lng custody transfer. lng value chain... · 2019-05-20 · 11 lng custody transfer: inspector ghv...
TRANSCRIPT
LNG Custody Transfer: LNG value chain and trade
Hans Buytaert - SGS Belgium
Klaipeda: 16/05/2019
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SGS IS THE WORLD’S LEADING INSPECTION, VERIFICATION, TESTING AND CERTIFICATION COMPANY
Version: April 2018
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SGS ORGANISATIONAL
GROWTH
HISTORY
SGS GLOBAL EXPANSION
1913 Leader in grain
inspection
(21 million tons)
1913 Pan-Europe
1878 Rouen,
France
1878 Agriculture and Food
1915 Headquarters moved
from Paris to Geneva
1919 Company
named SGS
1955 Africa
Asia
1939 South
America
1981 Listed on the Swiss
Stock Exchange
1878
ESTABLISHED
ONE BRAND SERVING
THE VALUE CHAIN
GLOBALLY AND
ACROSS INDUSTRIES TODAY
1955
1990 Consumer Testing
1980 Life Sciences
Automotive
Certification
SGS INDUSTRY EXPANSION
1981 Expands to
ex-USSR
1970 Environmental
1960 Oil and Gas
Chemical
Public Sector
1955 Industrial Manufacturing
1939 Mining
2001 SGS rebranded
1946 Inspection
of European
imports
2017
CHF 6.3 BILLION total revenue
2 400 offices and laboratories
95 000 employees
1985
CHF 1.5 BILLION total revenue
1981
CHF 780 MILLION total revenue
180 offices and laboratories
10 675 employees
1913
45 offices and laboratories
1928 21 further
global countries
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INSPECTION VERIFICATION TESTING CERTIFICATION CONSULTANCY
TRAINING OUTSOURCING
GLOBAL SERVICES TAILORED
TO INDIVIDUAL INDUSTRIES
5
Nº1
WORLD LEADER
> 97 000
EMPLOYEES
2 400
OFFICES AND LABORATORIES
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GLOBAL INDUSTRIES
GLOBAL SERVICE LOCAL EXPERTISE
AT A GLANCE
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LNG CUSTODY TRANSFER
LNG Custody Transfer: Custody Transfer involves the
physical and commercial transfer of LNG from one owner
to another
Value transaction: USD = P x Q
P = as per agreement
Q = as per agreement
GENERAL INTRODUCTION
8
LNG AGREEMENT
9
LNG AGREEMENT
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LNG CUSTODY TRANSFER: INSPECTOR
Voyage #:
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Page 1
SGS
LIQUEFIED NATURAL GAS
FINAL DISCHARGE REPORT
Phone Number : phone
SGS Office :
:
VOYAGE #
TERMINAL / PORT
2-3
4
5
SUMMARY OF FINDINGS
LNG QUANTITY REPORT
CLOSING CUSTODY TRANSFER REPORT - PRIMARY
CLOSING CUSTODY TRANSFER REPORT - SECONDARY
:
DATES
SGS FILE #
:
Shell
REFERENCE #
DATES
SGS FILE #
TERMINAL / PORT
REFERENCE #
:
:
:
CLIENTS
VESSEL NAME Vessel
FUEL OIL BUNKER REPORT
BOG CONSUMPTION
PAGEDOCUMENTS ENCLOSED
CERTIFICATE OF ANALYSIS
OPENING CUSTODY TRANSFER REPORT - PRIMARY
OPENING CUSTODY TRANSFER REPORT - SECONDARY 7
8
9
Date
14
15
12
13
11
date
“Unless otherw ise agreed, all orders and documents are executed and issued in accordance w ith our General Conditions. Upon
simple request the conditions w ill again be sent to you. Attention is draw n to the limitation of liability, indemnification and
jurisdiction issues defined therein.
