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ADDITIONAL DOCUMENTS
Annexure 1: Production Details
S. No.
Name of Products Production capacity in MT/M
Existing Proposed Total
1 98% Sulfuric Acid, 25%-65% Oleum, Liquid
SO3 & Liquid SO2 3900 6000 9900
2 Di Methyl Sulphate (DMS) 0 2000 2000
3 70% sulfuric Acid (Co-product) 0 100 100
Total 3900 8100 12000
Annexure 2: Existing consolidated consent and authorization (CC & A)
Annexure 3: Amended consolidated consent and authorization (CC & A)
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 10
Annexure 4: Site Location Map
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 11
Annexure 5: Project Boundary Map
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 12
Annexure 6: Site Layout Map
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 13
Table 1: Area Break up at Site
S. No.
Title Area, m2 % of total Area
1 Processing Area (Sulphur Melter, MCC & Control Room 159.29 0.31
2 Storage Area( Sulphar storage, Liq. SO2 cylinder filling storage area, SO2, Engineering Store)
1649.34 3.16
3 Utility Building, GEB Substation, Toilet Block, Compressor Room, Mechenical Work shop, Electrical Room, Blower, D.M Water Plant
733.71 1.41
4 Solid Hazardous Waste Area 12.25 0.02
5 Water Reservoir 111.72 0.21
6 Effluent Treatment Plant 500.00 0.96
7 Cooling tower RCC basin 42.82 0.08
8 Cooler Catch Basin 148.49 0.28
9 DG Sets (D.G.Room, D.G.shed) 327.17 0.63
10 U.G Condensate Tank, Tank Farm 703.14 1.35
11 Lorry Filling Tank 39.14 0.08
12 SO2 Tonner Loading Facility 110.00 0.21
13 Roads 5592.37 10.73
14 Administrative Building 209.48 0.40
15 Greenbelt Area 5214.06 10.00
16 Area for proposed Expansion 36587.65 70.17
Total 52140.623 100.00
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 14
Annexure 7: Manufacturing Processes
1(i): 98% Sulfuric Acid
Raw Material: Sulfur, compressed Air, Water
Process Description: The Sulfuric Acid Plant is based on the Double Contact and Double Absorption process. The three main steps of this process are:
Combustion of Sulfur to produce Sulfur Dioxide gas (S + O2 SO2)
Conversion of Sulfur Dioxide gas to Sulfur Trioxide gas in the presence of vanadium pentoxide catalyst (S O2 + 1/2 O2 SO3)
Absorption of Sulfur Trioxide in Sulfuric Acid solution and reaction of water with Sulfur Trioxide to form Sulfuric Acid (SO3 + H2O H2S O4)
The four main sections of the plant are the Sulfur section, Gas section, Acid section and Heat Recovery section.
Sulfur section: This section consists of melting pit, filter pump chamber and pumping pit. Solid sulfur is
fed into the melting pit. The melting pit is provided with steam coils and an agitator. Here sulfur is melted
under agitation by steam at 5 kg/cm2g pressure. Molten sulfur overflows to the filter pump chamber. Filter
pump chamber contains steam coils and sulfur filter pump. This pump delivers dirty sulfur through sulfur
filter. Clean and filtered sulfur is sent to pumping pit. The pumping pit is provided with three metering
pumps which pump molten sulfur into the furnace.
Gas section: Combustion of molten sulfur is carried out in furnace in the presence of dry air to produce
9.5 - 10.0% sulfur dioxide gas. Air required for combustion is supplied by main air blower and then passed
through drying tower (DT) to remove moisture content in the air. Hot combustion gases from the furnace
are cooled down by waste heat boiler # 1 (WHB1) to auto ignition temperature of catalyst before feeding it
to the first pass of the converter.
The conversion of SO2 to SO3 is an exothermic oxidation reaction and is carried out in the presence of
vanadium pentaoxide catalyst in a four/five pass converter. The extent of the reaction is limited by gas
temperature rise and by the formation of SO3. The extent of efficiency of conversion is increased by
carrying out the reaction in successive passes with partial cooling between passes. The SO2 to SO3
conversion is further optimized by providing intermediate absorption stage for the removal of SO3 formed
in the first three passes of the converter and thus making conditions more favorable for the final
conversion in the fourth/fifth pass.
