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Proyecto Capstone Desing, Ejercicios de Diseño Capstone

Universidad de CartagenaDiseño Capstone
Prof. Jose David Gutierrez Meza

Proyecto Capstone Desing de ingeniería química

Tipo: Ejercicios

2020/2021

Subido el 27/11/2022

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SECOND STAGE OF CAPSTONE DESIGN
AUTHORS
ISAIAS ARIZA JIMENEZ
ANDRES FELIPE GUEBELY MARTELO
LAURA MARCELA MERCADO GUERRERO
MANUEL ALEJANDRO SUAREZ BALLESTEROS
JUAN CARLOS VERGARA VILLADIEGO
TUTOR
JOSE ANGEL COLINA MARQUEZ
SUBJECT
PLANT DESIGN
CARTAGENA DE INDIAS
UNIVERSITY OF CARTAGENA
CHEMICAL ENGINEERING
25/10/2021
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SECOND STAGE OF CAPSTONE DESIGN

AUTHORS

ISAIAS ARIZA JIMENEZ

ANDRES FELIPE GUEBELY MARTELO

LAURA MARCELA MERCADO GUERRERO

MANUEL ALEJANDRO SUAREZ BALLESTEROS

JUAN CARLOS VERGARA VILLADIEGO

TUTOR

JOSE ANGEL COLINA MARQUEZ

SUBJECT

PLANT DESIGN

CARTAGENA DE INDIAS

UNIVERSITY OF CARTAGENA

CHEMICAL ENGINEERING

PROJECT: PRODUCTION AND RECOVERY OF STYRENE FROM

ETHYLBENZENE DEHYDROGENATION

Target: 80000 TPY (basis: 8000 h of continuous production)

Raw material: Liquid ethylbenzene

Styrene is a monomer belonging to the group of aromatic hydrocarbons whose appearance

ranges from colorless to oily yellow liquid which evaporates easily and has a sweet odor.

Its molecular chemical formula is C8H8, it has a molecular mass of 104.2 g/mol, a boiling

point of 145°C and a melting point of -30°C. Styrene is apolar, can be dissolved in some

liquids, but is poorly soluble in water.

Styrene is a product widely used worldwide having multiple applications, some of these

are: polystyrene which is frequently used in packaging and automotive components and

appliances, expanded polystyrene (EPS), also known as white cork, used both in insulation

and packaging in construction, there are also the ABS and SAN copolymers used for the

manufacture of toys, small appliances, medical devices, etc., styrenic rubbers used in the

manufacture of tires, hoses, shoe soles, among others, and unsaturated polyester resins

(UPR) used in construction, furniture, impact-resistant surfaces (floors, kitchens,

bathrooms, etc.).

Styrene has some health risks among which we can highlight: Irritation of the skin, eyes,

throat and nose, rashes, headache and dizziness, it can also be carcinogenic so care must be

taken with its handling and exposure for which established safety protocols must be

followed.

ECONOMIC ASPECTS OF STYRENE IN COLOMBIA

 Total imports in Colombia

 Total imported: 636,188,463 U$.

 Quantity imported: 505,392,466 kilograms

 Unit price: 1,259 U$/kg

 Number of imports of the product styrene in Colombia: 290250

MAIN IMPORTERS IN COLOMBIA:

 Americas Styrenics de Colombia

 LTDA 68.4% (428,588,096 U$)

 AJOVER SAS 9.5% (59,427,649 U$)

 AJOVER SA 22.1% (138,748,789 U$)

MAIN COUNTRIES OF ORIGIN:

 United States 99.5%

 United Kingdom 0.5%

PRODUCTION VOLUME AND FOREIGN TRADE (TONS)

Block Flow Diagrams (BFD)

Figure 1. Block Flow Process Diagram for the Production and Recovery of Styrene from Ethylbenzene Dehydrogenation

Process Flow Diagrams (PFD)

Figure 2. Process Flow Diagrams for the Production and Recovery of Styrene from Ethylbenzene Dehydrogenation.

