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Prefeasibility Report

New Project: 1 Manufacturing: Agro Chemicals

ON

PROPOSED PROJECT FOR THE MANUFACTURE

OF AGRO CHEMICALS LIKE PESTICIDE

INTERMEDIATES, INSECTICIDE, FUNGICIDE &

HERBICIDE PRODUCTS

Category – 5 (b)

of

M/S HERANBA INDUSTRIES LIMITED

Located at:

Plot No. C-195 & 196, Sayakha Industrial Estate,

Tal: Vagra, Dist: Bharuch, Gujarat

Prefeasibility Report M/S HERANBA INDUSTRIES LIMITED

New Project: Manufacturing: Agro Chemicals

Project prefeasibility report for obtaining prior Environmental Clearance in terms

of provisions of EIA Notification -2006

1. Executive Summary :

Name of the Project : Heranba Industries limited

Location : Plot No. C-195 & 196, Sayakha Industrial estate, Ta: Vagra, Di: Bharuch, Gujarat. Project Heranba intends to set up a plant for the manufacture of Pesticide intermediates, fungicide,

herbicide and insecticide products at Plot. No. C-195 & 196, Sayakha Industrial estate, Ta: Vagra,

Di: Bharuch, Gujarat. The unit has already obtained offer cum plot allotment letter from the GIDC.

The unit is falling under medium Scale category.

Proposed Project Cost: Rs. 169 Crore.

Applicability of EIA notification – 2006

Category as per the amended EIA notification- 2006: as proposed products (i.e. Agro Chemicals)

are covered under the Category 5 (b) A. Hence, Environmental Clearance is required.

Project Proponent

The company in India comprising 4 Directors

medium Scale Unit

List of finished products & by- products

Sr. No. Product Capacity, TPM

Pesticide Intermediates

1.1 Cyper methric Acid Chloride 50

Or

1.2 M-Phenoxy Benzaldehyde 75

Insecticides

2.0 Acephate Technical 50

3.0 Deltamethrin Technical 10

4.0 Alpha Cypermethrin Technical 30

5.0 Permethrin Technical 25

6.0 Chlorpyriphos Technical 80

Fungicides

7.0 Tri cyclazole Technical 10

8.0 Hexaconazole Technical 15

9.0 Propiconazole Technical 15

10.0 Mancozeb Technical 400

Herbicides

11.1 Glyphosate Technical 25

Or

11.2 Dicamba Technical 150

12.0 Pendimethlin Technical 30

Total 890



By-products

Sr. No. By- Product Capacity, TPM

1 Ammonium Chloride Powder (85%) 29.9

2 Sodium Sulphite Powder (80%) 127.5

3 Hydro Chloric Acid solution (30%) 114.7

4 Hydro Bromic Acid solution (20%) 97.4

5 Sodium Sulphate powder (80%) 86.1

6 Spent sulphuric acid acid (40-60%) 1296

7 Cypermethrin (2nd crop) 12

8 Aluminum Chloride soln (20%) 427.7

9 Bromo benzene 44

10 SS-CMAC 27.5

11 KCl powder 43.2

Total 2306.0

Manufacturing process with chemical reaction & mass balance is attached as Annexure-3

Resource Requirement

Components Proposed Resources availability

Power, KVA 2300 Will be sourced from Torrent Energy Ltd (TEL)

/ Dakshin Gujarat Vij Co. Ltd.

Fresh Water, kl/Day 774 Will be sourced from GIDC water supply dept.

Coal for boiler (15 TPH x 2 Nos), MT/Hr

16 Will be sourced Local Dealer

FO/LDO for Incinerator, kgs/Hr

300 Will be sourced from Local Dealer

Fuel (HSD) for D.G. Set (1000 KVA x 3) , Kgs/Hr

360 Will be sourced from Local Dealer

Chilling plant, TR 1000 In-house

Cooling Tower, TR 2000 In house



Raw material Consumption

Product Capacity, TPM

Name of RM RM consumption in MT

MT/MT of product

MT Per month

Cypermethric acid Chloride

50 Forcut (Recovered) 0.38 19

Acrylo nitrile 0.522 26.1

CTC 1.55 77.5

Catalyst 0.01 0.5

DEA-HCl 0.011 0.55

HCl 30 % (Recovered) 1.71 85.5

HCl 30% (Fresh) 0.09 4.5

DMF 0.02 1

TC 1.067 53.35

Soda Ash 0.005 0.25

Caustic Lye 48 % 3.315 165.75

Catalyst 0.01 0.5

n-Hexane (Recovered) 8.912 445.6

n-Hexane (Fresh) 0.228 11.4

IB (Recovered) 0.137 6.85

IB (Fresh) 0.457 22.85

TEA (Fresh) 0.01 0.5

TEA (Recovered) 0.824 41.2

Sulphuric Acid 1.199 59.95

DMF 0.01 0.5

Thionyl Chloride 0.606 30.3

Total 21.073 1053.65

M- Phenoxy Benzaldehyde

75

Ethylene Di chloride 2.778 208.35

Anhydrous aluminum chloride 1.155 86.625

Benzaldehyde 0.7 52.5

Bromine 0.578 43.35

Chlorine 0.245 18.375

Formic acid 0.025 1.875

30% Hydro Chloric acid 0.121 9.075

Sodium thio sulphate 0.011 0.825

Ethylene glycol 0.78 58.5

Phenol 0.582 43.65

Potassium hydroxide 0.384 28.8

Toluene 1.448 108.6

Cuprous chloride 0.0055 0.4125

Caustic lye 0.02 1.5

Sulphuric acid 1.09 81.75

Total 9.9225 744.1875

Acephate

50 DMPAT 1.18 59

Ac2O 0.96 48

DMS 0.12 6

Sulphuric acid 0.04 2

Ammonia 0.22 11

Ethyl Acetate (Recovered) 1.076 53.8

Ethyl Acetate (Fresh) 0.385 19.25

MDC (Recovered) 10.357 517.85

MDC (Fresh) 0.589 29.45



Total 14.927 746.35

Deltamethrin

10

C.S.Flakes 1.22 12.2

20% aq. Soln. of Cat-V 7.9 79

methylene dichloride (Recovered)

16.97 169.7

Methylene di chloride (Fresh) 0.71 7.1

HCl (30%) 4.63 46.3

Benzene 3.3 33

FeCl3 0.06 0.6

Bromine 5.5 55

Aluminium chloride 1.1 11

C.S.lye 0.82 8.2

sulphuric acid 1 10

Sodium bicarbonate 0.052 0.52

Methanol 0.5 5

toluene 6.34 63.4

Thionyl chloride 2.295 22.95

DMF 0.004 0.04

m-Phenoxy Benzaldehyde 0.6 6

sodium cyanide 0.25 2.5

soda ash 0.05 0.5

TEBA 0.05 0.5

Acetic acid 0.005 0.05

Hypo 1 10

Isopropyl alcohol (Recovered) 4.56 45.6

IPA (Fresh) 0.19 1.9

TEA (Recovered) 0.105 1.05

TEA (Fresh) 0.045 0.45

Activated carbon 0.004 0.04

hypo super cell 0.004 0.04

22% c.s.lye 7.433 74.33

Bromo benzene 0.475 4.75

Total 67.172 671.72

Alpha Cypermethrin

30 CMAC 0.9 27

Sodium cyanide 0.23 6.9

Catalyst 0.02 0.6

Soda ash 0.02 0.6

MPB 0.72 21.6

Hexane (Recovered) 7.661 229.83

Hexane (Fresh) 0.319 9.57

Tri ethyl Amine (Recovered) 0.644 19.32

Tri Ethyl Amine (Fresh) 0.056 1.68

Sodium hypo chlorite 1.5 45

Total 12.07 362.1

Permethrin

25 Cypermethric acid chloride 0.62 15.5

m-Phenoxy benzyl alcohol 0.52 13

Potassium Carbonate 0.015 0.375

Total 1.155 28.875

Chlorpyriphos

80 TCAC 1.25 100

ACNN 0.5 40

Catalyst 0.015 1.2



Caustic lye 1.915 153.2

EDC (recovered) 3.818 305.44

RDC (Fresh) 0.2 16

Salt 0.025 2

DETC 0.643 51.44

Total 8.366 669.28

Tri Cyclozole

10 4-HMBT 1 10

Formic acid 0.76 7.6

NaOH 20% 0.406 4.06

Total 2.166 21.66

Hexaconazole

15 2,4 Di chloro valerophenone 0.95 14.25

Di methyl Sulphate (Recovered)

