presentasi lng spill

8/10/2019 Presentasi LNG Spill

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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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presentasi lng spill

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