PAFL Report

8/14/2019 PAFL Report

1/25

Pak-American Fertilizer Plant

Iskandarabad Mainawali

Pakistan.

I


2/25

2

Report Submitted By

M. Saleem Iqbal (05)

M. Ahsan Nasir (10)

M. Umair Ashraf (16)

Basit Ali (17)

M. Usman (25)

Rameez-ul-Hassan (32)

M. Faheem Iqbal (37)

M. Imran Farooq (38)


3/25

3

CONTENTSHISTORY....................................................4

PROCESS DESCRIPTION............................4

AMMONIA SECTION.....................................5UREA SECTION............................................11

UTILITIES SECTION......................................15


4/25

4

HISTORY

The Plant is located at Iskanderabad, District Mianwali. It was the first nitrogenousPlant built in Pakistan. The project when commissioned in 1957, was designedto produce 40 metric tone per day of Ammonia to be fully converted into 150

metric tone per day of Ammonium Sulphate. The unit underwent expansion in 1968when the capacity was increased to 273 metric tones per day i.e. 90,000 metric tonesper annum of Ammonium Sulphate.

The Ammonium Sulphate Plant was closed in June, 1997 and a new Ammonia /Urea Complex having capacity of 600 metric tone per day of Ammonia and 1050metric tone per day of Urea, started commenced production in November, 1999.The annual production capacity of the Plant is 346,500 metric tone of urea.

Total completion cost of the Project was Rs.9, 700.060 million, out of which Rs.6;878.119 million was in foreign currency. The authorized and paid up capital of the

Company is Rs.3,000 million, which is subscribed by NFC.

The raw material used is Natural Gas from SNGPL Network.

Today the plant is running at 1176 tone per day which is the 112% of the designedcapacity 1050 tone per day of Urea and 650 tones per day of Ammonia.

PROCESS DESCRIPTION

The PAFL plant consist the following major section are

1. Ammonia Section

2. Urea Section

3. Utility Section

4. PH& S (Product Handling & Storage)Section


5/25

5

A view of ammonia section

AMMONIA SECTION

Ammonia is produced in a process in which nitrogen and hydrogen react in thepresence of an iron catalyst to form ammonia. The hydrogen is formed by reactingnatural gas and steam at high temperatures and the nitrogen is supplied from the air1.Other gases (such as water and carbon dioxide) are removed from the gas stream andthe nitrogen and hydrogen passed over an iron catalyst at high temperature andpressure to form the ammonia. The process is shown schematically in Figure 1.

STEP 1 - HYDROGEN PRODUCTIONHydrogen is produced by the reaction of methane with water. However, before this

can be carried out, all sulfurous compounds must be removed from the natural gas toprevent catalyst poisoning. These are removed by heating the gas to 400oC andreacting it with zinc oxide:


6/25

6

ZnO + H2S ZnS + H2O

Following this, the gas is sent to the primary reformer for steam reforming, wheresuper-heated steam is fed into the reformer with the methane. The gas mixture heatedwith natural gas and purge gas to 770oC in the presence of a nickel catalyst. At thistemperature the following equilibrium reactions are driven to the right,


7/25

7

converting the methane to hydrogen, carbon dioxide and small quantities of carbonmonoxide:

CH4 + H2O 3H2 + CO

CH4 + 2H2O 4H2 + CO2

CO + H2O H2 + CO2

This gaseous mixture is known as synthesis gas.

STEP 2 NITROGEN ADDITION

The synthesis gas is cooled slightly to 735oC. It then flows to the secondary reformerwhere it is mixed with a calculated amount of air. The highly exothermic reactionbetween oxygen and methane produces more hydrogen. Important reactions are:

CO + H2O CO2 + H2

O2 + 2CH4 2CO + 4H2

O2 + CH4 CO2 + 2H2

2O2 + CH4 2H2O + CO2

In addition, the necessary nitrogen is added in the secondary reformer.

