Showing posts with label LNG. Show all posts
Showing posts with label LNG. Show all posts

Wednesday, October 6, 2010

Do not Under-estimate The Impact of Altitude Change

Many LNG plants are built at the seaside to ease transportation, product loading and unloading. The atmospheric pressure with plant near seaside is 101325 Pa and all facilities are designed to the atmospheric pressure of 101325 Pa. However, if this plant is built in inland at high altitude, atmospheric pressure can seriously affect the design and operation of a LNG plant. Prior to discuss how the design and operation is impacted, lets step back to look at definition of pressure.



Operating pressure is commonly written as gauge pressure e.g. kPag, barg, etc in engineering whilst absolute pressure e.g kPaa, bara, etc. Absolute pressure equal to gauge pressure plus atmospheric pressure.

Example :
5 bar abs = 5 barg + 1.01325 bar = 6.01325 bara

The standard atmosphere pressure is pressure defined as being equal to 101,325 Pa or 101.325 kPa and normally refer to mean sea level (h=0 m). Atmospheric pressure is decreased with altitude (elevation from mean sea level or earth surface) with following relation.

where
Pb = Static pressure (Pa)
Tb = Standard temperature (K)
Lb = Standard temperature lapse rate -0.0065 (K/m) in ISA
h = Height above sea level (meters)
hb = Height at bottom of layer b (meters; e.g., h1 = 11,000 meters)
R = Universal gas constant for air: 8.31432 N.m /(mol.K)
g0 = Gravitational acceleration (9.80665 m/s2)
M = Molar mass of Earth's air (0.0289644 kg/mol)

Altitude = 0 – 11000m, Tb = 288.15 K, Lb = -0.0065 K/m, Pb = 101325 Pa
Altitude =  11000 – 20000m, Tb = 216.65 K, Lb = -1 x 10E-30 K/m, Pb = 22632.1 Pa
Altitude =  20000 – 32000m, Tb = 216.65 K, Lb = 0.001 K/m, Pb = 5474.89 Pa

By inclusion of specific parameters, for altitude = 0 – 11000m, atmospheric pressure is

Example
At altitude of 500m above mean sea level, atmospheric pressure is approximately 95460.84 Pa.
At altitude of 1000m above mean sea level, atmospheric pressure is approximately 89874.57 Pa.

How altitude impacting LNG production rate ?
Let compare LNG production rate change with a plant built at seaside (h = 0) and another LNG plant built at a site with altitude of 1000m. For both plant, LNG store at same gauge pressure (e.g. 50 mbarg), same LNG rundown temperature (e.g. -163 degC), same LNG tank dimension with same in-leak heat (normally higher altitude is with lower ambient temperature, lower in-leak heat is expected. However, the impact is negligible).

LNG from Main Cryogenic Heat Exchanger (MCHE) outlet is set at 50 barg and negative 164.8 degC. A JT valve is letting down pressure to LNG storage tank operating pressure of 50 mbarg. MCHE outlet mass flow set at 50000 kg/h. LNG is pure Methane (C1). Assumed same in-leak heat of 300 kW.

Case : Seaside
Altitude, h = 0m
Atmospheric pressure = 101.325 kPa abs
LNG operating pressure = 50 mbarg = 5 + 101.325 kPa abs = 106.325 kPa abs
From simulation (see below image), BOG flow = 1374 kg/h,
LNG production rate = 48626 kg/h


Case : Inland
Altitude, h = 1000m
Atmospheric pressure = 101325 (1 - 2.25577E-05 x 1000)^5.25588 = 89.8746 kPa abs
LNG operating pressure = 50 mbarg = 5 + 89.8746 kPa abs = 94.8746 kPa abs
From simulation (see below image), BOG flow = 1863 kg/h,
LNG production rate = 48137 kg/h


Same facilities and operating condition, the LNG production in Inland (at 1000m) reduced by 1%.

How altitude impacting Air Compressor / Blower power requirement ?
Air compressor at seaside is sucking air at atmospheric pressure of 101.325 kPa abs. If this air compressor is located at altitude of 1000m, air compressor is sucking air at atmospheric pressure of 89.8746 kPa abs. With same discharge pressure, higher head is expected at high altitude and higher power is required. Normally the head is rather large for air compressor, therefore the additional power may not be so significant. However, it could be significant for an air blower sent air to process with fix pressure. One shall remember, it may have no significant impact to an air blower sucking air from atmosphere and discharging air to atmosphere again.


