Thorat Piping Blog

Catia Implementation for Plant Design

2011-09-14T08:55:00.001+03:00

We are implementing CATIA for Plant design.
When we started it was bit confusing, the modules required for modelling a Plant as we do in PDMS and PDS was not clear.
Now after exposure, I would like to share the basic minimum modules required for Plant Design.
1. Piping (PIP and PID)
2. Multidiscipline Equipment Arrangement
3. Mechanical Design - Structural design.

I think above three modules will take care of all Plant modelling requirement as in PDMS or PDS.

One advantage we have here is PID module is bundled with Piping Module. THe PID is intelligent PID.

Disadvantages for PID, we need to customise lot of items to meet the CLient specific requirement.
Customisation over a period has become easier for me.

Any body having queries on CATIA plant design, please post a comment on the blog,
I will try and reply.

I will keep posting the experimentation with CATIA on this blog.
Thanks
Thorat

IPL 2011 Fixture, Excel Sheet

2011-04-06T09:31:00.001+03:00

Dear All,
This is the excel timetable for IPL 2011
Hope U will find it useful
Thanks
Excel Link

PDMS 12

2010-10-21T06:42:00.000+03:00

Here are the links for PDMS 12.
I have verified it personally. I need to do that.
http://www.fileserve.com/file/SmNW7er/AVEVA_PDMS_12.0_SP4_.part1.rar
http://www.fileserve.com/file/kNkrNvc/AVEVA_PDMS_12.0_SP4_.part2.rar
http://www.fileserve.com/file/W3DWYTy/AVEVA_PDMS_12.0_SP4_.part3.rar
http://www.fileserve.com/file/ZceMT3q/AVEVA_PDMS_12.0_SP4_.part4.rar
http://www.fileserve.com/file/XKhVpEV/AVEVA_PDMS_12.0_SP4_.part5.rar
http://www.fileserve.com/file/YKcRtTN/AVEVA_PDMS_12.0_SP4_.part6.rar
http://www.fileserve.com/file/H82PrB9/AVEVA_PDMS_12.0_SP4_.part7.rar

From the content, I could see that there is a ISO file which we need to burn on DVD for getting setup.
Hope you will find useful.
Request to post your feedback.

Piping Codes

2010-05-14T12:46:00.002+03:00

Collection of all Piping Codes in a Single sheet.
Useful for Piping Engineers

Separator Sizing Program

2010-04-19T14:49:00.000+03:00

This program has been developed to design both horizontal and vertical separators

Horizontal Separators
- Three Phase Flooded Weir
Three phase flooded weir separator is typically used where gas, water and oil

flowrates are very high. In this design oil NLL must be above the weir height.

- Three phase non flooded weir

Three phase flooded weir separator is typically used where gas and water flowrates

are very high with low oil flow rate. In this design oil NLL must be below the weir

height.

-Three Phase Boot
Three phase separator with boot is typically used where gas and oil flow rates are

very high with low water flow rate.

-Two phase Vapour Liquid
Two phase separator is a basic gas liquid separator. In case two liquid phases are

separated as one, a mixed liquid property is to be used.

- Two phase liquid Liquid

Two phase liquid liquid horizontal separator is designed based on residence time. In

this design it is preferable to keep the interface level at the centre of the

separator.

- Knock out Drum API
Two phase vapour liquid horizontal KO Drum desinged based on API 521. This design is

based on droplet settling velocity and does not check the KO drum adequacy based on

K velocity.

Vertical Separators
- Vapour Liquid Vertical - This is two phase vapour liquid separator
- Liquid Liquid Vertical - This is two phase liquid liquid separator.
link : http://rapidshare.com/files/372968742/Separator_sizing.rar

Low Pressure Hazard

2010-03-24T10:03:00.007+03:00

Do you consider low pressure to be less hazardous??
Than check this powerpoint presentation.
You will be amazed

http://rapidshare.com/files/367707664/Pressure_Safety.pps

Basic of Piping Engineering

2009-10-28T14:44:00.006+03:00

Basics of Piping Engineering

Excellent Presentation by one of my students.
Hope you will find it useful.
The presentation is in Powerpoint 2007 version.
I will try to upload 2003 version as well.
Wait and watch this post.
download link
http://rapidshare.com/files/365337009/Basic_Concept_of_Piping_Engineering.zip

CATView for PDMS

2009-10-09T06:14:00.004+03:00

CATVIEW
Catview is a freeware PDMS application for building and maintaining piping specifications. It is
designed to be largely independent of catalogue naming conventions, but requires some form of
catalogue organisation for it to work.

The principle features of Catview are as follows:

· Catalogue Listing and Browsing
Display a list of component types using the category description attribute.
Sort the catalogue by generic type and standard.
Display data sheets showing catalogue items and their parameters.
Search the catalogue for specific words or phrases
· Specification Building using the Browsing functionality
Create new piping specifications
Build components into Specifications using the browser to select appropriate component
types.
Add a list of items using size ranges.
Ignore non-preferred sizes using an exclusion list.
· Specification Editing
Display detailed list of Specification components sorted by Component Type.
Edit component details such as Name, Stype, Material, Component Reference, Bolt
Reference and Description.
Add wall thickness details.
· Specification Reporting
Automatic Spec Summaries
Pegs Specification Transfer
· Catalogue Documentation
Produce Catalogue datasheets via Daft
Catview Contents
Installation Guide

Install using setup
I suppose that it will get installed in
C:\AVeva\CATVIEW11.3

To add Catview to the PDMS applications.
Edit the standard evars.bat file in your PDMS directory to add a line to call the catview
evars.bat file.
Assuming you have a standard PDMS11.3 installation, the following line should be
inserted at the end of the evars.bat file:
call C:\aveva\catview11.3\evars.bat

The application will be visible in specon module.
In piping spec sub menu
Under utilities menu.
available at
http://rapidshare.com/files/224254956/cats.zip

Welding of Pipes with different internal diameters

2008-11-26T10:01:00.003+03:00

Query by KN Srinivas Rao
How to join the schedule 150 pipe with schedule 300 pipe

I think you want to ask that how to weld the pipes having different schedules as per 150 # and 300 #.
Smaller pipes of these ratings sometimes will have same schedule.