As the catalyst that is used to form the ammonia is pure iron, water, carbondioxide and carbon monoxide must be removed from the gas stream to preventoxidation of the iron. This is carried out in the next three steps.

STEP 3 - REMOVAL OF CARBON MONOXIDE

Here the carbon monoxide is converted to carbon dioxide (which is used later in the

synthesis of urea) in a reaction known as the water gas shift reaction:

CO + H2O CO2 + H2

This is achieved in two steps. Firstly, the gas stream is passed over a Cr/Fe3O4catalyst at 360oC and then over a Cu/ZnO/Cr catalyst at 210oC. The same reactionoccurs in both steps, but using the two steps maximizes conversion.


8/25

8

STEP 4 - WATER REMOVAL

The gas mixture is further cooled to 40oC, at which temperature the water condensesout and is removed.

STEP 5 - REMOVAL OF CARBON OXIDES

Carbon dioxide is highly soluble in K2CO3, and more than 99.9% of the CO2 in themixture dissolves in it. The remaining CO2 (as well as any CO that was not convertedto CO2 in Step 3) is converted to methane (methanation) using a Ni/Al 2O3 catalyst at325oC:

CO + 3H2 CH4 + H2O

CO2 + 4H2 CH4 + 2H2O

STEP 6 - SYNTHESIS OF AMMONIAThe gas mixture is now cooled, compressed and fed into the ammonia synthesis loop

(see Figure 1). A mixture of ammonia and unreacted gases which have already beenaround the loop are mixed with the incoming gas stream and cooled to 5oC. Theammonia present is removed and the unreacted gases heated to 400oC at a pressureof 330 barg and passed over an iron catalyst. Under these conditions 26% of thehydrogen and nitrogen are converted to ammonia. The outlet gas from the ammoniaconverter is cooled from 220oC to 30oC. This cooling process condenses more the halfthe ammonia, which is then separated out. The remaining gas is mixed with morecooled, compressed incoming gas. The reaction occurring in the ammonia converter is:

N2 + 3H2 2NH3


9/25

9

The ammonia is rapidly decompressed to 24 barg. At this pressure, impurities suchas methane and hydrogen become gases. The gas mixture above the liquid ammonia(which also contains significant levels of ammonia) is removed and sent to the ammoniarecovery unit. This is an absorber-stripper system using water as solvent.


10/25

10

The remaining gas (purge gas) is used as fuel for the heating of the primary reformer.The pure ammonia remaining is mixed with the pure ammonia from the initialcondensation above and is ready for use in urea production, for storage.


11/25

11

UREA SECTION

GENERAL

Urea [CO (NH2)2], also known as carbamide or carbonyl diamide, is marketed as a

solution or in solid form. Most urea solution produced is used in fertilizer mixtures, witha small amount going to animal feed supplements. Most solids are produced as prills orgranules, for use as fertilizer or protein supplement in animal feed, and in plasticsmanufacturing. Five U. S. plants produce solid urea in crystalline form. About 7.3million mega grams (Mg) (8 million tons) of urea were produced in the U. S.in 1991.About 85 percent was used in fertilizers (both solid and solution forms), 3 percent inanimal feed supplements, and the remaining 12 percent in plastics and other uses.

PROCESS DESCRIPTION

The process for manufacturing urea involves a combination of up to 7 major unitoperations.