1.262 18.93

Di Methyl Sulphate (Fresh) 0.315 4.725

Di Methyl Sulphite 1.577 23.655

Potassium hydroxide 0.913 13.695

DMF (Recovered) 3.138 47.07

DMF (Fresh) 0.35 5.25

Anhydrous potassium carbonate

0.082 1.23

1,2,4 Triazole 0.327 4.905

Methanol 1.125 16.875

Total 10.039 150.585

Propiconazole

15 2,4 Di Chloro Aceto phenone 0.926 13.89

1,2 propane diol 0.56 8.4

Toluene (Recovered) 3.299 49.485

Toluene (Fresh) 0.152 2.28

10% Sodium carbonate solution

1 15

Bromine 0.716 10.74

DMF (Recovered) 3.38 50.7

DMF (Fresh) 0.14 2.1

1,2,4 Triazole 0.372 5.58

KOH 0.332 4.98

Total 10.877 163.155

Mancozeb

400 EDA 0.206 82.4

Caustic lye (48%) 0.58 232

CS2 0.572 228.8

Manganese sulphate 1.906 762.4

Zinc sulphate 0.166 66.4

SLS 0.033 13.2

HMT 0.02 8

Total 3.483 1393.2

Glyphosate

25 DEA 0.908 22.7

Catalyst 0.182 4.55

NaOH (47%) 2.919 72.975

HCHO (37%) 0.782 19.55

PCl3 1.48 37

HCl (30%) 2 50

carbon 0.157 3.925

ammonia 20% 0.708 17.7



oxygen 0.3 7.5

Total 9.436 235.9

Dicamba

150 2,5 DCA 3.39 508.5

Sodium nitrite 1.46 219

Sulphuric acid (98%) 7.84 1176

Sulphamic acid 0.1 15

Potassium chloride 1.08 162

Xylene (Recovered) 10.93 1639.5

Xylene (fresh) 0.63 94.5

Carbon dioxide 1.7 255

Hydro Chloric acid (30%) 3.34 501

Sodium Hydroxide 1.66 249

Di Methyl Sulphate 3.66 549

Total 35.79 5368.5

Pendimethlin

30

Hydrogen gas 0.055 1.65

Di Ethyl Ketone (Recovered) 0.536 16.08

Di Ethyl Ketone (fresh) 0.347 10.41

4 Nitro-O- Xylene 0.62 18.6

Catalyst 0.002 0.06

EDC (Recovered) 1.158 34.74

EDC (Fresh) 0.232 6.96

Nitric Acid 1.121 33.63

Sulphuric acid 0.801 24.03

HCl 0.575 17.25

Sodium bi Carbonate 3.5 105

Total 8.947 268.41

Note: Total Raw Materials Consumption will be 10860 TPM.

Water and Waste Water Management

Total Fresh water requirement will be 774 m3/day which is met through GIDC water supply.

Total Industrial wastewater generation will be 412 m3/day. Out of which about 283 m3/day

of high TDS & high COD of effluent generated from the process will be collected separately,

neutralized, filtered & finally taken to solvent stripper & MEE. Average 9 m3/day of high COD

& high ammonia effluent will be collected, neutralized, filtered and incinerated in proposed

incineration system. Balance 120 m3/day of normal effluent from cooling tower, boiler blow

down, floor/container washing and scrubber will be collected separately and sent to RO

system. Thus 239 m3/day of condensate from MEE/ATFD and 20 m3/day of effluent from RO

rejection; total 259 m3/day will be treated in catalytic advance oxidation followed by soil bio

reactor and finally discharge into effluent drainage line to Arabian Sea. 100 m3/day of RO

permeate will be recycled back to the process.

Domestic Waste water (12 m3/day) will be disposed by septic tank & soak pit.



Air Emission and its Control Measures

Flue gas emission:

There will be flue gas emission from 15 TPH x 2 capacities of coal fired steam boiler in the form of

PM, SOx & NOx. Adequate capacity of electro static precipitator along with 55 meters height of

common chimney will be provided to both the boilers.

Also the unit will install 1000 KVA x 3 nos capacity of D G set, as standby. It will be used only

during power failure. 360 kgs/hr of HSD will be used as a fuel & 11 meters height of chimney will

be provided.

Process gas emission:

Total four numbers of two stage water followed by alkali scrubbers will be provided to scrub

Sulphur dioxide, hydrogen chloride, nitrous & bromine gases generated from the process.

Separate 11 meters height of vent will be provided.

The unit proposes to install FO/LDO (300 kgs/hr) fired incineration system having capacity is 1000

kgs/hr and ventury & wet scrubber along with 30 meters height of chimney to incinerate tarry

waste generated from the process & high COD & high Ammonia liquid effluent generated from

the process. (Details of Air pollution control measures are attached as Annexure-8.

Hazardous Wastes and its Management

No Type of waste Category Qty. MT/ Anum

Treatment Disposal

1 ETP waste) 34.3 13700

Dried, packed in bags

Dispose off into TSDF, BEIL, Ankleshwar &

Detox, Dahej

2 Salt from MEE 34.3 14040 Dried, packed in bags

Dispose off into TSDF, BEIL, Ankleshwar &

Detox, Dahej

3 Used Oil 5.1 0.2 Packed in carboys

Incinerated into own Incineration system

4 Discarded containers

33.3 5.0 De-contaminated,

stored

Sell to authorized recycler

5 Incineration ash 36.2 300 Packed in bags Sell to brick manufacturer

6 Process waste & residue

29.1 670 Packed in drums/bags

Sent for co-processing

7 Used rubber hand

gloves/pipes etc

X-08 1 Packed in drums/bags




2.

Introduction of Project / Back Ground Information :

(i) Identification of Project and proponent.

Name of the project Proponent: Heranba Industries Limited

Heranba Industries Limited is a medium scale proposed unit to be located at Plot. No. C-195

& 196, Sayakha Dahej industrial estate, Ta: Vagra, di: Bharuch, Gujarat having total plot area

33640 m2 & total investment for the proposed project will be Rs. 169 Crore. The proposed

Agrochemicals products are especially used as under as per requirement.

Cypermethric acid Chloride: - This is an important organic intermediate used in the

manufacture of Parathyroid class of Pesticides like Cypermethrin, Alphamethrin,

Permethrin and Deltamethrin.

M-Phenoxy Benzaldehyde: is a pesticide intermediate to manufacture synthetic

parathyroid insecticides.

Acephate: - Systemic insecticide with contact and stomach action. It controls a wide

range of chewing and sucking insects, eg. Aphids, trips, lepidopterist larvae, leaf

miners, leafhoppers, cutworms, etc. in fruit (including citrus), vines, cotton, peanut,

potatoes, rice, tobacco, ornamentals, forestry and other crops.

Deltamethrin: - This is also highly effective insecticide used in low dosages. It has

both crop protective usages similar to the above and also more effective in Public

Health control of measures. Used as preservative in grain storage and effective

against wood pests.

Alphacypermethrin: - This is non systemic insecticide used for the control of a wide

range of chewing and sucking insects in agricultural crops like cotton rice, potatoes,

oilseeds, etc. used in public health for the control of harmful insects.

Permethrin: - An insecticide effective against broad range of pests. Used as

preservation against insects and pests.

Chlorpyriphos: - Non-Systemic insecticide with contact, stomach and respiratory

action. It controls insects belonging to family Coleoptera, Dipters, Homoptera and

Lepidoptera in soil or on foliage in a wide range of crops, including pome fruit, stone

fruit, citrus fruit, nut crops, strawberries, figs, bananas, beet, tobacco, soya beans,

sunflower, sweet potatoes, peanuts, rice, cotton, alfalfa, cereals, maize, sorghum,

asparagus, glasshouse and outdoor ornamentals, turf and in forestry. Also used for

control of household pests (Blattelindae, Muscidae, isopteran), mosquitoes (larvae

and adults) and in animal houses.

Tri Cyclozole: Tricyclazole is a systemic and protective fungicide used to control

Magnaporthe grisea, also known as rice blast.

Hexaconazole: It is a Fungicide and can be used on fruit trees such as apple,



vegetable, fruits, pepper, peanut, coffee, cereal crop and ornamental plant.

Propioconazole: Propiconazole is used agriculturally as a systemic fungicide on turf

grasses grown for seed and aesthetic or athletic value, mushrooms, corn, wild rice,

peanuts, almonds, sorghum, oats, pecans, apricots, peaches, nectarines, plums and

prunes

Mancozeb: a fungicide to prevent growth of fungi (molds) and to protect plants and

crops against damage caused by fungi.

