lng-ld-009h1 sur09134 sk splendor 050809

D A T A E N T R Y F O R M

VESSEL NAME : SK SPLENDOR Program Version Number

TERMINAL : OMAN LNG LNG-LD-009H1 (07-AUG-09)

PORT : SUR, OMAN

DATE REPORT ISSUED : 5-Aug-2009

INTERTEK FILE NUMBER : SUR/09/134

CUSTOMER NAME : OMAN LNG

ADDRESS #1 : P.O. BOX 560

ADDRESS #2 : MUSCAT 116

ADDRESS #3 : SULTANATE OF OMAN

ADDRESS #4 :

ADDRESS #5 :

CONTACT NAME #1 : ACCOUNTS PAYABLE - NGF / 23

CONTACT NAME #2 : ATIQ AHMED

CONTACT NAME #3 :

CUSTOMER REFERENCE #1 : OF039/09-SL100-KG

CUSTOMER REFERENCE #2 :

SPA SUPPLIED BY : OMAN LNG / KOGAS CORPORATION

R E P O R T S E T U P & G U I D E L I N E S

1SELECT TYPE OF REPORT OF QUANTITY

SELECT TYPE OF REPORT OF QUANTITY ( STANDARD OR QUANTITY SPLIT).

0SELECT TO DISPLAY OR HIDE THE REPORT OF GAS-UP

IF GAS-UP IS REQUIRED, SELECT WHICH CALCUALTION METHOD IS TO BE USED.

0SELECT TO DISPLAY OR HIDE THE REPORT OF COOL DOWN

14SELECT WHICH CONTRACT (SPA) IS TO BE USED FOR CALCULATIONS

YESSELECT TO DISPLAY OR HIDE THE SECONDARY CUSTODY TRANSFER MEASUREMENTS.

0SELECT TO DISPLAY HOW MANY SNAPSHOT MEASUREMENT PAGES ARE NEEDED.

CHOSE FROM ZERO TO FOUR ADDITIONAL CTMS "SNAPSHOT" MEASUREMENT PAGES.

FOR INTERTEK USE ONLY

DO NOT ISSUE THIS

PAGE TO CUSTOMERS

IN ORDER FOR THIS PROGRAM TO WORK PROPERLY, MACROS MUST BE ENABLED

Report of

Quantity

Report of Gas Up

Report of

Cool DownIF COOL DOWN IS REQUIRED, SELECT WHICH COOL DOWN CALCULATION METHOD IS TO BE USED.

Contract Used

( SPA )ALL PAGES WILL AUTOMATICALLY CHANGE TO THE VALUES OF THE APPROPRIATE CALCULATION METHOD AS DESCRIBED IN THE RELEVANT CONTRACT (SPA)

Secondary Custody Transfer

Measurement

SECONDARY CUSTODY TRANSFER PAGE RECORDS AND CALCULATES THE VOLUMES OF THE SECONDARY GAUGING SYSTEM FOR OPENING & CLOSING AND COMPARES THE VOLUMES TO THE PRIMARY SYSTEMS.

CTMS "Snapshot"

Measurement

Page(s)

1SELECT TO WHICH OPERATIONAL CHECKLIST TO DISPLAY

SELECT THE APPROPRIATE CHECKLIST TO BE DISPLAYED AND REPORTED.

0SELECT TO DISPLAY OR HIDE THE VERIFICATION OF GC PAGE

NONESELECT TO DISPLAY OR HIDE THE BUNKER REPORTS

0SELECT TO DISPLAY HOW MANY LETTER OF PROTEST ARE NEEDED.

CHOSE FROM ZERO TO FOUR LETTERS OF PROTEST.

0SELECT TO DISPLAY OR HIDE CLIENT SPECIFIC REPORTS

SELECT IF ANY ADDITIONAL CLIENT SPECIFIC REPORT IS NEEDED OR NOT.

NoneSELECT TO IDENTIFY REVISED REPORT

SELECT IF REPORT WAS REVISED AND WHICH REVISION NUMBER IS TO BE ISSUED

NOSELECT TO PLACE PAGE NUMBERS ON BOTTOM OF REPORT PAGES

Operational Checklist

Verification of GC

IF NO VERIFICATION OF GC IS REQUIRED, OBTAIN A COPY OF THE TERMINAL'S VERIFICATION RECORDS BEFORE & AFTER. OBTAIN COPIES OF THE CERTIFICATIONS FOR THE SPAN GAS AND LAST CALIBRATION OF THE GC.

Bunker Reports IF NO BUNKER REPORTS ARE REQUIRED, OBTAIN A COPY OF THE VESSEL'S BUNKER

REPORT BEFORE & AFTER FROM THE CHIEF ENGINEER.

Letter(s) of

Protest

Client Specific

Reports

Report Revision

Number

Page Numbers Required

SELECT IF PAGE NUMBERS ARE NEEDED AT THE BOTTOM OF THE PAGES WITHIN THE REPORT

5-Aug-2009

OMAN LNGP.O. BOX 560MUSCAT 116SULTANATE OF OMAN

ATTN : ACCOUNTS PAYABLE - NGF / 23ATTN : ATIQ AHMED

REFERENCE : FOR SERVICES RENDERED TO ATTEND THE LOADING OF L.N.G.ON BOARD THE VESSEL "SK SPLENDOR" FOR THE ENERGYDELIVERED AT OMAN LNG / SUR, OMAN ON4-Aug-2009 TO 5-Aug-2009

OUR REFERENCE : SUR/09/134YOUR REFERENCE : OF039/09-SL100-KG

DEAR SIR / MADAM:

ENCLOSED FOR YOUR REVIEW IS OUR REPORT COVERING THE VESSEL "SK SPLENDOR" AT THE ABOVE LOCATION ON THE DATESINDICATED.

THE ENERGY VALUES WERE CALCULATED AS PER THE SPA SUPPLIED BYOMAN LNG / KOGAS CORPORATION

SHOULD YOU HAVE ANY QUESTIONS REGARDING THIS REPORTPLEASE DO NOT HESITATE TO CONTACT US AT YOUR CONVENIENCE.

WE THANK YOU FOR REQUESTING OUR SERVICES.

RESPECTFULLY FOR,INTERTEK CALEB BRETT

PONNAPPA CHOKIRAMANAGER

INTERTEK OIL CHEMICAL & AGRI

P.O. BOX 39, PC 114

MINA AL FAHAL

SULTANATE OF OMAN

TELEPHONE +968 (2) 448 0229

LNG-LD-009H1 (07-AUG-09) - 14

OUR REF : SUR/09/134

YOUR REF : OF039/09-SL100-KG

R E P O R T O F L O A D I N G

VESSEL : SK SPLENDOR DATE : 4-Aug-2009 TO 5-Aug-2009

TERMINAL/PORT : OMAN LNG / SUR, OMAN

1. LAST PORT INFORMATION

LAST PORT TERMINAL / PORT : KOGAS / INCHEON

LAST PORT C.C.T. QUANTITY : 1,553.335 CUBIC METERS

LAST PORT C.C.T. INSPECTION DATE : 20-Jul-2009 TIME : 15:48

2. OPENING CUSTODY TRANSFER INFORMATION

OPENING CUSTODY TRANSFER VOLUME : 404.978 CUBIC METERS

OPENING CUSTODY TRANSFER TEMPERATURES : -146.2 °C - Liquid -128.5 °C - Vapor

OPENING CUSTODY TRANSFER TANK PRESSURE : 1166 mbar

OPENING CUSTODY TRANSFER INSPECTION DATE : 4-Aug-2009 TIME : 10:28

3. CLOSING CUSTODY TRANSFER INFORMATION

CLOSING CUSTODY TRANSFER VOLUME : 136,292.944 CUBIC METERS

CLOSING CUSTODY TRANSFER TEMPERATURE : -160.2 °C - Liquid -152.0 °C - Vapor

CLOSING CUSTODY TRANSFER TANK PRESSURE : 1101.5 mbar

CLOSING CUSTODY TRANSFER INSPECTION DATE : 5-Aug-2009 TIME : 04:17

4. VESSEL COOL DOWN WAS NOT REQUIRED

COOL DOWN TRANSFER VOLUME : --- CUBIC METERS

COOL DOWN TRANSFER TEMPERATURE : --- °C - Liquid --- °C - Vapor

COOL DOWN TRANSFER TANK PRESSURE : --- mbar

COOL DOWN TRANSFER INSPECTION DATE : --- TIME : ---

5. LOAD INFORMATION

** VESSEL DELIVERED VOLUME (LIQUID) AT -160.2 °C : 135,888.000 CUBIC METERS

** VESSEL DELIVERED VOLUME (LIQUID) AT -160.2 °C : 135,888,000 LITERS

** VESSEL DELIVERED VOLUME (LIQUID) AT -160.0 °C : 135,971.000 CUBIC METERS

VESSEL DELIVERED VOLUME (GAS) : 2,876.574 MILLION CUBIC FEET @ S.R.C.

VESSEL DELIVERED VOLUME (GAS) : 81,455.497 1000 CUBIC METERS @ S.R.C.

** LIQUID TEMPERATURE AFTER LOADING : -160.2 °C

** VAPOR TEMPERATURE BEFORE LOADING : -128.5 °C

** TANK PRESSURE BEFORE LOADING : 1166 mbar

** LNG DENSITY AT -160.2 °C : 459.080

** LNG DENSITY AT -160.0 °C 458.800

MASS DELIVERED : 62,172.077 METRIC TONS

** GROSS HEATING VALUE (MASS) : 54.4361 MJ / kg

** GROSS HEATING VALUE (VOLUME) : 1115 BTU / SCF

** WOBBE INDEX : 1411 BTU / SCF

** INDICATED VALUES ARE ROUNDED IN ACCORDANCE WITH SPECIFIC S.P.A. REQUIREMENTS

6. ADDITIONAL INFORMATION AND COMMENTS

Mohamed-Hamid BOUABDELLI

FOR INTERTEK CALEB BRETT FOR TERMINAL FOR VESSEL

LNG-LD-009H1 (07-AUG-09) - 14

kg / m3

kg / m4



R E P O R T O F Q U A N T I T Y



1. CUSTODY TRANSFER DENSITY

LNG DENSITY AT -160.2 °C 459.080

2. CUSTODY TRANSFER VOLUME & MASS

CUBIC METERS KILOGRAMS METRIC TONS

QUANTITY RECEIVED BY VESSEL 135,888.000 62,172,077 62,172.077

QUANTITY CONSUMED BY VESSEL 0.000 0 0.000

QUANTITY USED FOR GAS-UP 0.000 0 0.000

QUANTITY USED FOR COOL DOWN 0.000 0 0.000

ADJUSTED QUANTITY DELIVERED 135,888.000 62,172,077 62,172.077

3. CUSTODY TRANSFER ENERGY

MEGAJOULES MMBTU KILOWATT HOURS

GROSS QUANTITY DELIVERED 3,395,719,322 3,218,508 943,255,367

QUANTITY DISPLACED 11,743,022 11,130 3,261,951

QUANTITY DELIVERED 3,383,978,343 3,207,380 939,993,417

QUANTITY CONSUMED BY VESSEL 0 0 0

QUANTITY USED FOR GAS-UP 0 0 0

QUANTITY USED FOR COOL DOWN 0 0 0

ADJUSTED QUANTITY DELIVERED 3,383,978,343 3,207,380 939,993,417

THE STANDARD REFERENCE CONDITIONS IDENTIFIES TEMPERATURE OF 60°F.




ROQ 1 - Standard LNG-LD-009H1 (07-AUG-09) - 14

kg / m3



R E P O R T O F Q U A N T I T Y



1. CUSTODY TRANSFER DENSITY


2. CUSTODY TRANSFER VOLUME & MASS

CUBIC METERS KILOGRAMS METRIC TONS

QUANTITY RECEIVED BY VESSEL 135,888.000 62,172,077 62,172.077

QUANTITY CONSUMED BY VESSEL 0.000 0 0.000

QUANTITY USED FOR GAS-UP 0.000 0 0.000

QUANTITY USED FOR COOL DOWN 0.000 0 0.000

ADJUSTED QUANTITY DELIVERED 135,888.000 62,172,077 62,172.077

3. CUSTODY TRANSFER ENERGY




QUANTITY DELIVERED 3,383,978,343 3,207,380 939,993,417


QUANTITY USED FOR GAS-UP 0 0 0

QUANTITY USED FOR COOL DOWN 0 0 0



4. QUANTITY SPLITS

CARGO NUMBER CUBIC METERS METRIC TONS MEGAJOULES MMBTU KILOWATT HOURS

1 T-54674-Y03 63,888.000 29,230.319 1,590,983,813 1,507,956 441,939,681

2 T-54674-Y04 42,000.000 19,216.025 1,045,913,476 991,331 290,531,346

3 T-54674-Y05 10,000.000 4,575.244 249,027,018 236,031 69,174,130

4 T-54674-Y06 20,000.000 9,150.488 498,054,036 472,062 138,348,260



ROQ 2 - Quantity Split LNG-LD-009H1 (07-AUG-09) - 14

kg / m3



R E P O R T O F A N A L Y S I S



1. DESCRIPTION

SAMPLE DESIGNATED AS : LIQUEFIED NATURAL GAS

SAMPLE TESTED BY : TERMINAL IN-LINE GC - VERIFIED PRIOR TO LOADING

SAMPLE REPRESENTING : COMPOSITE CONTINUOUS SAMPLING

2. ANALYSIS

TEST METHODLIQUID

COMPOSITION

METHANE GPA 2261 90.2400 % mol

ETHANE GPA 2261 5.9500 % mol

PROPANE GPA 2261 2.2400 % mol

ISO BUTANE GPA 2261 0.6900 % mol

N-BUTANE GPA 2261 0.5800 % mol

ISO PENTANE GPA 2261 0.0200 % mol

N-PENTANE GPA 2261 0.0000 % mol

N-HEXANE GPA 2261 0.0000 % mol

NITROGEN GPA 2261 0.2800 % mol

CARBON DIOXIDE GPA 2261 0.0000 % mol

OXYGEN GPA 2261 0.0000 % mol

MERCURY ng / Nm3 NOT TESTED

MERCAPTANS mg / Nm3 NOT TESTED

HYDROGEN SULFIDE mg / Nm3 NOT TESTED

CARBONYL SULFIDE mg / Nm3 NOT TESTED

TOTAL SULFUR mg / Nm3 NOT TESTED

HYDROCARBON DEWPOINT (MAX) °C NOT TESTED

3. QUALITY SPECIFICATIONS (SPA DEFINED)

TEST SPECIFICATION RESULT

NONE SPECIFIED N/A N/A




LNG-LD-009H1 (07-AUG-09) - 14

THE TEST RESULTS IN THIS DOCUMENT HAVE BEEN PROVIDED TO INTERTEK CALEB BRETT BY THE TERMINAL AND ARE

PASSED ON FOR INFORMATIONAL PURPOSES ONLY. INTERTEK CALEB BRETT MAKES NO REPRESENTATION AS TO THE

QUALITY OF THE MATERIAL AND ASSUMES NO RESPONSIBILITY FOR THE ACCURACY OF THE TEST RESULTS, WHICH

REMAINS SOLELY WITH THE ABOVE MENTIONED PRODUCER OF THE RESULTS. THE ISSUING OF THIS REPORT DOES NOT

CONSTITUTE ANY REPRESENTATION OR WARRANTY CONCERNING THE INFORMATION CONTAINED HEREIN.