It is always advisable to check where the joint is coming, if it coming after the flanged valve where the spec break is shown, in that case we can select valve & flange of 300# and only one deviation we can take is the flange schedule (For WN) should be compatible with the 150# spec.
(If the explanation is not sufficient, I will try to provide some images, let me know)

This part requires the study of various standard for permissible offset, as per ASME Sec III, following are the Maximum Allowable offset.

Thickness in Inch :: Longitudinal Joints :: Circumferential Joints
Up to ½ incl. ½ :: ¼ t :: ¼ t
Over ½ to ¾ , incl. :: 1/8 in :: ¼ t
Over ¾ to 1 ½ , incl. :: 1/8 in :: 3/16 in
Over 1 ½ to 2, incl. :: 1/8 in :: 1/8 t
Over 2inch :: Lesser of 1/16 t or 3/8 in :: Lesser of 1⁄8 t or 3⁄4 in

As far as possible, our aim to achieve the perfect alignment, in case alignment is not possible, we can for undercut of the heavier thickness pipe as shown in the figure. (For misalignment higher than 2 mm only. )

For Thickness difference less than 2 mm

For Thickness difference more than 2 mm

PFD and P & ID

2008-11-25T16:26:00.003+03:00

PFD – Process Flow Diagram.

Following are the items which are found in a Typical PFD.

Major Equipment Symbols, Names and Identification Number
Main Piping (Process)
Valves and Control Valves affecting the operation. (Responsible for change in process parameters)
System Interconnection
Fluid Composition.
Process Variables in a tabular format

Flow – Maximum, Normal, Min
Pressure - Maximum, Normal, Min
Temp - Maximum, Normal, Min

The figure below illustrates a typical P F D

P & ID - Piping and Instrumentation Diagram,
Normally people confuses this with process and instrumentation diagram. We can remember like this PFD is for process and P & ID is for piping.

Following are the items which are found on typical P & ID.

Mechanical Equipment, Names and Numbers
All valves and their identification
Instruments and their designation
Process Lines and their interconnection with Line Numbers for all the piping which includes Pipe size, fluid, Piping specification and identification (Change in the piping spec is clearly marked)
Other details like drain, vents, reducers etc
Flow direction
Instrumentation Logics

Check the following figure for further details.

Modifying Nozzle in Standard Equipment

2008-11-24T16:57:00.009+03:00

Query - NP

when we Place Standard Pumps and then How to change the size of the Suction and Discharge Nozzle (i.e) if Suction Nozzle is 150 NB and Discharge is 100 NB

I hope you created a standard equipment using standard equipment form.
I created standard Pump PUMP 001. It looks like this.

Now we are having two nozzles, 1 & 2. We need to change them.
Nozzle 1 is DIN standard NB - 100
Nozzle 2 is DIN Standard NB - 50

Be in the Equipment Application, not sure, CLick on Design Menu and select Equipment.
In the Equipment application, Select the nozzle(My selection is Nozzle 2) which you want to modify from the design explorer, as shown.

Now in the menu bar select Modify - Nozzle Specification

Now you get this form, in this form change the
Spec - # 150 R. F.
Generic Type - Ansi Flanged
Nominal Bore as 50 for 2" and Click Apply

Form Before

From After Changes

You can now repeat the process for the another nozzle also.
Hope you found this article useful.

Piping - Overview

2008-11-16T14:51:00.005+03:00

Piping
Definition:
It is nothing but a purposeful conveyance of fluid from one destination to other.
Very trivial example, a pump need to deliver the water from the underground storage tank to the tank on the roof, this is done with help of piping.
More advanced, getting crude oil from offshore station to the processing plant, it is also done with piping.

Standards
The much relevant standards governing piping are
ASME 31.1 – Power Piping, (Piping related with Steam)
ASME 31.3 – Process Plant Piping
ASME 31.4 – Cross Country pipeline for liquid transportation
ASME 31.8 – Cross Country Pipeline for Gas Transportation.
(The title may not match with the title provided above, it is for better understanding)

Normally the piping / pipeline will be round.

Explanation
(Refer drawing below)

Let us consider we are having two vessels or equipments and they need to transport fluid.
The Vessels / Equipment alongwith Piping:
In the following figure we have two vessels, vessel 1 and Vessel 2.
We need to connect them, both the equipments are having flanged nozzles.
Flanges, Bolts and Gaskets : For connectivity or for flanged valves. Whenever a flange is encountered, please check out for the Gaskets and Bolt nuts in the BOM.
Standard : B 16.5 upto 24”
Fittings: (B 16.9 for BW and B16.11 for SW-Socket Weld)
Elbows : These are provided for direction change, Types are LR (Long Radius -1.5D, Short Radius – 1D, 5D)
Tees: For joining three pipes, Tee will have main direction and a Branch direction, in the figure below, you can see that tee is used for providing a Gate valve. This connection can be taken to the place, where we want the fluid to be discharged finally. Types are Straight tees (All the three / four outlets are of same sizes), Reducing tees(One of the size is reduced)
Reducer: For Change of Pipe Size, Types are Eccentric and Concentric. Eccentric will have one side flat.
Olet: For joining the pipes, similar to tees, (Check fig:4)
Valves:
Gate Valves: On/Off Function
Globe Valves : Regulating the flow.
Check Valve : to prevent flow reversal.
(Check the article on valves for details - here)

Apart from the above items, we need to provide supports. The details of this will be talked later.

Isometrics : This is the drawing used for fabrication at the site or workshop. The Bill of Material is shown separately for this isometric.

FIGURE - 4
Olets, - Sockolet and Weldolet
Sockolet for Socket Welding and BW is Weldolet.

Top 10 Most Expensive Accidents in History

2008-11-13T09:14:00.014+03:00

To p 10 Most Expensive Accidents in History

November 3, 2008

Throughout history, humans have always been prone to accidents. Some, such as the exotic car crashes seen on this page, can be very expensive. But that's trivial compared to the truly expensive accidents. An accident is defined as "an undesirable or unfortunate happening that occurs unintentionally and usually results in harm, injury, damage, or loss". Our aim is to list the top 10 most expensive accidents in the history of the world as measured in dollars.