Glyphosate: is a broad-spectrum systemic herbicide used to kill weeds, especially

annual broadleaf weeds and grasses known to compete with commercial crops

grown around the globe.

3,6 Di Chloro 2 Methoxy Benzoic Acid: Dicamba controls annual and perennial rose

weeds in grain crops and highlands, and it is used to control brush and bracken in

pastures, as well as legumes and cacti. It kills broadleaf weeds before and after they

sprout.

Pendimethlin: It is used to control annual grasses and certain broadleaf weeds which interfere with growth, development, yield and quality of agricultural and horticultural crops by competing on nutrients, water and light.

The unit shall be managed by technocrat Mr. Sadashiv K Shetty having 30 years of

experience in manufacturing and marketing of various Agro Chemicals worldwide. Team

members having 20 years of experience of Agro Chemicals industries.

The company has prepared lay out & design well equips production plant which will be

managed by dedicated, qualified & skilled persons.

The proponent proposes to set up a plant of Agro Chemicals with total capacity of 890 MT

per month.

The proposed project site lies on 21046’26.96” N Latitude & 72050’40.28”E Longitude.

Heranba Industries Limited is to be located at plot. No. C-195,196, Sayakha industrial estate,

Ta: Vagra, di: Bharuch in Gujarat state.

No forests, national park, wild life sanctuary, etc. are envisaged in 15 Km from the nearest boundary of the project site. Basic facilities of infrastructure like storage area, processing area, internal roads etc. shall be

developed on the project site. Transportation of raw material and finished goods will be

carried out through proposed internal roads and finally through existing state highway SH-6.

During the construction phase around 100 workers and during the operational phase around

170 workers including contractors will be required. Local skilled and semi-skilled workers will

be engaged during construction phase. The positives impact includes enhanced direct

employment for technical/administrative works and indirect employment opportunities for

transporters of raw materials and finished goods.

https://en.wikipedia.org/wiki/Legumes

https://en.wikipedia.org/wiki/Cacti



Since the project will cater to industries in the region by providing a suitable source for

import, export and coastal movement of pesticides, it will encourage industrial growth in the

region and result in additional revenue for government.

Beside the rail connectivity, and also well connected by road transport. There is a good

network of roads in the area and contributes for the development and economic growth of

the area. The National Highway No. 8 (Ahmedabad – Mumbai) is now six lanes, double

tracked, more elevated and Jam free highway, which is developed by M/s L & T Company.

This highway has given a further boost to the economic growth of this area.

Heranba Industries Limited was incorporated in 1992 and is engaged in the business of

manufacturing and marketing of Agro Chemicals especially pesticides and their

intermediates since 1995 at GIDC Vapi. The company has its Registered Office at Mumbai.

It manufactures and markets a wide range of Pesticide technical and intermediates. Senior

personnel are available for providing support to the manufacturing unit in the areas of

technology, R&D, manufacturing, quality control and quality assurance.

(ii) Brief description of nature of the Project :

The proposed project involves the production of Agro Chemicals. As per the EIA notification-

2006 as amended products are covered under any category 5(f) requires Prior

Environmental Clearance.

For the proposed project, the company intends to procure the available latest technology for

manufacturing the products.

This project will manufacture various Agro Chemicals products. A typical plant shall house

distillation, reactors, agitated nutsch filter, fractionating columns, rotary vacuum paddle

dryer, Distillation columns, HDPE absorbers for hydro chloric acid, condensers, PTFE and

stainless steel pumps, high vacuum steam ejectors and SS water ring vacuum pumps etc.

The industrial sector in the past 5 to 7 years has witnessed a drastic boom and also keeping

in mind the globalization trend, it is identified that the demand for the product has been at

growing pace. With the continuous R & D, it can be developed in-house and can be produced

commercially for domestic market as well as eye can be set on export markets too.

(iii) Need for the project and its importance to the country and or region :

The proposed project provides a potential growth opportunity for the already running

business of the company. The company is already engaged in the business of manufacturing

of “Pesticide technical, intermediates & its formulation”. The project would increase the

overall export and also increase the foreign revenue.

India produces about 80,000-90,000 MT of pesticides a year. India’s Agro chemicals &

pesticide industries are the largest in Asia and the twelfth largest in the world. With over

400 million acres under cultivation and over 60% of the country’s population dependent on

agriculture, the country’s economy depends on the agricultural sector to a substantial

extent.



India loses nearly 30% of its potential crop to insects, weeds and rodent attacks. The

Pesticides/Crop Protection/Agrochemicals industry plays a crucial role in protecting crops

from damage by weeds, pests, insects and fungus, both before and after harvest. This helps

to increase crop yields, which is important given the rate at which cultivable land is

shrinking.

(iv) Demand –Supply Gap :

The production of pesticides started in India in 1952 with the establishment of a plant for

the production of BHC near Calcutta, and India is now the second largest manufacturer of

pesticides in Asia after China. There has been a steady growth in the production of technical

grade pesticides in India, from 5,000 metric tons in 1958 to 102,240 metric tons in 1998. In

1996–97 the demand for pesticides in terms of value was estimated to be around Rs. 22

billion (USD 0.5 billion), which is about 2% of the total world market. The products have very

high specific demand as they are especially used as herbicide etc. as per requirement.

(v) Imports vs. Indigenous production :

Manufacturing these proposed products in the country will be very much economical as

compared to Import of the same. The export of these Agrochemicals will earn revenue for

the country.

(vi) Export Possibility :

Proposed products have high export potential. Also these products have very good sale

potential in local market.

(vii) Domestic / export Markets :

The company’s product is used as raw material to manufacture various herbicides as per the

required applications and having very good market in domestic and also having very good

international markets.

(viii) Employment Generation (Direct and Indirect) due to the project :

During the construction phase around 100 workers and during the operational phase around

170 workers including contractors will be required. Local skilled and semi-skilled workers will

be engaged during construction phase. The positive impacts include enhanced direct

employment for technical/administrative works and indirect employment opportunities for

transporters of raw materials and finished goods.



3. Project Description :

(i) Type of Project including interlinked and interdependent projects, If any :

The proposed project is an interdependent project of the company.

(ii) Location (map showing general location, Specific location, and project boundary & project

site layout) with coordinates :

The map showing general location, specific location and project boundary and project site

lay out is enclosed as Annexure-1.

(iii) Details of alternate sites considered and the basis of selecting the proposed site,

particularly the environmental considerations gone into should be highlighted :

The proposed activity will be accommodated in the notified industrial area having proper

industrial infrastructure so; there is no alternate site consideration. (Land allotment letter is

attached as Annexure-6.

(iv) Size or magnitude of operation :

As per the proposed project cost the project is covered under medium Scale category of

manufacturing industries.

(v) Project description with process details (a schematic diagram/ flow chart showing the

project layout components of the project etc. should be given) :

Detailed project description with process details is enclosed as Annexure-2

(vi) Raw material required along with estimated quantity, likely source, marketing area of final

products/s, mode of transport of raw Material and finished product :

Detailed raw material requirement along with estimated quantity, likely source, marketing

are of final products mode of transport of raw material and finish product & characteristics

of hazardous chemicals are as below:

DETAILS ON PRODUCT/BY-PRODUCTS TRANSPORTATION

Sr. No.

Product Physical State Dispatch Means of Transportation

1 Cyper methric Acid Chloride Liquid In a drum Truck or container

2 M- Phenoxy Benzaldehyde Liquid In a drum Truck or container

3 Acephate Solid In a bags Truck or container

4 Deltamethrin Solid In a bags Truck or container

5 Alpha Cyper Methrin Solid In a bags Truck or container

6 Permethrin Liquid In a drum Truck or container

7 Chlorpyriphos Solid In a bags Truck or



container

8 Tricyclozole Solid In a bags Truck or container

9 Hexaconazole Solid In a bags Truck or container

10 Propiconazole Liquid In a drum Truck or container

11 Mancozeb Solid In a bags Truck or container

12 Glyphosate Solid In a bags Truck or container

13 DICAMBA Solid In a bags Truck or container

14 Pendimethlin Solid In a bags Truck or container

Sr. No.