R E P O R T O F G A S - U P



1. METHOD OF GAS-UP CALCULATION

2. CALCULATION OF VAPOR VOLUME USED FOR GAS-UP

TANK NAME 1 2 3 4

TANK CAPACITY 37,326.000 37,336.000 37,352.000 37,345.000

FACTOR 1.800 1.800 1.800 1.800

VOLUME USED 67,186.800 67,204.800 67,233.600 67,221.000

3. CALCULATION VALUES FOR GAS-UP OPERATIONS

VAPOR VOLUME USED FOR GAS-UP = 268,846.200 CUBIC METERS

VAPOR TEMPERTURE AFTER GAS-UP = 24.0 °C

VAPOR PRESSURE AFTER GAS-UP = 1171 mbar

DENSITY OF VAPOR VOLUME FOR GAS-UP = 0.7634 kg / m3 at 60°F (Ideal Gas)

DENSITY OF LIQUID (AT LNG LOADING TEMPERATURE) = 459.080 kg / m3 at -160.2°C

HIGHER HEATING VALUE (MASS) = 54.436 MJ / kg at 15°C

HIGHER HEATING VALUE (VOLUME) = 1115 BTU / SCF at 60/60°F & 14.696 psi

4. VOLUME, MASS, & ENERGY USED FOR GAS-UP OPERATIONS

LNG EQUIVALENT USED FOR GAS-UP = 501.918 CUBIC METERS at -160.2°C

MASS REQUIRED FOR GAS-UP = 230.420 METRIC TONS

ENERGY REQUIRED FOR GAS-UP = 12,542,489 MJ at @ 60°F

ENERGY REQUIRED FOR GAS-UP = 11,888 MMBTU at @ 60°F

ENERGY REQUIRED FOR GAS-UP = 3,484,025 MMBTU at @ 60°F

5. ADDITION INFORMATION AND COMMENTS



ROGU 1 - Factor Calculation LNG-LD-009H1 (07-AUG-09) - 14

GAS-UP VALUES ARE CALCULATED BY MULTIPLYING TANK CAPACITY BY A CONSTANT VOLUME FACTOR SUBMITTED BY THE VESSEL. THE FACTOR IS DETERMINED BY THE DESIGN OF THE VESSEL TANKS.

m3

m3



R E P O R T O F G A S - U P



1. METHOD OF GAS-UP CALCULATION

2. SUBMITTED VOLUME USED FOR GAS-UP

SUBMITTED VOLUME USED FOR GAS-UP = 263,487.600 CUBIC METERS (VAPOR)

3. CALCULATION VALUES FOR GAS-UP OPERATIONS

VAPOR VOLUME USED FOR GAS-UP = 263,487.600 CUBIC METERS

VAPOR TEMPERTURE AFTER GAS-UP = 24.0 °C

VAPOR PRESSURE AFTER GAS-UP = 1171 mbar

DENSITY OF VAPOR VOLUME FOR GAS-UP = 0.7634 kg / m3 at 60°F (Ideal Gas)

DENSITY OF LIQUID (AT LNG LOADING TEMPERATURE) = 459.080 kg / m3 at -160.2°C


HIGHER HEATING VALUE (VOLUME) = 1115 BTU / SCF at 60/60°F & 14.696 psi

4. VOLUME, MASS, & ENERGY USED FOR GAS-UP OPERATIONS

LNG EQUIVALENT USED FOR GAS-UP = 491.914 CUBIC METERS at -160.2°C

MASS REQUIRED FOR GAS-UP = 225.828 METRIC TONS

ENERGY REQUIRED FOR GAS-UP = 12,289,447 MJ at @ 60°F

ENERGY REQUIRED FOR GAS-UP = 11,648 MMBTU at @ 60°F

ENERGY REQUIRED FOR GAS-UP = 3,413,735 MMBTU at @ 60°F




ROGU 1 - Factor Calculation LNG-LD-009H1 (07-AUG-09) - 14

GAS-UP VALUES ARE CALCULATED BY MUTIAL AGREEMENT BETWEEN ALL PARTIES. THE VOLUME AS CALCUALTED BY FLOW METER LOCATED ASHORE. THE VOLUME REPORTED WAS SUBMITTED BY THE TERMINAL.



R E P O R T O F C O O L D O W N



1. METHOD OF COOL DOWN CALCULATION

COOL DOWN VALUES ARE CALCULATED BY THE LIQUID VOLUME PER VAPOR TEMPERATURE DIFFERENTIAL METHOD.

2. PROCEDURE FOR METHOD

THE DIFFERENCE OF THE VAPOR TEMPERATURES TAKEN DURING OPENING CUSTODY TRANSFER AND AFTER COOL DOWN

MEASUREMENT IS MULTIPLIED BY A LIQUID VOLUME PER 1°C. THIS LIQUID VOLUME IS DEFINED WITHIN THE VESSEL'S

CALIBRATION TABLES AND IS SUBMITTED BY THE CHIEF OFFICER.

THE TANK TEMPERATURE IS IDENTIFIED AS : THE AVERAGE OF ONLY THE BOTTOM 2 TEMPERATURE PROBES

LIQUID VOLUME REQUIRED TO LOWER THE VAPOR TEMPERATURE BY 1°C = 2.150 CUBIC METERS

CALCULATED DENSITY OF CARGO LOADED = 459.080 kg / m3 at -160.2 °C

HIGHER HEATING VALUE OF CARGO LOADED = 54.4361 MJ / kg at 15°C

3. TANK TEMPERATURE CALCULATIONS

TANK NAME 1 2 3 4

TEMP. PRIOR °C 28.00 28.00 27.00 27.00

TEMP. AFTER °C CASE #1 CASE #1 CASE #1 CASE #1

TEMP. DIFF °C #VALUE! #VALUE! #VALUE! #VALUE!

2.150 2.150 2.150 2.150

#VALUE! #VALUE! #VALUE! #VALUE!

4. REPORTING VALUES FOR COOL DOWN OPERATIONS

LIQUID VOLUME REQUIRED FOR COOL DOWN = #VALUE! CUBIC METERS at -160.2 °C

MASS REQUIRED FOR COOL DOWN = #VALUE! METRIC TONS

ENERGY REQUIRED FOR COOL DOWN = #VALUE! MJ at @ 60°F

ENERGY REQUIRED FOR COOL DOWN = #VALUE! MMBTU at @ 60°F

ENERGY REQUIRED FOR COOL DOWN = #VALUE! KWH at @ 60°F




ROCD 1 - Temperature Differential LNG-LD-009H1 (07-AUG-09) - 14

M3 PER 1°C

M3 PER TANK







COOL DOWN VALUES ARE CALCULATED BY THE COOL DOWN TABLES METHOD.


THE ENERGY REQUIRED TO COOL DOWN THE VESSEL TANKS TO THE REQUIRED LOADING TEMPERATURE IS OBTAINED

FROM VESSEL'S CERTIFIED COOL DOWN TABLES SUBMITTED BY THE CHIEF OFFICIER. THE TABLES ARE DIVIDED INTO

TWO SECTIONS. CASE #1 IS FOR WARM CONDITIONS (AVERAGE TEMPERTAURE BEING HIGHER THAN -40°C). CASE #2

IS FOR COLD CONDITIONS (AVERAGE TEMPERATURE BEING LOWER THAN -40°C).

THE TANK TEMPERATURE IS IDENTIFIED AS : THE AVERAGE OF ONLY THE TOP & BOTTOM TEMPERATURE PROBES

COOL DOWN TABLES PRESENTED USING : MMBTUS

TEMPERATURES FOR CASE #1 TABLES ARE BETWEEN 40.0 °C AND -40.0 °C

TEMPERATURES FOR CASE #2 TABLES ARE BETWEEN -40.0 °C AND -130.0 °C



3. TANK TEMPERATURE CALCULATIONS

TANK NAME 1 2 3 4

TEMPERATURE °C 28.00 28.00 27.00 27.00

TABLE USED CASE #2 CASE #2 CASE #2 CASE #2

MMBTUS 1625 2988 2988 2794


LIQUID VOLUME REQUIRED FOR COOL DOWN = 438.860 CUBIC METERS at -160.2 °C

MASS REQUIRED FOR COOL DOWN = 201.472 METRIC TONS

ENERGY REQUIRED FOR COOL DOWN = 10,967,349 MJ at @ 60°F

ENERGY REQUIRED FOR COOL DOWN = 10,395 MMBTU at @ 60°F

ENERGY REQUIRED FOR COOL DOWN = 3,046,486 KWH at @ 60°F




ROCD 2 - Vessel Tables LNG-LD-009H1 (07-AUG-09) - 14







COOL DOWN VALUES ARE CALCULATED BY THE SPRAY NOZZLE FLOW & PRESSURE METHOD.


THE VOLUME REQUIRED TO COOL DOWN THE VESSEL TANKS TO THE REQUIRED LOADING TEMPERATURE IS OBTAINED

BY CALCULATING THE VOLUME BASED ON THE NUMBER OF SPRAY NOZZLES PER TANK, FLOW CAPACITY PER NOZZLE,

DURATION OF COOL DOWN, AND THE DENSITY OF THE LNG.



3. TANK PROFILE

TANK NAME 1 2 3 4

# OF NOZZLES 22 34 34 32

FLOW RATE (L/MIN) 1.80 1.80 1.80 1.80

DURATION (HOURS) 9.80 9.80 9.80 9.80

DENSITY FACTOR 1.4759 1.4759 1.4759 1.4759

CUBIC METERS 34.366 53.111 53.111 49.987


LIQUID VOLUME REQUIRED FOR COOL DOWN = 190.575 CUBIC METERS at -160.2 °C








ROCD 3 - Nozzle Flow LNG-LD-009H1 (07-AUG-09) - 14







COOL DOWN VALUES ARE CALCULATED BY USING THE NIGERIA LNG TERMINAL SUBMITTED PROCEDURE.



LIQUID VOLUME REPORTED FOR COOL DOWN = 640.830 CUBIC METERS at -160.2 °C

DENSITY OF LNG = 459.080 kg / m3 at -160.2 °C









ROCD 4 - Submitted Shore LNG-LD-009H1 (07-AUG-09) - 14

THE ENERGEY REQUIRED TO COOL DOWN THE VESSEL TANKS TO THE REQUIRED LOADING TEMPERATURE IS OBTAINED BY THE COMMON INDUSTRY FORMULA OF "ENERGY = VOLUME * DENSITY * HIGHER HEATING VALUE (MASS BASED)". THE VOLUME OF LNG (IN CUBIC METERS) WAS SUBMITTED BY THE TERMINAL. THE DENSITY OF THE LNG WAS CALCULATED BY USING NBS TECHNICAL NOTE 1030 (1980). THE HIGHER HEATING VALUE (MASS BASED) WAS CALCULATED BY USING THE STANDARD ISO 6976.

PLEASE NOTE THAT WITH RESPECT TO THE CALCULATION OF COOL DOWN QUANTITY THE TERMINAL PROCEDURE DIFFERS FROM NORMAL ACCEPTED INDUSTRY PRACTISE, WE ARE HOWEVER REQUIRED TO REPORT THE QUANTITY IN ACCORDANCE WITH TERMINAL PROCEDURES.

14







COOL DOWN VALUES ARE CALCULATED BY THE COOL DOWN TABLES PLUS LIQUID FALL OUT METHOD.


THE ENERGY REQUIRED TO COOL DOWN THE VESSEL TANKS TO THE REQUIRED LOADING TEMPERATURE IS OBTAINED

FROM VESSEL'S CERTIFIED COOL DOWN TABLES SUBMITTED BY THE CHIEF OFFICIER. THE TABLES ARE DIVIDED INTO

TWO SECTIONS. CASE #1 IS FOR WARM CONDITIONS (AVERAGE TEMPERTAURE BEING HIGHER THAN °C). CASE #2

IS FOR COLD CONDITIONS (AVERAGE TEMPERATURE BEING LOWER THAN °C).