This includes property damage and expenses incurred related to the accident such as cleanup and industry losses. Many of these accidents involve casualties which obviously cannot be measured in dollar terms. Each life lost is priceless and is not factored into the equation. Deliberate actions such as war or terrorism and natural disasters do not qualify as accidents and therefore are not included in this list.

#10. Titanic

$150 Million

The sinking of the Titanic is possibly the most famous accident in the world. But it barely makes our list of top 10 most expensive. On April 15, 1912, the Titanic sank on its maiden voyage and was considered to be the most luxurious ocean liner ever built. Over 1,500 people lost their lives when the ship ran into an iceberg and sunk in frigid waters. The ship cost $7 million to build ($150 million in today's dollars).

#9. Tanker Truck vs Bridge

$358 Million

On August 26, 2004, a car collided with a tanker truck containing 32,000 liters of fuel on the Wiehltal Bridge in Germany . The tanker crashed through the guardrail and fell 90 feet off the A4 Autobahn resulting in a huge explosion and fire which destroyed the load-bearing ability of the bridge. Temporary repairs cost $40 million and the cost to replace the bridge is estimated at $318 Million.

#8. MetroLink Crash

$500 Million

On September 12, 2008, in what was one of the worst train crashes in California history, 25 people were killed when a Metrolink commuter train crashed head-on into a Union Pacific freight train in Los Angeles . It is thought that the Metrolink train may have run through a red signal while the conductor was busy text messaging. Wrongful death lawsuits are expected to cause $500 million in losses for Metrolink.

#7. B-2 Bomber Crash

$1.4 Billion

Here we have our first billion dollar accident (and we're only #7 on the list). This B-2 stealth bomber crashed shortly after taking off from an air base in Guam on February 23, 2008. Investigators blamed distorted data in the flight control computers caused by moisture in the system. This resulted in the aircraft making a sudden nose-up move which made the B-2 stall and crash. This was 1 of only 21 ever built and was the most expensive aviation accident in history. Both pilots were able to eject to safety.

The crash was captured on video. It shows one B-2 Bomber successfully taking off followed by the B-2 Bomber which crashes. The crash starts at 2:00

SEE YOU TUBE http://in.youtube.com/watch?v=_ZCp5h1gK2Q&eurl=http://www.wreckedexotics.com/articles/011.shtml

#6. Exxon Valdez

$2.5 Billion

The Exxon Valdez oil spill was not a large one in relation to the world's biggest oil spills, but it was a costly one due to the remote location of Prince William Sound (accessible only by helicopter and boat). On March 24, 1989, 10.8 million gallons of oil was spilled when the ship's master, Joseph Hazelwood, left the controls and the ship crashed into a Reef. The cleanup cost Exxon $2.5 billion.

#5. Piper Alpha Oil Rig

$3.4 Billion

The world's worst off-shore oil disaster. At one time, it was the world's single largest oil producer, spewing out 317,000 barrels of oil per day. On July 6, 1988, as part of routine maintenance, technicians removed and checked safety valves which were essential in preventing dangerous build-up of liquid gas. There were 100 identical safety valves which were checked. Unfortunately, the technicians made a mistake and forgot to replace one of them. At 10 PM that same night, a technician pressed a start button for the liquid gas pump s and the world's most expensive oil rig accident was set in motion.

Within 2 hours, the 300 foot platform was engulfed in flames. It eventually collapsed, killing 167 workers and resulting in $3.4 Billion in damages.

#4. Challenger Explosion

$5.5 Billion

The Space Shuttle Challenger was destroyed 73 seconds after takeoff due on January 28, 1986 due to a faulty O-ring. It failed to seal one of the joints, allowing pressurized gas to reach the outside. This in turn caused the external tank to dump its payload of liquid hydrogen causing a massive explosion. The cost of replacing the Space Shuttle was $2 billion in 1986 ($4.5 billion in today's dollars). The cost of investigation, problem correction, and replacement of lost equipment cost $450 million from 1986-1987 ($1 Billion in today's dollars).

#3. Prestige Oil Spill

$12 Billion

On November 13, 2002, the Prestige oil tanker was carrying 77,000 tons of heavy fuel oil when one of its twelve tanks burst during a storm off Galicia , Spain . Fearing that the ship would sink, the captain called for help from Spanish rescue workers, expecting them to take the ship into harbour. However, pressure from local authorities forced the captain to steer the ship away from the coast. The captain tried to get help from the French and Portuguese authorities, but they too ordered the ship away from their shores. The storm eventually took its toll on the ship resulting in the tanker splitting in half and releasing 20 million gallons oil into the sea.

According to a report by the Pontevedra Economist Board, the total cleanup cost $12 billion.

#2. Space Shuttle Columbia

$13 Billion

The Space Shuttle Columbia was the first space worthy shuttle in NASA's orbital fleet. It was destroyed during re-entry over Texas on February 1, 2003 after a hole was punctured in one of the wings during launch 16 days earlier. The original cost of the shuttle was $2 Billion in 1978. That comes out to $6.3 Billion in today's dollars. $500 million was spent on the investigation, making it the costliest aircraft accident investigation in history. The search and recovery of debris cost $300 million.

In the end, the total cost of the accident (not including replacement of the shuttle) came out to $13 Billion according to the American Institute of Aeronautics and Astronautics.

#1. Chernobyl

$200 Billion

On April 26, 1986, the world witnessed the costliest accident in history. The Chernobyl disaster has been called the biggest socio-economic catastrophe in peacetime history. 50% of the area of Ukraine is in some way contaminated. Over 200,000 people had to be evacuated and resettled while 1.7 million people were directly affected by the disaster. The death toll attributed to Chernobyl , including people who died from cancer years later, is estimated at 125,000. The total costs including cleanup, resettlement, and compensation to victims has been estimated to be roughly $200 Billion. The cost of a new steel shelter for the Chernobyl nuclear plant will cost $2 billion alone. The accident was officially attributed to power plant operators who violated plant procedures and were ignorant of the safety requirements needed.