Any holder of this document is advised that information contained hereon reflects SGS’ f indings at the time of its intervention
only and w ithin the limits of client’s instructions, if any. SGS’ sole responsibility is to its Client and this document does not
exonerate parties to a transaction from exercising all their rights and obligations under the transaction documents. Any
unauthorized alteration, forgery or falsif ication of the content or appearance of this document is unlaw ful and offenders may be
prosecuted to the fullest extent of the law . “
InspectorAdress # 3
Adress # 2
SGS off ice
Adress # 1
DIESEL OIL BUNKER REPORT
GENERAL NOTES ON SHORE OPERATIONS
GENERAL NOTES ON VESSEL OPERATIONS
SUMMARY OF FINDINGS
10
11
LNG CUSTODY TRANSFER: INSPECTOR
GHV (Volume) ideal gas @ 15/15 °C, 1013.25 mbar
2 966 847
10 769
527
2 955 551
MMBTU
MMBTU
MMBTU
VAPOR DISPLACED (Qr) @ 15 °C
NET ENERGY DELIVERED @ 15 °C
m³
MJ/kg
38.527 MJ/m³
136 551.759
55.358
4 617.007
kg/m³
131 935
-159.8
428.58
MMBTU
BOG CONSUMPTION (Qf) @ 15 °C
LIQUID TEMPERATURE BEFORE DISCHARGE
VESSEL C.C.T. VOLUME AFTER DISCHARGE
DENSITY @ -159,8 °C
VESSEL O.C.T. VOLUME BEFORE DISCHARGE
GHV (mass) @ 15 °C
GROSS ENERGY DELIVERED @ 15 °C
LOAD PORT INFORMATION
Vessel
SGS File # : SGS FILE #
DISCHARGE PORT INFORMATION
m³
LOAD PORT DATES :
m³140 355.699
BILL OF LADING VOLUME :
LOAD PORT C.C.T. VOLUME :
m³
Terminal / Port :
Vessel Name :
SUMMARY OF FINDINGS
SGS
Phone Number : phone
TERMINAL / PORT :
Date
Clients : ShellTERMINAL / PORT
Reference :
SGS Office :
Voyage :
Page
Date :
TERMINAL / PORT :
°C
m³139 748.760
Voyage #
2
REFERENCE #
DATES
VESSEL VOLUME DELIVERED (LIQUID)
EQUIVALENT NET LNG MASS DELIVERED* 56 329.420 Mton
* Calculated as per ISO 13398
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LNG CUSTODY TRANSFER: #SIZE
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LNG CUSTODY TRANSFER: LARGE SCALE
Quantity (LNG vessel)
Quality (terminal/FSRU)
Calculations
GHV (Volume) ideal gas @ 15/15 °C, 1013.25 mbar
2 966 847
10 769
527
2 955 551
MMBTU
MMBTU
MMBTU
VAPOR DISPLACED (Qr) @ 15 °C
NET ENERGY DELIVERED @ 15 °C
m³
MJ/kg
38.527 MJ/m³
136 551.759
55.358
4 617.007
kg/m³
131 935
-159.8
428.58
MMBTU
BOG CONSUMPTION (Qf) @ 15 °C
LIQUID TEMPERATURE BEFORE DISCHARGE
VESSEL C.C.T. VOLUME AFTER DISCHARGE
DENSITY @ -159,8 °C
VESSEL O.C.T. VOLUME BEFORE DISCHARGE
GHV (mass) @ 15 °C
GROSS ENERGY DELIVERED @ 15 °C
LOAD PORT INFORMATION
Vessel
SGS File # : SGS FILE #
DISCHARGE PORT INFORMATION
m³
LOAD PORT DATES :
m³140 355.699
BILL OF LADING VOLUME :
LOAD PORT C.C.T. VOLUME :
m³
Terminal / Port :
Vessel Name :
SUMMARY OF FINDINGS
SGS
Phone Number : phone
TERMINAL / PORT :
Date
Clients : ShellTERMINAL / PORT
Reference :
SGS Office :
Voyage :
Page
Date :
TERMINAL / PORT :
°C
m³139 748.760
Voyage #
2
REFERENCE #
DATES
VESSEL VOLUME DELIVERED (LIQUID)
EQUIVALENT NET LNG MASS DELIVERED* 56 329.420 Mton
* Calculated as per ISO 13398
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LNG CUSTODY TRANSFER: LARGE SCALE
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LNG CUSTODY TRANSFER: LARGE SCALE
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LNG CUSTODY TRANSFER: LARGE SCALE
Quantity (LNG vessel)
Volume
• Level
• Trim/list
• Tank capacity table
Temperature
Pressure
Gas flow meters
Quality (terminal/FSRU)
Sampling
Analysis
Calculations
#calculation methods
Cool Down – Gas up
QUANTITY
- Static
- Dynamic
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LNG CUSTODY TRANSFER: QUANTITY STATIC
Volume
Level
Trim/list
Temperature (pressure)
Tank capacity table
Mass
Weighbridge
Load Cell
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LNG CUSTODY TRANSFER: QUANTITY STATIC
Volume:
LNG Large scale
LNG bunkering vessel
Mass
Road tanker
container
A comparison of static and dynamic mass measurement methods of LNG utilizing
weighbridge and coriolis mass flow meters
Tore Mortensen and Henning Kolbjørnsen, Justervesenet, Fetveien 99, N-2007 Kjeller, NORWAY
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LNG CUSTODY TRANSFER: QUANTITY STATIC
Kongsberg
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LNG CUSTODY TRANSFER: QUANTITY
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QUANTITY CHALLENGES
Only 1 set of measurements
Depend on the LNG vessel, other party