Heat generated due to conversion of SO2 to SO3 in first and second pass is removed in 3 in the circulating
stream of 98% sulfuric acid. Gas from IPAT is heated to the reaction temperature in HE3 followed by HE2
before feeding to fourth pass. Heat generated in the fourth pass is recovered in economizer # 2 (Eco2).
Now, the gas is passed through final absorption tower (FAT) to absorb SO3 generated in fourth pass.
Residual gases from FAT are scrubbed in scrubber and then vented to atmosphere through the stack.
Acid section: Acid section consists of a common acid circulation tank (Acid CT), a common acid circulation
pump (Acid CT pump) and an acid plate heat exchanger (Acid PHE). Hot acid from the acid CT is pumped
by acid CT pump through acid PHE, where water is used as the cooling media. Cooled acid is then
circulated through IPAT and FAT for absorption of SO3from the converter gas and through DT for the
removal of moisture from atmospheric air. Outlet acid from IPAT and FAT becomes concentrated due to
formation of sulfuric acid by the reaction of SO3and H2O while, outlet of DT becomes diluted due to
addition of moisture from the air.
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 15
Acid concentration in acid CT is automatically controlled by addition of soft water to acid CT. Level in acid
CT is maintained by tapping out the acid into acid storage tanks (acid ST) at regular intervals.
Heat recovery section: Heat of combustion produced in furnace and heat of reaction produced in
converter is utilized to generate steam at 20-30 kg/cm2g pressure. DM water from boiler feed water tank is
pumped to Eco1 where it is preheated and then send to Eco2 where it is further heated. This preheated
water from Eco2 is fed to WHB1 and WHB2 where steam is produced which is again heated in super-
heater. Part of the steam is passed through pressure regulating valves to reduce steam pressure for
utilization in sulfur melting and the excess steam is supplied to various sections.
Process Flow Diagram:
Table 2: Material Balance of 98% Sulfuric Acid
S.
No.
INPUT/MT of Product
Raw Materials Quantity (kg)
1 Sulfur 0.34
2 Water (Process) 0.185
3 Air (oxygen) 0.475
4 Steam 0.415
Total 1.415
S.
No.
OUTPUT/kg of Product
Remark Components
Liquid
Effluent
Air
Emission
Recovery/
Product
Solid
Waste
1 Eq. Sulfuric acid 1 Product
2 effluent 0.015
3 evaporation loss 1.0
4 steam 0.4
Total 0.015 1.4 1
1.415
H2So4
H2O
Solid SulfurO2
Sulfur Dioxide (So2)
Sulfur Trioxide (So3)
1/2 O2
Vanadium Pentoxide
Cristal
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 16
1(ii): 25%-65% Oleum
1(iii): Liquid SO3
Process Description:
Sulphur trioxide gas from the steam heated Oleum Boiler is fed to a vertical shell and tube falling type
Condenser. The sulphur trioxide gas is on the shell side and the water from the cooling tower is falling
over the walls of tubes. This is specially designed from the safety point of view. Here the gas is cooled by
cooling water with the temperature not exceeding 280 C to 320 C. The outlet temp should not exceed 350
C to 400 C. The excess pressure with non-condensable of gases will be released by a scrubber irrigated
with sul acid from the plant. This will prevent any air pollution from the system.
The liquid sulphur trioxide from the condenser is taken to the any of the storage tanks. Storage tanks are
providing with hot water in jacket to maintain the temp. Steam tracing is provided to the liquid sulphur
trioxide line.
From the storage tanks lorry filling is carried out by tanker filling line with flexible hose made from S S wire
braided Teflon hose.
Vents from storage tanks as well as Tanker is connected to scrubber irrigated with Sulphuric Acid. A
flexible corrugated PTFE braided by stainless steel hose is connected from the tank lorry to the scrubber
for preventing any pollution during lorry filling operation.
Process Flow Diagram:
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 17
Liquid SO2
Process Description:
The main Reaction for production of liquid SO2 is S+ 2SO3 3 SO2
Sulphur trioxide gas from the SO3 generator is led to a vertical shell & tube ‘falling film’ type SO3
condenser. The liquid SO3 from the condenser will go to the jacketed storage tank.
