CDU/VDU Heat Integration
CDU/VDU Heat Integration
CDU/VDU Heat Integration
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<strong>CDU</strong>/<strong>VDU</strong> <strong>Heat</strong> <strong>Integration</strong><br />
Nov. 27th, 2008<br />
Hyundai Oilbank<br />
Technical Service Team
Table of Contents<br />
I. Company History<br />
II. Company Overview<br />
III. Refinery Process<br />
IV. Plant Capacity<br />
V. <strong>CDU</strong>/<strong>VDU</strong> <strong>Heat</strong> integration
COMPANY<br />
HISTORY<br />
1964. 11 Kukdong Oil Company Ltd established<br />
1965. 12 Pusan Refinery Plant completed (3,000 BPSD)<br />
1989. 11 Daesan Refinery Plant completed (110,000 BPSD)<br />
1994. 5 “OILBANK” concept adopted<br />
1996. 5 Expansion of refinery facilities completed<br />
(200,000 BPSD) in Daesan Plant<br />
1998. . 5 Aromatic Complex completed<br />
(BTX unit : 400,000 ton/year)<br />
1999. 12 Joint ownership with IPIC commenced<br />
2002. 4 Company name changed to “HYUNDAI OILBANK”<br />
※ IPIC : International Petroleum Investment Company
DAESAN REFINERY OVERVIEW<br />
Seoul Office<br />
Daesan Refinery<br />
14 Terminal<br />
seoul<br />
Kangwon<br />
• Process area : 300,000 m 2<br />
Kyungki<br />
• Storage facility : 560,000 m 2<br />
• Power plant : 99,000 m 2<br />
• Related Chungbuk facility : 660,000 m Chungnam<br />
2<br />
Kyungbuk<br />
• Total : 1,619,000 m 2<br />
STC<br />
LG/LOTTE<br />
10 Exchange<br />
Office<br />
Jeonnam<br />
Jeonbuk<br />
Kyungnam<br />
KNOC<br />
HDO<br />
Je-ju<br />
KCC
REFINERY PROCESS<br />
Fuel Gas<br />
Gas Recovery<br />
Sulfur Removal &<br />
Treating<br />
Propane<br />
Butane<br />
Crude<br />
Crude Distillation<br />
Naphtha<br />
Hydrotreating<br />
Kerosene<br />
Hydrotreating<br />
Gas Oil<br />
Hydrotreating<br />
Naphtha Reformer<br />
Aromatic<br />
Process<br />
Naphtha<br />
Gasoline<br />
Benzene/<br />
P-Xylene<br />
Kerosene/<br />
Jet Fuel Oil<br />
Diesel<br />
Bunker Oil<br />
Distillation<br />
Vacuum<br />
Hydrocracking<br />
Delayed Coking<br />
LPG<br />
Naphtha<br />
Kerosene<br />
Diesel<br />
Asphalt
PLANT<br />
CAPACITY<br />
Process<br />
Crude Distillation<br />
Vacuum Distillation<br />
Gas Recovery<br />
Naphtha Hydrotreating<br />
Naphtha Reformer<br />
Kerosene Hydrotreating<br />
Gas Oil Hydrotreating<br />
Hydrocracking<br />
Delayed Coking<br />
#1 Plant<br />
Design MAX<br />
Design<br />
Max<br />
(Unit: 1,000 B/D)<br />
#2 Plant Total<br />
Design<br />
Max<br />
100 110 200 280 310 390<br />
34 60 - - 34 60<br />
12 9 6 7.5 18 16.5<br />
7 12 20 24 27 36<br />
3 4 20 22 23 26<br />
9 9 48 51 57 60<br />
12 22 32 36 44 58<br />
18.5 27 - - 18.5 27<br />
19 31 - - 19 31<br />
BTX<br />
Benzene (1,000 T/year]<br />
P-Xylene [1,000T/year]<br />
Water/ Waste water<br />
treatment [T/day]<br />
Power Supply (SPS:T/hour / Elec:MW]<br />
100<br />
300<br />
110<br />
345<br />
100<br />
300<br />
Design 16,000 / 8,400<br />