By-Product Physical State Dispatch Means of Transportation

1 Ammonium Chloride Powder (85%)

Solid In a bags Truck or container

2 Sodium Sulphite Powder (80%) Solid In a bags Truck or container

3 Hydro Chloric Acid solution (30%) Liquid In a drum Truck or container

4 Hydro Bromic Acid solution (20%) Liquid In a drum Truck or container

5 Sodium Sulphate powder (80%) Solid In a bags Truck or container

6 Spent acid (40-60%) Liquid In a drum Truck or container

7 Cypermethrin (2nd crop) Liquid In a drum Truck or container

8 Aluminum Chloride soln (20%) Liquid In a drum Truck or container

9 Bromo benzene Liquid In a drum Truck or container

10 SS-CMAC Liquid In a drum Truck or container

11 KCl powder Solid In a bags Truck or container

DETAILS ON RAW MATERIAL TRANSPORTATION

Sr. No.

Substance Physical State

Source of Supply

Means of Transport

ation

Distance of

supplier from

project site (km)

1 1,2 propane diol Liquid Local/imported Container 300

2 1,2,4 Triazole Solid Local Truck 100

3 2,4 Di Chloro Aceto phenone

Solid Local Truck 200

4 2,4 Di chloro Valerophenone

Solid Local Truck 200

5 2,5 DCA Solid Local Truck 200

6 Hydro Chloric acid Liquid Local Tanker 50



7 4 Nitro-O- Xylene Crystals Local Truck 50

8 4-HMBT Solid Imported Truck 300

9 Ac2O (Acetic Anhydride) Liquid Local Tanker 50

10 Acetic acid Liquid Local Truck 50

11 Acrylo nitrile Liquid Local Tanker 100

12 Activated carbon Solid Local Truck 50

13 Aluminium chloride Solid Local Truck 200

14 Ammonia Liquid Local Tanker 50

15 Anhydrous aluminum chloride

Crystals Local Truck 50

16 Anhydrous potassium carbonate

Crystals Local Truck 50

17 Benzaldehyde Liquid Local Tanker 100

18 Benzene Liquid Local Tanker 200

19 Bromine Liquid Imported Tanker 300

20 Bromo benzene Liquid Local Truck 50

21 Caustic flakes Liquid Local Truck 150

22 Caustic lye Liquid Local Tanker 50

23 Activated carbon Solid Local Truck 50

24 Carbon dioxide Gas Local Cylinder 100

25 Catalyst Solid Local Truck 100

26 Chlorine Gas Local Cylinder 100

27 CS2 Liquid Local Tanker 150

28 Carbon Tetra chloride Liquid Local Tanker 250

29 Cuprous chloride Solid Local Tanker 150

30 DEA Liquid Local Tanker 450

31 DEA-HCl Solid Local Truck 300

32 DETC Powder Local Truck 100

33 Di Ethyl Ketone Liquid Local Tanker 150

34 Di Methyl Sulphate Liquid Local Tanker 100

35 Di Methyl Sulphite Liquid Local Tanker 150

36 DMF Liquid Local Tanker 150

37 DMPAT Liquid Local Tanker 150

38 EDA Liquid Local Tanker 150

39 Ethyl Acetate Liquid Local Tanker 150

40 Ethylene Di chloride Liquid Local Tanker 150

41 Ethylene glycol Liquid Local Tanker 150

42 FeCl3 Solid Local Truck 100

43 Formic acid Liquid Local Tanker 100

44 HMT Solid Local Truck 100

45 Hydrogen gas Cylinder Local Truck 100

46 Hypo super cell Solid Local Truck 200

47 IB Gas & liquid

Local Tanker 150

48 Isopropyl alcohol Liquid Local Tanker 500

49 Manganese sulphate Solid Local Truck 200

50 Methanol Liquid Local Tanker 100

51 Methylene dichloride Liquid Local Tanker 100

52 MPB Liquid Local Tanker 50

53 M-Phenoxy benzyl alcohol Liquid Local Tanker 100



(vii)

54 N-Hexane Liquid Local Tanker 150

55 Nitric Acid Liquid Local Tanker 150

56 Oxygen Cylinder Local Truck 100

57 PCl3 Liquid Local Tanker 50

58 Phenol Solid Local Truck 300

59 Potassium Carbonate Solid Local Truck 100

60 Potassium chloride Solid Local Truck 100

61 Potassium hydroxide Solid Local Truck 100

62 Sodium bicarbonate Solid Local Truck 100

63 Sodium cyanide Liquid Local Tanker 250

64 Sodium hypo chlorite Liquid Local Tanker 100

65 Sodium nitrite Powder Local Truck 100

66 Sodium thio sulphate Powder Local Truck 100

67 Sulphuric acid Liquid Local Tanker 100

68 TCAC Liquid Local Tanker 100

69 TEBA Solid Local Truck 390

70 Thionyl chloride Liquid Local Tanker 250

71 Toluene Liquid Local Tanker 200

72 Tri ethyl Amine Liquid Local Tanker 300

73 Xylene Liquid Local Tanker 300

74 Zinc sulphate Solid Local Truck 390

Resource optimization/ recycling and reuse envisaged in the project , if any , should briefly

outlined :

Resource optimization/recycling and reuse envisaged in the project (Solvent recovery

system) in detail are as mentioned below:

The raw materials will be stored in closed containers and will be handled through closed

system to avoid the handling losses.

The Reactor shall be connected to an efficient condenser system with cooling/chilling

water/brine circulation.

Reactor and solvent handling pumps shall have mechanical seals to prevent leakages.

Also provide with breather valve to prevent losses.



Solvent will be taken from storage tank to reactors through closed pipe line. Storage tank

shall be vented through trap receiver & condenser operated on cooling water.

The condensers shall be provided with sufficient HTA and residence time so as to

prevent any loss of solvent.

Proper earthing shall be provided were ever solvent handling is done.

Entire plant is flameproof.

Solvent will be stored as per statutory requirement. Solvent will be kept at a separate

specified area with all the safety measures.

RO Permeate will be recycled in the process to minimize the fresh water consumption.

Details of solvent used, recovered & recycled as under;

Sr.

No.

Solvent to be

used

Total

Consumption,

MT/Month

Recovered,

MT/Month

Fresh,

MT/Month

%

Recovery

1 N- Hexane 696.4 675.43 20.97 96.99

2 Iso Butanol 29.7 22.85 6.85 76.94

3 Tri Ethyl Amine 62.70 60.62 2.18 96.68

4 Ethyl Acetate 73.05 53.8 19.25 73.65

5 Methylene Di

Chloride

724.1 687.55 36.55 94.95

6 Ethylene Di

Chloride

363.14 340.18 22.96 93.68

7 Di Methyl

Formamide

105.12 97.77 7.35 93.01

8 Toluene 51.76 49.5 2.28 95.63

9 Xylene 1734 1639.5 94.5 94.55

(viii) Availability of water its source, Energy/power requirement and source should be given :



Availability of water its source, Energy/power required and its source is below.

WATER CONSUMPTION & EFFLUENT GENERATION (M3/Tone)

Sr.

No.

Product Water

Consumptio

n, M3/tone

Effluent Generation, M3/tone

High

COD/NH3

stream to

Incinerator

High TDS

stream to

MEE

Normal stream

to ETP

1.1 Cyper methric

Acid Chloride

13.997 0 3.192 2.061

Or

1.2 M- Phenoxy Benzaldehyde

7.194 0 3.613 0.215

Maximum 13.997 0 3.613 2.061

2.0 Acephate

Technical

1.24 2.51 0 0

3.0 Deltamethrin 31.827 0 13.229 20.215

4.0 Alpha

Cypermethrin

7.2 0 0 9.221

5.0 Permethrin 1.483 0 0 1.305

6.0 Chlorpyriphos 4.27 0 6.979 0

7.0 Tricyclozole 9.66 0 10.216 0

8.0 Hexaconazole 5.793 0 7.5 0

9.0 Propiconazole 2.6 0 4.228 0.185

10.0 Mancozeb 2.765 0 4.5 0

11.1 Glyphosate 4.438 4.35 7.159 0

Or

11.2 Dicamba 15.66 0 23.248 0

Maximum 15.66 4.35 23.248 0

12.0 Pendimethlin 2.853 0 6.639 0.222



WATER CONSUMPTION & EFFLUENT GENERATION (M3/Day)

Sr.

No.