Concluding Remark
Atmospheric pressure change with altitude and this will have impacts to facilities design. Do not under-estimate this impact.

Wednesday, September 29, 2010

Quick Way to Estimate Insulation for Cold Services

Earlier post "How Boil-Off-Gas (BOG) is Generated" and "Quick Way to Estimate BOG" discussed several ways result Boil-Off-Gas (BOG) generation and simple way to estimate BOG. Heat leak into piping wrapped with Cold insulation is one of the way possibly result significant BOG generation, in particular in large base load plant where product is loaded into ship. Long rundown and loading line from production plant and from storage tank to ship can generate significant BOG. Proper selection and determination of insulation thickness can minimize BOG generation economically.




Key Rule
Rule of thumb for economic heat flux for heat in-leaks range from 25 to 35 W/m2. This is the key rule to derive an economic insulation for cold service whilst minimizing BOG generation.

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Insulation Material & Thermal Conductivity
Common insulation material used in cold services (sometime called cryogenic service in extremely low temperature case e.g. LNG with operating temperature of approximately -162 degC) are typically Polyurethane and Polyisocyanurate Foam (PIR). These insulation material have very low conductivity minimizing heat from ambient entering cold fluid. Typical thermal conductivity for these material is approximately 0.023 W/mK @ 20 degC.

Insulated Piping In-Leak Heat
Estimation of piping in-leak heat from ambient starts with estimation of heat transfer coefficient using Nusselt number which is a function of Prandtle and Reynolds number.

Overall heat transfer cooefficient estimate from Nusselt number :


where Prandtle number
and Reynolds number

Piping in-leak heat can be estimated with following equation

with heat flux

Case study
Piping nominal size = 6"
Piping external diameter = 152.4 mm
Piping length = 100 m
Insulation material = Polyisocyanurate
Insulation thermal conductivity = 0.023 W/mK
Assumed Insulation thickness = 60 mm
Piping external diameter (including insulation) = 152.4 + 2x60 =  272.4mm

Air :
Air Velocity = 5 m/s
Air Thermal Conductivity = 0.029 W/mK
Air specific heat = 1009 J/kgK
Air density = 1.038 kg/m3
Air viscosity = 0.02 cP


Calculation :
Air Prandtle Number = 0.6959

Air Reynolds Number =70687.8
Overall Heat transfer Coefficienct = 18.096 W/m2K
Piping In-leak heat = 2125.72 W
Piping surface area = 85.58 m2
Average heat flux = 24.8 W/mK < 25 W/mK...OK

Similar calculation applied to 1" to 28"
1" - 50mm insulation thickness
2" - 50mm insulation thickness
3" - 60mm insulation thickness
4" - 60mm insulation thickness
6" - 60mm insulation thickness
8" - 70mm insulation thickness
10" - 70mm insulation thickness
12" - 70mm insulation thickness
16" - 70mm insulation thickness
20" - 70mm insulation thickness
24" - 70mm insulation thickness 
28" - 70mm insulation thickness

Sunday, August 29, 2010

Quick Way to Estimate BOG

Earlier post "How Boil-Off-Gas (BOG) is Generated" has discussed several ways can result Boil-Off-Gas generation. They are listed below :
  1. vaporized vapor due to barometric pressure decrease
  2. vaporized vapor due to ambient temperature increase
  3. cryogenic fluid rundown piping
  4. cryogenic fluid circulation / loading line
  5. ship / truck loading arm
  6. cryogenic fluid storage tank
  7. cryogenic fluid rundown pump
  8. cryogenic fluid in-tank pump
  9. flashed non-condensable gasses
  10. negative Joule-Thompson effect
  11. "hot" rundown cryogenic liquid into "cold" cryogenic liquid 
  12. cooling of loading arm
  13. cooling of ship / truck

This post will discuss quick way to estimate BOG flow.