These operations, illustrated by the flow diagram in Figure 8.2-1, are solution synthesis,solution concentration, solids formation, solids cooling, solids screening, solids coatingand bagging, and/or bulk shipping.In the solution synthesis operation, ammonia (NH3) and carbon dioxide (CO2) arereacted to form ammonium carbamate (NH2CO2NH4).Typical operating conditions include temperatures from 180 to200C (356 to 392F),pressures from 140 to 250 atmospheres (14,185 to 25,331 kilopascals) NH3:CO2 molarratios from 3:1 to 4:1, and a retention time of 20 to 30 minutes. The carbamate is thendehydrated to yield 70 to 77 percent aqueous urea solution. These reactions are asfollows:

The urea solution can be used as an ingredient of nitrogen solution fertilizers, or it canbe concentrated further to produce solid urea.The 3 methods of concentrating the urea solution are vacuum concentration,crystallization, and atmospheric evaporation. The method chosen depends upon thelevel of biuret (NH2CONHCONH2) impurity allowable in the end product. Aqueous ureasolution begins to decompose at 60C (140F) to biuret and ammonia. The mostcommon method of solution concentration is evaporation.


12/25

12

The concentration process furnishes urea "melt" for solids formation. Urea solids areproduced from the urea melt by 2 basic methods: prilling and granulation. Prilling is aprocess by which solid particles are produced from molten urea. Molten urea is sprayedfrom the top of a prill tower. As the droplets fall through a countercurrent air flow, theycool and solidify into nearly spherical particles.

There are 2 types of prill towers: fluidized bed and non fluidized bed. The majordifference is that a separate solid cooling operation may be required to produceagricultural grade prills in a non fluidized bed prill tower.The solids screening operation removes off size product from solid urea. The off size

material may be returned to the process in the solid phase or be redissolved in waterand returned to the solution concentration process.Clay coatings are used in the urea industry to reduce product caking and urea dustformation.

The coating also reduces the nitrogen content of the product. The use of clay coatinghas diminished considerably, being replaced by injection of formaldehyde additives intothe liquid or molten urea before solids formation. Formaldehyde reacts with urea tofrom methylenediurea, which is the conditioning agent. Additives reduce solids cakingduring storage and urea dust formation during transport and handling.


13/25

13


14/25

14

SYNTHESIS

ACES21 process synthesis section consists of a reactor, a stripper and a carbamate condenser.Liquid ammonia is fed to the reactor via the HP Carbamate Ejector which provides the driving

force for circulation in the synthesis loop instead of the gravity system of the original ACES. The

reactor is operated at an N/C ratio of 3.7, 182 C and 152 bar.

The CO2 conversion to urea is as high as 63%at the exit of the reactor. Urea synthesis

solution leaving the reactor is fed to thestripper where unconverted carbamate is

thermally decomposed and excess ammoniaand CO2 are efficiently separated by CO2

stripping. The stripped off gas from thestripper is fed to the Vertical Submerged

Carbamate Condenser (VSCC), operated at anN/C ratio of 3.0,180C and 152 bar.

Ammonia and CO2 gas condense to formammonium carbamate and subsequently urea

is formed by dehydration of the carbamate inthe shell side. Reaction heat of carbamate

formation is recovered to generate 5 bar steamin the tube side. A packed bed is provided at

the top of the VSCC to absorb uncondensed

ammonia and CO2 gas into a recyclecarbamate solution from the MP absorptionstage. Inert gas from the top of the packed bed

is sent to the MP absorption stage.


15/25

15

UTILITIES SECTION

General introduction of Utilities plants

WATER INTAKE FACILITY

FFoorr tthhee ssuuppppllyy ooffrraaww wwaatteerr,, PPAAFFLL hhaass iittss oowwnn wwaatteerr ppuummppiinngg ssttaattiioonn nneeaarr IInndduuss RRiivveerr

((BBaanniiaann TTrreeee ssiittee//aarreeaa..)).. TThhee RRaaww wwaatteerr ccoommiinngg ffrroomm BBaanniiaann TTrreeee aarreeaa iiss uusseedd ffoorr tthhee ffoolllloowwiinngg

ppuurrppoosseess::

MMaakkee uupp wwaatteerr ffoorr CCoooolliinngg TToowweerr ((oolldd ++nneeww))..

PPoottaabbllee wwaatteerr aatt PPllaannttss..