Detailed description of the process

1. Preheating

The reaction material, liquid phase ethylbenzene (stream 1), enters at a temperature of 25°C

and a pressure of 200 kPa into the heat exchanger (E-101) where the temperature is

increased from 25°C to 125°C, then exits the heat exchanger (stream 2) and passes to the

mixer (MX-101) where it enters a recirculated (stream 24) which has a temperature of

125°C with a composition of 99% ethylbenzene and 1% styrene, coming from the

distillation tower (T-103). The mixture coming from the mixer (MX-101) passes to the

exchanger (E-102) (stream 3) where its temperature is increased from 125°C to 171.111°C,

when leaving the exchanger (stream 4) it enters a steam mixer (MX-102) to increase its

temperature up to 600°C using the superheated steam (stream 8) which has a temperature of

620°C, coming from a divider (KV-101). All these temperature increases are performed to

meet the reaction conditions, finally the mixture comes out with a composition of 55%

water, 44,89551% ethylbenzene and 0,104489% styrene (stream 10) and enters the reactor

(R-101).

2. Overheating

The incoming water (stream 5) and the recirculated water (stream 18) from the three-phase

separator (V-101) enters the mixer (MX-103), reaching a temperature of 50ºC. This mixture

enters the boiler (H-101) (stream 6), which operates at constant pressure, where its

temperature rises to the saturation temperature, thus producing saturated steam, which

subsequently undergoes a superheating process because a higher temperature is required

with respect to the boiler's operating range (it should be noted that superheating is an

operation that occurs in conjunction with the boiler). In the superheat process the

temperature of the saturated steam is increased to a range between 580°C - 630°C, where it

becomes superheated steam (stream 7).

3. Reactor

In the Reactor (R-101) where the dehydrogenation reaction of ethylbenzene is carried out,

which works at a pressure of 200 kPa, a gaseous mixture enters (stream 10), which reacts

with the catalyst (Iron Oxide III). This reaction takes place at high temperatures (580°C -

630°C) so superheated steam is injected (stream 9) through the reactor jacket in order to

maintain a constant temperature. The reaction leaving the reactor (R-101) at a temperature

of 600°C (stream 12) had a conversion of 71.277%, generating the following products:

styrene, toluene, benzene, hydrogen, methane and ethylene, as well as unreacted

ethylbenzene and water. The reaction has a selectivity of 95% and comes out with a

composition of water 55%, styrene 32%, ethylbenzene 10.6666%, toluene 1.06666%,

benzene 0.71111%, hydrogen 0.53888%, methane 0.0094445% and ethylene 0.0072223%.

Reactions:

Formation of Styrene:

C 6 H 5 C 2 H 5 → C 6 H 5 C 2 H 3 + H 2

Formation of Benzene and Toluene:

C 6 H 5 C 2 H 5 → C 6 H 6 + C 2 H 4

Formation of Toluene and Methane:

C 6 H 5 C 2 H 3 + H 2 → C 6 H 5 C H 3 + C H 4

4. Cooling

To separate the styrene from the product obtained from the reactor (R-101), first the

product outlet temperature must be reduced (stream 12), it enters the heat exchanger (E-

103) where its temperature is reduced from 600°C to 370°C, then it exits (stream 13) to

another heat exchanger (E-104) where a second temperature reduction from 370°C to

250°C is performed, It then exits (stream 14) and enters a third heat exchanger (E-105),

lowering its temperature from 250°C to 104.444°C, then enters a fourth heat exchanger (E-

106) (stream 15) lowering its temperature from 104.444°C to 70°C. Finally, the mixture

passes to a three-phase separator (V-101) (stream 16).

5. Separation

To obtain the desired product (styrene) present in the mixture coming from the cooling, it

must go through a separation process. Since it is a liquid-liquid-steam mixture, it is sent to a

three-phase separator (V-101) (stream 16), which works at a pressure of 300 kPa and a

temperature of 70°C. This equipment was chosen because it provides greater efficiency at

the time of separating the water present in the mixture, it also has pressure control valves

and relief valves that do not allow the components to leave with a different pressure than

the desired one.