Bright yellow solid sulphur is charges into day tank and liquefied. This liquid sulphur and liquid SO3 are
pumped in the reactor by using metering pumps. Reactor is to be initially charged with Oleum from the
storage tank.
The reaction of liquid SO3 and molten sulphur is carried out under a pressure of 6-8 kg/cm2 in a special
reactor. The exothermic heat of reaction during production of sulphur dioxide is removed by circulating
cold water through the jacket of the reactor. The SO2 gases are then passed through polishing towers in
which lumps of solid sulphur react with unreacted sulphur trioxide. The gases then subsequently passed
through spargers for removal the acid mist if any.
Pure sulphur dioxide is then condensed in water cooled condenser and then stored in SO2 Receivers. The
liquid SO2 from the Receivers is then filled up in cylinders (of 900 kg.capacity) for sale.
Main reaction is very fast hence the volume of the reactor is very small. However safety valve and rupture
disc are provided for releasing any excess pressure vent line of safety valves & rupture disk is connected
with existing intermediate absorption tower of existing sulphuric acid plant.
The reactor agitator shaft is provided with proper gland seal to ensure leak free operation.
Process Flow Diagram:
H2O
Solid SulfurO2
Sulfur Dioxide (So2)
Sulfur Trioxide (So3)
1/2 O2
Vanadium Pentoxide
Cristal
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 18
2. Dimethyl Sulfate with Co- Product 70% Sulfuric acid
Raw Material: Methanol, Sulfur Trioxide & Alumina Catalyst
Process Description: Methanol is vaporized in a vaporizer and these vapors of Methanol is passed
through a converter containing Alumina catalyst at elevated temp and this methanol gets converted to Di
Methyl Ether and it is sulphonated with SO3 to get technical Di Methyl Sulphate ( 95%) which is purified by
vacuum distillation to get pure DMS. Bottom product is Sulphuric acid having 25-30% dimethyl sulphate.
Chemical Reaction:
2CH3OH CH3-O-CH3 + H2O
Methanol
Mol wt-32*2
DME
Mol wt-46
Water
Mol wt-18
CH3-O-CH3 +
SO3
H2SO4
CH3-SO4-CH3 + H2SO4
DME
Mol wt-46
Sulpur Trioxide
Mol wt-80
DMS
Mol wt-126
Process Flow Diagram:
Sulfur Dioxide (So2)1/2 O2
O2 Solid Sulfur
Vanadium Pentoxide
Cristal
1/2 O2 Sulfur Dioxide (So2)
H2O Sulfur Trioxide (So3)
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 19
Table 3: Material Balance of Dimethyl Sulphate
S.
No.
INPUT/MT of Product
Raw Materials Quantity (kg)
1 Methanol 0.525
2 Sulphur trioxide 0.68
3 Alumina catalyst 0.00006
8 Water 2
Total 3.2
S.
No.
OUTPUT/kg of Product
Remark Components
Liquid
Effluent
Air
Emission
Recovery/
Product
Solid
Waste
1 Product 1 Product
2 70% Sulfuric Acid 0.05 Co-Product
3 Waste Catalyst 0.00006
4 Evaporation loss-CT 2
2 Liquid Effluent 0.115
Total 0.115 2 1.05 0.00006
3.2
Methanol
Rec. Methanol-Recycle
Sulfur Trioxide
70% Sulfuric Acid
Distillation
Sulphonation
Dimethyl Sulphate
Distillation
Catalytic Reactor
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 20
Annexure 8: Raw Material & Product Storage Details
S.
No. Chemical State
Consumption
(KL/Annum)
Means of
Storage
Operating Condition
(Storage) Nos. of
vessel
Storage
capacity of
Tank (KL)
Maximum
Storage
Capacity
(KL) Press
(Kg/cm2) Temp. (°C)
1 Sulfur Solid 40392 Godown atmospheric ambient 1 1000 1000
2 Methanol Liquid 12600 Tank atmospheric ambient 1 100 100
3 Sulfur Trioxide Liquid 16320 Tank atmospheric ambient 6 10 10
Alumina Catalyst Solid 1.44 Mt|Annum Drums atmospheric ambient - 500 kgs 500 kgs
Storage Details of Products
S.