PPoottaabbllee wwaatteerr aatt PPAAFFLL HHoouussiinngg ccoolloonnyy..

WWaatteerr TTrreeaattmmeenntt ppllaanntt ttoo pprroodduuccee DDMM wwaatteerr..

AAss ccoooolliinngg wwaatteerr dduurriinngg eemmeerrggeenncciieess..

AAss ffiirree wwaatteerr..

Water intake facility comprises on the following:

TUBE WELLS

06 tube wells are in operative condition, designed capacity of these tube wells is 3.0

cusec but due to continuous operation, capacity of old pumps (installed in 1997and before)has dropped to 2.0 ~ 2.5 Cusec.

1. No of Tube Wells in operative condition, installed before 1997 01

2. No of Tube Wells in operative condition, installed in 1997 03

3. No of Tube Wells in operative condition, installed in 2004 02

(for these two tube wells, new bores were drilled,

one new pump and one old pump were installed)

PIPE LINE

1. 24 and 3948 meters length Pipe Line from Banian Tree to PAFL plants.

12 ~ 08 and 1500 meters length Pipe Line from PAFL plants to Housing Colony.


16/25

16

RAW WATER ANALYSIS

pH 7.5-7.6

M. Alkalinity 120-130 ppm CaCO3Calcium 112-125 ppm CaCO3

Magnesium 40-50

Total hardness 160-170

Chloride 10-17 ppm

Sulphate 40-50

Silica 12-16

Water Treatment plant

For the production of de-mineralized water, required for steam generation PAFL has

a water treatment plant of El-Car Company of Italy having 85-tons/hr capacity. This plant

comprises on three sand filters and two Ion Exchange Lines, each line comprising on

Cationic exchangers, de-gasifier, Anionic exchangers, mixed bed and Auxiliaries for the

regeneration of these Ion exchangers.

Operating hours of each line/train are:

Cation exchanger/Anion Exchanger = 1020 m3

Mixed Bed = 168 hrs

Following resins are being used at Water treatment Plant

i. Strong Cation resin (for Mixed bed exchanger) Amber jet 1200 Na

ii. Strong Anion resin (for Mixed bed exchanger) Amber jet 4200 Cl

iii. Weak Acid Cation resin (for Cationic exchanger) D 113/ Dulite C 433iv. Strong Acid Cation resin (for Cationic exchanger) Amber jet 1200 Na

v. Strong base Anion resin (for Anionic exchanger) Amber jet 4200 Na

For the regeneration of Cationic resins 98% H2SO4 is used and for the regeneration of

Anionic resins 50% NaOH is used.


17/25

17

Steam Generation

PAFL has the following steam generation facilities.

Boiler # 1

Boiler No. 1 is manufactured by Babcocks and Wilcox Company of U. S. A and was installed in

1954. Initially it was designed for coal firing, but in 1972 its firing method was modified and

changed from coal burning to Natural gas burning. Its steam generation capacity is 155000 Ibs/hr

and is used for supplying steam for power generation and to Phase-II for plant operation.

Manufacturer = Babcocks & wilcox Boilers

Type = Water tubeCapacity = 155000 Ib/hr

Steam pressure = 775 Psi (g)

Heating surface = 13948 sq. ft.

Fuel = Natural gas (modified) coal (design)

No. of Burner = 04

Boiler water holding capacity = 96,400 Ibs

(at normal level)

Furnace draft = Balance draft

Heat recovery system = Tubular type air pre-heater

Temperature control system = Attemprator, surface contact type.

Boiler # 3

The Mitsui Boiler is fitted with combination firing steam using oil and gas as fuel.

Burners firing is automatic and equipped with safety tripping devices.The unit is equipped with wind box housing adjustable blade type air regulator for

producing the necessary turbulence, air movement, provided with manual control device,

inspection and ignition doors, stainless steel damper impeller, explosion door etc.

For fuel oil firing, complete line starting from Furnace oil receiving station to all burners.


