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LPG cargo measurement and calculation procedure
Liquefied gas cargoes are measured and calculated in a similar manner to that of other bulk liquid
cargoes such as crude oils and petroleum products. However, as liquefied gases are carried as boiling
liquids in a closed containment system the quantity of vapour has also to be measured when
calculating the total quantity onboard.
It is common practice for gas tankers on a regular trade to retain onboard a quantity of liquid (heel) in
order to keep tanks cool on the ballast passage. In this way the vessel arrives at the load port ready to
commence loading with no cool down time necessary. At the load port the new cargo is added to the
heel. Equally if the ship has arrived with uncooled tanks a quantity is usually put onboard for tank cool
down purposes. It is therefore extremely important that a full survey of all tanks is carried out before
and after every operation.
Cargo being loaded may arrive at the manifold at various temperatures during loading. This may be
due to cargo being taken from different shore tanks or the initial cooling of ship/shore lines. It is
possible that because of this some stratification in the vessel’s tanks can occur.
It is very important
therefore that temperatures are taken at all available points in order to accurately assess the actual
average liquid temperature. Ships temperature sensors are usually provided at a number of different
levels. This is equally important for vapour temperature where temperatures in the tank dome are
usually higher than that of the vapour near the surface of the liquid. The positions of temperature
probes must be accurately known in order that only those actually submerged in the liquid are used for
liquid temperature and similarly for vapour temperature.
Density is by definition measured in vacuum at 15°C.
Density x volume M3 (at 15°C gives metric tonnes in vacuum).
The measurement of liquid gas density requires laboratory facilities or equipment not available on
ships. Modern terminals usually calculate this form from an analysis of liquid composition obtained
from a gas liquid chromatograph. The results of this are provided to the ship in order to carry out the
It is necessary to correct the density for the actual observed temperature of the cargo. For specialised
chemical gases, the storage facility normally provides their own density table for the cargo showing the
density for a range of temperatures. Some ports provide the density at a standard temperature of
60°F or 15°C. This has to be corrected to the density for the observed cargo temperature.
Density can be quoted as either being in air or in vacuum.
For a density quoted in vacuum subtract 0.0011 to obtain the density in air, i.e. 0.5074 in vacuum
corresponds to a density of 0.5063 in air.
Cargo's quantities worked out in vacuum are always heavier than those worked out in air. Liquid gas
quantification is more commonly expressed in terms of weight in air and indeed this is a requirement of
most customs authorities. It is extremely important that when a density is provided to the vessel it is
ascertained whether the density is in air or vacuum.
The liquid level is read direct from the tank level gauge on the tank dome. The remote readout must
not be used for cargo calculations. It is necessary to apply corrections to this figure before entering
the tables. These corrections are for tape shrinkage and float immersion. The float gauge tape passes
through the cold vapour space and depending on the space temperature contracts thus indicating a
higher liquid level than actually present. Float immersion will depend on the density of the cargo and
this will usually be different from the manufacturer’s initial determination. A small correction is
necessary for both these items to obtain the correct gauge reading before entering the tables.
All ships are provided with a calibration table for each tank by means of which the tank’s liquid (and
vapour) volume can be calculated from the measurement of the liquid level. These tables are obtained
from careful measurement of the tanks during the ship’s construction. These tables normally refer to
an upright vessel with no list. Corrections are therefore necessary for trim and list and these will be
included with the tank calibration tables. Instruction for use will be included with the tables.
The cargo tank volume will have been calculated at ambient temperature and the tables calculated for
a standard temperature of say 20°C. Cold cargo temperature will result in tank shrinkage and a
reduction in volume. A correction therefore is necessary and this is normally expressed as the Tank
The volume of vapour is found by subtracting the volume of liquid from the tanks 100% capacity. This is at
the calibration temperature for the tank before the Volume Correction Factor has been applied. It is
necessary to apply a Volume Correction Factor (tank shrinkage factor) to this figure and this correction is
obtained using the average vapour temperature.