THE TANK TEMPERATURE IS IDENTIFIED AS : THE AVERAGE OF TANK TEMPERATURES

COOL DOWN TABLES PRESENTED USING : MMBTUS



3. CALCULATIONS OF CONSUMED VALUES FOR COOL DOWN

TANK NAME 1 2 3 4

TEMP BEFORE °C 29.10 29.40 28.80 29.50

TEMP AFTER °C 30.10 29.40 28.80 29.50

MMBTUS 2473 3638 3626 3358

VOLUME OF LIQUID CONSUMED FOR COOL DOWN = 552.849 CUBIC METERS

MASS CONSUMED FOR COOL DOWN = 253.802 METRIC TONS

ENERGY CONSUMED FOR COOL DOWN = 13,815,237 MJ at 60°F

ENERGY CONSUMED FOR COOL DOWN = 13,090 MMBTU at 60°F

ENERGY CONSUMED FOR COOL DOWN = 3,837,566 KWH at 60°F

4. CALCULATIONS OF FALLOUT VALUES AFTER COOL DOWN

TANK NAME 1 2 3 4

VOLUME BEFORE m3 21.371 37.771 38.761 307.075

VOLUME AFTER m3 47.856 44.726 60.576 59.168

VOLUME LOADED m3 26.485 6.955 21.815 -247.907

VOLUME OF LIQUID FALLOUT AFTER COOL DOWN = 192.652 CUBIC METERS

MASS OF FALLOUT AFTER COOL DOWN = 88.443 METRIC TONS

ENERGY OF FALLOUT AFTER COOL DOWN = 4,814,205 MJ at 60°F

ENERGY OF FALLOUT AFTER COOL DOWN = 4,560 MMBTU at 60°F

ENERGY OF FALLOUT AFTER COOL DOWN = 1,337,279 KWH at 60°F

5. TOTAL VALUES FOR COOL DOWN OPERATIONS

TOTAL VOLUME OF LIQUID REQUIRED FOR COOL DOWN = 745.501 CUBIC METERS

TOTAL MASS REQUIRED FOR COOL DOWN = 342.245 METRIC TONS

TOTAL ENERGY REQUIRED FOR COOL DOWN = 18,629,442 MJ at 60°F

TOTAL ENERGY REQUIRED FOR COOL DOWN = 17,650 MMBTU at 60°F

TOTAL ENERGY REQUIRED FOR COOL DOWN = 5,174,845 KWH at 60°F



ROCD 5 - Vessel Tables + Fall Out LNG-LD-009H1 (07-AUG-09) - 14



R E P O R T O F C A L C U L A T I O N S



1. COMPOSITION FACTORS

MOLAR MOLAR WT. MOLAR VOL. MOLAR HHV

COMPONENTS FRACTION kg / kmole MJ / kg

(Xi) (Mi) (Vi) (Hi)

METHANE 0.902400 16.043 0.038122 55.574

ETHANE 0.059500 30.070 0.047925 51.95

PROPANE 0.022400 44.097 0.062478 50.37

ISO BUTANE 0.006900 58.123 0.078332 49.39

N-BUTANE 0.005800 58.123 0.076856 49.55

ISO PENTANE 0.000200 72.150 0.091700 48.95

N-PENTANE + HEAVIER 0.000000 72.150 0.091562 49.04

NITROGEN 0.002800 28.0135 0.046882 0

2. DENSITY CALCULATIONS

DENSITY = WITH C = K1 + ( K2 - K1 ) * Xn

0.0425

DENSITY = 459.166 kg/m3 at -160.2 °C K1 = 0.000427 K2 = 0.000685

3. HIGHER HEATING VALUES

= = 54.4355 MJ / kg

= = 41.63578.31451 * 288.15

= = 52.689528.9626

4. QUANTITIES DELIVERED

LIQUID TEMPERATURE AFTER LOADING = -160.2 °C VESSEL O.C.T. VOLUME = 404.978

VAPOR TEMPERATURE BEFORE LOADING = -128.5 °C VESSEL C.C.T. VOLUME = 136,292.944

ABSOLUTE PRESSURE BEFORE LOADING = 1166.000 mbar LOADED VOLUME = 135,887.966

5. ENERGY DELIVERED

GROSS QUANTITY DELIVERED = VOLUME * DENSITY * HIGHER HEATING VALUE (MASS BASED)

GROSS DELIVERED QUANTITY = 3,396,507,919 MJ

GROSS DELIVERED QUANTITY = 3,219,267.90 MMBTU

GROSS DELIVERED QUANTITY = 943,474,422 KWH


THE STANDARD REFERENCE CONDITIONS IDENTIFIES TEMPERATURE OF 15°C.

THE DENSITY CALCULATION (REVISED KLOSEK-MCKINLEY METHOD) IS BASED ON N.B.S. TECHNICAL NOTE 1030 (1980).

THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO I.S.O. 6976 (1995).



SPA Contract # 1 LNG-LD-009H1 (07-AUG-09) - 14

m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C

S ( Xi * Mi * Hi ) Hm (MASS) 15°CS ( Xi * Mi )

Hv (VOLUME) 15/15°C at 101.325 kPa

S ( Xi * Mi * Hi) * 101.325 Hv (VOLUME) 15/15°C at 101.325 kPa

MJ / m3

WOBBE INDEX 15/15°C at 101.325 kPa

Hv / ÖS ( Xi * Mi ) WOBBE INDEX

15/15°C at 101.325 kPa

MJ / m3

m3

m3

m3







MOLAR MOLAR WT. MOLAR VOL. MOLAR HHV MOLAR HHV SUMMATION

COMPONENTS FRACTION kg / kmole MJ / kg FACTOR

(Xi) (Mi) (Vi) (Hmi) (Hvi)

METHANE 0.902400 16.043 0.038118 55.574 37.706 0.0447

ETHANE 0.059500 30.070 0.047922 51.95 66.07 0.0922

PROPANE 0.022400 44.097 0.062475 50.37 93.94 0.1338

ISO BUTANE 0.006900 58.123 0.078328 49.39 121.40 0.1789

N-BUTANE 0.005800 58.123 0.076852 49.55 121.79 0.1871

ISO PENTANE 0.000200 72.150 0.091695 48.95 149.36 0.2280

N-PENTANE 0.000000 72.150 0.091558 49.04 149.66 0.2510

N-HEXANE 0.000000 86.177 0.104864 48.72 177.55 0.2950

NITROGEN 0.002800 28.0135 0.046876 0 0 0.0173

OXYGEN 0.000000 31.9988 0.031467 0 0 0.0283



0.0425



= = 54.4355 MJ / kg

= = 41.7448

= *0.99958

= 52.769228.9626 Z




ABSOLUTE PRESSURE BEFORE LOADING = 1166.000 mbar LOADED VOLUME = 135,887.966

5. ENERGY DELIVERED

QUANTITY = V * D * Hm - Qr WITH Qr = V * 288.15

*Pa

* 37.782 (Real Gas)( 273.15 + Tv ) 1013.25

GROSS QUANTITY = 3,396,458,942 MJ or 3,219,221.48 MMBTU or 943,460,817 KWH

ENERGY DISPLACED = 11,768,417 MJ or 11,154.31 MMBTU or 3,269,005 KWH

NET QUANTITY = 3,384,690,525 MJ or 3,208,067.18 MMBTU or 940,191,812 KWH



THE DENSITY CALCULATION (REVISED KLOSEK-MCKINLEY METHOD) IS BASED ON I.S.O. 6578 (1991).





m3 / kmole MJ / m3

(ÖBi)

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C

S ( Xi * Mi * Hmi ) Hm (MASS) 15°CS ( Xi * Mi )


S ( Xi * Hvi ) / ZHv (VOLUME) 15/15°C at 101.325 kPa

MJ / m3



15/15°C at 101.325 kPa

MJ / m3

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038122 55.574

ETHANE 0.0595 30.070 0.047925 51.95

PROPANE 0.0224 44.097 0.062478 50.37

ISO BUTANE 0.0069 58.123 0.078332 49.39

N-BUTANE 0.0058 58.123 0.076856 49.55

ISO PENTANE 0.0002 72.150 0.091700 48.95


NITROGEN 0.0028 28.0135 0.046882 0



0.0425



= = 54.4 MJ / kg

= * 26.8392 = 1117.5 BTU / SCF23.6449

= = 1414.2 BTU / SCF28.9626




ABSOLUTE PRESSURE BEFORE LOADING = 1166 mbar LOADED VOLUME = 135,887.000

5. ENERGY DELIVERED

Q = ( V * D * Hm - Qr ) / 1055.12 With Qr = V * 288.15

*Pa

* 37.7 (Ideal Gas)( 273.15 + Tv ) 1013.25

GROSS QUANTITY = 3,394,020,913 MJ or 3,216,911 MMBTU or 942,783,587 KWH

ENERGY DISPLACED = 11,742,891 MJ or 11,130 MMBTU or 3,261,914 KWH

NET QUANTITY = 3,382,277,424 MJ or 3,205,780 MMBTU or 939,521,673 KWH








m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C


Hv (VOLUME) 60/60°F at 14.696 PSI

S ( Xi * Mi * Hi) Hv (VOLUME) 60/60°F at 14.696 PSI

WOBBE INDEX 60/60°F at 14.696 PSI


60/60°F at 14.696 PSI

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.902400 16.043 0.038116 55.574

ETHANE 0.059500 30.070 0.047922 51.95

PROPANE 0.022400 44.097 0.062475 50.37

ISO BUTANE 0.006900 58.123 0.078328 49.39

N-BUTANE 0.005800 58.123 0.076852 49.55

ISO PENTANE 0.000200 72.150 0.091695 48.95


NITROGEN 0.002800 28.0135 0.046855 0



0.0425



= = 54.436 MJ / kg

= = 41.63623.6449

= = 52.69028.9626





5. ENERGY DELIVERED



GROSS DELIVERED QUANTITY = 3,219,720 MMBTU








m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C



S ( Xi * Mi * Hi) Hv (VOLUME) 15/15°C at 101.325 kPa

MJ / m3



15/15°C at 101.325 kPa

MJ / m3

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.902400 16.043 0.038122 55.516

ETHANE 0.059500 30.070 0.047925 51.9

PROPANE 0.022400 44.097 0.062478 50.33

ISO BUTANE 0.006900 58.123 0.078332 49.35

N-BUTANE 0.005800 58.123 0.076856 49.51

ISO PENTANE 0.000200 72.150 0.091700 48.91


NITROGEN 0.002800 28.0135 0.046882 0



0.0425



= = 54.3803 MJ / kg

= = 41.70308.31451 * 288.15 * Z

= *0.99958

= 52.716328.9626 Z





5. ENERGY DELIVERED


*Pa

* 38.8 (Real Gas)( 273.15 + Tv ) 1013.25

GROSS QUANTITY = 3,393,063,009 MJ or 3,216,002.76 MMBTU or 942,517,503 KWH

ENERGY DISPLACED = 12,086,344 MJ or 11,455.64 MMBTU or 3,357,318 KWH

NET QUANTITY = 3,380,976,665 MJ or 3,204,547.12 MMBTU or 939,160,185 KWH








m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 25°C



S ( Xi * Mi * Hi) * 101.325 Hv (VOLUME) 25/15°C at 101.325 kPa

MJ / m3



25/15°C at 101.325 kPa

MJ / m3

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038122 55.560

ETHANE 0.0595 30.070 0.047925 51.926

PROPANE 0.0224 44.097 0.062479 50.393

ISO BUTANE 0.0069 58.124 0.078332 49.402

N-BUTANE 0.0058 58.124 0.076857 49.544

ISO PENTANE 0.0002 72.151 0.091699 48.944

N-PENTANE 0.0000 72.151 0.091562 49.053

N-HEXANE 0.0000 86.178 0.104877 48.719

NITROGEN 0.0028 28.013 0.046866 0

CARBON DIOXIDE 0.0000 44.010 0.027180 0

OXYGEN 0.0000 31.999 0.031474 0



0.0425



= = 54.4233 MJ / kg

= = 1115.0 BTU / SCF

= = 1411.0 BTU / SCF28.9626





5. ENERGY DELIVERED

Q = ( V * D * Hm - Qr ) / 1055.12 With Qr = V * 288.15

*Pa

* 37.7 (Ideal Gas)( 273.15 + Tv ) 1013.25






THE DENSITY CALCULATION (REVISED KLOSEK-MCKINLEY METHOD) IS BASED ON N.B.S. INTERAGENCY REPORT 77-867.

THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO I.P. 251/76.




m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C


Hv (VOLUME) 60/60°F at 14.696 PSIA

1.13285 * S ( Xi * Mi * Hi )Hv (VOLUME) 60/60°F at 14.696 PSIA

WOBBE INDEX 60/60°F at 14.696 PSIA


60/60°F at 14.696 PSIA

m3

m3

m3







MOLAR MOLAR WT. MOLAR VOL. MOLAR HHV MOLAR HHV SUMMATION

COMPONENTS FRACTION kg / kmole MJ / kg FACTOR

(Xi) (Mi) (Vi) (Hmi) (Hvi)

METHANE 0.9024 16.0426 0.038123 55.574 39.777 0.0490

ETHANE 0.0595 30.0694 0.047925 51.95 69.69 0.1000

PROPANE 0.0224 44.0962 0.062479 50.37 99.09 0.1453

ISO BUTANE 0.0069 58.1230 0.078332 49.39 128.07 0.2049

N-BUTANE 0.0058 58.1230 0.076856 49.55 128.48 0.2069

ISO PENTANE 0.0002 72.1498 0.091699 48.95 157.57 0.2510

N-PENTANE 0.0000 72.1498 0.091562 49.04 157.87 0.2864

N-HEXANE 0.0000 86.1760 0.104868 48.72 187.30 0.3286

NITROGEN 0.0028 28.0134 0.046900 0 0 0.0224

OXYGEN 0.0000 31.9988 0.031474 0 0 0.0316



0.0425



= = 54.44 MJ / kg

= = 44.06

= *0.99941

= 55.6928.9626 Z





5. ENERGY DELIVERED












m3 / kmole MJ / m3

(ÖBi)

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C

S ( Xi * Mi * Hmi ) Hm (MASS) 15°CS ( Xi * Mi )


S ( Xi * Hvi ) / ZHv (VOLUME) 15/0°C at 101.325 kPa

MJ / m3



15/0°C at 101.325 kPa

MJ / m3

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038123 55.575

ETHANE 0.0595 30.070 0.047925 51.950

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076856 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104868 48.716

NITROGEN 0.0028 28.013 0.046900 0

CARBON DIOXIDE 0.0000 44.010 ----- 0

OXYGEN 0.0000 31.9988 0.031474 0



0.0425



= = 54.4361 MJ / kg

= = 1115.3 BTU / SCF

= = 1411.4 BTU / SCF28.9626


LIQUID TEMPERATURE AFTER LOADING = -160.2 °C VESSEL O.C.T. VOLUME = 405

VAPOR TEMPERATURE BEFORE LOADING = -128.5 °C VESSEL C.C.T. VOLUME = 136,293

ABSOLUTE PRESSURE BEFORE LOADING = 116.6 kPa LOADED VOLUME = 135,888

5. ENERGY DELIVERED







THE DENSITY CALCULATION (REVISED KLOSEK-MCKINLEY METHOD) IS BASED ON I.P. PART XII (1998).

THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO GPA 2145 SI (2000).




m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038122 55.575

ETHANE 0.0595 30.070 0.047925 51.950

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076857 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104877 48.716

NITROGEN 0.0028 28.013 0.046866 0

CARBON DIOXIDE 0.0000 44.010 0.027180 0



0.0425



= = 54.4361 MJ / kg

= = 1115.3 BTU / SCF

= = 1411.4 BTU / SCF28.9626



VAPOR TEMPERATURE BEFORE LOADING = -128 °C VESSEL C.C.T. VOLUME = 136,292.944


5. ENERGY DELIVERED

Q = ( V * D * Hm - DV ) / 1055.12 With DV = V * 288.15

*Pa

* 37.7 * C C = ( 0.5 )( 273.15 + Tv ) 1013.25







THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO GPA 2145 SI (1992).




m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038123 55.575

ETHANE 0.0595 30.070 0.047925 51.950

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076856 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104868 48.716

NITROGEN 0.0028 28.013 0.046900 0

CARBON DIOXIDE 0.0000 44.010 0.027183 0

OXYGEN 0.0000 31.9988 0.031474 0



0.0425



= = 54.4361 MJ / kg

= = 1115.3 BTU / SCF

= = 1411.4 BTU / SCF28.9626





5. ENERGY DELIVERED

Q = ( V * D * Hm - Qr ) / 1055.12 With Qr = V * 288.15

*Pa

* 37.707 (Ideal Gas)( 273.15 + Tv ) 1013.25







THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO GPA 2145 (2000).




m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038123 55.575

ETHANE 0.0595 30.070 0.047925 51.950

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076856 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104868 48.716

NITROGEN 0.0028 28.013 0.046900 0

CARBON DIOXIDE 0.0000 44.010 0.027183 0

OXYGEN 0.0000 31.9988 0.031474 0



0.0425



= = 54.4361 MJ / kg

= = 1115.3 BTU / SCF

= = 1411.4 BTU / SCF28.9626





5. ENERGY DELIVERED

GROSS QUANTITY DELIVERED = VOLUME * DENSITY * HHV (MASS BASED) / 1055.12











m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.042 0.038123 55.576

ETHANE 0.0595 30.069 0.047925 51.952

PROPANE 0.0224 44.096 0.062479 50.370

ISO BUTANE 0.0069 58.122 0.078332 49.389

N-BUTANE 0.0058 58.122 0.076856 49.547

ISO PENTANE 0.0002 72.149 0.091699 48.950

N-PENTANE 0.0000 72.149 0.091562 49.046

N-HEXANE 0.0000 86.175 0.104868 48.717

NITROGEN 0.0028 28.013 0.046900 0

CARBON DIOXIDE 0.0000 44.010 0.027183 0

OXYGEN 0.0000 31.9990 0.031474 0



0.0425



= = 54.4372 MJ / kg

= = 1115.2 BTU / SCF

= = 1411.3 BTU / SCF28.9626





5. ENERGY DELIVERED

GROSS QUANTITY DELIVERED = VOLUME * DENSITY * HHV (MASS BASED) / 1055.12









FOR INTERTEK FOR TERMINAL FOR VESSEL


m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038123 55.575

ETHANE 0.0595 30.070 0.047925 51.950

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076856 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104868 48.716

NITROGEN 0.0028 28.013 0.046900 0

CARBON DIOXIDE 0.0000 44.010 0.027183 0

OXYGEN 0.0000 31.9988 0.031474 0



0.0425



= = 54.4361 MJ / kg

= = 1115.3 BTU / SCF

= = 1411.4 BTU / SCF28.9626





5. ENERGY DELIVERED

Q = ( V * D * Hm - Qr ) / 1055.12 With Qr = V * 288.15

*Pa

* 37.707 * 0.50( 273.15 + Tv ) 1013.25











m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038122 55.575

ETHANE 0.0595 30.070 0.047925 51.95

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076857 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104877 48.716

NITROGEN 0.0028 28.013 0.046866 0

CARBON DIOXIDE 0.0000 44.010 0.027180 0

OXYGEN 0.0000 31.999 0.031474 0



0.0425



= = 54.4361 MJ / kg

= = 1115 BTU / SCF

= = 1411 BTU / SCF28.9626





5. ENERGY DELIVERED

QUANTITY = V * D * Hm - Qr

WITH Qr = V * 288.15

*Pa

* 37.7 (Ideal Gas)1055.12 ( 273.15 + Tv ) 1013.25







THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO G.P.A. 2145 SI (1989).




m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C


Hv (VOLUME) 60/60°F at 14.696 psia

S ( Xi * Mi * Hi) * 1.13285Hv (VOLUME) 60/60°F at 14.696 psia

WOBBE INDEX 60/60°F at 14.696 psia


60/60°F at 14.696 psia

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038122 55.575

ETHANE 0.0595 30.070 0.047925 51.95

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076857 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104877 48.716

NITROGEN 0.0028 28.013 0.046866 0

CARBON DIOXIDE 0.0000 44.010 0.027180 0

OXYGEN 0.0000 31.999 0.031474 0



0.0425



= = 54.4361 MJ / kg

= = 1115 BTU / SCF

= = 1411 BTU / SCF28.9626





5. ENERGY DELIVERED

GROSS QUANTITY DELIVERED = VOLUME * DENSITY * HIGHER HEATING VALUE (MASS BASED) / 1055.12







THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO G.P.A. 2145 SI (1996).




m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C


Hv (VOLUME) 60/60°F at 14.696 psia

S ( Xi * Mi * Hi) * 1.13285Hv (VOLUME) 60/60°F at 14.696 psia

WOBBE INDEX 60/60°F at 14.696 psia


60/60°F at 14.696 psia

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038123 55.575

ETHANE 0.0595 30.070 0.047925 51.950

PROPANE 0.0224 44.097 0.062479 50.368

ISO BUTANE 0.0069 58.123 0.078332 49.388

N-BUTANE 0.0058 58.123 0.076856 49.546

ISO PENTANE 0.0002 72.150 0.091699 48.949

N-PENTANE 0.0000 72.150 0.091562 49.045

N-HEXANE 0.0000 86.177 0.104868 48.716

NITROGEN 0.0028 28.013 0.046900 0

CARBON DIOXIDE 0.0000 44.010 ----- 0

OXYGEN 0.0000 31.9988 0.031474 0



0.0425



= = 54.4361 MJ / kg

= = 41.63628.314510 * 288.15

= = 52.690028.9626


LIQUID TEMPERATURE AFTER LOADING = -160.2 °C VESSEL O.C.T. VOLUME = 405

VAPOR TEMPERATURE BEFORE LOADING = -128.5 °C VESSEL C.C.T. VOLUME = 136,293

ABSOLUTE PRESSURE BEFORE LOADING = 116.6 kPa LOADED VOLUME = 135,888

5. ENERGY DELIVERED


*Pa

* 37.707 (Ideal Gas)( 273.15 + Tv ) 101.325











m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C



S ( Xi * Mi * Hi ) * 101.325 Hv (VOLUME) 15/15°C at 101.325 kPa

MJ / m3



15/15°C at 101.325 kPa

MJ / m3

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038123 55.574

ETHANE 0.0595 30.070 0.047925 51.950

PROPANE 0.0224 44.097 0.062479 50.37

ISO BUTANE 0.0069 58.123 0.078332 49.39

N-BUTANE 0.0058 58.123 0.076856 49.55

ISO PENTANE 0.0002 72.150 0.091699 48.95

N-PENTANE 0.0000 72.150 0.091562 49.04

N-HEXANE 0.0000 86.177 0.104868 48.75

NITROGEN 0.0028 28.0135 0.046900 0

CARBON DIOXIDE 0.0000 44.010 0.027192 0

OXYGEN 0.0000 31.9988 0.031474 0



0.0425



= = 54.4355 MJ / kg

= = 1115 BTU / SCF

= = 1411 BTU / SCF28.9626





5. ENERGY DELIVERED

Q = ( V * D * Hm - Qr ) / 1055.12 With Qr = V * 273.15

*Pa

* 39.78 (Ideal Gas)( 273.15 + Tv ) 1013.25





THE STANDARD REFERENCE CONDITIONS IDENTIFIES TEMPERATURE OF 60°F






m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3









(Xi) (Mi) (Vi) (Hi)

METHANE 0.9024 16.043 0.038122 55.560

ETHANE 0.0595 30.070 0.047925 51.926

PROPANE 0.0224 44.097 0.062479 50.393

ISO BUTANE 0.0069 58.124 0.078332 49.402

N-BUTANE 0.0058 58.124 0.076857 49.544

ISO PENTANE 0.0002 72.151 0.091699 48.944

N-PENTANE 0.0000 72.151 0.091562 49.053

N-HEXANE 0.0000 86.178 0.104877 48.719

NITROGEN 0.0028 28.013 0.046866 0

CARBON DIOXIDE 0.0000 44.010 0.027180 0

OXYGEN 0.0000 31.999 0.031474 0



0.0425



= = 54.4233 MJ / kg

= = 1115 BTU / SCF

= = 1411 BTU / SCF28.9626





5. ENERGY DELIVERED

Q = ( V * D * Hm - Qr ) / 1055.12 With Qr = V * 288.15

*Pa

* 37.7 (Ideal Gas)( 273.15 + Tv ) 1013.25





THE STANDARD REFERENCE CONDITIONS IDENTIFIES TEMPERATURE OF 60°F


THE HIGHER HEATING VALUES AND QUANTITY OF ENERGY DELIVERED IS DETERMINED ACCORDING TO I.P. 251/76.




m3 / kmole

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C






60/60°F at 14.696 PSIA

m3

m3

m3








COMPONENTS FRACTION kg / kmol MJ / kmol

(Xi) (Mi) (Vi) (Hi)

METHANE 0.902400 16.043 0.038123 891.56

ETHANE 0.059500 30.070 0.047925 1562.14

PROPANE 0.022400 44.097 0.062479 2221.1

ISO BUTANE 0.006900 58.123 0.078332 2870.58

N-BUTANE 0.005800 58.123 0.076856 2879.76

ISO PENTANE 0.000200 72.150 0.091699 3531.68

N-PENTANE 0.000000 72.150 0.091562 3538.6

N-HEXANE 0.000000 86.177 0.104868 4198.24

NITROGEN 0.002800 28.014 0.046900 0

OXYGEN 0.000000 31.999 0.031474 0



0.0425



= = 54.4346 MJ / kg

= = 41.63518.314510 * 288.15

= = 52.688628.9626





5. ENERGY DELIVERED

QUANTITY = V * D * Hm - Qr WITH Qr = V * ( 273.15 + 15 )

*Pa

* 37.7 (Ideal Gas)( 273.15 + Tv ) 1013.25











m3 / kmol

S ( Xi * Mi )

S ( Xi * Vi ) - Xm * C

Hm (MASS) 15°C

S ( Xi * Hi ) Hm (MASS) 15°CS ( Xi * Mi )


S ( Xi * Hi ) * 101.325 Hv (VOLUME) 15/15°C at 101.325 kPa

MJ / m3



15/15°C at 101.325 kPa

MJ / m3

m3

m3

m3



O P E N I N G C U S T O D Y T R A N S F E R

VESSEL : SK SPLENDOR DATE : 4-Aug-2009 TIME : 10:28


1. OPENING CUSTODY TRANSFER MEASUREMENTS

TANK NAME 1 2 3 4

SYSTEM TYPE PRIMARY PRIMARY PRIMARY PRIMARY

1ST READING m 0.035 0.033 0.033 0.287

2ND READING m 0.035 0.032 0.033 0.297

3RD READING m 0.035 0.032 0.033 0.290

4TH READING m 0.035 0.033 0.033 0.290

5TH READING m 0.035 0.032 0.032 0.290

AVG. GAUGE m 0.035 0.032 0.033 0.291

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m -0.003 -0.004 -0.004 -0.011

LIST CORR. m 0.007 0.010 0.010 0.000

CORR. GAUGE m 0.039 0.038 0.039 0.280

2. OPENING CUSTODY TRANSFER TEMPERATURES

TANK NAME 1 2 3 4

TEMP PROBE #1 °C -119.60 V -123.00 V -123.10 V -118.20 V

TEMP PROBE #2 °C -127.10 V -126.90 V -127.20 V -125.40 V

TEMP PROBE #3 °C -129.60 V -129.00 V -129.10 V -129.00 V

TEMP PROBE #4 °C -132.40 V -131.40 V -131.80 V -133.60 V

TEMP PROBE #5 °C -133.10 V -131.90 V -132.30 V -136.10 V

TEMP PROBE #6 °C -143.20 L -141.50 L -142.20 L -157.90 L

TANK AVERAGE °C -128.36 V -128.44 V -128.70 V -128.46 V

TANK AVERAGE °C -143.20 L -141.50 L -142.20 L -157.90 L

AVERAGE VAPOR TEMPERATURE = -128.5 °C AVERAGE LIQUID TEMPERATURE = -146.2 °C

3. OPENING CUSTODY TRANSFER PRESSURES

TANK NAME 1 2 3 4

PRESSURE 1166 1166 1166 1166

AVERAGE TANK PRESSURE = 1166 mbar ATMOSPHERIC PRESSURE = 998 mbar

4. OPENING CUSTODY TRANSFER VOLUMES

TANK NAME 1 2 3 4

TANK VOLUME 21.371 37.771 38.761 307.075

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 21.371 37.771 38.761 307.075