18/25

18

Each burners is provided with manual shut off and electro-preumatic shut off valve connected to

flame protection devices. Steam consumption for Furnace oil atomization is not more than 1.1%

of Boiler minimum production.

Turn down ration of the Boiler is not less than 4 to 1

Manufacturer Mitsui Engineering Corporation, Japan

Evaporation Capacity at peak 90,000 Kg/hr

at MCR 85, 000 Kg/hr

Design pressures 60 Kg/cm2 G.

Steam pressure at super heater outlet 50 Kg/cm2 G.

Steam temperature at super heater outlet 450 + 5 oC

Feed water temperature drum inlet 165oC

Draft system forced draft

Firing system oil & gas

Fuel natural gas

Furnace oil

Heat recovery system gas air heater

Package Boiler

Manufacturer HMC, Pakistan

Evaporation Capacity 30000 Kg/hr

Design pressures 45 Kg/cm2 G.

Steam temperature at super heater outlet 395 + 5oC

Air temperature at FDF inlet 25oC

Draft system forced draft

Fuel natural gas

Heat recovery system Economizer


19/25

19

Power Generation

The powers station is for the supply of electric power, heating steam and

condensed water to the factory. For this purpose two set of turbo generator set of A. E. G

Company are provided. The power production capacity of each unit is 11.5 MW. Normally oneunit remains in operation and other remains stop.

Main equipment involved

Power generation units consist on the following main equipment.

1) Main Turbine

2) Generator

3) Condensate & its auxiliaries

4) Deareator

Turbine

It is multi stage, condensing, extraction and compound type Turbine, used as prime mover for

three-phase synchronous generator. Turbine has total eleven (11) stages out of which first stage

is impulse type and rest of the stages are of reaction type.

For Power generation two Turbo generator set having 11.5 MW/each generation capacityavailable these generator were installed in 1954 and since these are in operation.

Turbine ratings

Out put (Rated) = 11.5 MW

Steam pressure (Max.) = 770 psig (54 atg)

(Nor.) = 642 psig (45 atg)

STEAM TEMPERATURE (MAX.) = 850 OF (455 OC)

(Nor.) = 830OF (443

OC)

Critical speed (rang) = 1290 to 2310 rpm

Normal speed = 3000 rpm


20/25

20

Generator Rating

Rated output = 15,000 kVA or 12,000 kV at 0.8 P. F

Rated voltage = 6300V

Rated Current = 1375 A

Frequency = 50 c/s

Speed = 3000 rev/ min

Power factor = 0.8

Cooling Tower section

Cooling Tower section is to supply cooling water to the Urea, Ammonia and Utilities

plants required for the cooling of different equipments and process streams.

For this purpose this section is equipped with 6 Nos. cooling fans. 3 Nos. cooling water

pumps, one motor driven cooling water pumps, 3 Nos. condensing Turbines for cooling water

pumps, surface condenser, cooling water chemical treatment unit and 2 Nos. side stream filters

for the filtration of cooling water.


21/25

21

Polisher unit

This unit is for supply Polished water to Ammonia plant required for steam generation for

this purpose 2 Nos. of Polishers are provided having 75 m3/hr capacity each.

Instrument air/ Plant air section

For the supply of plant air and Instrument air, a air compressor IGB 3601 A having

capacity of 3520 Nm3/hr is provided along with the provision of air supply from Ammonia plant

air compressor 101 J.

To meet power failure emergency air compressor IGB 3601 B and air reservoir IFA 3601

is also provided.

For Instrument air two set of air dryers are provided.

Inert gas generation unit

To supply low pressure and high pressure Nitrogen gas to Ammonia, Urea and Utilities

plants, Nitrogen generation unit of AG Linde Germany having generation capacity 450 Nm3/hr

(Max) is provided. This unit comprises on air compressor, 2 Nos. pressure swing adsorption

tower, deoxidation unit and Nitrogen dryer.

