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Study and Design of Crude Distillation Tower

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Besma ABDELLY

on 11 June 2015

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Transcript of Study and Design of Crude Distillation Tower

June 12th, 2015
abdellybesma@gmail.com
Tunis-TUNISIA
.
.
Overview of the Crude Distillation Unit "CDU"
Design of Crude Distillation Tower using AZERI crude oil
Results
Conclusion
Social
Study and Design of Crude Distillation Tower
Realised by:Besma ABDELLY
Design of Crude Distillation Tower
Architecture of the atmospheric column
CDU Volume and mass balance
Plane
Supervised by:Mm.Fatma ELLOUZE
Mr.Mohamed GUEZGUEZ

Conceptual Diagram of Crude Distillation Unit
Presentation Of Crude Distillation Unit

AZERI TBP curve
Light ends Analysis
Azeri general facts
AZERI Distribution
Gas+Naphtha: EP 149°C
Kerosene: 149-232°C
LGO:232-342°C
HGO:342-369°C
Residue:+369°C
CDU configuration
The flowrates of Stripping steam is adjusted using Jones and Pujado approach for which we assume:
1,2lbs of steam used to produce 1 gallon of residue
0,5lbs steam for 1 gallon of HGO or LGO
0,65lbs for 1 gallon of Kerosene
For kerosene side stripper, we are using a reboiled side stripper.
Reboiler duty is equal to heat provided by steam for which the rate is calculated using Jones approach .
DESIGN FILES
Step 1:Crude characetrization
Step 2:Inlet Parameters and architecture Specifications
Step 4:Estimation of Steam requirements in various sections
Step 6:Determination of Flash zone Temperature
Step 7: Energy balance across the flash zone
Step 9:Overall tower energy balance
and estimation of total reflux duties (condenser+BPA+TPA)
Step 11: Evaluation of Separation efficiency
Step 12: Calculation of column diameters at various sections
Calculation of temperatures Ratio using Maxwell Correlation
Calculation of FRL points for various V%
Calculation of EFV points for various V%
Calculation of DRL points for various V%
Step 8: Estimation of draw off tray temperatures
Total IN
Total OUT
Using the same procedure discussed in the previous section, we draw EFV curves for each cut at atmospheric pressure.
We calculate hydrocarbon partial pressure at draw off trays.
We finish by estimating trays temperatures at these pressures.

HGO draw off tray Temperature:
Packie's correlation
Draw off trays temperatures
Step 10: Estimation of Condenser duty
Total IN
Total OUT
Total IN
Total OUT

Step 3: Volume and Mass balances across the atmospheric tower
Geographical location of AZERI Well
Step 12: Modified Design
Step 5: Volume and mass Balances across the flash zone
Step 13:Side Strippers Diameters
Tray distribution in a Crude Distillation Tower
Step 14 :Cost Estimation
Final Design Recapitulative
3 pumparounds
Top tray reflux ratio=1,26
Top section diameter=4,47m
HGO section diameter=4,7m
Bottom section diameter=2,24m
HGO SS diameter=0,4478m
LGO SS diameter = 0,7218m
Kerosene SS diameter=0,8077m
Main Column Cost: 304SS=277.29$ , 316SS=335.633$
Sidestrippers cost : 304SS=96.0556$,316SS=113.8903$


Typical Refinery Process

Temperature ratio versus liquid volum % "Maxwell approach"
FRL slope versus DRL slope "Maxwell approach"
Maxwell approach for the determination of FRL50 for DRL slope
Vapor pressure data for hydrocarbons; "Maxwell approach"
HGO characteristics curves
Results Summary
Results Summary
Results Summary
Results Summary
Results Summary
Results Summary
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CONCLUSION
This work is a presentation of the crude distillation tower design procedure based on
Watkins
,
Jones
and
Pujado
assumptions which are considered as the best in this sector.
From the different designs, the
3 pumparounds
design seems to be the best in terms of separation efficiency and cost of trays, thus, it is taken as the final design.
Thank You For Your Attention...
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