Saturday, November 5, 2011

ASH HANDLING SYSTEM


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The Ash Handling of modern day boilers can be categorized into two major types i.e. Mechanical type and Pneumatic Type.
Pipe Rack for Ash handling System
 We can divide Mechanical type ash handling broadly into: 1.Use of Screw/Belt Conveyors and Bucket Elevators.
The use of screw/belt conveyors and bucket elevators is mostly done in small capacity plants with capacities not exceeding 2-3 TPH.The Limitation of screw conveyors and bucket elevators is that it cannot handle huge capacities and is maintenance prone.
Power Plant
Densveyor Arrangement


2. The use of Chain Conveyors.
Use of chain conveyors is highly successful in higher capacity plants up to 7-8 TPH. The chain conveyors use forged link chains and can operate extreme conditions with high degree of reliability and very less power consumption. Chain conveyors with high temperature of the bank ash as the bottom of chain conveyors can be lined with cast basalt.
 

·Pneumatic type ash handling is the most popular method used in medium level power plants. It uses dense phase conveying system for conveying ash is totally enclosed without any leakage.
Conveying material moves through the pipeline slowly as a coherent slug at a low velocity, which ensures minimum wear and tear. The system can convey materials up to a distance of around 200-250 mts. The general principle of operation for dense phase pneumatic conveying is as below.
General Principal Operation for Dense Phase Pneumatic Conveying
1. Conveying material from the ash collecting equipment is collected in hopper and is sensed by the permissive level probe provided in hopper and initiates conveying cycle. The system has dual operability either through level probe or through an auto timer. In timer mode of operation the system goes on continuous cycle after a preset time interval. Moreover the system has manual override facility.
2. The inlet valve on the top of vessel opens and allows material to gravitate into the vessel. The valve closes after the preset adjustable time delay.
3. Once the valve closing is ensured through a limit switch valve its circumferential inflatable seal inflates and ensures complete leak proof.
4. Now, convey air is injected into the vessel after ensuring seal pressure. Thus vessel is pressurised and material resistance leads to pressure build up which conveys material to destination point.
5. When conveying is complete, the pressure drops down to near atmospheric pressure and is sensed by control system. The conveying air supply to the system is then stopped.
6. Now the system is ready to accept next charge of material on command from level probe/auto timer.
7. Normally the destination side is also provided with high-level switch, which gives an alarm when filled up and prevents any further transfer of material into it.
8. The system is provided with various accessories like bag filters, ash conditioner to make the system environmental friendly. In a typical ash handling plant, the ash storage silo is designed for 1-day storage. The ash in silo is discharged on a lorry through an ash conditioner, which sprays water in mist form and prevents the ash from escaping to the atmosphere.













Low-velocity Dense-phase Pneumatic Conveying Systems
The ultimate system for handling difficult-to-convey materials; hot, abrasive, and wet materials; or for providing gentle handling of products to prevent degradation of friable materials or separation of blended materials.

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BASIC ELECTRICAL DESIGN





What is Ash Handling?

Ash handling refers to the method of collection, conveying, interim storage and load out of various types of ash residue left over from solid fuel combustion processes.
The most common types of ash include bottom ash, bed ash, fly ash and ash clinkers resulting from the combustion of coal, wood and other solid fuels.
Ash handling systems may employ pneumatic ash conveying or mechanical ash conveyors.
A typical pneumatic ash handling system will employ vacuum pneumatic ash collection and ash conveying from several ash pick up stations-with delivery to an ash storage silo for interim holding prior to load out and transport. Pressurized pneumatic ash conveying may also be employed.
Coarse ash material such as bottom ash is most often crushed in clinker grinders (crushers) prior to being transported in the ash conveyor system.
Very finely sized fly ash often accounts for the major portion of the material conveyed in an ash handling system. It is collected from baghouse type dust collectors, electrostatic precipitators and other apparatus in the flue gas processing stream.
Ash mixers (conditioners) and dry dustless telescopic devices are used to prepare ash for transfer from the ash storage silo to transport vehicles.
 

Ash System Components


Combination Vacuum/Pressure Ash Handling Conveying Systems

Combination vacuum/pressure pneumatic ash conveying systems can be beneficially applied to take advantage of the simplicity of a vacuum system for the collection and delivery of ash to a transfer hopper from which it is reclaimed through an air lock feeding device for pressurized pnueumatic conveyance to a remote location silo for subsequent load out.

