Saturday, November 13, 2010

How much can be done in Six days ?

What you can do with Six days ? Many things... Have you ever thought of a 15-story building erected within Six days ?
 
It took six days to build a level 9 Earthquake-resistant, sound-proofed, thermal-insulated 15-story hotel in Changsha, complete with everything, from the cabling to three-pane windows. This of course excludes the prefabrication of components and modules, earthing and foundation preparation. But believe it is sufficiently impress many peoples. This is the Ark Hotel in Changsha, HuNan county, China. May check Changsha using Google map.

Following video clip (Youtube) shows how a building is erected within 6 days.


This believe is another record... Nevertheless many out there still questioning on safety of this building. What do you think ?

The way Chinese do things, in particular this case, possibly may trigger another revolution in business...

Related Post

Saturday, October 9, 2010

CE Oct 2010

Chemical Engineering Digital Issue for Oct 2010... 




***********************

Rare-earth metals for the future 
Issues revolving around economics, workforce and technological innovation will be crucial as rare-earth metal production diversifies and demand for these critical technology metals grows

FAYF - MSMPR crystallization
This one-page reference guide describes examples of mixed-suspension, mixed-product removal crystallizers

Industrial Insulation Systems : Material Selection Factors
To provide the desired functions while beingexposed to harsh environments, insulation material should be carefully selected and specified to meet the design goals

Improving control valve performance
Control valves have a major impact on control-loop performance, so improvements in valve performance can have significant economic benefits. This article shows how poor control-valve performance can be identified and corrected to achieve these benefits

Crossover applications for the ASME-Bioprocessing Equipment Standard 
The ASME-BPE Standard was created for the pharmaceutical industry, but can be very useful in the biofuel and chemical industries as well

Lessons in feedstock changes
Switching to renewable feedstocks can offer financial and environmental benefits, but can also compound challenges associated with processing solids

***********************
TIPS
If you are subscriber, you may access previous digital releases. Learn more in "How to Access Previous Chemical Engineering Digital Issue".

If you yet to be subscriber of Chemical Engineering, requested your FREE subscription via this link (click HERE). Prior to fill-up the form, read "Tips on Succession in FREE Subscription".

Related Post

Friday, October 8, 2010

HP Oct 2010

FREE Hydrocarbon Processing for OCT 2010 is available now...


Click here to view the complete October issue


Articles from the October Issue in HP main focus on Advance control.

How to have a successful data reconciliation software implementation
Follow these guidelines to ensure success


Improve exploration, production and refining with 'add-at-will' wireless automation
After the technology was validated, a wireless infrastructure was installed blanketing 80% of a US refinery

Building and installing a reliable industrial Ethernet infrastructure
Here are six practical guidelines to consider

Increase your margin by 25%
Here's how to make sure that the planning LPs always match the plant

Advanced process control in the plant engineering and construction phases
Testing MVC performance using a dynamic model offers several benefits

Quick Way To Find Altitude of a Plant

Atmospheric pressure change with altitude and this will have impacts to facilities design. Do not Under-estimate The Impact of Altitude Change. Sometime you may want to find altitude of specific location in particular you are conducting feasibility study and identifying plant location. This post will provide a quick way to find altitude of a plant using Google Map.

Simple Steps
Following are some steps to find altitude of a specific location using Google Map :
Step 1 : Execute a "Find_Altitude.htm" by clicking here.
Step 2 : You may choose to Open the file using Internet Explorer or Save the file and execute later.
Step 3 : Google Map will shows map of Singapore island. You may zoom out the map by clicking "-" (in pull bar), left hand side of map
Step 4 : Zoom to the plant location you wish to find the altitude.
Step 5 : Double click the location. Altitude will be displaced in a box.



Example
Find altitude of "Nature Reserve" and "Sentosa Island Beach" in Singapore island.

Step 1 : Execute a "Find_Altitude.htm" by clicking here.
Step 2 : Open the file using Internet Explorer. Google Map will shows map of Singapore island.




Step 3 : Double click the "Nature Reserve". The altitude of "Nature Reserve" in Singapore is approximately 60.64 m. See below image.