For supply of high pressure Nitrogen a booster compressor IGB 3702 and an emergency

N2 reservoir is provided.

Emergency Diesel engine generator

To provide electricity power required at different sections of plants during power failure

a Diesel oil engine driven generator having generation power of 1250 KW is provided.

Natural gas receiving section

Natural gas received from SNGPL is fed to know out drum and then to dust filters from

where it is supplied to Ammonia plant.


22/25

22

Furnace oil/ Diesel oil section

PAFL has Furnace oil/ Diesel oil storage and piping facility. Furnace oil is used as fuel at

Boiler # 3 during emergency and Diesel oil is used at emergency Diesel engines.

Fire Water unit

Firewater pumping unit comprises of four pumps. Two are Diesel engine driven and two

are motor driven. The purpose of this unit is to supply Firewater to the firewater circuit and

keep pressurizing it with small jockey pump


23/25

23

ANALYTICAL & QUALITY CONTROL LABORATORIES.Analysis Report Of Effluents.

Dated : 01/07/09

Date Time pH6-9

NH340.00ppm

Urea 10.00ppm

Zinc5.0

ppm

Cr-1.0ppm

B.O.D80.00ppm

SuspendedMatter

150 ppm

01/06/09 0845 8.2 28.86 5.6 0.39 Nil 30.6 128

1700 8.3 35.4 6.8 --- --- --- ---

2300 8.4 38.8 7.6 --- --- --- ---

02/06/09 0730 8.3 35.8 6.4 0.42 Nil 30.8 136

1700 8.4 36.8 8 --- --- --- ---

2245 8.2 31.2 5.2 --- --- --- ---

03/06/09 0800 8.3 33.6 6 0.36 Nil 31.4 126

1530 8.4 34.5 5.6 --- --- --- ---

2315 8.3 31.2 5.8 --- --- --- ---04/06/09 0715 8.3 32.9 6.2 0.38 Nil 31.7 130

1700 8.4 38.8 7.6 --- --- --- ---

0015 8.2 27.3 6 --- --- --- ---

05/06/09 0745 8.3 34.1 6.4 0.32 Nil 32 126

1515 8.2 29.6 5.9 --- --- --- ---

2345 8.4 36.6 6.6 --- --- --- ---

06/06/09 0745 8.3 34.7 6.3 0.35 Nil 32.8 130

1700 8.3 35.28 6.4 --- --- --- ---

2245 8.5 39.9 7.8 --- --- --- ---

07/06/09 0745 8.5 37.96 7.4 0.37 Nil 32.8 128

1800 9.9 1200 2000 --- --- --- ---

2330 9.2 400 200 --- --- --- ---

08/06/09 0800 8 225 933.0 0.27 Nil 31.4 126

1600 8.8 88.2 22.7 --- --- --- ---

0030 8.5 48.92 16 --- --- --- ---

09/06/09 0845 8.4 38.8 9.4 0.37 Nil 31.5 140

1600 8.2 31.6 6.7 --- --- --- ---

0015 8.3 33.84 6.2 --- --- --- ---

10/06/09 0900 8.4 36.86 7.6 0.32 Nil 33 128

1600 8.4 35.6 7.2 --- --- --- ---

2300 8.4 34.8 7 --- --- --- ---

11/06/09 0830 8.3 32.7 6.8 0.34 Nil 32.4 136

1615 8.2 30.9 5.9 --- --- --- ---

2315 8.4 35.1 6.3 --- --- --- ---