Silo 500Ton Silo erection on site for Ash Handling System 3x500Mw:


The Silo column after erection a ring beam with heavy fabrication placed on base plate. The bolts are tightened and the tie beam with other member are fixed in alignment. The Complete Silo erection to be done in many stages. The photos shows the final stages.

The 1500T Silo fabrication of Coulmn in intial stages are taken into utmost care for welding with good quality electrodes having high tensile strength. The bending machine is to be installed for the rolling of 10mm plate for making shell.The heavy bending machine is always required for bending of 40mmplate for ring beam.

This is really very precision heavy work to make shell in many parts and then it assembled with utmost care. The ash handling silo fabrication and erection is the first priority job which is to be taken in the early stages of project work.

The Civil Work for Cable Routing and Compressor House Building work:

In fact the civil work for excavation for cable route planned and casting of pedestal with raft are completed to all over from the substation to the transformer which is placed near the MCC room.The Trenches in the Compressor House Building are completed according to the its installation,routing of cables and its fixing arrangements etc. The cable tray support and cable Trays are fixed on the cable routing. The erection of Transformer and Bus duct are simultaneously taken. The Panels are placed on their base fixing arrangement.The Switch Gear Panel are installed according to their layout location. It is a proper planning are to be taken to all the above work during the rainy season. The digging the excavation work, casting the slabs, the civil work is more and consume major duration of Project. All MCC Panel were placed with plastic sheet wrapping so moisture could not enter into the inner control circuit.


THE GENERAL PROJECT SCHEDULE FOR COMPLETION:
OF COMPRESSRE HOUSE :
  • Cable pool pit between compressor room & SWGR building cable trench Approx. 15Cum
  • Vinaratex on external of compressor house building Approx.1000Sq.m
  • Internal POP Approx.950Sq.m
  • Oil bound distemper Approx.950 Sq.m
  • Fixing of Doors & Windows 15Nos. --Approx.70Sq.m
  • Roof Water Treatment -Approx.500Sq.m
  • Plinth Protection And Drain- Approx. 70 Sq.m

ELECTRICAL TESTING TO BE CARRIED OUT.
HT & LT Transformers tests :
1) Insulation Resistance Test ( With 5KV Megger)
2) Magnetizing Current test ( at Normal Tap)
3) Magnetic Balance Test ( at Normal Tap)
4) Ratio test
5) Vector Group test ( at Normal Tap)
6) Winding resistance test at HV Side & LV Side
7) Short Circuit Current test
8) Open Circuit test
9) Functional Test of Transformer
10) NCT, CT testing
11) Transformer Oil Break down strength
12) Oil Filtration & others as per the requirement of commissioning of transformer.

HT Panels & LT panels:
1) Insulation resistance Value before HV test & after HV test
2) High Voltage test.
3) Circuit breaker testing.
4) Current transformer test, Potential transformer test
5) Relays Functioning test
6) Protection & interlock , functional test of panels.
Bus Ducts :
i) Resistance Check (Obtain milli-volt drop test results for bus bar joints
(welded joints&bolted joints)
2) Earth Resistance test before HV test & after HV test
3) Leakage Current .
HT Cable & LT Cables : 1) Insulation resistance ( HV test ) before HV test & after HV test
2) Continuity test.
HT MOTORS & LT MOTORS:
1) Insulation Winding resistance test
2) Polarization index test
3) Vibration & Noise level test
4)) Functional test
                     
Pipe connections
Cable Layout for 33KV

Friday, November 4, 2011

PROJECT PLANNING


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Description on dense phase conveying and dilute phase conveying.

The Zenz diagram is widely accepted as a description of pneumatic conveying.

Since the calculation of a Zenz diagram is now possible by an extensive computer program, it is also possible to investigate how the diagram is formed.
Bulkblog article “Pneumatic Conveying, Performance and Calculations!. By varying the air flow at constant capacity, the resulting partial pressure drops were calculated and combined into a table.Zenz diagram