Product Water

Consumption

, M3/day

Effluent Generation, M3/day

High

COD/NH3

stream to

Incinerator

High TDS

stream to

MEE

Normal

stream to

ETP

1.1 Cyper methric

Acid Chloride

26.9 0.0 6.1 4.0

Or

1.2 M- Phenoxy Benzaldehyde

20.8 0.0 10.4 0.6

Maximum 26.9 0 10.4 4.0

2.0 Acephate

Technical

2.4 4.8 0.0 0.0

3.0 Deltamethrin 12.2 0.0 5.1 7.8

4.0 Alpha

Cypermethrin

8.3 0.0 0.0 10.6

5.0 Permethrin 1.4 0.0 0.0 1.3

6.0 Chlorpyriphos 13.1 0.0 21.5 0.0

7.0 Tricyclozole 3.7 0.0 3.9 0.0

8.0 Hexaconazole 3.3 0.0 4.3 0.0

9.0 Propiconazole 1.5 0.0 2.4 0.1

10.0 Mancozeb 42.5 0.0 69.2 0.0

11.1 Glyphosate 4.3 4.2 6.9 0.0

Or

11.2 Dicamba 90.3 0.0 134.1 0.0

Maximum 90.3 4.2 134.1 0

12.0 Pendimethlin 3.3 0.0 7.7 0.3

Total 208.9 9.0 258.6 24.1



Note:

Total water consumption for processing & product washing will be 208.9

m3/day.

Total effluent generation from the process & product washing will be 291.7

m3/day.

OVERALL WATER CONSUMPTION & EFFLUENT GENERATION, M3/DAY

Sr. No.

Particulars WATER CONSUMPTION,

M3/day

Effluent Generation, M3/day

1.0 Domestic 15.0 12.0

2.0 Processing & product washing

208.9 291.7

3.0 Floor, container, equipment Washing

10.0 10.0

4.0 Cooling Tower 400.0 75.0

5.0 Boiler 215.0 25.0

6.0 Scrubber 10.0 10.0

7.0 Gardening 15.0 0

8.0 Total 873.9 423.7

9.0 Total Industrial 843.9 411.7

10.0 Treatment in RO Plant - 120.0

11.0 RO Rejection - 20.0

12.0 Treatment in MEE - 282.7

13.0 Treatment in SBT - 258.5

14.0 Recycled to process from RO permeate

100.0 -

15.0 Treatment in incinerator - 9.0

16.0 Net Fresh water 773.9 -

17.0 Net Discharge - 258.9

SOURCE: Water will be met through Sayakha Industrial Estate.



ENERGY REQUIREMENT AND ITS SOURCE

Sr. No.

Particulars Proposed Source

1 Steam

requirement 28500 kgs. /hrs.

Proposed 15TPH x 2 capacity of coal fired

steam boiler

POWER REQUIREMENT AND ITS SOURCE

Sr. No.

Particulars Proposed Source

1 Power –Electricity

requirement

2300 KVA Will be sourced from Dakshin Gujarat Vij Co. Ltd.

(ix) Quantity of waste to be generated ( liquid and solid) and scheme for their

Management/disposal :

WATER BALANCE DIAGRAM

Total Water Consumption: 873.9 M3/day (Fresh: 773.9 + Recycle from RO: 100 M3/Day)

Domestic: 15 Processing: 208.9 Cooling: 400 Boiler: 215 Washing: 10 Scrubber: 10 Gardening: 15

291.7 75 25 10 10

Holding tank: 258.5 M3/Day

RO Plant: 120 RO Permeate: 100 Recycle

RO Rejection: 20Collection tank: 282.7

Neutralization tankCa(OH)3: 18.7 MT/Day

Filtration 36.9 MT/Day ETPsludge to TSDF

Holding tank: 282.7

MEE Condensate from MEE: 195

39 MT/Day of Salt to TSDF

High COD/NH3: 9.0 High TDS + Normal: 282.7 (258.6+ 24.1)

Collection tank: 9.0

Neutralization tank

Filtration

Holding tank: 9.0

Incinerator

Ca(OH)3: 0.5 MT/Day

1.0 MT/Day ETPsludge to TSDF

ATFD: 82.5 Filtrate : 43.5

Loss: 5.2238.5

Soil Bio Reactor: 1

Treated effluent pipe line

Arabian Sea

Treated effluent holding tank

Catalytic Advance Oxidation system

Soil Bio Reactor: 2

Soil Bio Reactor: 3

Soil Bio Reactor: 4

Incineration ash: 0.7 MT/day

Solvent Stripper

0.2 MT Solvent Recovered



Quantity of waste to be generated (liquid and solid) and scheme for their Management/

disposal is enclosed as Anneuxure-3,4

(x) Schematic representations of the feasibility drawing which give information of EIA purpose:

A schematic representations of the feasibility drawing is attached as Annexure-7.

4. Site Analysis

(i) Connectivity :

The project is to be located in Plot. No. C-195 & 196, Saykha industrial estate, Ta: Vagra, di:

Bharuch, Gujarat which is very well connected to National Highway no.8, Western Railways.

And the nearest air port (Surat) and port are 50 KM away from the project site by road.

(ii) Land Form, Land use and Land ownership :

The land is in the form of industrial shed owned by Gujarat Industrial Development

Corporation.



(iii) Topography (along with map) :

Topography map showing the elevation of study area is below;

The catchment area of the proposed project site altitude is 35 m (a.m.s.l) consists of the

near site is flat topped, highly dissected plateaus and dyke ridges running in a west to east

direction. The Main River (Narmada) in the catchment area flows in incised meanders

forming steep geomorphologically ‘V’ shaped valleys with steep sides. The entire catchment

has a drainage pattern that shows the characteristics of the tributaries joining major channel

and eroding at right angle. Thus, the drainage pattern can be said as trellis pattern and

rectangular pattern of drainage. The piedmonts at the base of the steep plateaus and dyke

ridges are covered with thin soils, which support agriculture in very few areas. The river

valley, wherever flat, has good quality soil and is mostly cultivated based on the availability

of water. The river valley fills with thick alluvium provides the only area for cultivation.

The command area of the proposed project is surrounded by moderately dissected plateaus

and piedmont slopes. The slope of the land along the piedmont and the nature of flow of the

streams. The Narmada River with tributaries in the piedmont slope area show parallel

pattern, which are partly controlled by the lineaments. Along the river valley the flood plain

consists of good quality soil, suitable for cultivation. The largest portion of the command

area is the alluvial plain, which has been formed by the river Man. The alluvial plain is

studded with number of residual hills with degraded forests. The river man in the command

area also flows in straight channels, which shows that the river is structurally controlled.

Topography map showing the elevation of the study area below. The topographical map is

enclosed as Annexure-5.

(iv) Existing land use pattern (agriculture, non-agriculture, forest , water bodied ( including

area under CRZ)), shortest distances from the periphery of the project to periphery of the

forest, national park, wild life sanctuary , eco sensitive areas, water bodies (distance from

the HFL of the river), CRZ . In case of notified industrial area, a copy of Gazette notification

should be given :

The proposed project to be located at Sayakha industrial estate, Ta: Vagra, Di: Bharuch. Copy

of plot allotment letter is enclosed herewith as Annexure-6.



The existing land use pattern are as under;

Area Statistics of Land use / Land cover Map

Sr. No. Class Names Area (In

Hectares) Area (In Sq.Km.) Area %

1 Water Body 1363.73 13.64 4.34

2 Open/Barren Land 5076.01 50.76 16.17

3 Agriculture Land 1159.56 11.60 3.69

4 Fallow Land 6291.40 62.91 20.04

5 Open/Degraded Vegetation 412.59 4.13 1.31

6 Vegetation Medium Density 397.40 3.97 1.27

7 River & Canal 23.25 0.23 0.07

8 Marshy Land 919.33 9.19 2.93

9 Salt Affected Land 128.45 1.28 0.41

10 Settlement & Habitation 324.50 3.25 1.03

11 Mud Flat 863.17 8.63 2.75

12 Jetty 32.91 0.33 0.10

13 Salt Pans 2083.03 20.83 6.63

14 Mangrove(Sparse) 117.30 1.17 0.37

15 Mangrove(Dense) 223.00 2.23 0.71

16 Marshy Vegetation 46.55 0.47 0.15

17 Industrial Area 290.32 2.90 0.92

18 Sea 11589.46 115.89 36.91

19 Seasonal Water Body 59.04 0.59 0.19

Total 31400.99 314.01 100.00



Existing Infrastructure :

The proposed project to be located in Sayakha notified industrial area and notified industrial

area proposes the entire infrastructure like water, electricity, roads, rail, transportation,

availability of raw material and drainage system & CETP etc.