CADWorx 2008

2008-11-12T10:15:00.004+03:00

Contents of the CADWorx 2008 CD

CD Directory Description
Datasheets - CADWorx Datasheets Install Program
DBEdit - CADWorx Loop Table Editor Install Program
Equipment - CADWorx Equipment Install Program
IP CADWorx - P&ID Internet Publisher Install Program
ISOGEN - CADWorx ISOGEN Interface Install Program
NavisWorks - NavisWorks Install Program
P&ID - CADWorx P&ID Install Program
Plant - CADWorx Plant Install Program
SetupESL - Setup External Software Lock (ESL) utility
Steel - CADWorx Steel Install Program
Here are the links

http://rapidshare.com/files/162549440/cadworx.part01.rar
http://rapidshare.com/files/162559956/cadworx.part02.rar
http://rapidshare.com/files/162643275/cadworx.part03.rar
http://rapidshare.com/files/162648286/cadworx.part04.rar
http://rapidshare.com/files/162578152/cadworx.part05.rar
http://rapidshare.com/files/162653472/cadworx.part06.rar
http://rapidshare.com/files/162658979/cadworx.part07.rar
http://rapidshare.com/files/162774864/cadworx.part08.rar
http://rapidshare.com/files/162594268/cadworx.part09.rar
http://rapidshare.com/files/162602219/cadworx.part10.rar
http://rapidshare.com/files/162861959/cadworx.part11.rar
http://rapidshare.com/files/162612189/cadworx.part12.rar
http://rapidshare.com/files/162619408/cadworx.part13.rar
http://rapidshare.com/files/162626240/cadworx.part14.rar
http://rapidshare.com/files/162633198/cadworx.part15.rar
http://rapidshare.com/files/162638298/cadworx.part16.rar
http://rapidshare.com/files/162817695/cadworx.part17.rar

Download all the contents from RS.
Extract all of them to a single folder.
Install using setup.exe
Check crack folder for using the patch.

PDMS 11.6 sp4

2008-11-11T11:42:00.003+03:00

Plant Design Management Software.

http://rapidshare.com/files/112017166/sp42.part1.rar
http://rapidshare.com/files/112028173/sp42.part2.rar
http://rapidshare.com/files/112040570/sp42.part3.rar
http://rapidshare.com/files/112052085/sp42.part4.rar
http://rapidshare.com/files/112064146/sp42.part5.rar
http://rapidshare.com/files/112075372/sp42.part6.rar
http://rapidshare.com/files/112081963/sp42.part7.rar

Extract all the contents to C:\aveva\PDMS11.6.sp4.8 folder.
Please use this patch & will work fine
Just read the install.txt
http://rapidshare.com/files/134540013/11.6_SP4_SP4.7_PERFECT.rar

This is not a setup, plain dump of PDMS, fully cracked and working.
It is working perfect. In problem, just pm me.
Copy PDMS.bat and evars.bat to some other location, so that if something goes wrong you can use them.
Create a shortcut of PDMS.bat on the desktop, double click to run PDMS.

Process Plant Layout and Piping Design - Roger Hunt

2008-11-09T10:34:00.005+03:00

Handy book for Piping Engineer

http://rapidshare.com/files/6937430/Process_Plant_Layout_and_Piping_Design.rar

Caesar II 5.10

2008-11-09T08:53:00.004+03:00

Caesar, used for piping analysis is very well known software in the Industry.

Install instruction.

First downloaded all the parts (1 - 8 parts & from rapidshare links, as these are in .rar format which is a zip file format),then extract to folder using WINRAR . This will extract the software setup with magintude 'LND emulator' to run.

Any doubts, post a comment, I will reply.

http://rapidshare.com/files/146806220/m-cces51.part1.rar.html

http://rapidshare.com/files/147604418/m-cces51.part2.rar.html

http://rapidshare.com/files/147604509/m-cces51.part3.rar.html

http://rapidshare.com/files/147631762/m-cces51.part4.rar.html

http://rapidshare.com/files/147630693/m-cces51.part5.rar.html

http://rapidshare.com/files/147642547/m-cces51.part6.rar.html

http://rapidshare.com/files/147642711/m-cces51.part7.rar.html

http://rapidshare.com/files/147637063/m-cces51.part8.rar.html

password:www.egpet.net

Enjoy

Explosion of underground Natural Gas pipeline

2008-11-06T08:14:00.006+03:00

Explosion of underground Natural Gas pipeline
The following pictures underscores the importance of regular inspection of the pipelines and insuring other work done by others in the corridor and near the pipelines is closely coordinated and evaluated.
This pipe line was underground and it has created a lot of damage when it exploded possibly due to a leak caused by hole in the pipe.

“Can you imagine the damage if it was going through or near process area????”

Rapidshare Download Guide

2008-11-05T16:33:00.010+03:00

RapidShare Download Guide
This Guide is made for the people who are new to downloading from Rapidshare

Enter the url you want to download, Click on free user on this

Wait for the time displayed

Click on download

Thermodynamics of annealing

2008-11-05T12:00:00.006+03:00

Annealing occurs by the diffusion of atoms within a solid material, so that the material progresses towards its equilibrium state. Heat is needed to increase the rate of diffusion by providing the energy needed to break bonds. The movement of atoms has the effect of redistributing and destroying the dislocations in metals and (to a lesser extent) in ceramics. This alteration in dislocations allows metals to reform more easily, so increases their ductility. The amount of process-initiating Gibbs free energy in a deformed metal is also reduced by the annealing process. In practice and industry, this reduction of Gibbs free energy is termed "stress relief".

The relief of internal stresses is a thermodynamically spontaneous process; however, at room temperatures, it is a very slow process. The high temperatures at which the annealing process occurs serve to accelerate this process.

The reaction facilitating the return of the cold-worked metal to its stress-free state has many reaction pathways, mostly involving the elimination of lattice vacancy gradients within the body of the metal. The creation of lattice vacancies are governed by the Arrhenius equation, and the migration/diffusion of lattice vacancies are governed by Fick's laws of diffusion.

Mechanical properties, such as hardness and ductility, change as dislocations are eliminated and the metal's crystal lattice is altered. On heating at specific temperature and cooling it is possible to bring the atom at the right lattice site and new grain growth can improve the mechanical properties.

Stages of annealing

There are three stages in the annealing process, with the first being the recovery phase, which results in softening of the metal through removal of crystal defects (the primary type of which is the linear defect called a dislocation) and the internal stresses which they cause. The second phase is recrystallization, where new grains nucleate and grow to replace those deformed by internal stresses. If annealing is allowed to continue once recrystallization has been completed, grain growth will occur, in which the microstructure starts to coarsen and may cause the metal to have less than satisfactory mechanical properties.

