Steam 350-450 Water Air-Cl2 40-90 heavy solvent Steam 350-550 Water HCl 35-75 Mono and diethanolamine Steam 750-1 100 Water Air and steam 100-170 Organic acids - water Steam 300-500 Water Absorbing oil 400-560 Amine - water Steam 600-700 Steam Naphtha 75-100 Propylene Ethane-ethylene 600-700 Propylene-butadiene Butadiene-olefins 75-90 (1) Depending on the temperature range: 550-750 (– 10 to – 5°C) ; 125-250 (0 to 7°C).

BA

100 200 300 400 500 600 700 1000

U (kcal/hr/m2/°C)

Steam

Light HC - change in phase

Light HC - no change in phase

Middle HC - no change in phase

Heavy HC - no change in phase

Heavy hydrocarbons - residue(without change in phase)

Middle hydrocarbons - heavydistillate (without change in phase)

Light hydrocarbons - C3-C4 (without change in phase)

Light hydrocarbons(with change in phase)

Cooling water

Saturated water steam

D M

TE 2

085

B

Overall heat transfer coefficient

Cooling water

1000

1001 2 3 4 5 6 7 8 910 20 30 40 50 60 80 100 200 300 400 600 1000

200

300

400500600

800

100

60

80

1 2 3 4 5 6 7 8 9 10 20 30 40 50 60 80 100

200

300

400

500600700

300

400

500

535

kcal/h.m2.°C

kcal/h.m2.°C

kcal/h.m2.°C

306090150

© 2009 - IFP Training

LIQUID HYDROCARBON COOLER

GASEOUS HYDROCARBON COOLER

TOTAL HYDROCARBON CONDENSER

ESTIMATION OF THE OVERALL HEAT TRANSFER COEFFICIENT— Water - Hydrocarbons —

Pressure (bar.a)

Pressure (bar.a)

Fouling resistance

- Tube side water : 0.0004 h.m2.°C/kcaleau côté tube : ≈ 0.0020 h.ft2.°F/Btu- Shell side HC : 0.0004 h.m2.°C/kcal

- Tube side water : 0.0004 h.m2.°C/kcaleau côté tube : ≈ 0.0020 h.ft2.°F/Btu- Shell side HC : 0.0004 h.m2.°C/kcal

Tube side water : 0.0004 h.m2.°C/kcaleau côté tube : ≈ 0.0020 h.ft2.°F/Btu

Fouling resistances

Fouling resistances

Molecular weight

Isotherme

Viscosity (cP)

0.5 0.7 1 2 3 5 7 10 20 30 50 70 100

Temperature interval DT = 10°C

Temperature interval DT = 37.8°C

Temperature interval DT = 65.6°C

D M

TE 2

182

B

Low fouling

High fouling

— Chart 4 —

D M

TE 2

182

D


0030

2_A_

A

00.50.60.70.80.91.0

0.10.2

0.30.4

0.5e :

effic

iency

F1-2 : LMTDcc correction factor

0.60.7

0.80.9

r = 0.1

0.2

0.3

0.4

0.5

0.6

0.7

0.8

0.9

1.0

1.2

1.4

1.6

1.8

2.0

2.5

3.0

4.0

6.0

8.010

15r = 20

1.0

T 1

T 2

t 2 t 1

LMTD

cc C

ORRE

CTIO

N FA

CTOR

— 1

shell

pass

, 2 or

2 n t

ube p

asse

s —

e =

t 2 - t

1T 1

- t 1

r = T 1

- T 2

t 2 - t

1F 1

-2 =

DT

M 1-2

LMTD

cc

Area

corre

spon

ding

to o

utlet

tem

pera

ture

s cro

ss

LMTDCC CORRECTION FACTOR (F)

Q =

U . A

. MTD

1-2

=

U . A

. (F 1

-2 . L

MTD c

c)

– Chart 5 – 1/6


0030

3_A_

A

LMTDCC CORRECTION FACTOR (F)