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Atmospheric pressure at sea level is 101.325 kPa abs. Atmospheric pressure is reduced with increase in altitude. For example, at elevation of 1,000 meter, the atmospheric pressure can be as low as 89.81 kPa abs. Cryogenic storage may be designed to operate between 50-70 mbar gauge. If the cryogenic storage tank is at beach (sea level), the operating pressure in the tank is approximately 106.325 - 108.325 kPa abs. If this cryogenic storage is at 1,000 meter, the operating pressure in the tank is approximately 94.81 - 96.81 kPa abs. Lower operating pressure in tank can results higher vaporization and more BOG is generated. Therefore, it is always a good practice to use absolute pressure whenever dealing with cryogenic storage tank. Correct pressure modeling in process simulator is extremely important in finding quantity of BOG generated.

Heat leaks into cryogenic fluid can be via rundown / circulation piping, loading arm & storage tank. Proper selection, installation and maintenance of insulation is one of the key factor in minimizing heat leaks into cryogenic system, hence BOG generation. Besides insulation, other external factors such as wind speed, solar radiation, ambient temperature, sand conductivity and etc, affect heat leak. However, these factors are hard to be managed. Heat leaks into system can be calculated by considering heat conduction, convection and radiation. However, this type calculation involve a lot of uncertainties, assumption and rather complicated. Based on past experiences, an approximate method using vaporization coefficient in determining BOG generation due to heat leaks via storage tank, may be considered during conceptual phase.


Vaporization coefficient (k)  may range from 0.04% to 0.06% for LNG whilst 0.06% to 0.1% for Propane, Butane and LPG. One may take note that above are typical for large storage tank e.g. 160,000m3. Higher k factor should be used for smaller storage. For example, 60,000m3, k of 0.08 - 0.1% may be considered.



Above equation is applicable to storage tank which is low surface area-to-volume ratio. However, piping with very low volume and high surface area may experience higher heat input comparatively. Following equation may be used to estimate BOG generated due to piping.

Average heat flux subject to piping diameter. In general, kp of 25 -35 W/m2 may be considered.

Energy is transferred to pump to move quantity of liquid. Part of the energy will loss due to deficiency. and results BOG generation. Following equation may be considered to estimate BOG generated due to pump deficiency.


Pump efficiency can be range from 55% - 75% for common centrifugal pump.

Cryogenic liquid produced from main plant and transfer to cryogenic liquid storage tank. Inflow liquid will displaced vapor and add-on to BOG generation. Following equation may be used.


Other factors result generation of flashed vapor or BOG generation such as present of non-condensable gasses, negative Joule-Thompson effect and "hot" rundown cryogenic liquid into "cold" cryogenic liquid, will possibly be modeled in process simulator.


Cooling of loading arm and tank in ship / truck may generate substantial amount of vapor initially and reduce as loading arm and tank is cooled. This BOG generation may required dynamic simulation which will not be presented in this post.

Monday, August 23, 2010

How Boil-Off-Gas (BOG) is Generated

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Liquefied Petroleum Gas (LPG) contains mainly Propane (C3) and Butane (i-C4 & n-C4), Liquid Ethylene (C2=) and Liquefied Natural Gas (LNG) contains mainly Methane will evaporate at ambient condition e.g. 20 degC @ 101.325 kPag.

LPG, Liquid Ethylene and LNG can be stored in refrigerated vessel at its bubble point and atmospheric pressure. Their bubble point can be as low as -40, -104 and -162 degC are commonly known as cryogenic temperature and fluid as cryogenic fluid.

Heat leaks into the cryogenic fluid will results vaporization and lead to Boil-Off-Gas (BOG) generation. Other than heat leak, there are other scenarios can lead to BOG generation :
  1. vaporized vapor due to barometric pressure decrease
  2. vaporized vapor due to ambient temperature increase
  3. cryogenic fluid rundown piping
  4. cryogenic fluid circulation / loading line
  5. ship / truck loading arm
  6. cryogenic fluid storage tank
  7. cryogenic fluid rundown pump
  8. cryogenic fluid in-tank pump
  9. flashed non-condensable gasses
  10. negative Joule-Thompson effect
  11. "hot" rundown LNG into "cold" LNG 
  12. cooling of loading arm
  13. cooling of ship / truck



Vaporized vapor due to barometric pressure decrease & ambient temperature increase
Environment pressure and temperature change affects BOG generation. Maximum BOG generation during summer, noon and high elevation (with low barometric pressure). On the other hand, minimum BOG generation during winter, mid-night and near sea side (high barometric pressure). 