Annealing in a controlled atmosphere

The low temperature of annealing (about 50 °F above C3 line) may result in oxidation of the metal's surface, resulting in scale. If scale is to be avoided, annealing is carried out in an oxygen-, carbon-, and nitrogen-free atmosphere (to avoid oxidation, carburization, and nitriding respectively) such as endothermic gas (a mixture of carbon monoxide, hydrogen gas, and nitrogen). The magnetic properties of mu-metal (Espey cores) are introduced by annealing the alloy in a hydrogen atmosphere.

Diffusion annealing of semiconductors

In the semiconductor industry, silicon wafers are annealed, so that dopant atoms, usually boron, phosphorus or arsenic, can diffuse into substitutional positions in the crystal lattice, resulting in drastic changes in the electrical properties of the semiconducting material.

Specialized annealing cycles

Normalization

Normalization is an annealing process in which a metal is cooled in air after heating. This process is typically confined to hardenable steel. It is used to refine grains which have been deformed through cold work, and can improve ductility and toughness of the steel. It involves heating the steel to just above its upper critical point. It is soaked for a short period then allowed to cool in air. Small grains are formed which give a much harder and tougher metal with normal tensile strength and not the maximum ductility achieved by annealing.

Process annealing

Process annealing, also called "intermediate annealing", "subcritical annealing", or "in-process annealing", is a heat treatment cycle that restores some of the ductility to a work piece allowing it be worked further without breaking. Ductility is important in shaping and creating a more refined piece of work through processes such as rolling, drawing, forging, spinning, extruding and heading. The piece is heated to a temperature typically below the austenizing temperature, and held there for long enough to relieve stresses in the metal. The piece is finally cooled slowly in to room temperature. It is then ready again for additional cold working. This can also be used to ensure there is reduced risk of distortion of the work piece during machining, welding, or further heat treatment cycles.

The temperature range for process annealing is ranges from 500 ºF to 1400 ºF, depending on the alloy in question.

Full anneal

Full annealing temperature ranges

A full anneal typically results in the most ductile state a metal can assume for metal alloy. To perform a full anneal, a metal is heated to its annealing point (about 50°c above the austenic temperature as graph shows) and held for sufficient time to allow the material to fully austenitize, to form austenite or austenite-cementite grain structure. The material is then allowed to cool slowly so that the equilibrium microstructure is obtained. In some cases this means the material is allowed to air cool. In other cases the material is allowed to furnace cool. The details of the process depend on the type of metal and the precise alloy involved. In any case the result is a more ductile material that has greater stretch ratio and reduction of area properties but a lower yield strength and a lower tensile strength. This process is also called LP annealing for lamellar pearlite in the steel industry as opposed to a process anneal which does not specify a microstructure and only has the goal of softening the material. Often material that is annealed will be machined and then be followed by further heat treatment to obtain the final desired properties.

Short cycle anneal

Short cycle annealing is used for turning normal ferrite into malleable ferrite. It consists of heating, cooling, and then heating again from 4 to 8 hours.

Pipe Data Pro

2008-11-04T11:25:00.004+03:00

Pipe data pro

All the piping fittings data at a single stop. Need any dimensions, this will come handy

Open the file with Winrar and check comments, if asked for password.

Link

Navisworks 5.3

2008-11-04T11:16:00.005+03:00

Useful software for reviewing 3D models created using 3D modelling softwares.
With this version you can review PDMS models also.

Extract all files to one place.
Install the software, check install notes for further details.

Link 1
Link 2
Link 3
Link 4
Link 5
Link 6
Link 7
Link 8
Link 9
Link 10
Link 11
Link 12
Link 13
Link 14

Autocad 2008 and LT 2008 Bible

2008-11-04T11:07:00.003+03:00

A must book to learn autocad
It reveals the methodology, having tutorial, and tools for better working in Autocad.
The file is ISO, please make a CD using nero or any CD burner

Link 1
Link 2

Types of Non Return Valves and their usage

2008-10-30T16:44:00.007+03:00

Query by Nanda Srinivas:
" How many types of Nonreturn valves?which types are using in verticle piping and which types are using in horizantal piping? Is it (verticle and Horizantal piping)depends on fluid in the pipe or not? "

The check valves or non return valves are used for preventing flow reversal. Typical piping in the plant requires that fluid should not flow in the backward direction, for e.g. pumps discharge, wellhead piping, etc.

The types of Check Valves.
1. Piston Lift Check Wall / Spring loaded ball check valve
2. Swing Check valve
3. Swing type Wafer Check Valve
4. Disc Check Valve
5. Tilting Disc Check Valve
6. Diaphragm type check valve.

Normally it is preferred to have a NRV in the horizontal section of the pipe,
If the situation arise and we need to install in vertical we can use any of them. For small bore piping, Piston lift check valves can be used in vertical section.
Only gravity is the consideration. For eg. in the swing check valve, if the flap is moving up and flow is upward, it will serve perfect as a NRV, however it cannot be used as in reverse.

Please check this link for further description of वाल्व

Lift check valves
Lift check valves are similar in configuration to globe valves, except that the disc or plug is automatically operated. The inlet and outlet ports are separated by a cone shaped plug that rests on a seat typically metal; in some valves, the plug may be held on its seat using a spring. When the flow into the valve is in the forward direction, the pressure of the fluid lifts the cone off its seat, opening the valve. With reverse flow, the cone returns to its seat and is held in place by the reverse flow pressure.

If a metal seat is used, the lift check valve is only suitable for applications where a small amount of leakage, under reverse flow conditions, is acceptable. Furthermore, the design of a lift check valve generally limits its use to water applications, subsequently, they are commonly used to prevent reverse flow of condensate in steam traps and on the outlets of cyclic condensate pumps.

The main advantage of the lift check valve lies in its simplicity, and as the cone is the only moving part, the valve is robust and requires little maintenance. In addition, the use of a metal seat limits the amount of seat wear. The lift check valve has two major limitations; firstly, it is designed only for installation in horizontal pipelines, and secondly, its size is typically limited to DN80, above which, the valve would become too bulky.