00.50.60.70.80.91.0

0.10.2

0.30.4

0.50.6

0.70.8

0.91.0

e =

t 2 - t

1T 1

- t 1

r = T 1

- T 2

t 2 - t

1

r = 0.10.2

0.30.4

0.5

0.6

0.7

0.8

0.9

1.0

1.2

1.4

1.6

1.8

2.0

2.5

3.0

4.0

6.0

8.010

15r = 20

e : ef

ficien

cy


LMTD

cc C

ORRE

CTIO

N FA

CTOR

— 2

shell

pass

es, 4

or 4

n tub

e pas

ses —

T 2T 1

t 1t 2

Q =

U . A

. MTD

2-4

=

U . A

. (F 2

-4 . L

MTD c

c)F 2

-4 =

MT

D 2-4

LMTD

cc

Area

corre

spon

ding

to o

utlet

tem

pera

ture

s cro

ss

– Chart 5 – 2/6

00.50.60.70.80.91.0

0.10.2

0.30.4

0.50.6

0.70.8

0.91.0

e : ef

ficien

cy

F3-6: LMTDcc correction factor

LMTD

cc C

ORRE

CTIO

N FA

CTOR

— 3

shell

pass

es, 6

or 6

n tub

e pas

ses —

T 2

T 1

t 1t 2

0.4r = 0.2

0.6

0.8

1.0

1.2

1.4

1.6

1.8

2.0

2.5

3.0

4.0

6.0

8.010

15r = 20

Area

corre

spon

ding

to o

utlet

tem

pera

ture

s cro

ss

e =

t 2 - t

1T 1

- t 1

r = T 1

- T 2

t 2 - t

1Q

= U

. A . M

TD3-

6

= U

. A . (

F 3-6

. LMT

D cc)

F 3-6

=

MTD 3

-6LM

TDcc


0030

4_A_

A

LMTDCC CORRECTION FACTOR (F)– Chart 5 – 3/6

00.50.60.70.80.91.0

0.10.2

0.30.4

0.50.6

0.70.8

0.91.0

e : ef

ficien

cy


LMTD

cc C

ORRE

CTIO

N FA

CTOR

— 4

shell

pas

ses,

8 or 8

n tu

be p

asse

s —

Area

corre

spon

ding

to o

utlet

tem

pera

ture

s cro

ss

4sh

ells

T 2T 1

t 1t 2

0.2r = 0.40.6

0.8

1.0

1.2

1.4

1.6

1.8

2.5

2.0

3.0

4.0

6.0

8.0

10

15r = 20

e =

t 2 - t

1T 1

- t 1

r = T 1

- T 2

t 2 - t

1Q

= U

. A . M

TD4-

8

= U

. A . (

F 4-8

. LMT

D cc)

F 4-8

=

MTD 4

-8LM

TDcc


0030

5_A_

A


00.50.60.70.80.91.0

0.10.2

0.30.4

0.50.6

0.70.8

0.91.0

e : ef

ficien

cy


0.20.4r = 0.6

0.8

1.0

1.2

1.4

1.6

1.8

2.5

2.0

3.0

4.0

6.0

8.0

10

15r = 20

LMTD

cc C

ORRE

CTIO

N FA

CTOR

— 5

shell

pas

ses,

10 o

r 10 n

tube

pas

ses —

5sh

ells

T2T1

t1t2

e =

t2 - t

1T1

- t1

r = T1

- T2

t2 - t

1Q

= U

. A . M

TD5-

10

= U

. A . (

F5-1

0 . LM

TDcc

)F 5

-10 =

MT

D 5-1

0LM

TDcc

Area

corre

spon

ding

to o

utlet

tem

pera

ture

s cro

ss


0030

6_A_

A


00.50.60.70.80.91.0

0.10.2

0.30.4

0.50.6

0.70.8

0.9

0.20.4r = 0.6

0.8

1.0

1.2

1.4

1.6

1.8

2.5

2.0

3.0

4.0

6.0

8.0

10

15r = 20

1.0e :

effic

iency


Area

corre

spon

ding t

o outl

et tem

pera

tures

cros

s

LMTD

cc C

ORRE

CTIO

N FA

CTOR

— 6

shell

pas

ses,

12 o

r 12 n

tube

pas

ses —

Q =

U . A

. MTD

6-12

=

U . A

. (F 6

-12 .

LMTD

cc)

F 6-1

2 =

MTD 6

-12

LMTD

cc

Area

corre

spon

ding

to o

utlet

tem

pera

ture

s cro

ss

6sh

ells

T 2T 1

t 1t 2

e =

t 2 - t

1T 1

- t 1

r = T 1

- T 2

t 2 - t

1


0030

7_A_

A


c08.1 - Thermal Equipment (Charts)

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