Heat leaks into Cryogenic fluid rundown piping, circulation / loading line, ship / truck loading arm & storage tank
Ambient heat leaks cryogenic fluid will be limited by insulation layer. Heat  leaks into subjects to insulation thickness, thermal conductivity, installation quality, etc. Higher insulation thickness, lower thermal conductivity, high installation quality and etc maintain good heat insulation and reduce BOG generation.

Heat generated by rundown pump & in-tank pumpand leaks into Cryogenic fluid
Pumps is required for transferring cryogenic liquid from production plant to storage tank and from storage tank to ship/truck. Pump will absorb power to move cryogenic fluid and any deficiency will generate heat and it will transfer into cryogenic fluid. Pump heat leaks subject to pump capacity, develop head and efficiency. Larger pump, higher head and lower efficiency lead to excess heat generation and leaks into cryogenic fluid. 

Flashing of non-condensable gasses
Present of inert / non-condensable gasses such as nitrogen, carbon monoxide in cryogenic fluid may flash in the storage tank.

Negative Joule-Thompson effect
Another phenomenon is negative Joule Thompson (negative JT) where pressure decrease in rundown line lead to higher temperature. Typical gas is Hydrogen. 

"Hot" rundown into "cold" cryogenic fluid 
Hot cryogenic fluid from one train with hotter temperature which carries heat and rundown into cryogenic  tank with colder temperature can results vaporization.

Cooling of loading arm & tank in ship / truck
Loading arm is heated to ambient temperature when it is unrest for long time. Cryogenic tank in ship / truck is heated by ambient when it is returned with empty tank. All loading arm and tank in ship/truck will needs cooling prior to storage. Large amount of BOG is generated during cooling time.

Coming topic will discuss quick way to estimate BOG rate.

Sunday, August 8, 2010

Process Design of Turboexpander Based Nitrogen Liquefier

Hampson and Linde patented efficient air liquefiers with self-intensive or regenerative cooling of the high pressure air by the colder low pressure expanded air in long lengths of coiled heat exchanger. In this simple way, the complications of cascade precoolers employing liquid ethylene and other liquid cryogens were removed and removal of moving parts at low temperature. The cooling being produced by Joule-Thomson (JT) expansion through a nozzle or valve.




Georges Claude, in 1902 produced a piston expansion engine working at the low temperatures required for the liquefaction of air. The increase in cooling effect over the Joule-Thomson nozzle expansion of the Linde-Hampson designs. The expansion through an expansion valve is an irreversible process. energy is removed from the gas stream by allowing it to do some work in an expansion engine or expander.


Recommended :
The process is based on a suitable modified Claude cycle which minimizes the umber of heat exchangers and also takes care to accommodate the in house developed turbo xpander. The process design is carried out using the standard calculation procedure and is validated by using process simulation software, Aspen Hysys. parametric analysis is carried out to access the role of different component efficiencies in predicting overall system efficiency at the design and off design conditions. In this analysis, the available turbo expander efficiency is considered to evaluate the feasible heat exchanger efficiency in order to optimize the plant efficiency. The thermodynamic parameters (temperature, pressure, pinch point temperature) are evaluated to obtain the optimum mass fraction through turbo expander for maximum liquid yield. This investigation not only gives the analysis of nitrogen liquefier, but also it will act as a basic frame work for any liquefier and helium liquefier in particular as a future mission.

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Sunday, July 11, 2010

PFHE & CWHE Comparison in LNG Plant

Main Cryogenic heat exchanger (MCHE) is one of key equipment in natural gas liquefaction (LNG) plant. MCHE used in liquefaction of natural gas having some special characteristic :
  • Intensive/excessive heat exchange (230 - 400 kW / ton LNG)
  • Complex heat transfer - Heat transfer from one (or several) very high pressure natural gas stream to one or several low pressure refrigerant streams
  • Thermal stress/shock - Very large temperature difference between inlet (40 degC) and outlet temperature (-162 degC)
  • Operate at very low temperature (-162 degC)
  • High heat transfer efficiency - Very low temperature approach (2-3 degC) to maximize heat transfer per unit area
  • Involve phase change and risk of phase separation and proper distribution
  • High risk of leakage and safety related issue
  • High risk of blockage/plugging
  • Lightweight & easy transportation



Two type of compact MCHE widely used in LNG plant. There are Plate-Fin Heat Exchanger and Coil (Spiral) Wound Heat Exchanger. Below images are typical CWHE and PFHE.