OPENING CUSTODY TRANSFER VOLUME = 404.978 CUBIC METERS


FWD DRAFT = 9.60 m TRIM = 0.18 m VESSEL DECK LINES = EMPTY

AFT DRAFT = 9.78 m LIST = 0.21 °P



Arrival Inspection LNG-LD-009H1 (07-AUG-09) - 14

m3

m3



A F T E R G A S - U P M E A S U R E M E N T



1. OPENING CUSTODY TRANSFER MEASUREMENTS

TANK NAME 1 2 3 4


1ST READING m 0.000 0.000 0.000 0.000

2ND READING m 0.000 0.000 0.000 0.000

3RD READING m 0.000 0.000 0.000 0.000

4TH READING m 0.000 0.000 0.000 0.000

5TH READING m 0.000 0.000 0.000 0.000

AVG. GAUGE m 0.000 0.000 0.000 0.000

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m 0.000 0.000 0.000 0.000

LIST CORR. m 0.000 0.000 0.000 0.000

CORR. GAUGE m 0.000 0.000 0.000 0.000

2. OPENING CUSTODY TRANSFER TEMPERATURES

TANK NAME 1 2 3 4

TEMP PROBE #1 °C 24.02 V 23.77 V 23.99 V 25.22 V

TEMP PROBE #2 °C 23.91 V 23.52 V 23.67 V 25.10 V

TEMP PROBE #3 °C 23.93 V 23.50 V 23.63 V 25.13 V

TEMP PROBE #4 °C 23.80 V 23.49 V 23.64 V 24.99 V

TEMP PROBE #5 °C 23.74 V 23.37 V 23.52 V 24.90 V

TEMP PROBE #6 °C

TANK AVERAGE °C 23.88 V 23.53 V 23.69 V 25.07 V

TANK AVERAGE °C

AVERAGE VAPOR TEMPERATURE = 24.0 °C AVERAGE LIQUID TEMPERATURE = °C

3. OPENING CUSTODY TRANSFER PRESSURES

TANK NAME 1 2 3 4

PRESSURE 1172 1171 1172 1169

AVERAGE TANK PRESSURE = 1171 mbar ATMOSPHERIC PRESSURE = 1008 mbar

4. OPENING CUSTODY TRANSFER VOLUMES

TANK NAME 1 2 3 4

TANK VOLUME 0.000 0.000 0.000 0.000

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 0.000 0.000 0.000 0.000




AFT DRAFT = 9.20 m LIST = 0.00



After Gas Up Inspection LNG-LD-009H1 (07-AUG-09) - 14

m3

m3



A F T E R C O O L - D O W N M E A S U R E M E N T



1. AFTER COOL DOWN MEASUREMENTS

TANK NAME 1 2 3 4


1ST READING m 0.069 0.027 0.042 0.044

2ND READING m 0.069 0.027 0.042 0.044

3RD READING m 0.069 0.027 0.042 0.044

4TH READING m 0.069 0.027 0.042 0.044

5TH READING m 0.069 0.027 0.042 0.044

AVG. GAUGE m 0.069 0.027 0.042 0.044

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m -0.004 -0.003 -0.005 -0.004

LIST CORR. m 0.005 0.010 0.009 0.006

CORR. GAUGE m 0.070 0.034 0.046 0.046

2. AFTER COOL DOWN TEMPERATURES

TANK NAME 1 2 3 4

TEMP PROBE #1 °C -122.00 V -119.20 V -118.90 V -119.40 V

TEMP PROBE #2 °C -124.20 V -122.00 V -121.90 V -122.30 V

TEMP PROBE #3 °C -125.70 V -124.50 V -124.60 V -124.70 V

TEMP PROBE #4 °C -127.70 V -126.30 V -126.60 V -126.60 V

TEMP PROBE #5 °C -127.70 V -126.90 V -127.60 V -126.90 V

TEMP PROBE #6 °C -158.50 L -155.10 L -158.30 L -158.80 L




3. AFTER COOL DOWN PRESSURES

TANK NAME 1 2 3 4

PRESSURE 1069 1070 1070 1070

AVERAGE TANK PRESSURE = 1069.75 mbar ATMOSPHERIC PRESSURE = 998 mbar

4. AFTER COOL DOWN VOLUMES

TANK NAME 1 2 3 4

TANK VOLUME 47.856 44.726 60.576 59.168

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 47.856 44.726 60.576 59.168

AFTER COOL DOWN VOLUME = 212.326 CUBIC METERS




Data from Snapshot CTS



After Cool Down Inspection LNG-LD-009H1 (07-AUG-09) - 14

m3

m3



C L O S I N G C U S T O D Y T R A N S F E R



1. CLOSING CUSTODY TRANSFER MEASUREMENTS

TANK NAME 1 2 3 4


1ST READING m 26.360 26.236 26.257 26.232

2ND READING m 26.355 26.250 26.241 26.251

3RD READING m 26.385 26.243 26.242 26.243

4TH READING m 26.355 26.254 26.236 26.243

5TH READING m 26.393 26.250 26.248 26.237

AVG. GAUGE m 26.370 26.247 26.245 26.241

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m -0.030 -0.042 -0.042 -0.036

LIST CORR. m 0.000 0.001 0.000 0.000

CORR. GAUGE m 26.340 26.206 26.203 26.205

2. CLOSING CUSTODY TRANSFER TEMPERATURES

TANK NAME 1 2 3 4

TEMP PROBE #1 °C -145.40 V -155.00 V -155.10 V -152.40 V

TEMP PROBE #2 °C -160.20 L -160.20 L -160.20 L -160.30 L

TEMP PROBE #3 °C -160.20 L -160.30 L -160.20 L -160.30 L

TEMP PROBE #4 °C -160.20 L -160.30 L -160.30 L -160.20 L

TEMP PROBE #5 °C -160.20 L -160.20 L -160.20 L -160.20 L

TEMP PROBE #6 °C -160.30 L -160.30 L -160.20 L -160.30 L




3. CLOSING CUSTODY TRANSFER PRESSURES

TANK NAME 1 2 3 4

PRESSURE 1101 1101 1102 1102


4. CLOSING CUSTODY TRANSFER VOLUMES

TANK NAME 1 2 3 4

TANK VOLUME 24,159.419 38,797.660 38,818.221 34,517.644

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 24,159.419 38,797.660 38,818.221 34,517.644

CLOSING CUSTODY TRANSFER VOLUME = 136,292.944 CUBIC METERS


FWD DRAFT = 11.45 m TRIM = 0.05 m VESSEL DECK LINES = FULL


SAMPLES FOR OMAN LNG TESTING WERE SEALED (# 046725 / # 046769

SAMPLES FOR OMAN LNG RETAIN WERE SEALED (# 046797 / # 046736)

SAMPLES FOR SHIP SEALED (# 046707 / # 046761)

DRY LINES OF GC WERE DONE BEFORE START FIRST STANDARD GAS INJECTION



Departure Inspection LNG-LD-009H1 (07-AUG-09) - 14

m3

m3



S E C O N D A R Y C U S T O D Y T R A N S F E R



1. OPENING SECONDARY CUSTODY TRANSFER MEASUREMENTS

TANK NAME 1 2 3 4

1ST READING m 0.039 0.037 0.039 0.289

2ND READING m 0.035 0.038 0.037 0.290

3RD READING m 0.040 0.038 0.037 0.290

4TH READING m 0.039 0.036 0.037 0.295

5TH READING m 0.039 0.036 0.039 0.295

AVG. GAUGE m 0.038 0.037 0.038 0.292

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m -0.004 -0.004 -0.005 -0.012

LIST CORR. m 0.009 0.012 0.012 0.003

CORR. GAUGE m 0.043 0.045 0.045 0.283

2. OPENING SECONDARY CUSTODY TRANSFER VOLUMES

TANK NAME 1 2 3 4

TANK VOLUME 23.611 44.882 44.875 310.528

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 23.611 44.882 44.875 310.528

OPENING SECONDARY CUSTODY TRANSFER VOLUME = 423.896 CUBIC METERS


DIFFERENCE = 18.918 CUBIC METERS

3. CLOSING SECONDARY CUSTODY TRANSFER MEASUREMENTS

TANK NAME 1 2 3 4

1ST READING m 26.366 26.249 26.250 26.254

2ND READING m 26.367 26.256 26.253 26.256

3RD READING m 26.372 26.254 26.249 26.256

4TH READING m 26.368 26.253 26.248 26.256

5TH READING m 26.369 26.250 26.248 26.255

AVG. GAUGE m 26.368 26.252 26.250 26.255

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m -0.035 -0.047 -0.047 -0.044

LIST CORR. m 0.005 0.005 0.005 0.005

CORR. GAUGE m 26.338 26.210 26.208 26.216

4. CLOSING SECONDARY CUSTODY TRANSFER VOLUMES

TANK NAME 1 2 3 4

TANK VOLUME 24,157.993 38,801.440 38,822.552 34,526.897

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 24,157.993 38,801.440 38,822.552 34,526.897

CLOSING SECONDARY CUSTODY TRANSFER VOLUME = 136,308.882 CUBIC METERS

CLOSING CUSTODY TRANSFER VOLUME = 136,292.944 CUBIC METERS

DIFFERENCE = 15.938 CUBIC METERS


SEA CONDITION : ROLLING



LNG-LD-009H1 (07-AUG-09) - 14

m3

m3

m3

m3



V E S S E L M E A S U R E M E N T - R E F E R E N C E O N L Y

VESSEL : SK SPLENDOR DATE : 5-Jun-2007 TIME : 06:07


1. VESSEL TANK MEASUREMENTS

TANK NAME 1 2 3 4


1ST READING m 0.000 0.000 0.000 0.000

2ND READING m 0.000 0.000 0.000 0.000

3RD READING m 0.000 0.000 0.000 0.000

4TH READING m 0.000 0.000 0.000 0.000

5TH READING m 0.000 0.000 0.000 0.000

AVG. GAUGE m 0.000 0.000 0.000 0.000

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m 0.000 0.000 0.000 0.000

LIST CORR. m 0.000 0.000 0.000 0.000

CORR. GAUGE m 0.000 0.000 0.000 0.000

2. VESSEL TANK TEMPERATURES

TANK NAME 1 2 3 4

TEMP PROBE #1 °C 29.76 V 30.08 V 29.44 V 29.70 V

TEMP PROBE #2 °C 29.46 V 29.78 V 29.18 V 29.61 V

TEMP PROBE #3 °C 29.08 V 29.25 V 28.80 V 29.48 V

TEMP PROBE #4 °C 29.28 V 29.26 V 28.67 V 29.48 V

TEMP PROBE #5 °C 28.71 V 29.12 V 28.65 V 29.33 V

TEMP PROBE #6 °C


TANK AVERAGE °C


3. VESSEL TANK PRESSURES

TANK NAME 1 2 3 4

PRESSURE 1106 1107 1106 1107


4. VESSEL TANK VOLUMES

TANK NAME 1 2 3 4

TANK VOLUME 0.000 0.000 0.000 0.000

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 0.000 0.000 0.000 0.000

VESSEL VOLUME = 0.000 CUBIC METERS



AFT DRAFT = 9.02 m LIST = 0.02 °S

ABDELOUAHEB ZENNIR


Vessel Measurement 1 LNG-LD-009H1 (07-AUG-09) - 14

m3

m3







TANK NAME 1 2 3 4


1ST READING m 0.000 0.000 0.000 0.000

2ND READING m 0.000 0.000 0.000 0.000

3RD READING m 0.000 0.000 0.000 0.000

4TH READING m 0.000 0.000 0.000 0.000

5TH READING m 0.000 0.000 0.000 0.000

AVG. GAUGE m 0.000 0.000 0.000 0.000

DENSITY CORR. m 0.000 0.000 0.000 0.000

TEMP. CORR. m 0.000 0.000 0.000 0.000

TRIM CORR. m 0.000 0.000 0.000 0.000

LIST CORR. m 0.000 0.000 0.000 0.000

CORR. GAUGE m 0.000 0.000 0.000 0.000


TANK NAME 1 2 3 4

TEMP PROBE #1 °C 29.76 V 30.08 V 29.44 V 29.70 V

TEMP PROBE #2 °C 29.46 V 29.78 V 29.18 V 29.61 V

TEMP PROBE #3 °C 29.08 V 29.25 V 28.80 V 29.48 V

TEMP PROBE #4 °C 29.28 V 29.26 V 28.67 V 29.48 V

TEMP PROBE #5 °C 28.71 V 29.12 V 28.65 V 29.33 V

TEMP PROBE #6 °C


TANK AVERAGE °C



TANK NAME 1 2 3 4

PRESSURE 1106 1107 1106 1107



TANK NAME 1 2 3 4

TANK VOLUME 0.000 0.000 0.000 0.000

THERMAL CORR. 1.000000 1.000000 1.000000 1.000000

CORR. VOLUME 0.000 0.000 0.000 0.000





ABDELOUAHEB ZENNIR



m3

m3



G E N E R A L I N F O R M A T I O N



1. VESSEL - CUSTODY TRANSFER MEASUREMENT SYSTEMS

VESSEL TANK DESIGN TYPE : MEMBRANE NUMBER OF TANKS : 4

PRIMARY GAUGING DEVICE MAKE : FOXBORO TYPE : RADAR

SECONDARY GAUGING DEVICE MAKE : WHESSOE TYPE : FLOAT

TEMPERATURE DEVICE MAKE : FOXBORO NUMBER PER TANK : 6

PRESSURE DEVICE MAKE : FOXBORO RANGE : 800 MBAR TO 1400 MBAR

2. VESSEL - CARGO TANK CAPACITY & TEMPERATURE PROBE HEIGHT PROFILES

TANK NAME 1 2 3 4

GAUGE HEIGHT m 41.491 41.509 41.511 41.498

TANK CAPACITY 37,326.000 37,336.000 37,352.000 37,345.000

TEMP PROBE #1 26.586 26.471 26.495 26.496

TEMP PROBE #2 25.525 25.604 25.520 25.517

TEMP PROBE #3 22.847 22.839 22.849 22.844

TEMP PROBE #4 13.480 13.432 13.482 13.475

TEMP PROBE #5 6.791 6.776 6.794 6.789

TEMP PROBE #6 0.025 0.025 0.026 0.025

3. VESSEL - CARGO QUANTITY CONSUMED AS FUEL BY VESSEL

METER I.D. O.C.T. READING C.C.T. READING OBSERVED CONDITIONS APPLY

1. ENGINE ROOM OP : 0 kg CL : 0 kg MASS BASED CALCS YES

2.

3.

4.

5.

6.

7.