Step 4 : Double click the "Sentosa Island Beach". The altitude of "Sentosa Island Beach" in Singapore is approximately 0.0 m. See below image.


Shall take note that this is just for reference only.
Do you have better idea ?

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.

Recommended :
- Subscribes to FREE Hydrocarbon Processing
- Tips on Succession in FREE Subscription

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.

Recommended :
- Subscribes to FREE Hydrocarbon Processing
- Tips on Succession in FREE Subscription

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

Brazed Aluminium Heat Exchanger (BAHX) Standard

A brazed aluminium plate-fin heat exchanger consists of a block (core) of alternating layers (passages) of corrugated fins. The layers are separated from each other by parting sheets and sealed along the edges by means of side bars, and are provided with inlet and outlet ports for the streams. The block is bounded by cap sheets at the top and bottom. An illustration of a multi-stream plate-fin heat exchanger is shown below image.




The Standards of the Brazed Aluminium Plate-Fin Heat Exchanger Manufacturers' Association (ALPEMA) is the result of the work by a technical committee of all the Members to meet the objective of the Association to promote the quality and safe use of this type of heat exchanger. The Standards contain all relevant information for the specification, procurement, and use of Brazed Aluminium Plate-Fin Heat Exchangers. The First Edition was published in 1994, has proved extremely successful and popular. Changes in the industry, experience with using the Standards and feedback from users has resulted released of Second Edition. Now the Standards of the Brazed Aluminium Plate-Fin Heat Exchanger Manufacturers' Association (ALPEMA) is available FREE for download.


Related Post

How Boil-Off-Gas (BOG) is Generated

Recommended :
- Subscribes to FREE Hydrocarbon Processing
- Tips on Succession in FREE Subscription

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.

CE Aug 2010

Recommended :

Some of you may not received your FREE Chemical Engineering Digital magazine for past two months. If you still complete the subscription form in recent update, you may still possible to access latest issue of Chemical Engineering of that particular month. The changes would lead to more visit to Chemical Engineering website and potentially increase sales to CE. However, it could be less favorable to most of you. But you may still obtain FREE Chemical Engineering continuously. The only differences is you need to login to Chemical Engineering website.
Free article from Chemical Engineering for August 2010.

***********************
Synthetic natural gas
Technology developed 40 years ago to convert coal into substitute natural gas is making a comeback -  processes to make Bio-SNG are approaching


FAYF - Heat Transfer Fluid - Filtration
Indirect heating of processes by organic thermal-liquid fluids offers highly reliable operation, and the heat transfer systems are generally treated as low-maintenance utilities. Occasionally, the heat transfer fluid can become contaminated, resulting in the formation of sludge particles, or other sources of dirt can in-filtrate the system. This contamination can cause operational problems. The solid particulates can cause shaft-seal leakage in the circulation pump, valve stem wear, plugging of flow passages and sometimes fouling of heat exchange surfaces. After contamination, the fluid can sometimes be cleaned by in-system, side-stream filtration. For seriously fouled systems requiring more extensive cleaning, the heat transfer fluid can sometimes be cold filtered outside of the system. Side stream filtration may also enhance the performance of pump  suction strainers on startup of a system.

Oh What a Relief it is!
Improvements in pressure relief devices provide advanced process protection

Foolproofing Regulatory Document Generation
Software helps ensure that you always have the right data in the right format

pH Measurement And Control
When measured correctly, pH can be an invaluable tool for both product and process control

***********************
TIPS
If you are subscriber, you may access previous digital releases. Learn more in "How to Access Previous Chemical Engineering Digital Issue".

If you yet to be subscriber of Chemical Engineering, requested your FREE subscription via this link (click HERE). Prior to fill-up the form, read "Tips on Succession in FREE Subscription".

Related Post

The Scientist With No Cost

Right now an exciting offer that is being promoted exclusively through TradePub, our partners.


FREE ONE YEAR SUBSCRIPTION to "The Scientist" WITH NO COST.
*An annual subscription to "The Scientist" typically costs the subscriber $39.95. Now, you can have it with NO cost !