CWHE

CWHE is coils/tubes wound in spiral around a mandrel and all coils / tubes are contains within a pressure vessel. Multiple coils/tube in bundle can be flew simultaneously within the pressure vessel.



PFHE

PFHE is corrugated or serrated plate stacking on each and others to creates cross and/or counter flow paths to allow heat transfer of multiple fluids.

Although both type of HE have been widely used, CWHE and PFHE have their own special features and advantages. Below are simple comparison between both CWHE and PFHE.

FeaturesCoil Wound Heat Exchanger (CWHE) Plate-Fin Heat Exchanger (PFHE)
CompactnessCompact Extremely compact
Heat Transfer area (m²/m³) 20 - 300300 - 1400
Flow type in heat transferCross-CounterCross and/or Counter
Flow patternSingle and/or two phasesSingle and/or two phases
Flow streamsSingle or MultipleSingle or Multiple
ConfigurationSingle or multiple coil-in-vessel unitMultiple plate-fin units
Flow path8-12mm tube1-2 mm flow channel
Risk of contaminant built-upLess (smooth tube surface)More (multiple channels / cores increase crevices)
Risk of PluggingLowerHigher
Thermal Stress ResistanceHigher (tube robustness & flexibility)Lower (plate fin inflexible)
Risk of Thermal StressLowerHigher
Gas/Liquid distributionLess mal-distribution (single flow channel)Higher mal-distribution (multiple unit in parallel)
Risk of Thermal ShockLowerHigher (mal-distribution lead to imbalance heat transfer)
SafetyLower (tube contains within pressurized vessel - natural gas leaks to vessel)Higher (natural gas leaks to atmosphere)
AvailabilityHigher (production continue with some tube leaks until next shutdown)Lower (immediate production shutdown when leaks occur)
TransportationReasonable easy (with multiple bundles)Easy (Multiple units)
MaterialAluminum / Stainless Steel / Carbon Steel / Others AlloyAluminum
CostHigherLower


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Friday, December 25, 2009

Educating, Promoting and Awareness creation about LNG


Recommended :
Natural gas is known as one of the world’s cleanest fossil fuel and it burns to form Carbon Dioxide (CO2) and Water (H2O) without  or with minimal smoke subject to composition. Increased world crude demand and price has slowly pushing energy consumers shift from conventional crude based fuel i.e. gasoline, kerosene, etc to natural gas based fuel i.e. liquefied natural gas (LNG), liquefied petroleum gas (LPG), Gas-to-liquid (GTL), etc.

Natural gas conventionally is distributed in gas network. Distribution by gas network will only feasible and cost effective in limited distance i.e. 3000-3500 km. Natural gas may be compressed and stored in very high pressure storage tank. However, high capital cost in high pressure storage tank and high safety risk has driven users look for better transportation and storage option. Liquefying natural gas is one of the option can be most feasible and cost effective. Natural gas in the form of LNG,cooled to minus 160-163 degree Celcius at atmospheric pressure, approximate 600 times smaller than its gaseous state, make it so cost effective in storage and long distance transportation.



In recent net search, there are number of LNG related video clips available in educating, promoting and awareness creation about LNG.




Researchers at Idaho National Laboratory have developed a small-scale Liquid Natural Gas systems to expand the use of clean fuel at an affordable cost.



Pulse of the Port details a proposal for a Liquified Natural Gas Plant at the Port of Long Beach.




One of the largest gas field in the world is located in the sea between Qatar and Iran. Qatar is expanding its fleet of ships to deliver liquified natural gas (LNG) to world market.




BP LNG Tangguh



Terminal operated by Terminale LNG Adriatico Srl, a company owned by Qatar Terminal Limited (45%), ExxonMobil Italiana Gas (45%) and Edison (10%), will be the first offshore facility in the world for unloading, storing and regasifying natural gas. This facility will thus play a key role in increasing Italys energy security and will make the Italian natural gas market more competitive.




The world's largest oil and gas project Sakhalin-2 has begun to produce LNG for the world market. Russia's first LNG cargo will be delivered to Japan.



