Server was down for past few days... it resulted no posting... Anyway glad that it is up again and the speed is back again... will continue posting...
Monday, February 11, 2008
Wednesday, February 6, 2008
WELKER Jet Contorl Valve Handbook
With the advise from Kent (thanks), i have just included the following document link in the Useful Documents Related to Control Valve (click HERE).
WELKER JET CONTROL VALVE - A PRACTICAL APPLICATION HANDBOOK
Welker Eng
The current Welker Jet® and the earlier Jet Stream™ Control Valves are the most unique Control Valves on the market today. Over the last 44 years, Welker employees have discussed the Jet with thousands of people and users in over 15 countries worldwide. Because of its unique features and unparalleled performance, much has been said and misunderstood about this product. In an attempt to clarify some of these statements and to share the accumulated...READ MORE...CLICK HERE...
If you have any good articles (or links) that you think is interesting, please drop me a note.
WELKER JET CONTROL VALVE - A PRACTICAL APPLICATION HANDBOOK
Welker Eng
The current Welker Jet® and the earlier Jet Stream™ Control Valves are the most unique Control Valves on the market today. Over the last 44 years, Welker employees have discussed the Jet with thousands of people and users in over 15 countries worldwide. Because of its unique features and unparalleled performance, much has been said and misunderstood about this product. In an attempt to clarify some of these statements and to share the accumulated...READ MORE...CLICK HERE...
If you have any good articles (or links) that you think is interesting, please drop me a note.
Happy Chinese New Year... To All My Chinese Friends...
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To all my sincere Chinese friends and readers, GONG XI FAT CAI & XIN XIANG SHI CHEN...
Today is the first day of Chinese Lunar New Year, i would like to take this opportunity to wish all of you a very good Chinese Lunar year, good health and good wealth... and thanks all your support for past one year... Also would hope all take this opportunity to take the effort to forgive and learn to forget... towards a wonderful & peaceful new year...
Tuesday, February 5, 2008
Complicated Tube Rupture Scenario... Nightmare in Sizing a PRD
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Have you ever experienced sizing Pressure Relief Devices in the following condition or one of the configuration in your plant was setup in the following way?
A heat exchanger with gas on shell side with low operating pressure of 1 barg (design pressure of 3.5 barg) is heated with High pressure steam in tube side at 40 barg (design pressure of 46 barg).
From earlier discussion on tube rupture assessment in "Criteria for Requirement of Pressure Relief Device for Tube Rupture", it is obvious that tube rupture scenario is credible and shell side shall be protected from heat exchanger tube rupture.However, in the event of tube rupture, the relieving could be very complex. Why ?
In the event of tube rupture,
i) a complete sharp break will occurOne orifice is discharging high pressure steam and the other orifice is discharging high pressure condensate to shell side. The pressure relief device (PRD) may experience difference scenarios :
ii) the sharp break may occur at tubesheet
iii) two orifice relieving high pressure steam and condensate to shell side (for simplicity)
a) Pure hydrocarbon gas relief via PRD. The flowrate would be the volume discplacement by steam discharge through orifice + steam & condensate flash from condensate discharge via orifice
b) Steam mixed with hydrocarbon gas relief via PRD. The flowrate would be the volume discplacement by steam discharge through orifice + steam & condensate flash from condensate discharge via orifice. The mixtures of steam and hydrocarbon gas would varies.
c) Steam and hydrocarbon gas with condensate entrained relief via PRD. The flowrate would be the volume discplacement by steam discharge through orifice + steam & condensate flash from condensate discharge via orifice. The mixtures of steam, hydrocarbon gas and quantity of condensate would varies. Condensate in gas would varied from zero to 100% condensate.
d) Flashing condensate relief via PRD. The flowrate would be the volume displacement by steam discharge through orifice + steam & condensate flash from condensate discharge via orifice.
Above will results multiple complicated relieving scenario and it will be a great challenge to a PRD designer.
Apart, the discahrge of steam and flashing condensate into shell would be highly turbulence and potential leads to severe surging, vibration, support shaking, etc which may cause catatrophic failure of the heat exchanger. Surge analysis as well as detail study of liquid flowing dynamic may required to ensure above scenario will not occur.
Thus, the overpressure protection system against the tube rupture scenario for above configuration and condition may not as simple as just providing a pressure relief device on the shell. Additional measures shall be provided to eliminate potential of tube rupture scenarios.
Next post will discuss some measures may be taken to eliminate / avoid / minimize magnitude of complicated tube rupture scenarios.
Recommended utility : Recuva - Recover DELETED Files
Related Topic
- Two-third (2/3) rule or Ten-thirteen (10/13) rule ?