From The Graph following information can be Taken:
  1. Filter pressure drop increases with increasing air volume
  2. Gas pressure drop increases with increasing air volume
  3. Suspension pressure drop decreases with increasing air volume
  4. Elevation pressure drop decreases with increasing air volume
  5. Product pressure drop:
  • In case of sedimentation the product pressure drop decreases with increasing airflow.
  • Above sedimentation, the product pressure drop firstly increases with increasing airflow, due to the stronger influence of the velocity increase opposed to the influence of the SLR.
  • Above the airflow, whereby the influence of the decreasing SLR is stronger than the influence of the increasing velocity, the product pressure drop decreases with increasing airflow.
  • The acceleration pressure drop increases with increasing airflow.
6. The pressure drop for the material intake stays constant
7. The summation of the partial pressure drops for each airflow generates the Zenz curve.
8. The lowest point in the Zenz curve, where the pressure drop per meter is minimum, is the boundary between dense- and dilute phase conveying.
Left of this point, the pneumatic conveying is considered dense phase conveying.
In dense phase conveying the solid Loading Ratio (SLR) is higher than in dilute phase conveying.
As the absolute SLR is depending on the conveying length, the absolute SLR in it self is not an indication about the conveying regime being dense or dilute.
9. At lower airflows, sedimentation starts because of too low air velocities and at even lower velocities, the airflow changes from turbulent to non turbulent.
In that region the pneumatic conveying circumstances vary significantly with a small change in airflow.
Airflow changes can also occur through air surges, caused by material flow irregularities.
Induced pressure waves forces the pneumatic conveying conditions from f.i asub turbulent flow into a turbulent flow and combined with changes in sedimentation, the pneumatic conveying behavior can become unstable, which is often observed in practice.
When the graph is build up in the reverse order (from intake to filter), discontinuities show up in the curves for acceleration and product resistance.



The remarkable discontinuities in the graph are caused by the introduction of criteria for sedimentation and turbulence into the calculation algorithm.
10. The lowest energy consumption occurs at the point where the turbulence changes from turbulent to non turbulent.
Sedimentation is then already present.
The lowest pressure drop per meter is therefore not the most energy efficient conveying design.
This is because the energy is the multiplication of pressure and airflow.
Although the pressure is low, the airflow has increased more, resulting in a higher energy consumption.
In general an installation should be designed in dense phase in order to have the benefit of low energy consumption per ton. Although in dense phase, the installation is not necessarily optimal, regarding energy efficiency.
In case the design is in the region where sedimentation and turbulence changes are occurring and the material conveying properties are difficult under that regime, then additional measures have to be taken to ensure controlled “unstable” conveying or redesign to a stable conveying region.
Also irregular feeding can induce unstable behavior.
The magnitude in which these phenomena are occurring depends on installation time constants and -time responses to changes.
Whether an installation is operating in the dense phase mode or the dilute phase mode can only be concluded after calculations for different air flows have been executed.
Judging whether a conveying installation is in dense- or dilute phase just by the Solid Loading Ratio is useless, because a long pipe line (low SLR) can be in dense phase and a short pipe line (high SLR) van be in dilute phase.
These examples show that dense- and dilute phase pneumatic conveying are 2 regions by definition, but belong to the same pneumatic conveying technology.
In theoretical discussion, the interpretation can be very useful, but in practice it is not so important, because a properly designed installation should always be the installation with the lowest energy demand and still meeting the desired performance.
This could be a dense phase installation but a dilute installation as well.
The interpretation of dense- and dilute phase conveying should now be clear.
Que: Sir we are running the f.k.pump for last 20 Years@155-166tph with two Compressor having designed FAD of 56 m3/min each but measured value of FAD of 45m3/min each at @2kg/cm2 pressure. We are upgrading the cement mill for 225tph by installing V-seprator in the circuit so we are redesigning it for 225tph. I am doubtful wheather it will work smoothly at FAD of 60.6m3/min. Normal back pressure is coming around 1.0 bar but sometime we are facing tripping of the F.K.Pump due to high back pressure even at 155-160tph.Please clarify our doubt for smooth functioning at FAD of 60.6m3/min@225tph.
Ans. : Dear, The FK pump is the feeder of a pneumatic system.
The feeder function of the FK pump is 150-165 tons/hr against the pneumatic pressure. For FK pump,this pressure is limited at approx.1.8bar(O)
(For 150 tons /hr,the drive motor of the FK pump should be approx.110KW at 980rpm)
Increasing the FK pump capacity from 150tons/hr to 225 tons/hr will at least require a drive change to 165KW at 1500rpm or a new FK pump or an additional FK pump.
As you experience overloading tripping of your present FK pump drive motor,due to high conveying pressure,this is an indication that the pneumatic conveying system needs to be redesigned,to keep the conveying pressure at maximum of 1.8bar at225 tons/hr
Que:Can anybody give me the suggestion for the equation of calculation of pressure drop in pneumatic conveying of spherical granular material in horizontal pipe ?