Second LNG tanker for the Sakhalin-2 field




The following video clips were presented earlier in "LNG and Supply Chain".








Monday, June 22, 2009

Comparison for LNG Production Processess

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Recommended :Liquefied Natural Gas (LNG) is one of the cleanest energy among all other energy sources.LNG and Supply Chain discussed briefly entire production, transportation, receiving and distribution path of LNG. There are still many peoples who are safety, environment & security concerns, not agreeing with the LNG production as discussed in "LNG SES Issues...".

Liquefy Natural gas is a process of cooling down the natural gas to form liquid for easy storage and transportation. There are few ways to cool down natural gas. Typically are mechanical refrigeration, JT valve and expansion turbine. More discussion in "Techniques to Achieve Cryogenic Temperature". Nowadays, liquefying LNG processes generally adopting combination of two or three techniques as discussed above. Following is a tabulation of a few well-known LNG processes.

Process
C3MR
Cascade
SMR
DMR
MFC
N2 Exp
Thermal Eff.
High
High
Med.
High
High
Low
Equip. no
Med.
High
Low
Med.
Med.
Med.
Precooling HX
Kettle
Core-in
-Kettle
Plate-fin
Spiral
Wound
Plate-fin
Kettle
Liq. HX
Spiral
Wound
Core-in
-Kettle
Plate-fin
Plate-fin
Spiral
Wound
Spiral
Wound
Plate-fin
Refrig. Storage
Large
Large
Med.
Med.
Med.
None
CAPEX
Med.
Med.
Low
Med.
Med.
High

Tuesday, March 3, 2009

Pneumatic Test Explosion in Shanghai LNG Terminal

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An explosion occurred in Shanghai LNG Terminal when the construction worker conducting pneumatic test of the equipment on Feb 06 2009. ONE worker was killed and 15 injured in an explosion on a construction site at Shanghai's Yangshan Deep Water Port. The accident happened at a Shanghai LNG Co Ltd work site on Ximentang Isle, north of the Yangshan Deep Water Port, an international shipping center about 45 kilometers from Pudong International Airport. This LNG terminal is expected to receive 3 million tons of the fuel annually after the first phase becomes operational this year. When the facility is online, LNG shipped by sea from Malaysia will be transformed into a gaseous state and sent to downtown Shanghai through pipes.



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The man who died was pierced by a flying steel rod while lying in his dormitory bed. He was pronounced dead at the scene, his co-workers told reporters. The explosion occurred during a pressure test of the equipment, according to the city government media office. Workers were pumping air into a gasifier when some 500 meters of the piping network burst into fragments, buckling cement crossbeams.




Following are collection of article that helps you to educate yourself or your operators related to Pneumatic test :

Pneumatic Test Accident in Singapore
On May 22, 2002, a fatal accident occurred in Singapore involving the failure of a refrigerant receiver during a pneumatic test. In light of this incident, it is appropriate to again remind our readers of the hazards involved in pneumatic tests and to review the precautions that must be taken in conducting such tests.

Hazards of Trapped Pressure and Vacuum
A leak test on a heat exchanger was being conducted using low pressure gas when the tube bundle was ejected with great force striking two employees. One of them died on massive internal injuries...

Pipeline fails under air pressure test - Kills worker
Two workers had completed laying a 30 metre length of 300 mm diameter PVC pipe, in order to connect it to an existing steel pipe, along a suburban roadside. The pipe was then to be pneumatically tested up to a pressure of 690 kPa (100 psi)...

Pneumatic Test Operation Maintenance

This tank is intended for use vented to atmosphere. For outdoor applications, install a weatherproof vent hood or cap on the vent riser pipe and on the interstitial space vent of double wall tanks.

Pneumatic Test - Incident in Brazil
Incident happened in a non-ExxonMobil facility in Brazil during a pneumatic test of the tank associated piping. A blind was NOT installed to isolate the ...
Pdf

Pneumatic Test - IncidentASTM A1047 / A1047M - 05
ASTM A1047 / A1047M - 05 Standard Test Method for Pneumatic Leak Testing of Tubing

Read others incident...Click HERE

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Friday, January 9, 2009

LNG SES Issues...