THE ENERGY OF GAS CONSUMED AS FUEL IS BASED ON : THE HIGHER HEATING VALUE OF LNG CARGO

4. TERMINAL - GAS CHROMATOGRAPHY EQUIPMENT

TESTING EQUIPMENT MAKE : AC.AGILENT MODEL : 6890

CERTIFIED REFERENCE GAS SUPPLIER : SCOTT GAS SERIAL # : 7800102

GC VERIFICATION BEFORE : YES AFTER : NO

5. TERMINAL - PRIMARY SAMPLING SYSTEM

SAMPLE COLLECTOR : GAS SAMPLE HOLDER SAMPLING SYSTEM TYPE : CONTINUOUS

# OF SAMPLES PER SET : 3 SIZE OF SAMPLE : 2250 cc

FREQUENCY OF SAMPLING : SAMPLED AFTER COMPLETION OF BULK LOADING

6. TERMINAL - SHORE STORAGE & CAPACITY

TANKS 1 2

TANK ID # T 3101 T 3102

135,000 135,000




LNG-LD-009H1 (07-AUG-09) - 14

m3

CAPACITY (M3)



O P E R A T I O N A L C H E C K L I S T



1. SHORE OPERATIONS - PRIOR TO LOAD

DID THE TERMINAL SUPPLY A CURRENT REPORT OF CALIBRATION FOR THE GC ? YES

WAS THE GC VERIFIED AGAINST A CERTIFIED REFERENCE GAS PRIOR TO LOADING / USAGE ? YES

DOES THE CERTIFIED REFERENCE GAS HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

2. VESSEL OPERATIONS - ON ARRIVAL

ARE ALL PRIMARY CUSTODY GAUGING DEVISES OPERATIONAL ON ARRIVAL ? YES

DOES THE PRIMARY SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

ARE ALL SECONDARY CUSTODY GAUGING DEVISES OPERATIONAL ON ARRIVAL ? YES

DOES THE SECONDARY SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

ARE ALL CUSTODY REMOTE TEMPERATURE DEVISES OPERATIONAL ON ARRIVAL ? YES

DOES THE TEMPERATURE SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

ARE ALL CUSTODY PRESSURE DEVISES OPERATIONAL ON ARRIVAL ? YES

DOES THE PRESSURE SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

WERE THE TANKS "BOTTLED UP" DURING OPENING CUSTODY TRANSFER MEASUREMENT ? YES

DOES THE VESSEL HAVE CURRENT CERTIFIED TANK STRAPPING TABLES ? YES

ARE THE TANK STRAPPING TABLES WRITTEN IN ENGLISH ? YES

DOES THE TANK STRAPPING TABLES EXPLAIN HOW TO UTILIZED THE TABLES ? YES

DOES THE TANK STRAPPING TABLES HAVE GAUGE CORRECTION FACTORS (TRIM, LIST, ETC) ? YES

DOES THE TANK STRAPPING TABLES HAVE 100% CAPACITIES FOR INDIVIDUAL TANKS ? YES

DOES THE TANK STRAPPING TABLES HAVE GAUGE HEIGHTS FOR INDIVIDUAL TANKS ? YES

DOES THE TANK STRAPPING TABLES HAVE TEMPERATURE PROFILES FOR INDIVIDUAL TANKS ? YES

3. SHORE OPERATIONS - DURING LOAD

WAS CORRECT NUMBER OF SAMPLES PULLED AT THE PROPER TIME DURING LOAD ? YES

4. VESSEL OPERATIONS - ON DEPARTURE

ARE ALL PRIMARY CUSTODY GAUGING DEVISES OPERATIONAL ON DEPARTURE ? YES

ARE ALL SECONDARY CUSTODY GAUGING DEVISES OPERATIONAL ON DEPARTURE ? YES

ARE ALL CUSTODY REMOTE TEMPERATURE DEVISES OPERATIONAL ON DEPARTURE ? YES

ARE ALL CUSTODY PRESSURE DEVISES OPERATIONAL ON DEPARTURE ? YES

WERE THE TANKS "BOTTLED UP" DURING CLOSING CUSTODY TRANSFER MEASUREMENT ? YES

5. SHORE OPERATIONS - AFTER LOAD

WAS THE GC VERIFIED AGAINST A CERTIFIED REFERENCE AFTER LOADING / USAGE ? YES

DID THE TERMINAL SUPPLY A CERTIFICATE OF VERIFICATION FOR THE GC ? YES

DID THE TERMINAL SUPPLY A COMPOSITIONAL PRINT OUT OF THE GC DURING LOAD ? YES




Checklist 1 - Discontinuous Sampling System LNG-LD-009H1 (07-AUG-09) - 14



O P E R A T I O N A L C H E C K L I S T



1. SHORE OPERATIONS - PRIOR TO LOAD

WAS THE GAS SAMPLING EQUIPMENT (LINES, TANK, ETC.) INSPECTED AND PURGED ? YES

WAS THE GAS SAMPLING EQUIPMENT SET UP PROPERLY TO RECEIVE SAMPLE ? YES

2. VESSEL OPERATIONS - ON ARRIVAL

WERE ALL PRIMARY CUSTODY GAUGING DEVISES OPERATIONAL ON ARRIVAL ? YES

DID THE PRIMARY SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

WERE ALL SECONDARY CUSTODY GAUGING DEVISES OPERATIONAL ON ARRIVAL ? YES

DID THE SECONDARY SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

WERE ALL CUSTODY REMOTE TEMPERATURE DEVISES OPERATIONAL ON ARRIVAL ? YES

DID THE TEMPERATURE SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

WERE ALL CUSTODY PRESSURE DEVISES OPERATIONAL ON ARRIVAL ? YES

DID THE PRESSURE SYSTEM HAVE A CURRENT CERTIFICATE OF CALIBRATION ? YES

WERE THE TANKS "BOTTLED UP" DURING OPENING CUSTODY TRANSFER MEASUREMENT ? YES

DID THE VESSEL HAVE CURRENT CERTIFIED TANK STRAPPING TABLES ? YES

WERE THE TANK STRAPPING TABLES WRITTEN IN ENGLISH ? YES

DID THE TANK STRAPPING TABLES EXPLAIN HOW TO UTILIZED THE TABLES ? YES

DID THE TANK STRAPPING TABLES HAVE GAUGE CORRECTION FACTORS (TRIM, LIST, ETC) ? YES

DID THE TANK STRAPPING TABLES HAVE 100% CAPACITIES FOR INDIVIDUAL TANKS ? YES

DID THE TANK STRAPPING TABLES HAVE GAUGE HEIGHTS FOR INDIVIDUAL TANKS ? YES

DID THE TANK STRAPPING TABLES HAVE TEMPERATURE PROFILES FOR INDIVIDUAL TANKS ? YES

3. SHORE OPERATIONS - DURING LOAD

WERE THE CORRECT NUMBER OF SPOT SAMPLES PULLED AT THE PROPER TIME DURING LOAD ? YES

4. VESSEL OPERATIONS - ON DEPARTURE

WERE ALL PRIMARY CUSTODY GAUGING DEVISES OPERATIONAL ON DEPARTURE ? YES

WERE ALL SECONDARY CUSTODY GAUGING DEVISES OPERATIONAL ON DEPARTURE ? YES

WERE ALL CUSTODY REMOTE TEMPERATURE DEVISES OPERATIONAL ON DEPARTURE ? YES

WERE ALL CUSTODY PRESSURE DEVISES OPERATIONAL ON DEPARTURE ? YES

WERE THE TANKS "BOTTLED UP" DURING CLOSING CUSTODY TRANSFER MEASUREMENT ? YES

5. SHORE OPERATIONS - AFTER LOAD

DID THE GAS SAMPLING EQUIPMENT WORK PROPERLY THROUGHOUT THE ENTIRE LOAD ? YES

WERE THE CORRECT NUMBER OF TESTING SAMPLES COLLECTED FROM THE GAS SAMPLE HOLDER ? YES

DID THE TERMINAL SUPPLY A CURRENT REPORT OF CALIBRATION FOR THE GC ? YES

WAS THE GC VERIFIED AGAINST A CERTIFIED REFERENCE GAS PRIOR TO TESTING ? YES

WAS THE GC VERIFIED AGAINST A CERTIFIED REFERENCE GAS AFTER TESTING ? YES

DID THE CERTIFIED REFERENCE GAS HAVE A CURRENT CERTIFICATE OF ANALYSIS ? YES

DID THE TERMINAL SUPPLY A CERTIFICATE OF VERIFICATION FOR THE GC AFTER TESTING ? YES

DID THE TERMINAL SUPPLY A COMPOSITIONAL PRINT OUT OF THE GC ANALYSIS ? YES




Checklist 2 - Continuous Sampling System LNG-LD-009H1 (07-AUG-09) - 14



V E R I F I C A T I O N O F G C



1. OPENING VERIFICATION OF GC

COMPONENTCERTIFIED VARIANCE TEST GC VARIANCE TEST GC VARIANCE TEST GC VARIANCE

RESULTS ALLOWED RUN #1 PCT. RUN #2 PCT. RUN #3 PCT.

METHANE 91.9398 1.00% 91.9301 0.01% 91.9397 0.00% 91.9355 0.00%

ETHANE 5.0400 10.00% 5.0499 -0.20% 5.0412 -0.02% 5.0422 -0.04%

PROPANE 1.0020 10.00% 1.0028 -0.08% 1.0034 -0.14% 1.0020 0.00%

ISO BUTANE 0.1520 10.00% 0.1526 -0.39% 0.1523 -0.20% 0.1530 -0.66%

N-BUTANE 0.2030 10.00% 0.2031 -0.05% 0.2027 0.15% 0.2030 0.00%

ISO PENTANE 0.0531 10.00% 0.0532 -0.19% 0.0528 0.56% 0.0535 -0.75%

N-PENTANE 0.0538 10.00% 0.0543 -0.93% 0.0534 0.74% 0.0540 -0.37%

HEXANE + HVR 0.0503 10.00% 0.0501 0.40% 0.0500 0.60% 0.0508 -0.99%

NITROGEN 1.0130 10.00% 1.0130 0.00% 1.0139 -0.09% 1.0150 -0.20%

CARBON DIOXIDE 0.4930 10.00% 0.4909 0.43% 0.4906 0.49% 0.4910 0.41%

OXYGEN 0.0000 10.00% 0.0000 0.00% 0.0000 0.00% 0.0000 0.00%

TOTAL 100.0000 100.0000 100.0000 100.0000

OPENING VERIFICATION FOUND WITHIN VARIANCE YES DATE : 26-May-2007 TIME : 08:00

2. CLOSING VERIFICATION OF GC

COMPONENTCERTIFIED VARIANCE TEST GC VARIANCE TEST GC VARIANCE TEST GC VARIANCE

RESULTS ALLOWED RUN #1 PCT. RUN #2 PCT. RUN #3 PCT.

METHANE 91.9398 1.00% 91.9301 0.01% 91.9397 0.00% 91.9355 0.00%

ETHANE 5.0400 10.00% 5.0499 -0.20% 5.0412 -0.02% 5.0422 -0.04%

PROPANE 1.0020 10.00% 1.0028 -0.08% 1.0034 -0.14% 1.0020 0.00%

ISO BUTANE 0.1520 10.00% 0.1526 -0.39% 0.1523 -0.20% 0.1530 -0.66%

N-BUTANE 0.2030 10.00% 0.2031 -0.05% 0.2027 0.15% 0.2030 0.00%

ISO PENTANE 0.0531 10.00% 0.0532 -0.19% 0.0528 0.56% 0.0535 -0.75%

N-PENTANE 0.0538 10.00% 0.0543 -0.93% 0.0534 0.74% 0.0540 -0.37%

HEXANE + HVR 0.0503 10.00% 0.0501 0.40% 0.0500 0.60% 0.0508 -0.99%

NITROGEN 1.0130 10.00% 1.0130 0.00% 1.0139 -0.09% 1.0150 -0.20%

CARBON DIOXIDE 0.4930 10.00% 0.4909 0.43% 0.4906 0.49% 0.4910 0.41%

OXYGEN 0.0000 10.00% 0.0000 0.00% 0.0000 0.00% 0.0000 0.00%

TOTAL 100.0000 100.0000 100.0000 100.0000

CLOSING VERIFICATION FOUND WITHIN VARIANCE YES DATE : 26-May-2007 TIME : 10:00

3. EQUIPMENT INFORMATION AND CERTIFIED REFERENCE GAS

TESTING EQUIPMENT MAKE : AC.AGILENT MODEL : 6890

LAST CALIBRATION DATE : 15-Feb-2007 TIME : 17:00

CERTIFIED REFERENCE GAS SUPPLIER : SCOTT GAS SERIAL # : 7800102

CERTIFICATION DATE : 15-Feb-2007 TIME : 17:00




Verification of GC 1 - Site Specific LNG-LD-009H1 (07-AUG-09) - 14



V E R I F I C A T I O N O F G C

VESSEL : SK SPLENDOR DATE : 13-Nov-2007 TIME : 15:00


INSTRUMENT : GC C (HP 5890) LABORATORY TEMP : 23-23.5 °C

1. REFERENCE STANDARD GAS Cylinder # : GS 66889

COMPONENT Repeatability

(A) (B)

METHANE CH4 90.4013 272,701 272,177 0.19 272,439.0

ETHANE C2H6 4.4400 607,832 606,946 0.15 607,389.0

PROPANE C3H8 3.3500 701,594 702,057 0.07 701,825.5

ISO BUTANE i-C4H10 0.7080 198,953 198,637 0.16 198,795.0

N-BUTANE n-C4H10 0.6850 193,667 193,331 0.17 193,499.0

ISO PENTANE i-C5H12 0.0286 10,224 10,178 0.45 10,201.0

N-PENTANE n-C5H12 0.0286 9,937 9,918 0.19 9,927.5

NITROGEN N2 0.2870 32,521 32,198 1.00 32,359.5

OXYGEN O2 0.0297 3,283 3,195 2.72 3,239.0

CARBON DIOXIDE CO2 0.0418 5,636 5,791 2.71 5,713.5

TOTAL 100.0000

2. SAMPLE GAS Cylinder # : CPC-01 Seal # : 004659

COMPONENT Repeatability

(C) (C) x (A) / (B) (D) (D) x (A) / (B)

METHANE CH4 276,238 91.662 276,313 91.687 0.03

ETHANE C2H6 692,500 5.062 692,706 5.064 0.03

PROPANE C3H8 440,672 2.103 440,935 2.105 0.06

ISO BUTANE i-C4H10 89,076 0.317 89,110 0.317 0.04

N-BUTANE n-C4H10 72,378 0.256 72,288 0.256 0.12

ISO PENTANE i-C5H12 0 0.000 0 0.000 0.00

N-PENTANE n-C5H12 0 0.000 0 0.000 0.00

NITROGEN N2 2,494 0.022 2,488 0.022 0.24

OXYGEN O2 0 0.000 0 0.000 0.00

CARBON DIOXIDE CO2 0 0.000 0 0.000 0.00

TOTAL 99.422 99.451

3. NORMALIZATION

COMPONENT

(E) (E) x (A) / (B)