No. Product State
Production, MTPA Mode of Storage Nos. of vessel
Capacity of Storage
Means, KL Total Storage Capacity
Existing Proposed
1
98% Sulfuric Acid Liquid
3900 6000
Tank 3 300 900
25%-65% Oleum Liquid Tank 3 50 150
Liquid SO3 Liquid Tank 3 50 150
Liquid SO2 Liquid Tank 6 8 48
2 Di Methyl Sulphate (DMS) 0 2000 Tank 3 200 600
3 70% sulfuric Acid (CO
product of DMS) Liquid 0 100
Tank 2 20 40
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 21
Annexure 9: Water Consumption and Waste Water Generation Details
Water is sourced from GIDC Water Supply. Existing water demand is 260 Kld and proposed water
demand will be 642 Kld. So after expansion total water consumption will be 902 Kld.
Table 4: Water Consumption Details
S. No.
Area of Consumption
Water Consumption Quantity, KLD
Total after Expansion
Existing Proposed
1 Waste Heat Recovery Boiler 54 83 137
2 Cooling Tower 162 340 502
3 Process 24 172 196
Washing 0 2 2
4 Domestic 15 15 30
5 Gardening 0 25 25
6 Fire Fighting 5 5 10
Total 260 642 902
Existing wastewater generation is 55 KLD. Proposed wastewater generation will be 106. So after
proposed expansion total wastewater generation will be 161.0 KLD. In which 91 KLD will be
discharged in to CETP and 30 KLD domestic wastewater is disposed through Septic tank/soak pit
system.
Table 5: Effluent Generation Details
S. No.
Area of Consumption
Waste water generation Quantity,
KLD Total After Expansion
Disposal / Treatment
Facility Existing Proposed
1 Waste Heat Recovery Boiler 3 5 8
To ETP 2 Cooling Tower 35 73 108
3 Process 2 11 13
4 Washing 0 2 2
5 Domestic 15 15 30 To Septic Tank
Total 55 106 161
132.0 KLD will be discharged in
CETP and Domestic 30 KLD
is disposed through Septic tank/soak pit
system
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 22
Existing Water Balance Diagram:
260
54 162 24 15 0 5
127.0
128.6 15
35
3 35 2.0
40
Note: All values are in KLD
Raw Water from GIDC
Waste Heat Recovery
Boiler
Cooling Tower
Domestic Gardening
Septic Tank/ Soak Pit System
Evap + Drift Losses
ETP
Fire Fighting
Process
Fresh Water
Effluent
Losses
Recycled Water
RecoveredSteam to
other plants
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 23
Proposed Water Balance Diagram:
642
83 340 172 2 15 25 5
267
1 15
By Product
Sulphuric Acid
73
5 73 11 2
91
Note: All values are in KLD
Raw Water from Borewell
ETP
Fire Fighting
Fresh Water
Effluent
Losses
Recycled Water
Raw Water from Borewell
ETP
Fire Fighting
Fresh Water
Effluent
Losses
Recycled Water
Raw Water from Borewell
ETP
Fire Fighting
Fresh Water
Effluent
Losses
Recycled Water
Raw Water from GIDC
Waste Heat Recovery
Boiler
Cooling Tower
Domestic Gardening
Evap + Drift Losses
ETP
Fire Fighting
Process
Fresh Water
Effluent
Losses
Recycled Water
RecoveredSteam to
other plants
Washings
Septic Tank/ Soak Pit System
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 24
Water Balance Diagram after Expansion:
902
137 502 196 2 30 25 10
394.0
1 30
By Product
Sulphuric Acid
108
8 109 13 2
131
Note: All values are in KLD
Raw Water from Borewell
Boiler Cooling Tower
Washings Domestic Gardening
Evap + Drift Losses
ETP
Fire Fighting
Process
Fresh Water
Effluent
Losses
Recycled Water
Raw Water from Borewell
Boiler Cooling Tower
Washings Domestic Gardening
Evap + Drift Losses
ETP
Fire Fighting
Process
Fresh Water
Effluent
Losses
Recycled Water
Raw Water from Borewell
Waste Heat Recovery
Boiler
Cooling Tower
Washings Domestic Gardening
Septic Tank/ Soak Pit System
Evap + Drift Losses
ETP
Fire Fighting
Process
Fresh Water
Effluent
Losses
Recycled Water
RecoveredSteam to
other plants
Raw Water from GIDC
Waste Heat Recovery
Boiler
Cooling Tower
Washings Domestic Gardening
Evap + Drift Losses
ETP
Fire Fighting
Process
Fresh Water
Effluent
Losses
Recycled Water
RecoveredSteam to
other plants
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 25
Figure 1: Existing Membership Certificate of NCTL for water supply and Waste water Discharge
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 26
Annexure 10: Details of Effluent Treatment Plant
Description of Effluent Treatment:
Primary treatment is available at ETP, Amal.
