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Pendahuluan
A. SIFAT-SIFAT DASAR DAN KARAKTERISTIK LNG :
Tergantung jumlah kandungan methane,ethane,propane,buthane
Uap LNG > dari udara
C O M P O S I T I O N
METHANE 83.0 % - 99.0 %
ETHANE
1.0 % - 13.0 %
PROPANE 0.1 % - 3.0 %
BUTANE
0.2 % - 1.0 %
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P H Y S I C A L P R O P E R T I E S
Normal boiling point
-255 0F(-159 0C) to - 263 0F(-
164 0C)
Density liquid at nbp 3.5 lb./gal. to 4 lb./gal.
Specific gravity of vapor @
69 0F0.55
Liquid to vapor expansion
620 : 1 (approx.)
Solubility in water
None
Heat of vaporization220 BTU/lb. - 248 BTU/lb.
770 BTU/gal. - 990 BTU/gal.
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C O M B U S T I O N P R O P E R T I E S
Flammable range of vapor
5 % - 14 % (atmospheric)
6 % - 13 % (cryogenic)
Minimum ignition temperatur
0.2 - 0.3 milli joules
Auto Ignition Temperature
9990
F (5370
C)
Heat of Combustion
22.000 BTU/lb.
Burn Rate, steady state
0.2 - 0.6 inch./min.
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B. Tumpahan LNG Pada Tanah
Tumpahan LNG pada tanah yang tidak mempunyai pembatas.
Unconfined Spill on Land.
LNG SPILL
INITIAL BOILING
RATE 10 Cufm/ft2
21 0C Warm ground
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Tumpahan LNG pada tanah yang mempunyai pembatas
Confined Spill on Land
LNG SPILL
INITIAL BOILING
RATE 10 Cfm/ft2
DOWN WIND
PLUME
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C. Bahaya Tumpahan LNG
Tumpahan LNG dapat menimbulkanbeberapa bahaya baik terhadap manusia
/operator maupun fasilitas kilang di
sekitarnya.Bahaya-bahaya tersebut meliputi cryogenic
burns, frosbite, hypothermia, lung damage,
asphysia dan thermal radiation, kebakaran,ledakan
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2. Permasalahan
Pada Tanggal 5 Juni 2010, jam 12.30 am, terjadi kebocoran sebuah tangki LNG
di LNG Badak Indonesia . Volume tangki 98000 m3. Tinggi tangki 78 m
vertical. Diameter Tangki 40 meter. Tangki LNG (Methane) tersebutmempunyai tekanan yang sangat kecil (0,1 bar) dengan temperatur minus
160C. Pada saat kebocoran terjadi,
(diukur pada ketinggian 10 meters oleh Fire Brigade Departemen) . Cuaca
pada saat itu mendung (completely overcast) Dan kelembaban udara 70%.
Tidak ada low-level inversion.
Tangki tersebut perlu dikosongkan dengan jalan mentrasnfer LNG ke tangkilainya. Selama proses transfer tersebut dengan menggunakan pompa LNG
ada kemungkinan terjadinya bahaya kabakaran, ledakan.
Possible failure scenarios include:
A sudden catastrophic failure leading to a Boiling Liquid Expanding Vapor
Explosion (BLEVE); A leak leading to a flash fire or a vapor cloud explosion; or
A breach leading to a jet of flame from the tank.
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Vapour Claud
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BLEVE
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Leaking Tank Chemical is burning as Jet Fire
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Rekomendasi
1. PPE yang sesuai
2. Hindari tumpahan LNG ke shower line
3. Water Certain
4. Mengkuti SOP tanggap darurat
5. Koordinasi
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Hole Size/
Spilled Volume
Liquid
Vaporization
Liquid Spread
Fire Increases
Vaporization
Thermal Damage
Due to Fire
Wind Tilts
Fire
Fire Entrains AirWaves AffectLiquid Spread
If Igni t ion Occurs
Analysis Requires
Adequate Representat ion
of K ey Features
Damage from
LNG Spill
Artists Rendering
Not to Scale
Other possib le hazardsFireball
Late igni tion and vapor
cloud f i re
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Typical LNG Receiving
Terminal Plot Plan
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Potential Thermal Hazards for
Spills from Common LNG Vessels
*Nominal case: Expected outcomes of a potential breach and thermal
hazards based on credible threats, best available experimental data, and
nominal environmental conditions for a common LNG vessel
HOLESIZE
(m2)
TANKSBREACHED
DISCHARGECOEFFICIENT
BURNRATE(m/s)
SURFACEEMISSIVEPOWER(kW/m2)
POOLDIAMETER
(m)
BURNTIME(min)
DISTANCETO 37.5kW/m2
(m)
DISTANCETO 5
kW/m2
(m
ACCIDENTAL EVENTS
1 1 .6 3X10-4 220 148 40 177 554
2 1 .6 3X10-4
220 209 20 250 784
INTENTIONAL EVENTS
5 3 .6 3 x 10-4 220 572 8.1 630 2118
5* 1 .6 3 x 10-4 220 330 8.1 391 1305
5 1 .9 3 x 10-4
220 405 5.4 478 1579
5 1 .6 8 x 10-4
220 202 8.1 253 810
12 1 .6 3 x 10-4 220 512 3.4 602 1920
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Side View Top View
H
Wind direction
Heat transfer from water to LNG
pool
LNG pool
Vapor cloud
Water
W
L
Qualitative
gas
concentration
contours
Vapor cloud
Dispersion distances are limited by closest ignition source
HOLESIZE
(m2)
TANKSBREACHED
POOLDIAMETER
(m)
SPILLDURATION
(min)
DISTANCETO LFL
(m)
Accidental Events
2 1 256 20 1710
Intentional Events
5 1 405 8.1 2450
5 3 701 8.1 3614
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HOLESIZE
(m2)
TANKSBREACHED
WIND SPEED(m/sec)
DISTANCE TOLFL(m)
Dispersion Distances for Potential Intentional Events
7 2 2 ~10,000
7 2 6 (avg) ~7,000
Example hazard distances are for intentional spills
of ~200,000 m3 of LNG in open areas without risk management
HOLESIZE
(m2)
TANKS
BREACHED
POOLDIAMETER
(m)
DISTANCE
TO
37.5 kW/m2
(m)
DISTANCE
TO
5 kW/m2
(m)
Thermal Distances for Potential Intentional Events
7 2 640 ~750 ~2500
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