On completion of measurement calculation of the total cargo quantity can be carried out.
There is no internationally agreed standard for gas cargo calculations and procedures can vary
particularly with the chemical gases.
In the absence of any instructions concerning calculations the following procedure using the standard
temperature of 15°C which is widely used should be followed.
The co-mingling operation can also cause “apparent” losses, as the density of the mixture will not be a
mathematical average of the densities of the components as the molecular component is different.
Calculation of cargo densities in such circumstances is discussed in Appendices 3 & 4 of the SIGTTO
publication “Quantity Calculations for LPG and Chemical Gases”. Copies are available direct from
Calculation procedure (Typical)
- Determine by measurement the average liquid and vapour space temperature (degrees C) and
the vapour space pressure (barg or mbarg).
- Read the tank liquid level and calculate the liquid volume (V1) at tank conditions using the
ship’s calibration tables for that tank and making all necessary corrections for temperatures, list and
- Determine the liquid density noting the temperature at which it is determined and using ASTM*
table 53 convert this to liquid density at 15°C.
- Using the liquid density at 15°C and the measured average liquid temperature, enter ASTM*
table 54 to derive the appropriate volume correction factor to convert to the volume at 15°C.
- Calculate the liquid mass. Volume x Density.
- Calculate the vapour volume at tank conditions by subtracting the apparent liquid volume
(liquid quantity before applying tank shrinkage factor) from the tank total volume.
N.B. ASTM tables 53 & 54 have been revised for densities in the range 610.0 to 1076.0
kg/m3 however below this range covering LPG no revision has been carried out and ASTM-IP tables 53
& 54 are to be used.
- Using the average vapour temperature correct the apparent volume of vapour for tank
- Determine the vapour density at vapour space conditions using the following formula.
Density of Vapour = Ts x Pv x Mm Kg/m³/
Tv x Ps x I
Where Ts is standard temperature of 288 K
Tv is average temperature of vapour in K
Pv is absolute pressure of vapour space in bars
Ps is standard pressure of 1.013 bar
Mm is molecular mass of vapour mixture in Kg/Kmol (sometimes called molecular weight)
I is ideal gaseous molar volume at standard temperature (288K) and standard pressure (1.013
bar). This is 23.645 m³ / Kmo1).
- Calculate the vapour mass by multiplying vapour volume and vapour density.
- Add the liquid mass and the vapour mass to give the total cargo mass in the tank.
- Convert the total to weight in air.
Below is more guideline for safe cargo operation on board gas carriers
Liquefied gas cargo vapour characteristics
Liquefied gas cargo - low temperature effects
Liquefied gas carrier -monitoring cargo pressure
Cargo emergency shutdown requirement for liquefied gas carrier
Gas analyzing equipment
Custody Transfer Measurement (CTM) System
Use of cargo as fuel -Cargo conditioning, reliquefaction and boil-off control for LNG carriers
- Various type LPG tanker - Design characteristics and usability
- LPG tanker cargo work equipments & product line system
- Carriage of LPG cargo at sea & safety guideline
- LPG reliquefaction plant safety guideline
- Preparations for LPG cargo discharging, pumping & stripping guideline
- Preparations for loading compatible cargo onboard LPG tanker
- Preparation for changing different grade cargo or drydocking -LPG tanker guideline
- Cargo tank inerting prior to gassing up - LPG tanker procedure
- LPG cargo tank purging & safety guideline
- LPG cargo tank cooling safety procedure
- LPG cargo loading special guideline
- Tackling fire onboard LNG & LPG ships
- Detail guideline for Ballast operation at sea by LPG carrier
- Handling cargo related documents for LPG carrier
- Cargo sampling procedure for liquefied gas cargo
- Cargo measurement and calculation guideline for LPG carriers
- Handling Propylene oxide, Ethylene oxide mixtures
- Special characteristics of Vinyl Chloride Monomer & Butadiene
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