METHANE CH4 276,275.5 91.674 92.19 92.8085 -0.6185

ETHANE C2H6 692,603.0 5.063 5.09 4.7397 0.3503

PROPANE C3H8 440,803.5 2.104 2.12 1.8893 0.2307

ISO BUTANE i-C4H10 89,093.0 0.317 0.32 0.2689 0.0511

N-BUTANE n-C4H10 72,333.0 0.256 0.26 0.2151 0.0449

ISO PENTANE i-C5H12 0.0 0.000 0.00 0.0022 -0.0022

N-PENTANE n-C5H12 0.0 0.000 0.00 0.0000

NITROGEN N2 2,491.0 0.022 0.02 0.0762 -0.0562

OXYGEN O2 0.0 0.000 0.00 0.0000

CARBON DIOXIDE CO2 0.0 0.000 0.00 0.0000

TOTAL 99.436 100.00 100.000



Verification of GC 2 - Site Specific LNG-LD-009H1 (07-AUG-09) - 14

Concent Mol % First RSG

Count Peak AreaSecond RSG Count Peak Area

Average RSG Count Peak

Area

First Sample Count Peak

AreaUnnormal

Mol %

Second Sample Count

Peak AreaUnnormal

Mol %

Average Sample Count Peak Area

Unnormal Mol % Reported

Value Mol%Load Port

Mol %

Difference

%



B U N K E R S U R V E Y



1. VESSEL HISTORY FROM CHIEF ENGINEER

BUNKER PRODUCT : FUEL OIL DAYS AT SEA : 9.00 AT ANCH : 0.00

LAST PORT OF CALL : SINGAPORE AVERAGE BUNKER CONSUMPTION PER DAY

BUNKERS ON DEPARTURE : 1337.000 METRIC TONS AT SEA : 200.000 METRIC TONS

BUNKERS AT E.O.S.P. : 1463.160 METRIC TONS AT LOAD : 20.000 METRIC TONS

BUNKERS RECEIVED INTRANSIT : 3713.910 METRIC TONS AT DISC : 20.000 METRIC TONS

BUNKERS RECEIVED IN PORT : 0.000 METRIC TONS AT ANCHOR : 20.000 METRIC TONS

2. INSPECTION UPON ARRIVAL

VESSEL'S ULLAGES G.O.V. TEMP. V.C.F. G.S.V. DENSITY M. TONS

TANK METERS m3 °C T54B - 2004 m3 @ 15°C ( AIR )

TANK 1 FWD 24.200 0.000 20.0 0.99658 0.000 0.9894 0.000

TANK 2 STB 4.970 481.000 42.8 0.98092 471.823 0.9894 466.302

TANK 2 PORT 8.401 474.000 49.0 0.97664 462.927 0.9894 457.511

TANK 4 STB 3.633 141.000 39.7 0.98306 138.611 0.9894 136.990

TANK 1 SETTLING 8.790 212.000 60.0 0.96902 205.432 0.9894 203.029

TANK 2 SETTLING 5.476 197.000 60.0 0.96902 190.897 0.9894 188.663

TOTALS 1505.000 G.S.V. = 1469.691 M.T. = 1452.495

DATE : 3-Jun-2008 TIME : 07:40 DRAFT FWD : 9.60 m DRAFT AFT : 9.78 m

3. INSPECTION PRIOR TO SAILING



TANK 1 FWD 0.000 0.000 20.0 0.99658 0.000 0.9894 0.000

TANK 2 STB 4.950 482.000 43.0 0.98078 472.736 0.9894 467.205

TANK 2 PORT 8.420 474.000 44.0 0.98009 464.563 0.9894 459.127

TANK 4 STB 3.630 140.000 39.0 0.98354 137.696 0.9894 136.085

TANK 1 SETTLING 8.790 213.000 55.0 0.97249 207.140 0.9894 204.717

TANK 2 SETTLING 5.130 123.000 55.0 0.97249 119.616 0.9894 118.217

TOTALS 1432.000 G.S.V. = 1401.751 M.T. = 1385.351



QUANTITY OF BUNKERS CONSUMED DURING VOYAGE : 3598.415 METRIC TONS

QUANTITY OF BUNKERS CONSUMED DURING LOAD : 67.144 METRIC TONS



Bunker - Fuel Oil LNG-LD-009H1 (07-AUG-09) - 14

G.O.V. =

G.O.V. =



B U N K E R S U R V E Y



1. VESSEL HISTORY FROM CHIEF ENGINEER

BUNKER PRODUCT : MARINE DIESEL OIL DAYS AT SEA : 9.00 AT ANCH : 0.00

LAST PORT OF CALL : SINGAPORE AVERAGE BUNKER CONSUMPTION PER DAY

BUNKERS ON DEPARTURE : 159.890 METRIC TONS AT SEA : 0.000 METRIC TONS

BUNKERS AT E.O.S.P. : 133.800 METRIC TONS AT LOAD : 0.000 METRIC TONS

BUNKERS RECEIVED INTRANSIT : 0.000 METRIC TONS AT DISC : 1.000 METRIC TONS

BUNKERS RECEIVED IN PORT : 0.000 METRIC TONS AT ANCHOR : 0.000 METRIC TONS

2. INSPECTION UPON ARRIVAL



D.O TK 6.062 80.200 25.0 0.99180 79.542 0.8600 68.319

D.O SERVICE 3.908 77.300 25.0 0.99180 76.666 0.8600 65.849

TOTALS 157.500 G.S.V. = 156.209 M.T. = 134.168


3. INSPECTION PRIOR TO SAILING



D.O TK 6.063 80.200 25.0 0.99180 79.542 0.8600 68.319

D.O SERVICE 3.908 77.300 25.0 0.99180 76.666 0.8600 65.849

TOTALS 157.500 G.S.V. = 156.209 M.T. = 134.168



QUANTITY OF BUNKERS CONSUMED DURING VOYAGE : 25.722 METRIC TONS

QUANTITY OF BUNKERS CONSUMED DURING LOAD : 0.000 METRIC TONS



Bunker - Diesel Oil LNG-LD-009H1 (07-AUG-09) - 14

G.O.V. =

G.O.V. =



T I M E L O G



1. TIMES

DATE HOUR EVENT

4-Aug-2009 05:15 END OF SEA PASSAGE

4-Aug-2009 09:15 NOTICE OF READINESS TENDERED

4-Aug-2009 06:54 PILOT ON BOARD

4-Aug-2009 08:15 FIRST LINE ASHORE

4-Aug-2009 09:15 VESSEL ALL FAST

4-Aug-2009 09:22 TERMINAL GANGWAY DOWN & SECURE

4-Aug-2009 09:22 INSPECTOR ON BOARD

4-Aug-2009 09:32 COMMENCED CONNECTION OF CARGO & VAPOR ARMS

4-Aug-2009 09:49 COMPLETED CONNECTION OF CARGO & VAPOR ARMS

4-Aug-2009 10:00 COMMENCED PRE-LOAD KEY / SAFETY MEETING

4-Aug-2009 10:30 COMPLETED PRE-LOAD KEY / SAFETY MEETING

4-Aug-2009 10:33 COMMENCED TESTING OF E.S.D.

4-Aug-2009 09:15 NOTICE OF READINESS ACCEPTED

4-Aug-2009 10:27 COMMENCED OPENING CUSTODY TRANSFER INSPECTION

4-Aug-2009 10:28 COMPLETED OPENING CUSTODY TRANSFER INSPECTION

4-Aug-2009 10:40 COMMENCED COOL DOWN OF CARGO ARMS & VESSEL LINES

4-Aug-2009 12:15 COMPLETED COOL DOWN OF CARGO ARMS & VESSEL LINES

4-Aug-2009 12:20 COMMENCED LOADING OF CARGO

4-Aug-2009 12:59 FULL RATE LOADING

5-Aug-2009 02:47 LOADING RATE DOWN START

5-Aug-2009 03:25 COMPLETED LOADING

5-Aug-2009 04:21 COMMENCED CLOSING CUSTODY TRANSFER INSPECTION

5-Aug-2009 04:22 COMPLETED CLOSING CUSTODY TRANSFER INSPECTION

5-Aug-2009 04:25 COMMENCED DISCONNECTION OF VARGO & VAPOR ARMS

5-Aug-2009 04:39 COMPLETED DISCONNECTION OF CARGO & VAPOR ARMS

5-Aug-2009 05:00 POST LOADING MEETING & DOCUMENTATION

5-Aug-2009 05:15 VESSEL CLEAR

5-Aug-2009 06:30 ETS

5-Aug-2009 06:05 ANALYSIS COMPLETED

5-Aug-2009 06:25 COMMENCED CLOSING CUSTODY TRANSFER INSPECTION

5-Aug-2009 06:26 COMPLETED CLOSING CUSTODY TRANSFER INSPECTION

5-Aug-2009 06:52 COMMENCED DISCONNECTION OF CARGO & VAPOR ARMS

5-Aug-2009 07:17 COMPLETED DISCONNECTION OF CARGO & VAPOR ARMS

5-Aug-2009 07:30 POST LOADING MEETING & DOCUMENTATION

5-Aug-2009 07:40 VESSEL CLEARED

5-Aug-2009 08:00 VESSEL SAILED

5-Aug-2009 08:00 ANALYSIS COMPLETED


Sampling started : 17:15 0n 31st July 2008 and completed at 06:20 0n 01st August 2008

Analysis completed : 09:15 on 1st August 2008



Time Log - Page 1 LNG-LD-009H1 (07-AUG-09) - 14



T I M E L O G



1. TIMES

DATE HOUR EVENT







L E T T E R O F P R O T E S T

VESSEL : SK SPLENDOR DATE : TIME :


TO :

SIR :

RECEIVED BY YOURS FAITHFULLY,


FOR INTERTEK CALEB BRETT

LOP 1 LNG-LD-009H1 (07-AUG-09) - 14

ON BEHALF OF OUR CLIENT(S), WE HAVE BEEN APPOINTED INSPECTORS ON THE ABOVE NAMED VESSEL. ACTING FOR AND ON THEIR BEHALF, WE HEREBY NOTIFY YOU THAT ON THE LISTED DATE AND TIME THE FOLLOWING OCCURRED.

WE HEREBY RESERVE THE RIGHT OF OUR PRINCIPALS TO REFER TO THIS MATTER AT A LATER DATE AND TAKE SUCH ACTION AS MAY BE DEEMED NECESSARY.

KINDLY ACKNOWLEDGE RECEIPT ON THE COPY THEREOF AND RETURN IT TO US. THE SIGNATURE THUS OBTAINED ARE FOR RECEIPT ONLY AND IN NO WAY ACKNOWLEDGE RESPONSIBILITY FOR THE INCIDENT.






TO :

SIR :




LOP2 LNG-LD-009H1 (07-AUG-09) - 14









TO :

SIR :




LOP 3 LNG-LD-009H1 (07-AUG-09) - 14









TO :

SIR :




LOP 4 LNG-LD-009H1 (07-AUG-09) - 14






N I G E R I A L N G C E R T I F I C A T E O F L O A D I N G

VESSEL : SK SPLENDOR DATE : 15-Apr-2008


1. IDENTIFICATION

(a) CARGO RECEIVER (NLNG CUSTOMER) : BRITISH GAS

(b) NIGERIA LNG CARGO NUMBER : 963

(c) COMMENCED LOADING OF LNG DATE : 11-May-2008 TIME : 23:00

(d) COMPLETED LOADING ON LNG DATE : 13-May-2008 TIME : 01:00

2. BASIC DATA

(a) LIQUID LNG VOLUME LOADED : 135,888.000 CUBIC METERS

(b) AVERAGE TEMPERATURE OF LIQUID AFTER LOADING : -160.2 °C

(c) AVERAGE TEMPERATURE OF VAPOR BEFORE LOADING : -128.5 °C

(d) AVERAGE ABSOLUTE PRESSURE BEFORE LOADING : 1166 mbar

(e) LNG CARGO COMPOSITION:

COMPONENTS MOLE PERCENTAGE

NITROGEN 0.28

METHANE 90.24

ETHANE 5.95

PROPANE 2.24

ISO BUTANE 0.69

N-BUTANE 0.58

ISO PENTANE 0.02

N-PENTANE & HEAVIER 0

(f) IMPURITIES

CARBON DIOXIDE : 0 mol %

MERCURY : N/A ng / Nm3

MERCAPTAN : N/A mg / Nm3

HYDROGEN SULFIDE : N/A mg / Nm3

CARBONYL SULFIDE : N/A mg / Nm3

TOTAL SULFUR : N/A mg / Nm3

(g) HYDROCARBON DEWPOINT (MAX - between 1-80 bar gauge) : N/A °C

3. RESULTS

(a) LNG DENSITY AT -160.2 °C : 459.080

(b) GROSS CALORIFIC VALUE (MASS) : 54.4361 MJ / kg

(c) GROSS CALORIFIC VALUE (VOLUME) : 1115 BTU / SCF

(d) WOBBE INDEX (VOLUME) : 1411 BTU / SCF

4. TOTAL QUANTITY OF LNG UNLOADED





QUANTITY FOR GAS-UP 0 0 0

QUANTITY FOR COOL DOWN 0 0 0






CSR 1 - Nigeria LNG Certificate of Loading LNG-LD-009H1 (07-AUG-09) - 14

N2

C1

C2

C3

i-C4

n-C4

i-C5

n-C5 +

kg / m3

BG DATA SHEET - LOAD

Vessel Name: SK SPLENDOR Terminal / Port: OMAN LNGCargo No: OF039/09-SL100-KG Last Port of Call: INCHEON

Dates: JAN 4-5, 2009 Dates at Last Port: 20-Jul-2009File #: SUR/09/134 Last Port CCT Volume: 1,553.335 m3

LNG DataTotal Load Volume 135,888.000 m3

Total Load Quantity 3,207,380 MMBtu (60°F)BG - Total Load Quantity 3,207,380 MMBtu (60°F)

Total Load Quantity 62,172.077 MTCooldown Volume 0.000 m3Cooldown Volume 0 MMBtu (60°F)

Gas up Volume 0.000 m3Gas up Volume 0 MMBtu (60°F)

Vessel OCT Volume before loading 404.978 m3Vessel CCT Volume after loading 136,292.944 m3

Vessel Volume Received 135,888.000 m3Observied Liquid Temp after loading -160.2 Deg. C

LNG Density @ -160.2 °C 459.080 KG/M3LNG Density @ -160.0 °C 458.800 KG/M3

Higher Heating Value (mass) 54.4361 MJ / kg (15°C)BG - Higher Heating Value (mass) 51593 BTU / kg (60°F)