From the upper part of the three-phase separator (V-101) come the components: hydrogen

(which can be used as an alternative fuel since it pollutes much less due to the fact that

water and not CO2 is generated as a by-product of combustion), methane (which can be

used for electricity or energy generation), and ethylene (which can be used as a raw

material for the manufacture of various monomers and polymers), which are then sent to a

storage tank (TK-101) (stream 17). In the lower part, water is separated from the mixture

and recirculated (stream 18). Finally, a stream containing 72% styrene, 24% ethylbenzene,

2.4% toluene and 1.6% benzene is obtained from the central part (stream 19).

6. Distillation

To separate the styrene from the mixture (stream 19), it enters the distillation tower (T-101)

working at a pressure of 200 kPa, where the toluene and benzene were removed by the top

Design Heat Exchanger

When designing heat exchangers some restrictions must be taken into account, among these

is the percentage of excess area, taking into account that the ideal range would be between

5% and 25%, if it exceeds 25% it is considered that the exchanger is oversized and if it is

less than 5% it is considered that the exchanger is small, an ideal value for this percentage

would be around 15%. Another important factor in determining whether the heat exchanger

is adequate to perform its function is the pressure drop, which should not exceed 10 psi,

otherwise the exchanger is not suitable for operation.

 Heat Exchanger (E-101)

To increase the temperature of ethylbenzene from 25°C (Stream 1) to 125°C (Stream 2), a

heat exchanger (E-101) using steam at a pressure of 8 bar (800 kPa) (low pressure steam)

was chosen. Steam enters the heat exchanger (E-101) into the shell side with a temperature

of 170,411°C, while ethylbenzene enters into the tube side.

The heat exchanger (E-101) was designed with CHEMCAD 7 software, obtaining the

following results:

Simulation: Heat Exchanger E- FLOW SUMMARIES Stream No. 1 2 3 4 Stream Name Stream 1 LPS Stream 2 LPS Temp F 77.0000 338.7398 257.0000 330. Pres psia 29.0000 116.0200 29.0000 116. Enth MMBtu/h -1.1900 -12.474 0.77130 -14. Vapor mole frac. 0.00000 1.0000 0.00000 0. Total lbmol/h 224.9449 122.1011 224.9449 122. Total lb/h 23881.7305 2199.6506 23881.7305 2199. Total std L ft3/hr 438.8038 35.2351 438.8038 35. Total std V scfh 85361.80 46334.75 85361.80 46334. Flow rates in lbmol/h Ethylbenzene 224.9449 0.0000 224.9449 0. Water 0.0000 122.1011 0.0000 122. SUMMARY REPORT General Data: Heat Transfer Data: Exch Class/Type C/CEL Effective Transfer Area 120. Shell I.D. 0.83 Area Required 106. Shell in Series/Parallel 1/1 COR LMTD 149. Number of Tubes 53 U (Calc/Service) 122.45/108. Tube Length 12.00 Heat Calc 2. Tube O.D./I.D. 0.0625/0.0517 Heat Spec 1.