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Recommended :Natural gas is used in industry and household to provide heating energy. It is explored from gas well, treated transported to customer via large and long pipeline. It is become non-cost effective once the pipeline length is exceeded 3000 - 3500 km. Thus, another mode of transportation, Liquefied Natural Gas (LNG) is considered cost effective. Liquefied Natural gas (LNG) is a process of cooling down the natural gas to form liquid for easy storage and transportation. A LNG is normally contains of Methane (CH4) which is more than 90% and other light hydrocarbon such as Ethane (C2H6), Propane (C3H8), Butane (C4H10) and Nitrogen (N2) inert gas. LNG is non-corrosive, non-toxic, non-carcinogenic, odorless and colorless. However, it is flammable and explosive and create greenhouse effect to environment. With the tremendous high oil price and dropping in oil reserve, this has pushed many energy company shifting their business towards LNG. No doubt LNG is one of the energy alternative, many peoples who are safety, environment & security concerns, not agreeing with the implementation of LNG production.

Three main issues are their concerns : Safety, Environment and Security.

Safety
For the past 40 years, there are more than 25 accidents related to LNG from production plant, storage and transportation.
  1. Methane Princess Spill, 1965
  2. Jules Verne Spill, May 1965
  3. La Spezia, Italy, 1971
  4. Montreal East, Quebec, Canada, 1972
  5. Staten Island Tank Fire, USA, 1973
  6. Massachusetts Barge Spill, July 1974
  7. Aquarius Spill, September 1977
  8. Das Island, United Arab Emirates, March 1978
  9. Cove Point, Maryland, 1979
  10. Mostafa Ben Bouliad Spill, April 1979
  11. Pollenger Spill, April 1979
  12. Bontang, Indonesia, 1983
  13. Nevada Test Site, Mercury, NV, 1987
  14. Bachir Chihani, Hull Cracking, 1990
  15. Mediterranean Off Gibraltar
  16. Algeria, LNG Facility Explosion, January 19, 2004
  17. Trinidad Tobago, June 13, 2004
  18. Belgium, July 31, 2004
  19. Norway, September 20, 2004
  20. USA, March 2005
  21. Nigeria, August 2005
  22. Savannah, GA March 14, 2006
  23. Trinidad & Tobago May 18 & May 21 & June 6, 2006
  24. Jordan July 13, 2006
  25. Cape Cod February 11, 2008
This has raised an serious alarm to many energy company. Serious safety review are conducted for each LNG related project. As the attraction of LNG business, high energy demand, pressure from government in sourcing energy, many new LNG production and receiving projects still in the planning and implementation phase. Serious and additional safety review are in place to minimize safety risk.

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Environment Impact
Carbon Dioxide (CO2) is known to create severe greenhouse effect and contribute serious global warming. Many efforts such as Co2 capture and sequestration are in research and implementation in order to minimize release of Co2 to atmospheric. It is aware that 1 mole of methane is about 21 time CO2 equivalent. Those any similar quantity of LNG release would seriously results severe global warming. Again, serious safety, facilities and operational review in place to minimize the potential of LNG release to atmospheric.

Security
Following the terrorist attack to twin tower in 911 case, many security agent has postulated the danger of similar attack to plant with flammable product i.e LNG plant. This is another push to minimize LNG plant implementation. Having say that, similar risk is still applicable to other plant i.e refinery, petrochemical plant, etc. Are we going to stop implementation of all these facilities due to this factor ?

Following are some video clip related danger of LNG.


The Risks & Danger of LNG Liquefied Natural Gas


"LNG is Safe, Clean & Affordable" Liquefied Natural Gas


Another Fire Near LNG Terminal: Everett


Just say NO to LNG


Stop Global Warming - Embrace Our Live Earth


No LNG !





Saturday, December 13, 2008

Techniques to Achieve Cryogenic Temperature

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In gas processing and LNG production industry, heavy hydrocarbon (C5+) is removed from natural gas. One of the common way being used is cool natural gas to cryogenic temperature (-40 to -60 degC) so that C1 to C4 remain in gas phase while C5+ is knocked out as liquid phase. This is normally known as Condensate Recovery. Some natural gas is cooled to lower temperature (-70 to -90 degC) to remove C3+ and produce C3 for propylene related product. This is normally known as Propane Recovery. Similarly, the natural gas is cooled to temperature around -90 to -110 degC to remove C2+ and produce C2 for ethylene related product. This is normally known as Ethane Recovery. In LNG production, after the C2+ is removed from natural gas, it is further cooled to about -160 degC to separate inert gas (N2) and storage LNG at -160degC.