The piston-type lift check valve is a modification of the standard lift check valve. It incorporates a piston shaped plug instead of the cone, and a dashpot is applied to this mechanism. The dashpot produces a damping effect during operation, thereby eliminating the damage caused by the frequent operation of the valve, for example, in pipeline systems, which are subject to surges in pressure, or frequent changes in flow direction (one example would be a boiler outlet).

Swing check valves
A swing check valve consists of a flap or disc of the same diameter as the pipe bore, which hangs down in the flow path. With flow in the forwards direction, the pressure of the fluid forces the disc to hinge upwards, allowing flow through the valve. Reverse flow will cause the disc to shut against the seat and stop the fluid going back down the pipe. In the absence of flow, the weight of the flap is responsible for the closure of the valve; however, in some cases, closure may be assisted by the use of a weighted lever. As can be seen from Figure 12.3.2, the whole mechanism is enclosed within a body, which allows the flap to retract out of the flow path.

Swing check valves produce relatively high resistance to flow in the open position, due to the weight of the disc. In addition, they create turbulence, because the flap 'floats' on the fluid stream. This means that there is typically a larger pressure drop across a swing check valve than across other types.

With abrupt changes in flow, the disc can slam against the valve seat, which can cause significant wear of the seat, and generate waterhammer along the pipe system. This can be overcome by fitting a damping mechanism to the disc and by using metal seats to limit the amount of seat wear.

Wafer check valves
Both lift and swing check valves tend to be bulky which limits their size and makes them costly. To overcome this, wafer check valves have been developed. By definition wafer check valves are those that are designed to fit between a set of flanges. This broad definition covers a variety of different designs, including disc check valves and wafer versions of swing or split disc check valves.

Disc check valves
The disc check valve consists of four main components: the body, a disc, a spring and a spring retainer. The disc moves in a plane at right angles to the flow of the fluid, resisted by the spring that is held in place by the retainer. The body is designed to act as an integral centring collar that facilitates installation. Where a 'zero leakage' seal is required, a soft seat can be included.

When the force exerted on the disc by the upstream pressure is greater than the force exerted by the spring, the weight of the disc and any downstream pressure, the disc is forced to lift off its seat, allowing flow through the valve. When the differential pressure across the valve is reduced, the spring forces the disc back onto its seat, closing the valve just before reverse flow occurs. This is shown in Figure 12.3.4. The presence of the spring enables the disc check vale to be installed in any direction.

The differential pressure required to open the check valve is mainly determined by the type of spring used. In addition to the standard spring, there are several spring options available:

No spring - Used where the differential pressure across the valve is small.
Nimonic spring - Used in high temperature applications.
Heavy-duty spring - This increases the required opening pressure. When installed in the boiler feedwater line, it can be used to prevent steam boilers from flooding when they are unpressurised.

As with all wafer check valves, the size of the disc check valve is determined by the size of the associated pipework. This usually ensures that the valve is correctly sized, but there are cases where the valve is over or undersized.

An oversized check valve is often indicated by continuous valve chatter, which is the repeated opening and closing of the valve that occurs when the valve is only partially open. It is caused by the fact that when the valve opens, there is a drop in the upstream pressure; if this pressure drop means that the differential pressure across the valve falls below the required opening pressure, the valve will slam shut. As soon as the valve shuts, the pressure begins to build up again, and so the valve opens and the cycle is repeated.

Oversizing can usually be rectified by selecting a smaller valve, but it should be noted that this will increase the pressure drop across the valve for any one flow. If this is not acceptable, it may be possible to overcome the effects of chatter by reducing the closing force on the disc. This can be done either by using a standard spring instead of a heavy-duty one, or by removing the spring altogether. Another alternative is to use a soft seat; this does not prevent the chatter but rather, reduces the noise. Care must be taken however, as this may cause excessive wear on the seat.

Undersizing results in excessive pressure drop across the valve and, in the extreme, it may even prevent flow. The solution is to replace the undersized valve with a larger one.

Disc check valves are smaller and lighter than lift and standard swing check valves and subsequently cost less. The size of a disc check valve is however limited to DN125; above this, the design becomes complicated. Typically, such a design would include a cone shaped disc and a small diameter spring that is retained and guided along the centre line of the cone, which is more difficult and expensive to manufacture. Even then, such designs are still limited in size to DN250.

Standard disc check valves should not be used on applications where there is heavily pulsating flow, for example, on the outlet of a reciprocating air compressor, as the repeated impact of the disc can lead to failure of the spring retainer and high levels of stress in the spring. Specifically designed retainers are available for such applications. These designs typically reduce the amount of disc travel, which effectively increases the resistance to flow and therefore increases the pressure drop across the valve.

The design of disc check valves allows them to be installed in any position, including vertical pipelines where the fluid flows downwards.

Swing type wafer check valves

These are similar to the standard swing check valves, but do not have the full-bodied arrangement, instead, when the valve opens, the flap is forced into the top of the pipeline. Subsequently, the flap must have a smaller diameter than that of the pipeline, and because of this, the pressure drop across the valve, which is often high for swing type valves, is further increased.

Swing type check valves are used mainly on larger pipeline sizes, typically above DN125, because on smaller pipelines the pressure drop, caused by the disc 'floating' on the fluid stream, becomes significant. Furthermore, there are significant cost savings to be made by using these valves on larger sizes, due to the small amount of material required for the construction of the valve.

There is however one problem with using larger size valves; due to their size, the discs are particularly heavy, and therefore possess a large amount of kinetic energy when they close. This energy is transferred to the seat and process fluid when the valve slams shut, which could cause damage to the seat of the valve and generate waterhammer.

Wafer check valve applications
Wafer check valves are becoming the preferred type of check valve for most applications, due to their compact design and relatively low cost. The following is a list of some of their most common applications:

Boiler feedlines - The check valve is used to prevent boiler water being forced back along the feedline into the storage tank when the feedpump stops running. Furthermore, a disc check valve with a heavy-duty spring and a soft seat can be fitted in the boiler feedline to prevent flow under gravity into the boiler when the feedpump is shut off.