I have used the Ergun equation but it gives higher pressure drop than the expected.

My Parameters:
Particle Diameter:- 3mm
Density of Fluid (Air) :- 1.2
Porosity:- 54.8%
Length of Pipe :- 1.5 m
Viscosity of Fluid (Air):- 1.8E-05
Superficial Velocity (Assumed):- 5m/s
I have used this book and on the page 232-233. I could find the equation for the calculation of pressure drop. Through that I could find expected pressure drop.

http://books.google.com/books?id=wnFRV_rZAwUC&printsec=frontcover&dq=Pneumatic+Conveying+of+Solids#v=onepage&q=&f=false

The equation is as follows,

Delta P = [fri.factor(fluid)*density(gas)*velocity(gas)*velocity(gas)*length(pipe)/2*Dia(pipe)*gravity]
+
[fri.factor(solid)*density(gas)*velocity(gas)*velocity(gas)*length(pipe)*solid loading ratio/2*Dia(pipe)*gravity]


But still I am confused about the exact value of gas(air) friction factor and loading ratio.


Here, I have attached one paper which is quite similar to my topic, from which I have used the Ergen equation (Equation no.5) for the calculation of pressure drop.
Ans :The equation you give,


Delta P = [fri.factor(fluid)*density(gas)*velocity(gas)*velocity(gas)*length(pipe)/2*Dia(pipe)*gravity]
+
[fri.factor(solid)*density(gas)*velocity(gas)*velocity(gas)*length(pipe)*solid loading ratio/2*Dia(pipe)*gravity]


is the summation of the gas only pressure drop plus the product loss pressure drop as a factor times the gas only pressure drop and proportional to the Solids Loading Ratio.

The SLR is defined as:

(mass flow of material)/(mass flow of gas) in f.i (kgs material/sec)/(kgs air/sec)

The above equation does not account for keeping the material in suspension, accelerating the material and elevating. This shortcoming cannot be incorporated in the fri.factor(solid), as these conditions vary widely for different installations.


Neither the material velocity (or slip velocity) is accounted for.
The slip velocity is depending on the suspension velocity of the material particles and the material loss factor.

The value of gas(air) friction factor is the fanning factor, which can be calculated by the
Swamee-Jain equation.

The formula, which you used is for Horizontal Low Velocity Slug Flow and not for dense- or dilute pneumatic conveying.

The research in pneumatic conveying has revealed many important phenomena, however, it never resulted in a uniform mathematical approach and easy, flexible to use calculation program (apart from some simple spreadsheets) that showed a transparent output.
Therefore, it is not safe, just to pick an equation from a book or article and apply that formula to your own situation.

It is understandable that universities and research laboratories focus on the theory of pneumatic conveying, but the manufacturers must develop working calculation programs that are in conformity with practice.
However, those manufacturers keep that information to themselves for commercial reasons.
In this forum, many pneumatic conveying questions are put forward and I try to answer them in such a way that a discussion about the principles of pneumatic conveying would emerge.
The latter, unfortunately, is not really happening.
.>>
There is no simple, reliable equation from which you can find out the pressure drop in your system.

There are a set of equations that can calculate the pressure drop over a short pipe distance dL.
Newton’s laws to calculate accelerations and velocity equations supplement these equations.
The integration of these calculated pressure drops over the total length gives you the total pressure drop.
The pressure drop for product losses requires a product loss factor and formula.
This product loss factor is determined from existing installations or tests.
Suspension velocity and SLR are some of the main parameters in these equations.

The integration method (plus an iteration process) is necessary because of the compressibility of the conveying gas.
The application of a computer facilitates the possibility of executing the high number of calculations to get to this result. (Visual Basic is a great tool to achieve this)

In addition, there are extra pressure drops involved, s.a. filters.

The parameters you supplied in your initial thread are not sufficient to perform a calculation.
At least the following values are needed:

Material
particle size
particle density
bulk density
(suspension velocity)
pipe geometry
capacity
Any other important information s.a. temperatures, altitude, etc.

Que:Dear sir,

I am an engineer working in plastic factory. Could you please give me the calculated results from following data.