There are three important process to bring the natural gas temperature down to cryogenic temperature region :
  • Mechanical Refrigeration (force cooling)
  • Joule-Thompson (JT) valve pressure reduction
  • Gas expansion with Turbo expander
Mechanical Refrigeration
The common refrigeration loop used are propane, ethane, methane, nitrogen, etc. These components are found in natural gas and it is normally extracted, purified and make-up to any losses in the refrigeration loop. As pure component is having contant heat of vaporization at particular pressure level, it would to low efficiency and high capex refrigeration system. Mixture of above component are used. Read more about refrigeration...

Joule Thompson (JT) valve
As fluid is forced through a valve with pressure reduction while minimising heat losses to surrounding, the fluid will experience isenthalpic process (constant enthalpy) and lead to temperature drop at low pressure level. This is a throttling process common called Joule-Thomson (JT) process and the valve used is JT valve. This phenomena is known as JT effect.
Mojority of gases are respecting JT rules except hydrogen, helium, neon , etc. Read more about JT...

Expansion Turbine
High pressure gas is allowed to flow through turboexpander or turbo-expander or expansion turbine (centrifugal or axial), works is produced and used to drive another equipment. This type of expansion process is an isentropic process (constant entropy) which could lead to very low temperature. Read more about Expansion Turbine...

Cryogenic Chilling Technique Video Clip
Following is a video clip presented the three processes to achieve cryogenic chilling.

Saturday, November 29, 2008

LNG and Supply Chain

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Natural gas is used in industry and household to provide heating energy. It is explored from gas well, treated, transported to customer via large and long pipeline. It is become non-cost effective once the pipeline length is exceeded 3000 - 3500 km. Thus, another mode of transportation, Liquefied Natural Gas (LNG) is considered cost effective.

Liquefied Natural gas (LNG) is a process of cooling down the natural gas to form liquid for easy storage and transportation. A LNG is normally contains of Methane (CH4) which is more than 90% and other light hydrocarbon such as Ethane (C2H6), Propane (C3H8), Butane (C4H10) and Nitrogen (N2) inert gas. LNG is non-corrosive, non-toxic, non-carcinogenic, odorless and colorless. However, it is flammable and explosive and create greenhouse effect to environment.

Natural gas may contains of other contaminants such as Carbon Dioxide (CO2), Hydrogen Sulfide (H2S), Water (H2O), Mercury (Hg), Nitrogen (N2), Helium (He), BTEX, etc. These contaminants potentially cause corrosion, cracking and freezing problem in the natural gas liquefaction process. and drop in Higher Heating Value (HHV). Thus they shall be removed prior to liquefaction process. Read more in "Typical Gas Processing Flow Scheme" and "Gas Processing, NGL Extraction & LPG Fractionation".



Entire LNG supply chain consist of LNG production, transportation and regassification process. Natural gas produced from gas well will be treated in order to remove contaminants as mentioned above prior feed to cryogenic section for liquefaction. In the liquefaction process, Natural gas is chilled down to about -160 degC. Ethane (C2), Propane (C3) and Butane (C4) will be recovered as Ethylene feedstock and production of Liquefied Petroleum Gas (LPG). Heavy hydrocarbon (C5+) will be removed from natural gas and sale as stablised condensate. In the process of liquefaction, the natural gas volume will reduce roughly about 600 times and this ease for LNG storage and transportation. Once the LNG is produced, it will store in LNG tank at atmospheric pressure prior pumped to LNG tanker for transportation.

LNG pumped into LNG tanker via LNG loading station will be send to customer. Good insulation is one of the key factor in keep LNG in liquid form during the transportation process. Any vaporized LNG will be compressed and used as fuel to generate power and drive all equipment in LNG tanker.

Once the LNG tanker arrived at LNG terminal, it is unloaded from the LNG tanker to the LNG storage tank. From the LNG storage, LNG is pumped and regassified using seawater or closed loop heated water. Vaporized natural gas is then injected into natural gas grid and deliver to customer.

Following are few video clips for the LNG supply chain, LNG liquefaction and terminal.