Excess % 13. Tube Pattern TRI60 Foul(S/T) 1.500E-003/1.500E- Tube Pitch 0.08 Del P(S/T) 0.23/3. Number of Tube Passes 4 SS Film Coeff 1743. Number of Baffles 0 SS CS Vel 0. Baffle Spacing 0.00 TW Resist 0. Baffle Cut, % Diameter 15 TS Film Coeff 354. Baffle Type NOBF TS Vel 4. Baffle space def. Edge-Edge Thermodynamics: K: NRTL H: Latent Heat D: Library Number of Components: 2 Calculation Mode: Design Engineering Units: Temperature F Flow/Hour (lb/h)/h Pressure psia Enthalpy MMBtu Diameter/Area ft/ft Length/Velocity ft/(ft/sec) Film Btu/hr-ft2-F Fouling hr-ft2-F/Btu TEMA SHEET 1 2 Customer Ref No. 3 Address Prop No. 4 Plant Loc. Date Rev 5 Service of Unit Item 6 Size 0.8ft x 12.0ft Type CEL (Hor/Vert) H Connected in 1 Para 1 Seri 7 Surf/Unit(G/E) 124.9/120.9 ft2; Shell/Unit 1.000000 Surf/Shell 124.9/120.9 ft 8 PERFORMANCE OF ONE UNIT 9 Type of Process Horiz Cond Sensible 10 Fluid Allocation Shell Side Tube Side 11 Fluid Name LPS Stream 1 12 Flow 2199.7 23881.7 lb/h 13 Liquid 0.0 23881.7 lb/h 14 Vapor 2199.7 0.0 lb/h 15 NonCondensable 0.00000 0.00000 lb/h 16 Steam 2199.7 0.0 lb/h 17 Evap/Cond 2199.7 0.0 lb/h 18 Density 0.25/55.98 / 0.25/56.29 0.00/53.91 / 0.00/48. lb/ft 19 Conductivity 0.02/0.39 / 0.02/0.39 0.00/0.07 / 0.00/0. Btu/hr-ft-F 20 Specific Heat 8.28/18.79 / 8.28/18.73 0.00/43.74 / 0.00/53. Btu/lbmol-F 21 Viscosity 0.02/0.16 / 0.02/0.16 0.00/0.64 / 0.00/0. cP 22 Latent Heat 882.54 0.00 Btu/lb 23 Temperature(In/Out) 338.739/330.000 77.000/257.000 F

pressure drop showed values lower than 10 psi and the excess area was 13.05 %, so it can

be concluded that the equipment is in optimal conditions to comply with its operation.

 Heat Exchanger (E-102)

To increase the temperature of the mixture from 125°C (stream 3) to 171,111°C (stream 4),

a heat exchanger (E-102) using steam at a pressure of 9 bar (900 kPa) (medium pressure

steam) was chosen. The steam enters the heat exchanger (E-102) into the shell side with a

temperature of 175.807°C, while the mixture enters into the tube side.

The heat exchanger (E-102) was designed with CHEMCAD 7 software, obtaining the

following results:

Simulation: Heat Exchanger E- FLOW SUMMARIES Stream No. 1 2 3 4 Stream Name Stream 3 MPS Stream 4 Water Temp F 257.0000 348.4529 340.0000 348. Pres psia 29.0000 131.0000 29.0000 131. Enth MMBtu/h 0.99931 -36.749 6.6491 -42. Vapor mole frac. 0.00000 1.0000 1.0000 0. Total lbmol/h 292.9861 359.2557 292.9861 359. Total lb/h 31104.0703 6471.9912 31104.0703 6471. Total std L ft3/hr 571.4508 103.6715 571.4508 103. Total std V scfh 111181.97 136329.86 111181.97 136329. Flow rates in lbmol/h Water 0.0000 359.2557 0.0000 359. Styrene 0.6869 0.0000 0.6869 0. Ethylbenzene 292.2992 0.0000 292.2992 0. SUMMARY REPORT General Data: Heat Transfer Data: Exch Class/Type C/CEL Effective Transfer Area 2522. Shell I.D. 2.25 Area Required 2324. Shell in Series/Parallel 1/1 COR LMTD 24. Number of Tubes 660 U (Calc/Service) 101.01/93. Tube Length 20.00 Heat Calc 6. Tube O.D./I.D. 0.0625/0.0517 Heat Spec 5. Excess % 8. Tube Pattern TRI60 Foul(S/T) 1.000E-003/1.000E- Tube Pitch 0.08 Del P(S/T) 0.29/1. Number of Tube Passes 2 SS Film Coeff 2277. Number of Baffles 0 SS CS Vel 0. Baffle Spacing 0.00 TW Resist 0. Baffle Cut, % Diameter 15 TS Film Coeff 171. Baffle Type NOBF TS Vel 13. Baffle space def. Edge-Edge

