Milt Beychok from www.air-dispersion.com has shared a schematic flow diagram of a typical oil refinery that depicts the various unit processes and the flow of intermediate product streams that occurs between the inlet crude oil feedstock and the final end products. This image has given a brief idea how crude oil is refined. Products included LPG, Butanes, Jet Fuel, Kerosene, Diesel Oil and Fuel Oil and side product Sulfur.
Wednesday, August 29, 2007
Tuesday, August 28, 2007
Different Equation for Pitting Resistance Equivalent Number (PREN)
As discussed in earlier post <<Pitting Corrosion - Mechanism & Prevention>>, pitting corrosion is one of the most common localized corrosion attack and most destructive form of corrosion in metal and alloy. Out of so many type of alloy, how to differential the
pitting resistivity of particular metal and alloy compare to the other ? Pitting Resistance Equivalent Number is used.
pitting resistivity of particular metal and alloy compare to the other ? Pitting Resistance Equivalent Number is used.Pitting Resistance Equivalent Number (PREN) is an index common used to measure and compare resistance level of a particular metal and alloy to pitting corrosion.
PREN can be calculated , using the alloy chemical composition, to estimate relative pitting resistance of metal and alloys.
Common equation for PREN calculation as followed :
PREN = %Cr + m.(%Mo) + n.(%N)
Per experiments, m range from 3.0 to 3.3 whilst n range from 12.8 to 30.
For ferritic grades Stainless Steel, the formula employed is :
PRE = % Cr + 3.3 (% Mo)
For austenitic grades Stainless Steel, the formula employed is :
PREN = %Cr + 3.3(%Mo) + 30(%N)
For duplex (austenitic-ferritic) grade Stainless Steel, the formula employed is :
PREN = %Cr + 3.3(%Mo) + 16(%N)
For high Ni-Cr-Mo alloys e.g. Inconel 625, Hastelloy, etc, the formula employed is :
PREN = %Cr + 1.5(%Mo + %W + %Nb)
where...
Cr - Chromium
Mo - Molybdenum
W - Tungsten
Nb - Niobium
Pitting is one of main problem for material expose to seawater. Minimum PREN required for material expose to seawater is 40. Duplex Stainless steel, Super duplex stainless steel, etc are exhibiting PREN > 40.
Related topics
Sunday, August 26, 2007
Discussion on ISENTROPIC and ISENTHALPIC process via Relief Valve

This question has been raised by many engineers and debated in many discussion.
Careful review on the relief valve structure, process fluid passing through a nozzle instead of an orifice. Those many researchers such as Dr. Ron Darby for multiphase flow in Direct Integration method (HDI), Dr Fauske & Dr Henry for two phase relief in Homogeneous Non-equilibrium model (HNE), Dr. Joseph Leung for two phase flow in Omega method, etc have modelled a relief valve as a nozzle.
Classical and conventional studies informed us that vena contracta (VC) will only occur in sharp edge orifice. However, the flow restricting area in a relief valve as decribed by many well knowed specialists is not an orifice, but is actually a nozzle. Thus there is NO vena contracta downstream of the nozzle.
Phenomenon of flow through a nozzle in relief valve is extremely fast. Choked flow is possible occur in some location "A" in the nozzle instead of outside the nozzle (may be closed to the exit end), from the inlet to "A" will be a REVERSIBLE process which generally accepted by most of the specialists. Thus, it is ISENTROPIC process. From location "A" to PSV outlet, the system is expanded and change in state. It will be slow down. There will be transformation energy loss however the enthalpy is maintain constant (ISENTHALPIC). This process is IRREVERSIBLE. "A" is viewed as vena contracta in the relief valve's nozzle. Those in sizing a relief valve, we ignore the frictional loss in the nozzle and consider ISENTROPIC process. However, from expansion process via safety valve (Vena contracta to relief outlet), the process will be ISENTHALPIC.
Related topics
If you benefits from this post, buy me some sweets
Saturday, August 25, 2007
Floating Gas Refinery Unit