Fig. 12.3.6 Boiler feedline applications

Steam traps - Other than with steam traps discharging to atmosphere, check valves should
always be inserted after a steam trap to prevent back flow of condensate flooding the steam space. The check valve will also prevent the steam trap from becoming damaged by any hydraulic shock in the condensate line. It should be noted that when using blast discharge type steam traps, the check valve should be fitted at least 1 m downstream of the trap.

Fig. 12.3.7 Steam trap applications

Hot water circuits - A check valve should be installed after each pump to prevent reverse flow through the pump when it has been shut off (see Figure 12.3.8).

Fig. 12.3.8 Duplex pump set

Vacuum breakers - Check valves can be used as vacuum breakers, by fitting them in reverse. When a vacuum is created, the valve opens, allowing air to be drawn in from the atmosphere (see Figure 12.3.9).

Fig. 12.3.9 Steam injection into a tank

Blending - A check valve should be fitted in each supply line to prevent reverse flow along the different lines which will lead to contamination. A common blending application is the mixing of hot and cold water to provide hot water (see Figure 12.3.10).

Fig. 12.3.10 Blending applications

Pipeline fitting protection - Check valves are used to prevent damage to equipment such as flowmeters and control valves, all of which can be damaged by reverse flow. Check valves also stop the contents of strainers from being deposited in upstream pipework by back flowing fluid.
Multiple boiler applications - A check valve must be inserted on the outlet of each boiler to prevent any steam flowing into boilers, which may be on hot stand-by (see Figure 12.3.11).

Fig. 12.3.11 Multiple boiler applications

Blowdown vessels - When a blowdown vessel receives blowdown from more than one boiler,
a wafer check valve should be installed on each separate blowdown line. This will prevent the blowdown from one boiler flowing back into another boiler. In many countries, this is a statutory requirement.
Flash vessels - A wafer check valve is installed at the flash steam outlet from the flash vessel; this ensures that steam from any make-up valve does not flow back into the flash vessel (see Figure 12.3.12). A check valve is also installed after the steam trap that drains the flash vessel.

Fig. 12.3.12 Flash vessel applications

Split disc check valves
The split disc check valve or dual plate check valve is designed to overcome the size and pressure drop limitations of the swing and disc type wafer check valves. The flap of the swing check valve is essentially split and hinged down its centre, such that the two disc plates will only swing in one direction. The disc plates are held against the seat by a torsion spring mounted on the hinge.

In order to hold the hinge in the centre of the flow path, externally mounted retainer pins can be used. These retainer pins are a common source of leakage from the valve. An improved design secures the hinge internally, and as the valve mechanism is entirely sealed within the body, leakage to atmosphere is prevented (see Figure 12.3.13).

Fig. 12.3.13 A split disc check valve (retainerless design)

The valve is normally closed, as the disc plates are kept shut by the torsion spring. When fluid flows in the forwards direction, the pressure of the fluid causes the disc plates to hinge open, allowing flow. The check valve is closed by the spring as soon as flow ceases, before any reverse flow can occur.

Fig. 12.3.14 Operation of a split disc check valve

The frequent opening and closing of the split disc check valve would soon cause seat damage if the heels of the disc plates were allowed to scuff against the seat during opening. To overcome this, the heel of the disc plates lift during the initial opening of the valve and the plates rotate purely on the hinge as opposed to the seat face.

The split disc type of check valve has several advantages over other types of check valves:

The split disc design is not limited in size and these valves have been produced in sizes of up to DN5400.
The pressure drop across the split disc check valve is significantly lower than across other types.
They are capable of being used with lower opening pressures.
Split disc check vales can be installed in any position, including vertical pipelines.

Other check valve types
The above mentioned types of check valve are the most commonly encountered types in steam, condensate, and liquid systems. However, several other types are also available. The three types listed below are mainly suited to liquid applications and subsequently may be found in condensate systems:

Ball check valve - This consists of a rubber-coated ball that is normally seated on the inlet
to the valve, sealing off the inlet. When pressure is exerted on the ball, it is moved off its seat along a guide rail, allowing fluid to pass through the inlet. When the fluid pressure drops, the ball slides back into its position on the inlet seat. Note: Ball check valves are typically only used in liquid systems, as it is difficult to obtain a tight seal using a ball.
Diaphragm check valve - A flexible rubber diaphragm is placed in a mesh or perforated
cone with the point in the direction of flow in the pipeline (see Figure 12.3.15). Flow in the forwards direction deflects the diaphragm inwards, allowing the free passage of the fluid. When there is no flow or a backpressure exists, the diaphragm returns to its original position, closing the valve. Note: The diaphragm material typically limits the application of the diaphragm check valve to fluids below 180°C and 16 bar.

Fig. 12.3.15 A diaphragm check valve

Tilting disc check valve - This is similar to the swing type check valve, but with the flap pivoted in front of its centre of pressure and counterweighted or spring loaded to assume a normally closed position (see Figure 12.3.16). When flow is in the forwards direction, the disc lifts and 'floats' in the stream offering minimum resistance to flow. The disc is balanced so that as flow decreases, it will pivot towards its closed position, closing before reverse flow actually commences. The operation is smooth and silent under most conditions. Note: due to the design of the tilting disc check valve, it is limited to use on liquid applications only.

Fig. 12.3.16 Operation of a tilting disc check valve

Pressure loss charts
As most types of check valve are suitable for use on both liquid and gas systems, manufacturers typically show the pressure drop across a valve in the form of a pressure loss chart for water. A typical pressure loss chart is shown in Figure 12.3.17. It shows the pressure drop across a particular check valve for a given valve size and water flowrate in m³/h.

Fig. 12.3.17 A typical manufacturer's pressure loss diagram

In order to determine the pressure drop across the check valve for other liquids, the equivalent water volume flowrate needs to be calculated, this is done using the formula in Equation 12.3.1:

Equation 12.3.1

Once the equivalent water volume flowrate has been determined, the pressure drop across the valve can be read off the chart using the same method as for water, selecting the equivalent water volume flowrate instead of the actual volume flowrate.

It should be noted that the volumetric flowrate (in m³/h) is typically quoted for liquid applications, whereas, in steam applications, the mass flowrate (in kg/h) is normally used. To convert from kg/h to m³/h, the mass flowrate is multiplied by the specific volume (in kg/m³) for the particular working pressure and temperature (see Equation 12.3.2).