The Scientist is the magazine for life science professionals. For 20 years they have informed and entertained life scientists everywhere. Their target audience is active researchers that are interested in maintaining a broad view of the life sciences by reading articles that are current, concise, accurate and entertaining.

The Scientist is complimentary to qualified professionals in USA and Canada only. The publisher determines qualification and reserves the right to limit the number of free subscriptions. 

Click to Subscribe FREE The Scientist

Related Post

HP Aug 2010

FREE Hydrocarbon Processing for AUGUST 2010 is available now...




Select Articles from the August 2010 Issue

****************************
Prevent electric erosion in variable-frequency drive bearings
Here are the reasons and remedial actions 

Valve design reduces costs and increases safety for US refineries
The goals were achieved by using alloys with superior corrosion resistance

Pump aftermarket offers solutions for abrasive services
Upgrades substantially increased MTBR

How the inertia number points to compressor system design challenges
It facilitates predicting compressor system performance

Gas refineries can benefit from installing a flare gas recovery system
Take a look at these environmental and economic paybacks

Estimating tank calibration uncertaintyUse these calculations for a specific tank calibration

Thursday, August 12, 2010

Design guideline for subsea oil systems

Design and operating guidelines for subsea oil systems have been developed to ensure the control of hydrates, wax, and other solids, which may impede flow. System designs are primarily driven by the need to avoid the formation of a hydrate plug in any portion of the system. Remediation of hydrate plugs may require system shut-in for weeks or even months. Design and operation guidelines for wax management are also well developed. Asphaltenes present a new challenge to subsea system design and operation. A number of projects now under development (Europa, Macaroni) are likely to experience some asphaltene deposition in flowlines and wellbores. Strategies have been developed to manage asphaltenes, but have not yet been tested in the field. The design and operating guidelines for control of solids in subsea oil systems are a product of the flow assurance process.

by S. E. LORIMER & B. T. ELLISON, Shell Deepwater Development Inc.

Download

Related Topic

Access to Facts At Your Fingertips (FAYF)

Chemical Engineering magazine allows subscriber to access to their monthly  issue for current month. Free subscription to Chemical Engineering for qualify subscriber already provided since 2008. You may only view current issue. If you need to view past issue, you may have to subscribe full version.  Fact At Your Fingertips (FAYF) is one of the simple factsheet publish monthly which provide brief description, compilation of simple equation and tips for a special chosen topic. Following is a typical image of FAYF.


Following is the listing of FAYF since April 2007.
  • July 2010: Conservation economics: Carbon pricing impacts
  • June 2010: Distillation Tray Design
  • May 2010: Burner Operating Characteristics
  • April 2010: Measurement guide for replacement seals
  • March 2010: Steam Tracer Lines and Traps
  • February 2010: Positive Displacement Pumps
  • January 2010: Low-Pressure Measurement for Control Valves
  • December 2009: Creating Installed Gain Graphs for Control Valves
  • November 2009: Aboveground and underground storage tanks
  • October 2009: Chemical Resistance of Thermoplastics
  • September 2009: Heat Transfer: System Design II
  • August 2009: Adsorption
  • Juy 2009: Flowmeter Selection
  • June 2009: Specialty Metals
  • May 2009: Choosing a Control System
  • April 2009: Energy Efficiency in Steam Systems
  • March 2009: Membrane Configurations
  • February 2009: Pipe Sizing
  • January 2009: Column Internals
  • December 2008: Fluid Flow
  • November 2008: Alternative Fuels
  • October 2008: Heat Transfer
  • September 2008: Crystallization 
  • August 2008: Valves
  • July 2008: Vacuum Processing
  • June 2008: Humidity Control
  • May 2008: Acid Handling
  • April 2008: Tower Packing
  • March 2008: Membranes
  • February 2008: Pressure Relief
  • January 2008: Centrifuging
  • December 2007: Sealing Systems
  • November 2007: Pump Selection and Specification
  • October 2007: Pristine Processing
  • September 2007: Heat Transfer
  • August 2007: Materials of Construction
  • July 2007: Fuel Selection
  • June 2007 (1): Solvent Selection
  • June 2007 (2): Controlling Crystal Growth
  • May 2007: Hazardous Area Classification
  • April 2007: Reaction Engineering
If you are subscriber to Chemical Engineering, you may download all above FAYF. You may try you luck to apply for Free subscription by clicking here.