Material to convey : Calcium carbonate
Conveying rate : 1500 kg / hrs.
Line diameter : 2 inch
Starting from the inlet, line is 4 meter horizontal, then 90 degree long radius bend, then line is 6 meter vertical, then 90 degree long radius bend connected to the inlet of receiving bin.
Conveying line material : stainless steel pipe
Use ambient air at standard conditions.

Need to know : pressure drop in a vacuum type conveying system and
: type of blower and power used

Your assistance is much appreciated.
How is the marerial fed into the pipe line.
Suction nozzle or rotary airlock or gravity mixing inlet?

Is there a rotary lock underneath the filter-receiver bin?

Material feeding influences the initial intake pressure drop.
A rotary lock underneath the receiving bin causes air leakage, which has to be compensated for by the vacuum pump.

Ans:I did a quick design calculation of which the results are given in the attached pdf.

These calculations can only be regarded as an indication.

1500 kg/hr is not much. (2 buckets per minute) and the distance (10 m) is very short.

Que :Theory and Design of Dilute Phase Pneumatic Conveying Systems ,Article:

The paper is a straight forward approach to the subject and is easy to follow, however,
- are there inconsistencies in the attached worksheet?
-- the roughness factor used seems to be 0.00015 instead of 0.0005
-- the pipe section in worksheet 2 section 9 was moved to section 10 in worksheet 3

- I do not feel comfortable when a pressure is given as mass/area rather than force/area, but this is just my problem with Newtons/sqm.

- Is it possible that the calculation method
-- does not represent the pressure drop minimum at the point of saltation velocity properly?
-- is wrong in regard to assuming a constant product friction multiplier over the whole velocity range?

- I miss some limits within which the formulae are applicable, like
-- maximum solid/gas ratio
-- minimum velocity depending on different products and particle sizes

- The Zenz equation also considers acceleration of the carrier gas, however, though the dp is small, it is not listed in the calculation table.
- What are common criterion for stepping up a pipe? Shall this be based on dynamic gas pressure, same pressure ratio for same diameter sections, Reynold number minimum, Froude number minimum?
- The gas pressure drop for bends can be calculated fairly accurately with a factor of 0.12. Is there a different way to calculate the pressure drop due to the product rather than using an equivalent length? Solids deceleration to xx% gas speed and re-acceleration as per W*Vp/4640 might be an option.

I have concerns whether the approach is as "easy" to apply to reality as it looks. I appreciate your comments ;-)

Ans :Thanks very much for your comments and questions on my article. My responses to these are given below:

1. The calculation method given in the article is correct. There are a few “typos”, i.e., mistakes that were made by the publisher in the process of printing. But most people who are conversant with Excel and the calculation method given in the article should be able to easily spot them out.

2. One mistake is in the equation for the Fanning Friction Factor. I will be happy to send the correct equation if you need it.

3. The other mistake is in Worksheet No. 3. Row Nos. 11 to 14 should all be moved up by one row.

4. The pipe line friction factor used in the sample calculations is for internally shot-peened pipe. This factor is 0.0005, not 0.00015.

5. All of the units used in the equations are correct. You may change them if you prefer any other units.

6. Calculation method is applicable to dilute phase only, up to the minimum pressure point. For calculations to be correct, solids velocity must be higher than the saltation velocity.

7. Please send your data that shows a relationship between the Solids Friction Factor and Solids Velocity. Information that I have does not show that there is this relationship.

8. Regarding putting limits in the calculations for maximum solids to gas ratio, this can be hone but the conveying system should be designed by people who know what they are doing. As regards putting a limit on minimum conveying velocity, this limit is the saltation velocity with an adequate safety factor. This velocity should be calculated using well-known co-relations given in the literature. It varies depending upon thm conveyed material, pipe line diameter, etc. I can send this co-relation to you if you need it.

9. For all practical purposes pressure drop due to the acceleration of gas is so small that it can be ignored, but it can be included in the calculations if someone wants to include it.

10. As regards criteria for stepping up a pipe line, this is another subject. It is not covered in the present article.

11. For bend pressure drop, the method given in the article is empirical but gives fairly correct results. The analytical method that you are thinking of requires accurate data on the effect of solids properties on decrease of solids velocity going through a bend. This complicated relationship can be mathematically derived, but its results may not be much better. This subject however is worth more study.

12. At the end you are saying “I have concerns whether the approach is as “easy” to apply to reality as it looks”. I am sure the calculation method given in the article can be converted into a software program to make it easier to use. But for those people who know Excel, I think that this method is quite easy to follow.

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