12/06/09 0900 8.3 34.6 7.2 0.35 Nil 33.1 128

1730 8.2 32.9 6 --- --- --- ---


24/25

24

2300 8.2 30.4 5.5 --- --- --- ---

13/06/09 0930 8.4 36.8 7.2 0.29 Nil 32.8 120

1700 8.3 34.2 5.6 --- --- --- ---

0000 8.5 39.8 7.6 --- --- --- ---

14/06/09 0830 8.3 31.96 5.2 0.33 Nil --- 1281600 8.3 33.6 5 --- --- --- ---

0030 8.4 38.4 7.9 --- --- --- ---

15/06/09 0800 8.3 34.5 6.5 0.3 Nil 33 125

1800 8.2 28.4 5.2 --- --- --- ---

2330 8.3 31.9 5.8 --- --- --- ---

16/06/09 0900 8.5 38.9 8.8 0.35 Nil 33.2 138

1700 8.2 28.6 5.6 --- --- --- ---

0015 8.4 34.8 7.2 --- --- --- ---

17/06/09 0815 8.3 35.6 6.2 0.31 Nil 33.2 144

1710 8.2 26.44 4.8 --- --- --- ---

0030 8.3 30.8 6.7 --- --- --- ---

18/06/09 0800 8.3 31.4 6.2 0.37 Nil 33.8 128

1500 8.4 35.4 7 --- --- --- ---

0030 8.3 32.6 6.8 --- --- --- ---

19/06/09 0800 8.4 35.8 7.4 0.38 Nil 32.6 134

1530 8.4 36.7 7.1 --- --- --- ---

0015 8.3 32.8 6.4 --- --- --- ---

20/06/09 0745 8.2 26.84 5.2 0.33 Nil 32.8 128

1545 8.4 39.4 7.2 --- --- --- ---

0030 8.2 32.6 6.4 --- --- --- ---

21/06/09 0800 8.3 30.42 5 0.39 Nil --- 1321630 8.4 34.7 7.2 --- --- --- ---

2300 8.4 36.6 7 --- --- --- ---

22/06/09 0830 8.2 27.34 4.9 0.33 Nil 33.1 122

1600 8.3 31.9 5.6 --- --- --- ---

2245 8.5 37.9 7.9 --- --- --- ---

23/06/09 0900 8.3 30.92 5.2 0.39 Nil 32.8 130

1500 8.3 32.6 5.9 --- --- --- ---

2245 8.4 35.2 6.2 --- --- --- ---

24/06/09 0830 8.3 31.6 5.8 0.39 Nil 32.4 136

1630 8.4 34.7 6.4 --- --- --- ---

2245 8.3 32.9 5.6 --- --- --- ---

25/06/09 0830 8.3 30.4 4.8 0.33 Nil 33 134

1630 8.4 36.8 8.2 --- --- --- ---

2330 8.4 37.6 7.8 --- --- --- ---

26/06/09 0915 8.5 39.8 8.2 0.39 Nil 32.7 148

1640 8.4 34.8 7.2 --- --- --- ---


25/25

2300 8.4 35.3 7.6 --- --- --- ---

27/06/09 0915 8.3 36.4 6.7 0.32 Nil 32.9 136

1530 8.4 37.9 7.9 --- --- --- ---

2300 8.5 38.8 8 --- --- --- ---

28/06/09 0815 8.4 33.9 7.6 0.36 Nil --- 1281700 8.4 34.6 7.2 --- --- --- ---

0015 8.2 27.22 4.8 --- --- --- ---

29/06/09 0715 8.3 31.9 5.9 0.4 Nil 33.2 134

1700 8.4 36.9 7.84 --- --- --- ---

0030 8.2 28.46 5 --- --- --- ---

30/06/09 0715 8.3 33.6 6.9 0.36 Nil 33.24 130

1615 8.4 37.2 7.6 --- --- --- ---

2345 8.3 32.16 5.6 --- --- --- ---

Avg. 8.4 53.9 41.4 0.35 Nil 32.53 131.23

Exhaust and Noise

Annex -III

Sr.

NoParmaeters NEQ Standards

Avg. Results for

the month of June2009

1 Smoke

40 % or 2 on the Ringleman Scale during engine accelerationmode. N.A

PAFL Report

Documents