- Tube Rupture : Pressure Relief Valve (PSV) or Rupture Disk (RD) ?
- Criteria for Requirement of Pressure Relief Device for Tube Rupture
- Requirement of Overpressure Protection Device on "Final Vessel"
- FREE & Reliable Pressure Relief Valve Sizing Software
- Extra Caution When Eliminating Overpressure by Fire Attacks
- Should maximum recommended wall temperature (Tw) for carbon steel vessel used as design temperature ?
- Should we install Butterfly valve for Pressure Relief Valve (PSV) isolation ?
Monday, February 4, 2008
Methane Conversion Challenge - An effort to minimise gas emission...
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In 1st quarter of 2007, we have spread the news on "Methane Conversion Challenge" where Dow Chemical Company was accepting proposals for funding in the area of methane conversion chemistry with the goal of producing ethylene, propylene, or reasonable precursors for ethylene and propylene. Finally out of approximate 100 proposals from around the world submitted, the Dow Chemical Company on January 24th, 2008 announced that Cardiff University and Northwestern University have been awarded research grants which together total over $6.4 million as part of the 2007 Dow Methane Challenge.
The Methane Challenge is on purpose to provide a new foundation for production of chemicals and liquid fuels, bringing an alternative to petroleum and enabling the use of natural gas in an efficient manner. It also reduce gas emission via venting and flaring and potential of upgrading landfill gas. Read in detail...Hope that there are more oil and gas company will initiate the effort in similar direction to minimum gas emission and subsequent lead to greenhouse effect and global warming.
Recommended utility : drop.io
Related Topic
- Methane Conversion Challenge
- Several Concerns in High CO2 Field Development
- Use Ultra-Sonic Flowmeter in FLARE Gas Header for emission monitoring
- How does Supercritical fluid looks like ?
- OGT - Others FREE articles related to Amine & CO2...
- Optimized Gas Treating, Inc. (OGT) - Experts in CO2-Amine
Sunday, February 3, 2008
Parallel Valve Technology Increase Safety & Reduce Nuisance Trips
A new parallel valve technology, consisting of two block valves mounted into a parallel pipe manifold, promises more efficient diagnostics of the fluid handling system, reducing the number of investigative equipment shutdowns. This new parallel valve technology provides 90-95% diagnostic coverage.
This parallel valve technology (Click here) has much improvement compare to two-out-of-two-diagnostic architecture (2oo2D) introduced in 1990s. 2002D architecture significantly increases safety level of production plant, however the draw back is increases the nuisance trips.This parallel valve technology (Click here) substantially increase the level of safety in the process industries, while significantly reducing the number of nuisance trips, therefore it is justifiable from life cycle cost of the installation in terms of both safety and production.
Recommended Utility : Sprout - A FREE Flash Builder...
Related Topic
- Two-third (2/3) rule or Ten-thirteen (10/13) rule ?
- Tube Rupture : Pressure Relief Valve (PSV) or Rupture Disk (RD) ?
- Criteria for Requirement of Pressure Relief Device for Tube Rupture
- Requirement of Overpressure Protection Device on "Final Vessel"
- 12 Features required for Shutdown Valve (SDV)
- Requirement of overpressure protection devices on system design to PIPING code
Friday, February 1, 2008
CETD - Technical Visit to Process Plant
Simple update to IEM members (MALAYSIA), Chemical Engineering Technical Division (CETD) of IEM would be organized the following visit from 9 to 10 March 2008.
TECHNICAL VISIT TO PROCESS PLANT
BAN HENG BEE RICE MILL SDN BHD
PETRONAS FERTILIZER (KEDAH) SDN BHD &
MALAYAN SUGAR MANUFACTURING CO. BHD
9 MARCH 2008 & 10 MARCH 2008 (SUNDAY & MONDAY)
BAN HENG BEE RICE MILL SDN BHD
PETRONAS FERTILIZER (KEDAH) SDN BHD &
MALAYAN SUGAR MANUFACTURING CO. BHD
9 MARCH 2008 & 10 MARCH 2008 (SUNDAY & MONDAY)
For details, please read this flyer (Click HERE)
BEM Approved CPD Hours : 8 hours
Maximum participants : 30 on 1st-come-n-pay-1st-serve basis
Commitment fees : RM 150 (IEM member), RM 200 (non-member) inclusive of accomodation
BEM Approved CPD Hours : 8 hours
Maximum participants : 30 on 1st-come-n-pay-1st-serve basis
Commitment fees : RM 150 (IEM member), RM 200 (non-member) inclusive of accomodation
If you are interested to join the trip, you may download this flyer and return the reply slip to IEM secretariat (+603-7957 7678) before 1 March 2008 .
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