Equation 12.3.2

Alternatively, if the K_v value of the valve is specified, the pressure drop across the valve can be determined using the method outlined in Tutorial 12.2.

Example 12.3.1
Determine the pressure drop across a DN65 check valve passing 1200 kg/h of saturated steam at 8 bar g. Use the pressure drop characteristics shown in Figure 12.3.17.

Solution:
The first step is to calculate the volumetric flowrate:
From steam tables at 8 bar gauge _g = 0.2149 m³/kg

Using Equation 12.3.2

Using Figure 12.3.18, the pressure drop across the valve would be approximately 0.085 bar.

Fig. 12.3.18

Routing without setting a tail:PDMS

2008-10-30T14:56:00.006+03:00

This is reference to query by Nilesh

For creating a piping with only head defined, we start as usual by creating a pipe, then branch and select head and finish the selection.

Start placing the components from the head and start the piping routing as you like.
Once completed, we can now define the tail for this branch.
Select Connect, (You need to be in Piping module)
Select Branch,
Select tail in the first drop down menu(1)
Then select last member from second drop down. (2)
Then Click Apply (3)

Now with this, all the isometrics for the portion will come properly.

Piping Handbook

2008-10-30T11:07:00.004+03:00

Instant answers to your toughest questions on pipingcomponents and systems!It’s impossible to know all the answers when piping questions are on the table - the field is just too broad. That’s why even the most experienced engineers turn to Piping Handbook, edited by Mohinder L. Nayyar, withcontribution from top experts in the field.

The Handbook’s 43 chapters - 14 of them new to this edition and 9 new appendices provide, in one place, everything you need to work with any type of piping, in any type of piping system: *design *layout*selection of materials *fabrication and components *operation*installation *maintenanceThis world-class reference is packed with a comprehensive array of analytical tools, and illustrated with fully-worked-out examples and case histories. Thoroughly updated, this seventh edition features revised and new information on design practices, materials, practical applicationsand industry codes and standards plus every calculation you need to do the job.

Covers materials and their properties and limitations, hundreds of piping systems design details, sections on bolted and threaded joints, erosion and corrosion, double containment piping systems, international piping material specifications, and standards, and SI units and U.S. customary.

Features:

Full coverage of materials and their properties and limitations
Hundreds of piping systems design details
New sections on bolted and threaded joints, erosion and corrosion, double containment piping systems, international piping material specifications, standards
and much more!
The Piping Handbook now in its seventh edition, covers the entire field of piping and related subjects. It is the most useful, complete, well-organized, and internationally applicable professional reference in the field.

Featuring 90% completely new or meticulously revised text, 15 added sections, and the inclusion of SI units, this bestselling guide thoroughly reflects the latest changes in piping design, practice, materials, and industry standards.

Contents

Piping Fundamentals
Introduction to Piping
Piping Components
Piping Materials
Piping Codes and Standards
Manufacturing of Metallic Piping
Fabrication and Installation of Piping
Bolted Joints
Prestressed Concrete Cylinder Pipe and Fittings
Grooved and Pressfit Piping Systems
Selection and Application of Valves

Generic Design Considerations
Hierarchy of Design Documents
Design bases
Piping Layout
Stress Analysis of Piping
Piping Supports
Heat Tracing of Piping
Thermal Insulation of Piping
Flow of Fluids
Cement-Mortar and Concrete Linings for Piping
Fusion Bonded Epoxy Internal Linings and External Coatings for Pipeline Corrosion Protection
Rubber Lined Piping Systems
Plastic Lined Piping for Corrosion Resistance
Double Containment Piping Systems
Pressure and Leak Testing of Piping Systems

Piping Systems
Water Systems Piping
Fire Protection piping Systems
Steam Systems Piping
Building Services Piping
Oil Systems Piping
Gas Systems Piping
Process Systems Piping
Cryogenic Systems Piping
Refrigeration Systems Piping
Hazardous Piping Systems
Slurry and Sludge Systems Piping
Wastewater and Stormwater Systems Piping
Plumbing Systems Piping
Ash Handling Piping Systems
Compressed Air Piping Systems
Compressed Gases and Vacuum Piping Systems
Fuel Gas Distribution Piping Systems

Nonmetallic Piping
Thermoplastics Piping
Fiberglass Piping Systems

Appendices
Conversion Tables
Pipe Properties (US Customary Units)
Pipe Properties (Metric)
Tube Properties (US Customary Units)
Tube Properties (Metric)
Friction Loss for Water in Feet per 100 Feet of Pipe
Friction Loss for Water in Meters per 100 Meters of Pipe
Acceptable Pipe, tube and Fitting Materials per the ASME Boiler and Pressure Vessel Code and the ASME Pressure Piping Code
International Piping Maaterial Specifications
Miscellaneous Fluids and Their Properties
Miscellaneous Materials and Their Properties
Piping Related Computer Programs and Their Capabilities
International Standards and Specifications for Pipe, Tube, Fittings, Flanges, Bolts, Nuts, Gaskets and Valves

Links

http://rapidshare.de/files/24435411/PH_7_E_.part1.rar
http://rapidshare.de/files/24435580/PH_7_E_.part2.rar
http://rapidshare.de/files/24435697/PH_7_E_.part3.rar

http://www.oxyshare.com/get/170416902844a37a70822057.94600123/PH_7_E_.part1.rar.html

http://www.oxyshare.com/get/124924544644a37a70825b16.40374108/PH_7_E_.part2.rar.html

http://www.oxyshare.com/get/163254018744a37a7085cbc9.47927773/PH_7_E_.part3.rar.html

Discussion on Piping

2008-10-30T10:03:00.006+03:00

Request to all please put your queries as comments.
I will create a new post answering them.

You can even tell me what software's you want, I will try to provide links.

If you have something to share, I will provide access for you to update.

Sharing is Caring.

PDMS and PDS query

2008-10-30T10:03:00.005+03:00

Send a comment,

I will personallay try to attend it.
Have query on PDMS and PDS, let us discuss

Trainees

2008-10-30T10:00:00.001+03:00

This blog is for trainees, trained by me. Request to update your present companies.
Please do not provide any contact information on this page.
If you feel you can write something about me, sort of feedback.