You have heard about Floating Production Storage Offloading (FPSO) unit...you have heard about Floating LNG Unit...have you ever heard about Floating Gas Refinery Unit ?
Read HERE...
Friday, August 24, 2007
Pitting Corrosion - Mechanism & Prevention
Pitting Corrosion on Metal Surface
Pitting is one of the most destructive forms of corrosion as it will potential cause equipment failures due to perforation / penetration. pitting generally occurs on metal surfaces protected by oxide film such as Stainless steel, aluminum, etc. Typically for boiler and feed water system, pitting corrosion rate increase dramatically with the increase of oxygen content in the fluid.
Pitting can occur in any metal surfaces. Following are some pictures of pitting corrosion.
Pitting corrosion on external pipe surface
Pitting corrosion on external pipe surface
H2S Pitting corrosion on internal pipe surface
Mechanism
Lets look at figure below, oxygen rich fluid in contact with metal surface (at the top of the pit) will becomes the cathode. At the bottom of the pit, low in oxygen level becomes the anode. this will form a complete circuit where metal at the pit (FE) will be ionized to release electron (e) and form ion Ferum (FE2+), this electron will travel to the top of pit to react with Oxygen (O2) (and water, H2O) to form ion hydroxides (OH-). Ion Ferum (FE2+) will react with ion hydroxides (OH-) to form Ferum Oxide (Fe2O3) which typically a brown rust. Deeper the pit leeser the oxygen content and higher the potential and pitting corrosion rate.
Severity of pitting corrosion
Knowing that pitting can cause failure due to perforation while the total corrosion, as measured by weight lossm might be rather minimal, experience shown that rate of penetration may be 10 to 100 times that by general corrosion, pitting corrosion has been considered to be more dangerous than the uniform corrosion damage because it is very difficult to detect, predict and design against. General metal weight loss method almost impossible to detect the internal pitting corrosion.
Pitting corrosion shape
Pits formed due to pitting corrosion can become wide and shallow or narrow and deep which can rapidly perforate the wall thickness of a metal. Following picture demonstrate several types of pitting corrosion shape. This has made it even more difficult to be detected especially undercutting, subsuface and horizontal type.
Preventive measures
There are several preventive approah to avoid pitting. There are :
- Proper material selection e.g. SS316 with molydenum having higher pitting resistance compare to SS304
- Use higher alloys (ASTM G48) for increased resistance to pitting corrosion
- Control oxygen level by injecting oxygen scavenger in boiler water system
- Control pH, chloride concentration and temperature
- Cathodic protection and/or Anodic Protection
- Proper monitoring of oxygen & chloride contents by routine sampling
- Agitation of stagnant fluid
- Chloride stress corrosion cracking and use of correct MOC for seawater
- How Chloride stress corrosion cracking Lookslike ?
- Unified Numbering System for Metals and Alloys
Thursday, August 23, 2007
How a Chloride Stress Corrosion Cracking Lookslike ?
The following are some images of metal experienced Chloride Stress Corrosion Cracking.
Inter granular SCC of an Inconel heat exchanger tube
Trans granular SCC of 316 stainless steel chemical processing piping system
CSCC occured on insulated vessel
CSCC occured on insulated vessel
CSCC occured on Condenser tube
CSCC on pipe
Inter granular SCC of a pipe
Related Topics
- Chloride stress corrosion cracking and use of correct MOC for seawater
- Unified Numbering System for Metals and Alloys
Wednesday, August 22, 2007
Chloride Stress Corrosion Cracking & Use correct MOC for seawater service
Chloride stress - corrosion cracking (CSCC) is initiation and propagation of cracks in a metal or alloy under tensile stresses and a corrosive environment contains Chloride compounds. Once the crack is initiated, it will propagate rapidly and potentially lead to catastrophic failure.
Factors that influence the rate and severity of cracking include
- chloride content
- oxygen content
- temperature
- stress level
- pH value of an aqueous solution
Higher chloride content in process fluid will increase potential of CSCC.
It has been established that oxygen is required for CSCC to occur. Detail may refer to HERE.
The severity of cracking increases with temperature. Figure below shows several Stainless Steel materials increases it susceptibility to CSCC as temperature is increased.
It has been established that oxygen is required for CSCC to occur. Detail may refer to HERE.
The severity of cracking increases with temperature. Figure below shows several Stainless Steel materials increases it susceptibility to CSCC as temperature is increased.

Source : Sandvik Material Technology
SAF 2205 (UNS 31803) = Duplex Stainless Steel
SAF 2507 (UNS 32750) = Super Duplex Stainless Steel
SAF 2205 (UNS 31803) = Duplex Stainless Steel
SAF 2507 (UNS 32750) = Super Duplex Stainless Steel
Material under pressure without Post weld heat treatment will experience high stress level. Higher the stress level, higher the potential of CSCC.
Acidic process(low pH) with chloride content in it tends to increase the CSCC potential.
CASE STUDIES
Hot gas (Shell) is cooled by seawater (Tube) from 220 degC to 180 degC in a Shell & Tube heat exchanger. Seawater is being heated from 30 degC to 35 degC and return to sea. The Shell and Tube material of construction are Carbon steel (CS) and Duplex Stainless Steel (DSS) respectively. After 2 months in operation, cracks occurred at the tube (DSS) and leads to major platform shutdown. Investigation found crack was caused by CSCC at tube. Why a CSCC occurred at DSS tube although the seawater temperature only 35 degC maximum ?
Eventhough the inlet and outlet temperature are below 150 degC, thermal designer may design the heat exchanger with high heat flux in order to reduce the heat exchanger area and this result tube skin temperature exceeded 150 degC. Condition with Seawater which contains ~20,000 mg/l Chloride, high in dissolved oxygen, slightly acidic and skin temperature exceeded 150 degC is perfect combination conditions for CSCC to occur for DSS. Those heat exchanger designer shall always check skin temperature profile especially for low flow condition or specify better material i.e. Super DSS for above service.
Further Reading
Eventhough the inlet and outlet temperature are below 150 degC, thermal designer may design the heat exchanger with high heat flux in order to reduce the heat exchanger area and this result tube skin temperature exceeded 150 degC. Condition with Seawater which contains ~20,000 mg/l Chloride, high in dissolved oxygen, slightly acidic and skin temperature exceeded 150 degC is perfect combination conditions for CSCC to occur for DSS. Those heat exchanger designer shall always check skin temperature profile especially for low flow condition or specify better material i.e. Super DSS for above service.
Further Reading
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