TIPS
If you are subscriber, you may access previous digital releases. Learn more in "How to Access Previous Chemical Engineering Digital Issue".

If you yet to be subscriber of Chemical Engineering, requested your FREE subscription via this link (click HERE). Prior to fill-up the form, read "Tips on Succession in FREE Subscription".

Related Post

Sunday, August 8, 2010

Compression Prediction Gap & Highlights

Earlier post "Compression Prediction - Compressor Vendor, GPSA & HYSYS" has presented equation in determining Polytropic head, polytropic exponent, gas horse power and compressor discharge temperature.

Recommended :
Subscribes to FREE Hydrocarbon Processing

From data presented, two main findings are (i) GPSA method may be used but shall keep in mind GPSA potentially overpredicted discharge temperature. This potential results over conservative design and excessive cooling required. (ii) HYSYS prediction is using rigorous method which adjusting prediction rigorously and within a good range of prediction. This post will look at the influence of compressibility  (z) on predicted temperature difference for several ordinary components.

Check Case Basis
Following tabulating the basis of compression calculation using GPSA and HYSYS.
1) Component used : Methane (C1), Ethane (C2), Propane (C3) and Iso-Butane (i-C4)
2) Suction temperature fixed at 45 degC for all calculation
3) Suction pressure range : 1, 3, 4.5,  5, 10, 20, 50 barg
4a) Discharge pressure for Methane (C1) case : 4, 8, 15, 30, 55 & 150 barg
4b) Discharge pressure for Ethane (C2) case : 4, 8, 15, 30, 55 & 150 barg
4c) Discharge pressure for Propane (C3) case : 4, 8, 15 & 30 barg
4d) Discharge pressure for Is-Butane (I-C4) case : 4, 8 & 15 barg
5) Polytorpic efficiency artificial set at 73% for all cases



Results
Calculation results shows that
i) GPSA predicted discharge temperature (Td) consistently higher than HYSYS rigorous prediction.
ii) As discharge pressure (Pd) increase, discharge compressibility (Zd)  decrease consistently.
iii) As compressibility decrease (Zd) , the discharge temperature difference / gap (dT) increase significantly. See following chart.


iv) Considering discharge temperature difference / gap (dT) of 10 degC as limit, the compressibility is limited to 0.90 for discharge pressure 8 barg (and below).
v) Considering discharge temperature difference / gap (dT) of 10 degC as limit, the compressibility is limited to 0.96 for discharge pressure 15 barg (and below).
v) As discharge pressure increase above 15 barg, discharge temperature difference / gap (dT) will possibly higher than of 10 degC limit.

Highlights
i) Pressure lower than 15 barg, the GPSA and HYSYS prediction are considered acceptable.
ii) Once pressure higher than 15 barg, GPSA can severely overpredicts discharge temperature. Shall consider to use rigorous compression calculation (like HYSYS).

Related Topic

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.

Download


Sunday, August 1, 2010

HYSYS OLGA Link User Guide

Recommended :
This user guide details all the procedures you need to work with the OLGA Link extension which will help you learn how to use OLGA Link efficiently, this manual thoroughly describes the views and capabilities of the OLGA Link as well as outlining the procedural steps needed for running the extension. The basics of building a simple OLGA Link model is explored in the tutorial (example) problem. The case is presented as a logical sequence of steps that outline the basic procedures needed to build an OLGA Link case. This guide also outlines the relevant parameters for defining the entire extension and its environment. Each view is defined on a page-by-page basis to give you a complete understanding of the data requirements for the components and the capabilities of the extension.