Higher Heating Value (Volume) 1115 BTU / SCF (60/60°F & 14.696 psi)BG - Higher Heating Value (Volume) 1117.6 BTU / SCF (60/60°F & 14.73 psi)

Wobbe Index 1411 BTU / SCF (60/60°F & 14.696 psi)BG - Wobbe Index 1414.3 BTU / SCF (60/60°F & 14.73 psi)

Gross Energy Received 3,218,508 MMBtu (60°F)Vapor Return 11,130 MMBtu (60°F)

Energy Delivered 3,207,380 MMBtu (60°F)Gas Consumed During Load 0 MMBtu (60°F)

Net Energy Received 3,207,378 MMBtu (60°F)Intransit Difference 1148.357 m3

Last Port of call CCT inspection: 20-Jul-2009 Date 15:48 TimeLoad Port OCT inspection 4-Aug-2009 Date 10:28 Time

Time zone adjustment between ports Hrs E to WLength of Voyage Days

Estimated LNG Boil-off per day % per dayVessel Design Limits % per day

Bunker Data (Fuel Oil)Bunkers on Closing Last Port 1,337.000 MT

Bunker Survey Date TimeBunkers on Opening Load Port 1452.495 MT

Bunker Survey 3-Jun-2008 Date 07:40 TimeBunkers on Closing Load Port 1385.351 MT

Bunker Survey 5-Jun-2008 Date 15:00 TimeBunkers Received intransit 3713.910 MT

Average Daily Consumption Rates:At Load 20.000 MT

At Discharge 20.000 MTAt Sea 200.000 MT

At Anchorage: 20.000 MTQuality

Methane CH4 90.2400 % mol

Ethane C2H6 5.9500 % mol

Propane C3H8 2.2400 % mol

i-Butane i-C4H10 0.6900 % mol

n-Butane n-C4H10 0.5800 % mol

i-Pentane i-C5H12 0.0200 % mol

n-Pentane n-C5H12 0.0000 % mol

n-Hexane n-C6H14 0.0000 % mol

Nitrogen N2 0.2800 % mol

Carbon Dioxide CO2 0.0000 % molImpurities

Mercury ng/Nm3Mercaptans mg/Nm3Mercaptans ppm

Hydrogen Sulphide mg/Nm3Hydrogen Sulphide ppm

Total Sulphur mg/Nm3Total Sulphur ppm

Time log Summary AdditionsOCT Inspection Completed 4-Aug-2009 Date 10:28 Time

CCT Inspection Completed 5-Aug-2009 Date 04:17 Time



B P C E R T I F I C A T E O F L O A D I N G

VESSEL : SK SPLENDOR DATE : 15-Apr-2008


1. QUALITY

COMPONENTS IMPURITIES

METHANE 90.24 Mol % NITROGEN 0.28 Mol %

ETHANE 5.95 Mol % CARBON DIOXIDE 0 Mol %

PROPANE 2.24 Mol % OXYGEN 0 Mol %

ISO BUTANE 0.69 Mol % MERCURY N/A ng / Nm3

N-BUTANE 0.58 Mol % MERCAPTAN N/A mg / Nm3

ISO PENTANE 0.02 Mol % HYDROGEN SULFIDE N/A mg / Nm3

N-PENTANE 0 Mol % CARBONYL SULFIDE N/A mg / Nm3

N-HEXANE 0 Mol % TOTAL SULFUR N/A mg / Nm3

AVERAGE TEMPERATURE OF LIQUID AFTER LOADING -160.2 °C

AVERAGE TEMPERATURE OF VAPOR BEFORE LOADING -128.5 °C

AVERAGE ABSOLUTE PRESSURE BEFORE LOADING 1166 mbar


GROSS CALORIFIC VALUE (MASS) 54.4361 MJ / kg

GROSS CALORIFIC VALUE (VOLUME) 1115 BTU / SCF

WOBBE INDEX (VOLUME) 1411 BTU / SCF


2. QUANTITY

VESSEL VOLUME ON ARRIVAL ( OPENING CUSTODY TRANSFER ) 404.978 CUBIC METERS

VESSEL VOLUME ON DEPARTURE ( CLOSING CUSTODY TRANSFER ) 136,292.944 CUBIC METERS

VESSEL VOLUME DELIVERED ( ROUNDED AS PER THE S.P.A. ) 135,888.000 CUBIC METERS

ADJUSTED MASS DELIVERED 62,172.077 METRIC TONS





QUANTITY FOR GAS-UP 0 0 0

QUANTITY FOR COOL DOWN 0 0 0


3. STATEMENT OF FACTS

DATE HOUR EVENT

13-Apr-2008 11:30 END OF SEA PASSAGE

13-Apr-2008 11:30 NOTICE OF READINESS TENDERED

14-Apr-2008 02:36 PILOT ON BOARD

14-Apr-2008 06:42 VESSEL ALL FAST

14-Apr-2008 06:42 NOTICE OF READINESS ACCEPTED

14-Apr-2008 08:12 CARGO ARMS CONNECTED

14-Apr-2008 09:00 COMMENCED CARGO OPERATIONS

15-Apr-2008 00:18 COMPLETED CARGO OPERATIONS

15-Apr-2008 00:48 CARGO ARMS DISCONNECTED

15-Apr-2008 02:54 VESSEL DEPARTURE




CSR 3 - BP Certificate of Loading LNG-LD-009H1 (07-AUG-09) - 14

kg / m3

LOADING REPORT CAPTIONINPUT CELLS

TELEX TREATMENT DATE : 5/5/2009 DD/MM/YYYY FORMS AAAAAATO BE ADJUSTED (drop-down list)

TANKER NAME : SK SPLENDOR CAPITAL (depending on operation, reference temperature...)

PORT : SUR, OMAN (NO COUNTRY ex : Idku)

CARGO REFERENCE NUMBER : OF039/09-SL100-KG CAPITAL

1.QUALITY:---------- VOLUMETRIC/METERING REFERENCE TEMPERATURE (for calculations) : 60

COMBUSTION REFERENCE TEMPERATURE (for calculations) : 60LNG CARGO COMPOSITION REFERENCE PRESSURE : 14.696 PSIAMESURED ON OPERATION

COMPONENTS UNIT

METHANE : 90.24 %ETHANE : 5.95 %

PROPANE : 2.24 %ISOBUTANE : 0.69 %

NORMAL BUTANE : 0.58 %ISOPENTANE : 0.02 %

NORMAL PENTANE : 0 %NORMAL HEXANE : 0 %

NITROGEN : 0.28 %CARBON DIOXIDE : 0 %

MERCURY : ng / Nm3HYDROGEN SULFIDE : mg / Nm3

MERCAPTAN : mg / Nm3TOTAL SULFUR : mg / Nm3

LNG DENSITY (@ observed Temp) : 459.080 KG/M3 (GNL)AVERAGE TEMPERATURE OF LNG DELIVERED : -160.2 °C

LNG GROSS CALORIFIC VALUE (MASS) : 54.4361 MJ / kg (@15°C)VAPOUR AVERAGE PRESSURE : 1166 mbar

VAPOUR GROSS CALORIFIC VALUE (VOLUME) : 1115 BTU / SCF (@60/60°F)VAPOUR AVERAGE TEMPERATURE : -128.5 °C

WOBBE INDEX : 1411 BTU / SCF (@60/60°F)

2.QUANTITY :----------INSPECTOR FIGURES ( WITHOUT COOLING DOWN AND GASSING UP IF ANY)

UNIT COOLING DOWN + GASSING UP QUANTITY IF APPLICABLEVOLUME BEFORE OPERATION : 404.978 M3 (GNL) UNIT

VOLUME AFTER OPERATION : 136,292.944 M3 (GNL) VOLUME : 0.000 M3 (GNL)TOTAL VOLUME DELIVERED : 135,888.000 M3 (GNL) ENERGY USED : 0 MMBTU (@60°F)

GROSS MASS DELIVERED : 62,172,077 KG (COOLING DOWN + GASSING UP)NET MASS DELIVERED (less gas return & ship consumption) : 62,172,077 KG

TOTAL ENERGY DELIVERED (less gas return & ship consumption) : 3,207,380 MMBTU (@60°F)

ENERGY OF GAS RETURN : 11,130 MMBTU (@60°F)

3.STATEMENT OF FACTS :------------------

END OF SEA PASSAGE : 5/5/2009 2:30 DD/MM/YY HH:MMARRIVAL AT ANCHOR AREA : 5/5/2009 2:30 DD/MM/YY HH:MM

PILOT ON BOARD : 5/5/2009 2:30 DD/MM/YY HH:MMBERTHING COMPLETED : 5/5/2009 2:30 DD/MM/YY HH:MM

NOTICE OF READINESS TENDERED : 5/5/2009 2:30 DD/MM/YY HH:MMNOTICE OF READINESS RECEIVED : 5/5/2009 2:30 DD/MM/YY HH:MM

OPEN CUSTODY TRANSFER COMPLETED : 5/5/2009 2:30 DD/MM/YY HH:MMOPERATION COMMENCED (1rst pump) : 5/5/2009 2:30 DD/MM/YY HH:MM

OPERATION COMPLETED : 5/5/2009 2:30 DD/MM/YY HH:MMCLOSING CUSTODY TRANSFER COMPLETED : 5/5/2009 2:30 DD/MM/YY HH:MM

DOCUMENTS ON BOARD : 5/5/2009 2:30 DD/MM/YY HH:MMVESSEL DEPARTURE : 5/5/2009 2:30 DD/MM/YY HH:MM

ETA NEXT PORT : 5/5/2009 2:30 DD/MM/YY HH:MMNEXT PORT CALL : BONNY ISLAND, NIGERIA (NO COUNTRY ex : MONTOIR)

4.OBSERVATIONS :-----------Delay before berthing / Delay before loading / Stops during loading / etc...



S A I L I N G S U M M A R Y R E P O R T

VESSEL : SK SPLENDOR DATE : 12-May-2009


1. TIME LOG

DATE HOUR EVENT

11-May-2009 06:30 VESSEL END OF SEA PASSAGE

11-May-2009 07:00 PILOT ON BOARD

11-May-2009 08:15 FIRST LINE ASHORE

11-May-2009 08:45 NOTICE OF READINESS TENDERED

11-May-2009 08:45 VESSEL ALL FAST

11-May-2009 09:00 COMMENCED PRE-LOAD KEY / SAFETY MEETING BETWEEN VESSEL & TERMINAL

11-May-2009 09:05 COMMENCED CONNECTION OF CARGO & VAPOR ARMS

11-May-2009 09:10 NOTICE OF READINESS ACCEPTED

11-May-2009 09:35 COMPLETED CONNECTION OF CARGO & VAPOR ARMS

11-May-2009 10:40 COMPLETED PRE-LOAD KEY / SAFETY MEETING BETWEEN VESSEL & TERMINAL

11-May-2009 10:45 COMPLETED TESTING OF E.S.D. (WARM CONDITION)

11-May-2009 10:54 COMPLETED OPENING CUSTODY TRANSFER INSPECTION

11-May-2009 11:05 COMPLETED OPENING CUSTODY TRANSFER CALCULATIONS

11-May-2009 12:12 COMMENCED COOL DOWN OPERATIONS OF CARGO ARMS & SHIP'S TANKS

11-May-2009 20:13 COMPLETED COOL DOWN OPERATIONS OF CARGO ARMS & SHIP'S TANKS

11-May-2009 20:23 COMPLETED TESTING OF E.S.D. (COLD CONDITION)

11-May-2009 20:33 COMMENCED LOADING OF CARGO

11-May-2009 22:20 VESSEL REACHED FULL LOADING RATE

12-May-2009 09:20 VESSEL COMMENCED REDUCTION OF LOADING RATE

12-May-2009 09:46 COMPLETED LOADING OF CARGO

12-May-2009 10:53 COMPLETED CLOSING CUSTODY TRANSFER INSPECTION

12-May-2009 11:10 COMPLETED CLOSING CUSTODY TRANSFER CALCULATIONS

12-May-2009 11:54 COMPLETED DISCONNECTION OF CARGO & VAPOR ARMS

12-May-2009 13:15 DOCUMENTS ON BOARD

12-May-2009 13:45 DOCUMENTATION COMPLETED

2. QUALITY

COMPONENTS METHOD SPA SPECIFICATIONS RESULTS UNITS

METHANE GPA 2261 NOT LESS THAN 85 % 90.24 mol %

ETHANE GPA 2261 NOT MORE THAN 8 % 5.95 mol %

PROPANE GPA 2261 NOT MORE THAN 3 % 2.24 mol %

ISO BUTANE GPA 2261

NOT MORE THAN 2 %

0.69 mol %

N-BUTANE GPA 2261 0.58 mol %

ISO PENTANE GPA 2261 0.02 mol %

N-PENTANE & HEAVIER GPA 2261 0.00 mol %

NITROGEN GPA 2261 NOT MORE THAN 1 % 0.28 mol %

CARBON DIOXIDE GPA 2261 0.00 mol %

HYDROGEN SULFIDE NOT MORE THAN 5 mg / Nm3 N/A mg / Nm3

TOTAL SULFUR NOT MORE THAN 30 mg / Nm3 N/A mg / Nm3

3. QUANTITY

LIQUID LNG VOLUME ON BOARD BEFORE LOADING : 404.978 CUBIC METERS

LIQUID LNG VOLUME ON BOARD AFTER LOADING : 136,292.944 CUBIC METERS

LIQUID LNG VOLUME LOADED : 135,888.000 CUBIC METERS

LNG DENSITY AT -160.2 °C : 459.080

GROSS CALORIFIC VALUE (VOLUME) : 1115 BTU / SCF

AVERAGE TEMPERATURE OF LIQUID AFTER LOADING : -160.2 °C

MASS DELIVERED (Liquid Delivered - Vapor Return + Consumed as Fuel) : 62,172.077 METRIC TONS

QUANTITY DELIVERED (Liquid Delivered - Vapor Return + Consumed as Fuel) : 3,207,380 MMBTU

GAS-UP QUANTITY : 0 MMBTU

COOL DOWN QUANTITY : 0 MMBTU

BEST REGARDS

kg / m3

PONNAPPA CHOKIRACSR 5 - Chubu Sailing Summary Report LNG-LD-009H1 (07-AUG-09) - 14

lng-ld-009h1 sur09134 sk splendor 050809

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