Design 860 / 94<br />
110<br />
345
Summary of <strong>CDU</strong>/<strong>VDU</strong> <strong>Heat</strong> <strong>Integration</strong><br />
• The feed of <strong>VDU</strong>, AR, fed directly from <strong>CDU</strong> Plant<br />
and max capacity of <strong>VDU</strong> is 60 MBD.<br />
• One of LSAR streams exchanges its heat<br />
with one of Crude Oil stream fed to <strong>CDU</strong> <strong>Heat</strong>er<br />
through the 5 heat exchangers.<br />
• Modification of <strong>Heat</strong> integration was implemented<br />
to this 5 exchangers line-up, and we can raise inlet<br />
temperature of <strong>VDU</strong> heater from 155 → 241℃.<br />
Overall saved heat is 1.8 mmkcal/hr
Schematic_Before<br />
<strong>CDU</strong><br />
Tower<br />
<strong>CDU</strong> <strong>Heat</strong>er<br />
155℃<br />
<strong>VDU</strong> <strong>Heat</strong>er<br />
<strong>VDU</strong><br />
Tower<br />
Crude Oil<br />
264℃<br />
TT-1,2,3<br />
TT-4,5<br />
Fuel Gas<br />
2,308 Nm3/hr<br />
VR
Schematic_After<br />
<strong>CDU</strong><br />
Tower<br />
<strong>CDU</strong> <strong>Heat</strong>er<br />
<strong>VDU</strong> <strong>Heat</strong>er<br />
<strong>VDU</strong><br />
Tower<br />
246℃<br />
Crude Oil<br />
241℃<br />
Fuel Gas<br />
1,883 Nm3/hr<br />
TT-1,2,3<br />
TT-4,5<br />
VR
<strong>Heat</strong> Balance_AR<br />
• The data of heater inlet Stream is as follows,<br />
due to the rising of inlet temperature we can<br />
saved 4.0 mmkcal/hr and reduce the fuel gas<br />
for heating the AR.<br />
A.R to <strong>VDU</strong><br />
AR Feed (bbl/hr)<br />
Before<br />
9,600<br />
After<br />
11,443<br />
<strong>Heat</strong>er Inlet Temp.(℃)<br />
<strong>Heat</strong> Capacity (kcal/kg)<br />
Saved <strong>Heat</strong> ( mmkcal/hr )<br />
155 241<br />
73 122<br />
4.0 mmkcal/hr<br />
• Saved <strong>Heat</strong> Basis is 9,600 bbl/hr
<strong>Heat</strong> Balance_Crude Oil<br />
• The data of <strong>CDU</strong> heater inlet Stream is as follows,<br />
due to the dropping of inlet temperature we losed<br />
2.2 mmkcal/hr and increase the fuel gas<br />
for heating the Crude Oil.<br />
Crude Oil to <strong>CDU</strong><br />
<strong>CDU</strong> Feed (bbl/hr)<br />
Before<br />
24,463<br />
After<br />
23,862<br />
<strong>CDU</strong> <strong>Heat</strong>er Inlet Temp.(℃)<br />
<strong>Heat</strong> Capacity (kcal/kg)<br />
Loss <strong>Heat</strong> ( mmkcal/hr )<br />
264 246<br />
145 133<br />
2.2 mmkcal/hr<br />
• Basis : 24,463 bbl/hr, LS crude
<strong>Heat</strong> Balance_Overall<br />
• We can save the cost of energy about 1.12 mmUSD<br />
per year.<br />
• In 2008, this project was certified as the CO2<br />
reduction project by government.<br />
mmkcal/hr<br />
Saved <strong>Heat</strong> ( AR Stream )<br />
Loss <strong>Heat</strong> ( Crude Stream )<br />
Sum<br />
Saved Cost<br />
4.0<br />
-2.2<br />
1.8<br />
1.12 MM USD/yr
Thank you for your attention.
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