Thermodynamics: K: PSRK H: Mixed Model D: Library Number of Components: 3 Calculation Mode: Design Engineering Units: Temperature F Flow/Hour (lb/h)/h Pressure psia Enthalpy MMBtu Diameter/Area ft/ft Length/Velocity ft/(ft/sec) Film Btu/hr-ft2-F Fouling hr-ft2-F/Btu TEMA SHEET 1 2 Customer Ref No. 3 Address Prop No. 4 Plant Loc. Date Rev 5 Service of Unit Item 6 Size 2.3ft x 20.0ft Type CEL (Hor/Vert) H Connected in 1 Para 1 Seri 7 Surf/Unit(G/E) 2591.8/2523.0 ft2; Shell/Unit 1.000000 Surf/Shell 2591.8/2523.0 ft 8 PERFORMANCE OF ONE UNIT 9 Type of Process Horiz Cond Forced Evap 10 Fluid Allocation Shell Side Tube Side 11 Fluid Name MPS Stream 3 12 Flow 6472.0 31104.1 lb/h 13 Liquid 0.0 31104.1 lb/h 14 Vapor 6472.0 0.0 lb/h 15 NonCondensable 0.00000 0.00000 lb/h 16 Steam 6472.0 0.0 lb/h 17 Evap/Cond 6472.0 31104.1 lb/h 18 Density 0.29/55.63 / 0.29/55.65 0.39/48.17 / 0.38/45. lb/ft 19 Conductivity 0.02/0.39 / 0.02/0.39 0.01/0.06 / 0.01/0. Btu/hr-ft-F 20 Specific Heat 11.39/18.91 / 11.39/18.88 44.85/53.09 / 45.48/57. Btu/lbmol-F 21 Viscosity 0.02/0.15 / 0.02/0.15 0.01/0.26 / 0.01/0. cP 22 Latent Heat 872.49 139.69 Btu/lb 23 Temperature(In/Out) 348.452/348.000 257.000/340.000 F 24 Operating Pressure 131.00 29.00 psia 25 Fouling Factor 0.001000 0.001000 hr-ft2- F/Btu 26 Velocity 0.26 13.58 ft/sec 27 Press Drop Allow/Calc 10.000/0.286 10.000/1.544 psi 28 Heat Exchanged 5.650e+000 MMBtu/h; MTD(Corrected): 24.06 F 29 Transfer Rate, Service: 93.1 Calc: 101.0 Clean: 130.0 Btu/hr- ft2-F

 Heat Exchanger (E-103)

To decrease the temperature of the vapor mixture from 600°C (stream 12) to 370°C (stream

13), a heat exchanger (E-103) using water at a pressure of 4.826 bar (482.6 kPa) as the

coolant was chosen. The water enters the heat exchanger (E-103) into the tube side with a

temperature of 25°C, while the mixture enters into the shell side.

The heat exchanger (E-103) was designed with CHEMCAD 7 software, obtaining the

following results:

Simulation: Heat Exchanger E- FLOW SUMMARIES Stream No. 1 2 3 4 Stream Name Stream 12 Water Stream 13 Water Temp F 1112.0000 77.0000 698.0000 320. Pres psia 29.0000 70.0000 29.0000 70. Enth MMBtu/h -169.26 -94.628 -185.18 -78. Vapor mole frac. 1.0000 0.00000 1.0000 1. Total lbmol/h 2591.6895 770.4193 2591.6897 770. Total lb/h 69120.1563 13879.1025 69120.1719 13879. Total std L ft3/hr 1241.5964 222.3222 1241.5966 222. Total std V scfh 983490.75 292357.63 983490.81 292357. Flow rates in lbmol/h Ethylbenzene 69.4457 0.0000 69.4457 0. Styrene 212.3671 0.0000 212.3671 0. Water 2110.2473 770.4193 2110.2478 770. Toluene 8.0019 0.0000 8.0019 0. Benzene 6.2923 0.0000 6.2923 0. Methane 0.4067 0.0000 0.4067 0. Ethylene 0.1779 0.0000 0.1779 0. Hydrogen 184.7502 0.0000 184.7502 0. SUMMARY REPORT General Data: Heat Transfer Data: Exch Class/Type C/AEL Effective Transfer Area 411. Shell I.D. 1.27 Area Required 337. Shell in Series/Parallel 1/1 COR LMTD 592. Number of Tubes 192 U (Calc/Service) 79.52/65. Tube Length 11.00 Heat Calc 19. Tube O.D./I.D. 0.0625/0.0517 Heat Spec 15. Excess % 21. Tube Pattern TRI60 Foul(S/T) 1.000E-003/2.000E- Tube Pitch 0.08 Del P(S/T) 6.29/4. Number of Tube Passes 2 SS Film Coeff 120. Number of Baffles 0 SS CS Vel 119. Baffle Spacing 0.00 TW Resist 0.

Baffle Cut, % Diameter 15 TS Film Coeff 1970. Baffle Type NOBF TS Vel 48. Baffle space def. Edge-Edge Thermodynamics: K: NRTL H: Latent Heat D: Library Number of Components: 8 Calculation Mode: Rating Engineering Units: Temperature F Flow/Hour (lb/h)/h Pressure psia Enthalpy MMBtu Diameter/Area ft/ft Length/Velocity ft/(ft/sec) Film Btu/hr-ft2-F Fouling hr-ft2-F/Btu TEMA SHEET 1 2 Customer Ref No. 3 Address Prop No. 4 Plant Loc. Date Rev 5 Service of Unit Item 6 Size 1.3ft x 11.0ft Type AEL (Hor/Vert) H Connected in 1 Para 1 Seri 7 Surf/Unit(G/E) 414.7/411.2 ft2; Shell/Unit 1.000000 Surf/Shell 414.7/411.2 ft 8 PERFORMANCE OF ONE UNIT 9 Type of Process Sensible Forced Evap 10 Fluid Allocation Shell Side Tube Side 11 Fluid Name Stream 12 Water 12 Flow 69120.2 13879.1 lb/h 13 Liquid 0.0 13879.1 lb/h 14 Vapor 69120.2 0.0 lb/h 15 NonCondensable 0.00000 0.00000 lb/h 16 Steam 38016.1 0.0 lb/h 17 Evap/Cond 0.0 13879.1 lb/h 18 Density 0.05/0.00 / 0.06/0.00 0.16/62.22 / 0.15/57. lb/ft 19 Conductivity 0.05/0.00 / 0.03/0.00 0.02/0.35 / 0.02/0. Btu/hr-ft-F 20 Specific Heat 15.64/0.00 / 13.96/0.00 8.23/18.01 / 8.25/18. Btu/lbmol-F 21 Viscosity 0.03/0.00 / 0.02/0.00 0.01/0.92 / 0.01/0. cP 22 Latent Heat 0.00 911.21 Btu/lb 23 Temperature(In/Out) 1112.000/697.999 76.999/320.000 F 24 Operating Pressure 29.00 70.00 psia 25 Fouling Factor 0.001000 0.002000 hr-ft2- F/Btu 26 Velocity 127.85 48.99 ft/sec

 Heat Exchanger (E-104)

To decrease the temperature of the vapor mixture from 370°C (stream 13) to 250°C (stream

14), a heat exchanger (E-104) using water at a pressure of 4.826 bar (482.6 kPa) as the

coolant was chosen. The water enters the heat exchanger (E-104) into the tube side with a

temperature of 25°C, while the mixture enters into the shell side.