Static not always feasable on different scale
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LNG CUSTODY TRANSFER: QUANTITY DYNAMIC
Mass Coriolis
Ultrasonic
(Orifice)
(Turbine)
QUALITY
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LNG QUALITY: GLOBAL OVERVIEW
Based on quality LNG (re)loaded last 3 year
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LNG SAMPLING
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LNG CUSTODY TRANSFER: QUALITY - SAMPLING
ISO 8943
Phase envelope
Operational circumstances
Pressure
Stable flow
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LNG CUSTODY TRANSFER: QUALITY - ANALYSIS
ISO 6974 – ASTM D 1945 – GPA 2261
Calibration – Validation
Repeatability – Reproducability
ISO 10723
Proficiency testing/correlation test
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LNG CUSTODY TRANSFER: QUALITY - ANALYSIS
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GAS ANALYSIS: ROUND ROBIN CASE STUDY
3.280.000
3.300.000
3.320.000
3.340.000
3.360.000
3.380.000
3.400.000
3.420.000
3.440.000
3.460.000
3.480.000
0 5 10 15 20 25 30 35 40
Lab N°
En
erg
y [
MM
BT
U]
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QUALITY CHALLENGES
LNG quality change
ageing
Influence Heel
Quality determination onboard
Specifications (methane number)
Quality loaded vs quality onboard
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MODEL HISTORICAL DATA
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MODEL HISTORICAL DATA
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Vessel:
Port: Discharge Bunkering Bunkering Discharge
OCT date/time: date date date date date date
OCT volume (m³): 1 330.891 770.806 Yes 3 567.889 1 596.170 Yes 3 538.344 1 475.000
OCT Temperature (°C): -158.7 Combined Tk 1 & Tk 2 -157.6 -158.2 -158.1 -157.9 -158.1
CCT date/time: date date date date date date date
CCT volume (m³): 1 410.435 569.883 967.321 3 655.787 1 684.544 3 684.937 1 591.711
Tliq CCT (°C): -158.3 -158.6 -158.6 -157.2 -158.2 -158.0 -158.1
Discharge Port Bunkering 1 Combined Tk 1 & Tk 2 Load Port Heel Loaded Load port OBQ Bunkering 2 Load Port Heel Loaded Load port OBQ Bunkering 3 Dsicharge
Methane 92.3442 91.9562 92.0925 90.6583 93.0332 92.5253 92.3820 92.0099 93.6074 92.9146 92.6815 92.1563
Ethane 7.3184 7.7408 7.5948 9.0089 6.7773 7.2545 7.4301 7.8282 4.9272 6.1855 6.4352 6.9222
Propane 0.2037 0.2155 0.2114 0.2510 0.0734 0.1114 0.1141 0.1202 0.8581 0.5380 0.5598 0.6024
Iso Butane 0.0335 0.0354 0.0347 0.0412 0.0057 0.0133 0.0136 0.0143 0.2411 0.1427 0.1485 0.1598
N-Butane 0.0319 0.0338 0.0331 0.0393 0.0053 0.0126 0.0129 0.0136 0.2234 0.1324 0.1378 0.1483
Iso Pentane 0.0005 0.0005 0.0005 0.0006 0.0003 0.0004 0.0004 0.0004 0.0083 0.0049 0.0051 0.0055
N-Pentane 0.0002 0.0002 0.0002 0.0002 0.0001 0.0001 0.0001 0.0001 0.0000 0.0000 0.0000 0.0000
N-Hexane 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
Nitrogen 0.0676 0.0176 0.0328 0.0005 0.1047 0.0824 0.0468 0.0133 0.1345 0.0819 0.0321 0.0055
Oxygen 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
Carbon Dioxide 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
Total 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000
GHV Volume * [Btu/scf] 1069.5 1073.5 1072.1 1084.0 1061.8 1066.6 1068.3 1071.8 1069.7 1070.6 1073.6 1078.7
Load
Blend
Vessel Tank 1
Load
Blend
Bunkering
Vessel:
Port: Discharge Bunkering Bunkering Discharge
OCT date/time: date date date date date date
OCT volume (m³): 1 390.033 30.584 Yes 3 504.488 3 361.696 Yes 3 565.489 3 470.000
OCT Temperature (°C): -158.7 Combined Tk 1 & Tk 2 -156.6 -158.2 -158.1 -157.7 -157.7
CCT date/time: date date date date date date date
CCT volume (m³): 1 402.774 397.438 967.321 3 675.623 3 491.276 3 681.042 3 556.638
Tliq CCT (°C): -158.3 -158.5 -158.6 -157.2 -158.2 -158.1 -157.7
Discharge Port Bunkering 1 Combined Tk 1 & Tk 2 Load Port Heel Loaded Load port OBQ Bunkering 2 Load Port Heel Loaded Load port OBQ Bunkering 3 Discharge
Methane 92.3442 92.2883 92.0925 90.6583 93.0332 93.0132 92.7559 92.5052 93.6074 92.6009 92.3799 92.1985
Ethane 7.3184 7.3848 7.5948 9.0089 6.7773 6.7961 7.1183 7.3860 4.9272 7.1724 7.3999 7.5814
Propane 0.2037 0.2056 0.2114 0.2510 0.0734 0.0749 0.0785 0.0815 0.8581 0.1490 0.1538 0.1576
Iso Butane 0.0335 0.0338 0.0347 0.0412 0.0057 0.0060 0.0063 0.0065 0.2411 0.0269 0.0278 0.0285