Raw effluent is collected in tank. Neutralization is done by means of Caustic. The neutralized
effluent is then transferred to collection tank and then sent to NTCL.
Figure 2: Process Block Diagram of ETP
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 27
Annexure 11: Fuel Consumption
Table 6: Fuel Consumption
S. No.
Stack Attached to
Capacity Stack Nos.
Type of Fuel used
Fuel consumption
Remark
Existing
1
Waste heat boiler
6 ton/hr -
Waste heat boiler
-
This is waste heat boiler. Sulfuric Acid
production is exothermic reaction and hence heat is being generated.
The same is used for steam generation. Hence there is no
fuel or stack involved in it.
Proposed
1 Waste heat
boiler 2 Nos.
6 Ton/hr - Waste heat
boiler -
This is waste heat boiler. Sulfuric Acid
production is exothermic reaction and hence heat is being generated.
The same is used for steam generation. Hence there is no
fuel or stack involved in it.
2 DG Set 600 KVA 1 Diesel 6-8 kl/year
*Note: DG Set will be used only during power failure
M/S. AMAL LTD. ADDITION OF NEW PRODUCTS AND EXPANSION OF EXISTING
PRODUCTS IN SULFURIC ACID PLANT AT GIDC ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 28
Annexure 12: Hazardous Waste Generation
Table 7: Hazardous Waste Generation and Disposal
S. No.
Type of Waste Hazardous Waste Category as per
2016
Quantity kg per Year Source
Method of Collection
Treatment / Disposal Existing Additional Total
1 Catalyst 17.2 60 92 152 Process Drums TSDF-BEIL
2 Used oil 5.1 50 77 127 DG set, Gear
boxes Drums re-refiners
3 ETP Sludge 35.3 3000 4615 7615 Wastewater Treatment
Bags TSDF-BEIL
4 Sulfur sediment 17.1 20000 30769 50769 Process Bags TSDF-BEIL 5 Waste catalyst 17.2 0 1440 1440 Process Drums TSDF-BEIL
6 Waste
Drums/Liners/Carboys| 33.1 0 3000 3000 Packaging - Sell to authorized party/TSDF-BEIL
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 29
Figure 3: Existing Provisional Membership Certificate of M/s. BEIL for Hazardous Waste
M/S. AMAL LTD.
ADDITION OF NEW PRODUCTS AND
EXPANSION OF EXISTING PRODUCTS
IN SULFURIC ACID PLANT AT GIDC
ANKLESHWAR FORM I
KADAM ENVIRONMENTAL CONSULTANTS |MAY 2017 30
Annexure 13: Stack Details
Table 8: Details of Flue Gas Stacks
Stack Attached
to Sources Capacity
Nos. of
Stacks
Stack Height,
m
Air pollution
Control measures
Attached
Remark
Existing
Boiler 6 Ton/hr 1 30 Adequate Stack Height
Already dismantled.
Proposed
DG Set 600 KVA 1 - Adequate Stack
Height -
*Note: DG Set will be used only during Power failure.
Table 9: Details of Process Vents
Stack Attached to Nos. of Stacks
Stack Height in m
Pollutants Emitted
Air Pollution Control Measures Attached
Existing
Sulphuric Acid Plant 1 50 SO2, Acid Mist Alkali Scrubber
Proposed
Sulphuric Acid Plant 1 50 SO2, Acid Mist Alkali Scrubber
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