The heat exchanger (E-104) was designed using CHEMCAD 7 software, obtaining the

following results:

Simulation: Heat Exchanger E- FLOW SUMMARIES: Stream No. 3 5 6 7 Stream Name Stream 13 Water Stream 14 Water Temp F 698.0000 77.0000 482.0000 320. Pres psia 29.0000 70.0000 29.0000 70. Enth MMBtu/h -185.18 -44.730 -192.70 -37. Vapor mole frac. 1.0000 0.00000 1.0000 1. Total lbmol/h 2591.6897 364.1715 2591.6897 364. Total lb/h 69120.1719 6560.5503 69120.1719 6560. Total std L ft3/hr 1241.5966 105.0901 1241.5966 105. Total std V scfh 983490.81 138195.31 983490.81 138195. Flow rates in lbmol/h Ethylbenzene 69.4457 0.0000 69.4457 0. Styrene 212.3671 0.0000 212.3671 0. Water 2110.2478 364.1715 2110.2478 364. Toluene 8.0019 0.0000 8.0019 0. Benzene 6.2923 0.0000 6.2923 0. Methane 0.4067 0.0000 0.4067 0. Ethylene 0.1779 0.0000 0.1779 0. Hydrogen 184.7502 0.0000 184.7502 0. SUMMARY REPORT General Data: Heat Transfer Data: Exch Class/Type C/CEL Effective Transfer Area 448. Shell I.D. 1.27 Area Required 366. Shell in Series/Parallel 1/1 COR LMTD 284. Number of Tubes 192 U (Calc/Service) 72.11/58. Tube Length 12.00 Heat Calc 9. Tube O.D./I.D. 0.0625/0.0517 Heat Spec 7. Excess % 22. Tube Pattern TRI60 Foul(S/T) 1.000E-003/2.000E- Tube Pitch 0.08 Del P(S/T) 5.33/2.

Number of Tube Passes 2 SS Film Coeff 106. Number of Baffles 0 SS CS Vel 80. Baffle Spacing 0.00 TW Resist 0. Baffle Cut, % Diameter 15 TS Film Coeff 1448. Baffle Type NOBF TS Vel 23. Baffle space def. Edge-Edge Thermodynamics: K: NRTL H: Latent Heat D: Library Number of Components: 8 Calculation Mode: Design Engineering Units: Temperature F Flow/Hour (lb/h)/h Pressure psia Enthalpy MMBtu Diameter/Area ft/ft Length/Velocity ft/(ft/sec) Film Btu/hr-ft2-F Fouling hr-ft2-F/Btu TEMA SHEET 1 2 Customer Ref No. 3 Address Prop No. 4 Plant Loc. Date Rev 5 Service of Unit Item 6 Size 1.3ft x 12.0ft Type CEL (Hor/Vert) H Connected in 1 Para 1 Seri 7 Surf/Unit(G/E) 452.4/448.9 ft2; Shell/Unit 1.000000 Surf/Shell 452.4/448.9 ft 8 PERFORMANCE OF ONE UNIT 9 Type of Process Sensible Forced Evap 10 Fluid Allocation Shell Side Tube Side 11 Fluid Name Stream 13 Water 12 Flow 69120.2 6560.6 lb/h 13 Liquid 0.0 6560.6 lb/h 14 Vapor 69120.2 0.0 lb/h 15 NonCondensable 0.00000 0.00000 lb/h 16 Steam 38016.1 0.0 lb/h 17 Evap/Cond 0.0 6560.6 lb/h 18 Density 0.06/0.00 / 0.08/0.00 0.16/62.22 / 0.15/57. lb/ft 19 Conductivity 0.03/0.00 / 0.02/0.00 0.02/0.35 / 0.02/0. Btu/hr-ft-F 20 Specific Heat 13.96/0.00 / 12.89/0.00 8.23/18.01 / 8.25/18. Btu/lbmol-F 21 Viscosity 0.02/0.00 / 0.02/0.00 0.01/0.92 / 0.01/0. cP 22 Latent Heat 0.00 911.22 Btu/lb 23 Temperature(In/Out) 698.000/482.000 77.000/320.000 F