N-Butane 0.0319 0.0322 0.0331 0.0393 0.0053 0.0056 0.0059 0.0061 0.2234 0.0250 0.0258 0.0264
Iso Pentane 0.0005 0.0005 0.0005 0.0006 0.0003 0.0003 0.0003 0.0003 0.0083 0.0010 0.0010 0.0010
N-Pentane 0.0002 0.0002 0.0002 0.0002 0.0001 0.0001 0.0001 0.0001 0.0000 0.0001 0.0001 0.0001
N-Hexane 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
Nitrogen 0.0676 0.0546 0.0328 0.0005 0.1047 0.1038 0.0347 0.0143 0.1345 0.0247 0.0117 0.0065
Oxygen 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
Carbon Dioxide 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
Total 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000 100.0000
GHV Volume * [Btu/scf] 1069.5 1070.2 1072.1 1084.0 1061.8 1062.0 1065.2 1067.5 1069.7 1067.7 1069.7 1071.2
Bunkering
Vessel Tank 2
Load Load
Blend Blend
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LNG CUSTODY TRANSFER: CALCULATIONS
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ENERGY BALANCE: LNG CONTRACTS
Energy Balance Discharge
Liquid – Vapour Displaced – BOG
Liquid – Vapour Displaced
Energy Balance Loading
Liquid – Vapour Displaced + BOG
Liquid
Liquid + BOG
Liquid – Vapour Displaced
Gas up + Cool Down + Liquid – Vapour Displaced + BOG
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INFLUENCE REFERENCE CONDITIONS
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INFLUENCE REFERENCE CONDITIONS
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GHV VS. NHV
Gross Heating Value
Amount of heat that would be released by the complete combustion with
oxygen of a specified quantity of gas, in such a way that the pressure, p1,
at which the reaction takes place remains constant, and all the products of
combustion are returned to the same specified temperature, t1, as that of
the reactants, all of these products being in the gaseous state except for
water, which is condensed to the liquid state at t1
Gross Heating Value = Higher Heating Value = Superior Heating Value
GHV = HHV = SHV
Net Heating Value
Amount of heat that would be released by the complete combustion with
oxygen of a specified quantity of gas, in such a way that the pressure, p1,
at which the reaction takes place remains constant, and all the products of
combustion are returned to the same specified temperature, t1, as that of
the reactants, all of these products being in the gaseous state.
Net Heating Value = Lower Heating Value = Inferior Heating Value
GHV = HHV = SHV
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GHV VS. NHV
Calculated as per ISO 6976 (2016) for volume of 155 000 m³ @ -159,5 °C, grade middle LNG
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METHANE NUMBER
Methane number is the measure of resistance of fuel gases to
engine knock, as well known as detonation.
Detonation is produced by the auto-ignition of the fuel/air mixture
ahead of the propagating flame, this phenomenon produces some
shock waves that could lead to serious loss of power (efficiency)
and damage to the engine. It is similar to the octane number for
petrol engines. The loss of efficiency could be about 2 %
The MN is used to define the knock resistance of a gaseous fuel in
pure gas and dual fuel engines. MN is a scale based on the
combustion characteristics of methane and hydrogen
Pure methane is assigned as the knock resistant reference fuel with a
methane number of 100.
Pure hydrogen is used as the knock sensitive reference fuel with a
methane number of 0.
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METHANE NUMBER
Different Calculation methods – all with a different outcome
Current Methods
AVL Method: uses correlations based on experimental work to
predict the methane number (only available in commercial software)
The CARB (California Air Resources Board) method based on a
MON (Octane number) approach
ISO 15403 provides an alternative method of calculating MON
MVM method – still under development and is likely to result in a new
ISO standard. The methodology has been accepted by the engine
manufacturer’s group Euromot. The approach is similar to the AVL
method but the equations have been published in EN 16726
• A WG through ISO is set up to bring clarity (and maybe uniformity)
amongst the calculation methods
• ISO TC 28 SC 4 WG 17
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METHANE NUMBER
Hans Buytaert - SGS Belgium
LNG Business Development manager