(vi) Soil classification :

Soil Characteristics under Project Area are as below Table;

CATEGORY AREA-

SQ KM

DESCRIPTION TAXONOMY1 TAXONOMY2 CLASS SUB

CLASS

A 88.93 Very deep, moderately well

drained, calcareous, fine

soils on very gently sloping

alluvial plain with slight

erosion and moderate

salinity; associated with very

deep moderately well

drained, calcareous, fine

soils with moderate erosion.

Fine,

montmorillonitic

(calcareous),

hypothermic

Typic

Chromusterts

Fine,

montmorillo

nitic

(calcareous)

hyperthermi

c Udic

Chromuster

s

Soils of

west

coast

(soils of

Gujarat

plain)

Soils of

alluvial

plains

C 108.64 Very deep, poorly drained,

calcareous fine-loamy soils

on very gently sloping

coastal plain with moderate

erosion and strong salinity;

associated with very deep ,

Fine-loamy,

mixed

(calcareous),

hyperthermic

Aeric

Haplaquepts

Fine, mixed

(calcareous)

,

hyperthermi

c Typic

Halaquepts

Soils of

west

coast

(soils of

Gujarat

plain)

Soils of

coastal

plains



imperfectly drained,

calcareous, fine soils with

severe erosion and strong

salinity.

- 116.43 Sea - - - -

(Courtesy: Environmental Information Centre, New Delhi)

(vii) Climate data from secondary sources :

Climatic data from secondary sources will be incorporated in EIA Study.

(viii) Social Infrastructure available :

A) Natural Resource Management – The main focus of this program will be to maximize the

yield returns of the farmers through efficient management of existing resources & extension

of new agricultural practices.

1) Integrated Agricultural Growth Project – For improvement and use of the modern

techniques and thereby would certainly contribute to prosperity in the agriculture

sector and reduce the rural poverty by programs like Farmers Training, Nursery

Growing Trainings, Modern agriculture equipment distribution programs etc.

2) Animal Husbandry Projects – Various programs like health checkups & treatment,

vaccination program, Anti sterility camps, breed improvement etc. will be carried



out.

B) Income Generation Program -

1) Establishment of Self help groups.

2) Rural Entrepreneurship Development Program

3) Handcrafts Development Program

4) Vocational Training

5) Business process outsourcing

C) Health, Education & Infrastructure

1) Aids Awareness Program

2) General Health Camps

3) Innovative Teaching Methods

4) Adult Education

5) Sanitation

6) Infrastructure Development Projects

5. Planning Brief :

(i) Planning Concept ( Type of industries, facilities, transportation etc) Town and Country

Planning /Development authority Classification :

Type of Industry: Proposed Agro Chemical Unit

There is a cluster of numerous large-scale & medium-scale industries, engaged in manufacture of variety of products, for example pharmaceuticals, dyes and chemicals, specialilty chemicals, pesticides and others in the Gujarat Industrial Development Corporation (GIDC) of Sayakha.

(ii) Population Projection :

Name Population

(Persons)

Population

Density

(Person / sq.

km.)

Sex ratio

(No. of females

per 1000 males)

Within 5 km Radius (1991) 13674 174 797

Within 10 km Radius (1991) 21790 69 855

Taluka Vagra (1991) 68874 80 927

Taluka Vagra (2001) 82569 94 916

District Bharuch (1991) 1546145 171 931

District Bharuch (2001) 1370104 210 920



(iii) Land use Planning (breakup along with green belt etc) :

The proposed project is to be located within the Sayakha Industrial Area by Government of

Gujarat and due to the proposed project there will not be any change in the land use pattern

of the region. Proposed Green belt planning in the project area is as below.

For Green Belt Development, the company proposes to develop a green belt on a land of 11101 sq. meter Area i.e. 33% area of the total land, which is 33640 sq. meters. The company shall develop green belt along the periphery of the proposed site and in common premises available outside the company premises.

Site plan with Area table



Area Table

Sr. No Particulars Area in m2

1 Production plant 3600

2 Boiler & coal storage 816

3 Other utilities 200

4 Solid Raw material storage 500

5 Finished product storage 816

6 Solvent tank farm 500

7 Liquid Raw material storage 816

8 ETP/MEE/Incineration & Solid waste storage

612

9 Plantation 11100

10 Weigh bridge, Parking & Security area 200

11 Office & Admn 500

12 Laboratory 250

13 Internal road 3500

14 Open space 9230

15 Scrap Yard 1000

Total 33640

(iv) Assessment of Infrastructure demand ( Physical & Social) :

Employment would be as per prevailing norms of state government for skilled and

unskilled people for the proposed project activity.

Social Welfare

Cordial relation with the industry shall be established and representation shall be made

to villagers for help for creation of facilities related to health, education, etc.

(v) Amenities/ Facilities :

Details of amenities available in study area are as under;

Taluka Village Educationa

l

Medical Drinking

Water

Post &

Telegra

ph

Commun

ication

Approach

to Village

Nearest

Town

Power

Supply

Vagra Galenda P(2),Ac,O RP,CH

W

T,W,TK PO BS PR,KR Bharuch EA

Samatp

o

r

P(2),Ac RP,CH

W

W,TK -(-5

Kms)

BS PR,KR Bharuch EA

Vav P(2),Ac RP,CH

W

T,W,TK,

HP

-(-5

Kms)

BS,RS PR,KR Bharuch EA

Jolva P(2),Ac,O PHS,FP W,TK -(-5 BS,NW PR,KR Bharuch EA



C,RP,C

HW

Kms)

Vadadla P(2),Ac CHW W,TK PO BS PR,KR Bharuch EA

Dahej P(4),H,Ac(

4),O

PHC,D,

FPC,RP

,

CHW

T,W,TK PTO,

Phone

BS,RS,N

W

PR,KR Bharuch EA

Lakhiga

m

P(2) PHS,RP

,CHW

W,TK po BS,NW PR,KR Bharuch EA

Luvara P(2),Ac RP,CH

W

W,TK -(-5

Kms)

BS,NW PR,KR,NR Bharuch EA

Jageshw

ar

P(2),Ac,H RP,CH

W

W,TK PO BS,NW PR,KR,NR Bharuch EA

Ambhet

a

P(2),Ac CHW T,W,TK PO BS,NW KR,NR Bharuch EA

Suva P(2),Ac -(5-10

Kms)

W,TK,R -(-5

Kms)

BS,NW PR,KR,NR Bharuch EA

Rahiad P(2),Ac(2),

O

RP,CH

W

W,TK PO BS,NW PR,KR.NR Bharuch EA

Harinag

ar

Un

inhabite

d

Padariy

a

P(2),Ac RP,CH

W

W,TK PO BS PR,KR Amod EA

Kadodar

a

P(2),Ac(2),

H

PHS,FP

C,

RP,CH

W

W,TK PO BS PR,KR Bharuch EA

Sambhe

ti

P(2),Ac -

(10+K

ms)

W,TK PO BS,RS PR,KR Bharuch EA

ABBREVIATIONS

1. Education

P-Primary Elementary School

H-Matriculation or Secondary

O-Other Educational Institution

PUC-Higher Secondary/Intermediate/pre-University/junior Collage



AC – Adult literacy class

TR – Training center

2. Medical Facilities

RP-Registered Private Practitioner

PHS-Primary Health Centre

FPC-Family Planning Centre

D- Dispensary

CHW - Community Health Worker/Health Worker

H - Hospital

NH - Nursing Home

MH - Maternity Home

PHC - Public Health Centre

CWC - Child Welfare Centre

TB - T.B Clinic

O - Others

3. Drinking Water

T-Tap Water

HP-Hand Pump

TK-Tank Water

W-Well Water

R-River Water

C-Canal

N - Nallah

S - Spring

4. Post & Telegraph

PO-Post Office

PTO-Post & Telegraph

Phone-Telephone Communication

5. Transportation

RS- Railway Station

BS-Bus Station

NW-Navigable Waterway

6. Approach to Village



6.

PR-Pucca Road

KR-Kuccha Road

7. Power Supply

EA-Electricity for all purposes

EAG - Electricity for Agriculture

ED - Electricity for domestic

EO - Electricity for other purpose like Industrial, Commercial etc.

Proposed Infrastructure :

(i) Industrial Area (Processing Area).

The proposed infrastructure to manufacture products will be built with standard engineering

design considering all the relevant parameters related to environment, health and safety.

(ii) Residential Area (Non Processing Area) :

No residential area is involved in the proposed project

(iii) Green Belt :

Green belt will be provided and maintained at the tune of 33 % of the total land area.