The OLGA Link User Guide does not detail HYSYS procedures and assumes that you are familiar with the HYSYS environment and conventions. If you require more information on working with HYSYS, please refer to the HYSYS Manuals. Here you will find all the information you require to set up a case and work efficiently within the simulation environment. Throughout this document, when describing OLGA keywords that are required in the *.inp file for your OLGA model, capital letters will be used for the complete keyword. For example BOUNDARY represents the keyword and specification of a boundary node and its relevant boundary conditions in the OLGA model. Throughout this document (and when you are using distributed computing with one computer for HYSYS and the OLGA Link, and another computer for the OLGA software), you will see the reference to the HYSYS PC (local computer) and the OLGA PC (remote computer).

Download

Compression Prediction - Compressor Vendor, GPSA & HYSYS

Recommended :
Compressor is commonly used to compress gas and vapor to higher delivery pressure. Energy is supplied to the compressor to develop compression head. Part of the energy is lost when energy is transferred via shaft and part of energy lost due to compression activity. Energy lost via shaft will convert to vibration and noise. Energy lost due to compression activity (instead of carry out compression work) will turn to fluid internal energy of fluid. As fluid internal energy is increased, temperature of fluid will rise. How much energy is lost to compression activity ? How much internal energy is increased and how fluid temperature is increased ? All this relates to one well known parameter in compression field, Polytropic efficiency.

There are two paths compression is carried out :

1. isentropic reversible path - a process during which there is no heat added to or removed from the system
and the entropy remains constant, pvk = constant
2. polytropic reversible path - a process in which changes in gas characteristics during compression are considered, pvn = constant

One shall take note that most compressors operate along a polytropic path but approaches the isentropic. Most compressor will use polytropic efficiency to account for true behavior.
Compression following polytropic path,



Polytropic head 

where
Zavg = Average compressibility factor
Ts = Suction temperature (degK)
M = Molecular weight
n = polytropic exponent
Pd = Discharge pressure (bara)
Ps = Suction pressure (bara)

Polytropic exponent (n) can be calculated base on following equation


where
k = isentropic exponent
np = Polytropic efficiency

Gas Horse Power,


where
W = gas flowrate (kg/h)

Compressor discharge temperature


where
Td = Discharge temperature (K)
Ts = Suction temperature (K)


Above equations were extracted from GPSA section 13.

Recent compression studies using several cases to find compressor gas horse power and discharge temperature with specific polytropic efficiency. The studies have used
  • GPSA method (as tabulated above) 
  • HYSYS 
to estimate compressor gas horse power and discharge temperature. Results from several international compressor suppliers.
CaseItems Supplier GPSA HYSYS
1aDischarge temperature(degC) 117.6117.5 117.2

Gas Horse Power (kW)2696.02678.42690.1





1bDischarge temperature(degC) 121.2121.0 120.6

Gas Horse Power (kW)2877.02858.42871.4





2aDischarge temperature(degC) 117.2117.5 116.5

Gas Horse Power (kW)10828.01074010651.4





2bDischarge temperature(degC) 88.088.0 87.4

Gas Horse Power (kW)4628.04575.14532.6





3aDischarge temperature(degC) 124.1140.9 124.7

Gas Horse Power (kW)8966.09147.89039.0





3bDischarge temperature(degC) 85.0117.9 86.1

Gas Horse Power (kW)3682.03798.03736.6





4aDischarge temperature(degC) 122.5139.5 125.8

Gas Horse Power (kW)9090.49210.79162.0





4bDischarge temperature(degC) 86.3120.7 87.1

Gas Horse Power (kW)3829.63926.73859.7





5aDischarge temperature(degC) 123.2142.3 125.6

Gas Horse Power (kW)9104.09262.29149.5





5bDischarge temperature(degC) 95.7121.0 87.2

Gas Horse Power (kW)4293.03937.83844.0






Several observations :
i) HYSYS consistently predict discharge temperature similar to compressor supplier results.
ii) GPSA overpredict discharge temperature for several cases.
iii) HYSYS & GPSA predict gas horse power proximity to compressor supplier results with HYSYS in better prediction.


Above results give us some indication that
i) GPSA method may be used but shall keep in mind GPSA potentially overpredicted discharge temperature. This potential results over conservative design and excessive cooling required.
ii) HYSYS prediction is using rigorous method which adjusting prediction rigorously and within a good range of prediction.

Related Topic