(iv) Social Infrastructure :

Water Supply by GIDC

Power supply by TEL/DGVCL

(v) Connectivity (Traffic and Transportation Road/ Rail/ Metro/ Water ways etc) :

The project site is very well connected by road through National Highway no. 8, railways.

Major factors involved in the selection of site are listed below:

Site is very well connected by road

Proximity to Raw Material suppliers

Availability of sufficient land free from cultivation and will have single crop pattern

Availability of power facilities

Availability of water for industrial use

(vi) Drinking Water management ( Source & Supply of water ) :

Source of water is from GIDC water supply services.

(vii) Sewerage System :

GIDC has proposes sewerage system to dispose the sewage effluent.

(viii) Industrial Waste Management :

Industrial liquid effluent generation during the manufacturing of proposed products

will be treated and discharge into treated effluent drainage line proposed by GIDC

for ultimate disposal into Arabian Sea.



Generated domestic liquid waste is being disposed off through soak pit system to

drainage.

(ix) Hazardous/ Solid Waste Management :

No Type of waste Category Qty. MT/

month

Treatment Disposal

1 ETP waste) 34.3 13700

Dried, packed in bags Dispose off into TSDF, BEIL, Ankleshwar &

Detox, Dahej

2 Salt from MEE 34.3 14040 Dried, packed in bags Dispose off into TSDF, BEIL, Ankleshwar &

Detox, Dahej

3 Used Oil 5.1 0.2 Packed in carboys Incinerated into own Incineration system

4 Discarded containers

33.3 5.0 De-contaminated, stored

Sell to authorized recycler





7 Used rubber hand

gloves/pipes etc



(x) Power Requirement & Supply / Source :

Power requirement for proposed project will be taken from TEL/DGVCL.

7. Rehabilitation and Resettlement (R&R) Plan:

(i) Policy to be adopted (Central/ State) in respect of the project affected persons including

home oustees, land oustees and landless laborers (a brief outline to be given):

There is no habitation on the proposed project activity area and it is barren land, so R & R

policy is not applicable to this project.

There shall not be displacement of any population in project area. Any major activity that

may lead to resettlement of the people is considered as permanent impact. Hence, there is

no permanent impact on this account. The increasing industrial activity will boost the

commercial and economical status of the locality up to some extent.

8. Project Schedule & Cost Estimates :

(i) Likely date of start of construction and likely date of completion ( Time schedule for the

project to be given ) :

After obtaining Environmental clearance and Consent to Establish from GPCB, the company

shall start the proposed construction and commissioning of the proposed project.



(ii) Estimated project cost along with analysis in terms of economic viability of the project:

Estimated project cost along with the analysis in terms of economic viability of the project is

given as below;

Plant & Machinery, Pipeline & Fittings, Electrical Installation, Safety systems, etc. are the

major heads considered in the Capital Cost Projection for the proposed project. Environment

Protection has also been considered in planning the Cost Projection, which will include

Green belt development, safety systems, etc.

CAPITAL COST PROJECTION

Sr. No. Particulars Cost in Rs.(Lacs)

1.0 Land 33640 m2 656.25

2.0 Building 2343.79

3.0 Plant & Machinery 10475.35

4.0 Furniture & Fixture 90.0

5.0 Electrical installation 202.95

6.0 D G Set 150.0

7.0 Laboratory equipments 71.70

8.0 Environmental management system

1000.0

9.0 Computers 10.0

10.0 Preliminary & pre-operative expenses

975

11.0 Margin money for working capital

1000.0

12.0 Total Project Cost 16975.04

1.0 Utilities

1.1 Boiler, kgs/hr 30000

1.2 Cooling Tower, TR 2000

1.3 Chilling plant, TR 1000

1.4 D.G. Set (Standby), KVA 1000 x 3

1.5 Power from TEL/DGVCL, KVA 2300

2.0 Fuel

2.1 Coal, kgs/hr 16000

2.2 HSD, kgs/hr 360

2.4 LDO/FO for incinerator, kgs/hr 300

3.0 Water from GIDC KL/day 400

3.1 Waste Water Generation(Industrial) KL/day

412

3.2 Waste Water Disposal(Industrial) KL/day

259



PROJECT VIABILITY

Sr. No. PARTICULARS AMOUNT IN Cr./Year

1 Proposed Sale 900

2 Raw Material Cost 503.1

3 Power & Fuel 119.25

4 Labor Cost 75.375

5 Environmental Management System 51.525

6 Maintenance Cost 13.5

7 Selling, packing & Office Expenses 58.5

8 Proposed Profit 78.75

The company will provide budgetary provision for the recurring expenses for environmental

issues while planning the allocation of funds during the annual budgetary planning.

Recurring Cost per annum

Sr. No. Component

Proposed

(Rs. In

Lacs/annum

1. Environment & Safety Management System 1450

2. Greenbelt Maintenance 240

3. Solid waste Disposal 600

Total 2290

9.

Analysis of Proposal ( Final Recommendations):

(i) Financial and social benefits with special emphasis on the befit to the local people

including tribal population, if any, in the area:

Proposed project activity will provide benefits to the local people in terms of financial and

social welfare.

Local people will get direct financial benefit by way of employment.

Local people will get some contracts of supply and services to get indirect income.

Company will contribute in improving education and health facilities in nearby area.



ANNEXURES

ANNEXURES



ANNEXURE-1 The map showing general location, specific location and project boundary and project site layout of Heranba Industries Limited, located at Plot. No. C-195, 196, Sayakha industrial estate, Ta: Vagra, di: Bharuch, Gujarat. The location of the project site can be viewed in Figure 1.1

Fig. 1.1: Location map showing the Project site



ANNEXURE-2

Detailed project description with process details - MANUFACTURING PROCESS The company is using the latest available process technology for the production. This chapter includes the

manufacturing process of the product, chemical reactions, and material mass balance for the product.

(1) Cyper methric Acid Chloride:

Stage -1:- Preparation of tetra Chloro Butyro Nitrite (TBN)

Reaction of Carbon Tetra Chloride with Acrylonitrile at 100°Cto 125°C in present of cupric chloride catalyst,

DEA HCI as a buffer and Acetonitrile as solvent gives Tetra Chloro Butyro Nitrile (TBN (.Excess CTC and

Acetonitrile is removed by distillation. In water wash cupric chloride DEA HCI is removed.

Stage - 2:- Preparation of tetra Chloro Butyic Acid. (TBA)

Acid hydrolysis of crude TBN using 30 % HCI solution gives tetra Chloro Butyic Acid (TBA). After reaction

TBA is separated from bottom and dehydrated up to moisture contain level of 0.1 %.

Stage - 3:- Preparation of tetra Chloro Butyric Acid Chloride (TBAC)

Reaction of TBA with Thionyl Chloride in presence of Dimethyl Formamide at 60°C gives tetra Chloro

Butyric Acid Chloride (TBAC), during reaction SO2 and HCI gas is evolved which is scrubbed in scrubber.

Crude TBAC is further distilled under high vacuum. The purity of Distilled TBAC is 98 %.

Stage-4:- Preparation of 2 - Chloro CycIo Butanone Derivative (2 CB)

TBAC is reacted with isobutylene in presence of Tri Ethyl Amine (TEA) at 70°C under 5.0 Kg/cm2 pressure, n-

Hexane is used as solvent. After reaction excess Isobutylene is recovered. The whole mass is washed with

water to remove TEA. The organic mass is neutralized with Sodium bi carbonate and organic mass is

transferred for further process.

Stage - 5:- Preparation of Sodium Salt of Cypermerhric Acid (Na-CMA)

2 CB is isomerised to 4 CB in presence of catalyst and then directly reacted with caustic lye solution which

gives Na-CMA.

Stage - 6:- Preparation of Cypermerhric Acid (CMA)

Na- CMA is acidified with dilute Sulphuric Acid at room temperature. CMA is extracted in n-Hexane.

Aqueous layer (sodium sulphate + sodium chloride + organic impurities) is drain to ETP

Stage - 7:- Preparation of Cypenmerhric Acid Chloride (CMAC)

Reaction of CMA with Thionyl Chloride in presence of Dimethyl Formamide at 60X gives Cypermethric Acid

Chloride (CMAC). During reaction SO2, and HCI gas is evolved which is scrubbed in scrubber. Crude CMAC is

further distilled under high vacuum. The purity of Distilled CMAC is 98 %.



(2) M- Phenoxy Benzaldehyde (MPBD):

Benzaldehyde is react with bromine in presence of aluminum chloride as catalyst and Ethylene dichloride as

a solvent to obtained m-bromo Benzaldehyde, which is further react with mono ethylene glycol to get

acetal of m-bromo Benzaldehyde.

Acetal of m-bromo Benzaldehyde is react with phenol in presence of KOH to obtain acetal of m-phenoxy

Benzaldehyde, which is subjected to hydrolysis to obtained m-Phenoxy Benzaldehyde.

(3) Acephate Technical

DMPAT in MDC as solvent is ‘Isomerised’ by aid of Di methyl Sulphate (DMS) to give Methamidophos

(MMP). This MMP is then further ‘Acetylated’ by Acetic Anhydride to yield Acephate. This reaction

generates Acetic Acid, which is neutralized by Ammonia solution.

The neutralized mass is then further extracted repeatedly with MDC. The aqueous layer generated contains

‘Ammonium Acetate and is incinerated. The organic mass obtained is fed to MDC recover unit.

MDC is recovered by atmospheric and vacuum distillation. This recovered MDC is recycle back in the

process. The residual mass of the distillation is carried forward for Acephate recovery by crystallization

Ethyl Acetate is added to the residual mass and crystallized to get Acephate. The wet Acephate thus

obtained from filtration is further dried in rotary vacuum dryer.

The mother liquor obtained from filtration is further used to recover Ethyl Acetate under vacuum. The Ethyl

Acetate recovered is recycled back in the process. The residue obtained after Ethyl Acetate recovery is

incinerated

(4) Delta Methrin:

Solution of Cypermethric acid is reacted with HBr gas in presence of AlCl3 to obtain Tribromo Cypermethric

acid. Tri bromo Cypermethric acid is converting into Di bromo Cypermethric acid in alkaline condition Di

bromo Cypermethric acid is reacting with methanol in acidic condition to form Di bromo Cypermethric

ester. This Di bromo Cypermethric ester is taken for fraction distillation and makes pure Di bromo

Cypermethric ester. Di bromo Cypermethric ester is hydrolyzed under alkaline condition at elevated

temperature to form Di bromo Cypermethric acid. Di bromo Cypermethric acid is reacting with Thionyl

chloride in presence of catalytic amount of DMF to generated which is scrub in NaOH solution. Di bromo

Cypermethric acid chloride. During the reaction SO2 and HCl Di bromo Cypermethric acid chloride is

condensed with m-phenoxy Benzaldehyde and sodium cyanide in presence of toluene as solvent. out

toluene to obtain RS-Deltamethrin crude. Separated organic layer and distilled out toluene to obtain RS-

Deltamethrin crude. Make solution of crude RS-Deltamethrin in isopropyl alcohol and add triethyl amine

and maintain for 20 hrs to obtain S-Deltamethrin which is filtered and wash with IPA to obtain wet cake of

Deltamethrin. This wet cake is dry to obtain pure Deltamethrin technical.



(5)Alpha Cypermethrin:

Solution of CMAC (in – house manufacture as well as procured from the market) and Meta Phenoxy

Benzaldehyde ( MPBD) reacts with solution of Sodium Cyanide in water in presence of phase transfer

catalyst at 20°C to 30°C to give Cypermethrin. After reaction, water and Cyanide layer is separated. This

layer is treated with Sodium Hypochlorite to destroy Sodium Cyanide .The organic mass is washed with

water to remove impurities. The obtain Cypermethrin is subjected to Epimerization at 25°C in presence of

Tri Ethyl Amine (TEA) in solvent n- Hexane to obtain Alphamethrin. Then it is filtered and dried under

vacuum. N-Hexane and Tri Ethyl Amine (TEA) is recovered and recycled. The purity of Alphamethrin obtain

will be minimum 95 %.

(6) Per Methrin:

Cypermethric Acid Chloride (CMAC) reacts with Meta Phenoxy Benzyl Alcohol (MPBAL) at 70°C to 80°C to

give Permethrin. The evolved HCL gas during reaction is scrubbed in water. The reaction mass is washed

with Potassium Carbonate solution to remove the dissolve HCl gas. Permethrin is dehydrated under high

vacuum to remove traces of water. The purity of the Technical product Permethrin obtained will be

minimum 92 %.

(7) Chlorpyriphos technical:

Stage-I HTCP :

Charge the specified amount of raw material in order of solvent, TCAC, Acrylonitrile and Catalyst and mass

is heated upto 140 C under reflex condition. During reaction HCl will be generated and same is absorbed in

water scrubber.

Solvent recovered under vacuums at 730 mm Hg & temperature is maintained at about 110 C. recovered

solvent is recycled in the process and part quantity transferred to Incinerator. Cool the mass temperature

to 105 C and slowly release the vacuum.

Stage-II Sodium HTCP :

Maintain the temperature of the 15 % Sodium Hydroxide solution between 10 – 15 C and slowly add the

hot reaction mass of ‘Stage I’ in it. The reaction mass temperature would increase, however it should not

go above 65 C. Again cool it down to 15 C and digest for 1.0 hours. Filter the entire mass and collect the

ML and transfer to Incinerator. Remove the wet cake.

Stage III: Slurry Preparation :

Take water and charge wet cakes and makes slurry. Also charge calculated amount of caustic lye solution.

Heat the mass. Once the temperature is around 60 - 65 C, shut the autoclave and increase the reaction

mass temperature up to 130 C.



Stage IV: Toxification reaction.

Based on calculation of active content of HTCP in the slurry add catalyst. Also add EDC as a solvent and

maintain the reaction temperature around 50 C. Add DETC over a period of 3 – 4 hours maintaining the

reaction temperature around 50 2 C. Once the reaction is completed settle the mass for 1.0 hour. Filter

the mass through filter. Separate out the organic and aqueous layer. Aqueous transfer to Incinerator and

organic mass is transfer to EDC recovery section

Stage V: EDC Recovery :

Slowly raise the temperature and vacuum and recover EDC at 755 mm of Hg and temperature at 70 C.

Recover EDC is recycled in the stage IV. After recovery of EDC, CPP technical is drum out for final packing

(8) Tricyclozole:

4 HMBT is react with formic acid at elevated temperature to form precipitated of Tricyclozole. Then filter

precipitated & wash with water followed by drying to obtain Tricyclozole.

(9) Hexaconazole technical:

2,4-dichloro valerophenone is made to react with dimethyl sulphate and potassium hydroxide in presence

of dimethyl sulphide to give Oxirane. Solvent dimethyl sulphide is recovered by distillation and the Oxirane

is separated from the reactor. Then water is adding to the reactor to dissolve salt from during the reaction

and transferred to ETP.

In dimethyl formamide, potassium carbonate, 1,2,4-triazole is added and then the above prepared Oxirane

is added at reflux temperature. After completion of the reaction the mass is filtered and then solvent DMF

is distilled out. Then the product Hexaconazole is isolated by adding water . the slurry is filtered, centrifuge

and dry. The filtered potassium carbonated is washed with DMF to recovered product.

(10) Propiconazole technical:

2,4-Dichloro Acetophenone is reacting with 1,2-Propanediol in presence of solvent as a toluene to give 1,3-

dioxolane -2-(2,4-Dichloro phenyl)-2-Methyl-4-n-Propyl, which is further reacting with Bromine to give 1,3-

dioxolane -2-(2,4-Dichloro phenyl)-2-bromo methyl-4-n-Propyl ,which is further reacting with 1,2,4-Triazole

in alkaline media to give crude Propiconazole which is distilled out to give pure Propiconazole technical.

(11) Mancozeb Technical:

Stage 1: Carbon disulphide and Ethylene Diamine and Sodium hydroxide are reacted in the presence of

water to form the disodium salt of Ethylene Bis Dithio Carbamate hexhydrate(DBH).

Stage 2: Disodium salt of Ethylene Bis Dithio carbamate hexahydrate is reacted with Manganese sulphate

to form manganese salt of Bis Dithio Carbamate.

Stage 3: The Manganese salt further reacts with Zinc sulphate to convert to Mancozeb.Slurry is initially

spray dried and subsequently vacuum dried for Mancozeb powder formulation.



(12) Glyphosate:

Di ethyl amine is reacted with sodium hydroxide in presence of catalyst under pressure of nitrogen at an

elevated temperature. This results into formation of Di sodium salt of Imino di acetic acid along with

hydrogen. The product is isolated and catalyst is recovered & recycled in the next batch.

Di sodium salt of Imino Di acetic acid is reacted with formaldehyde and phosphorus tri chloride at elevated

temperature resulting into phosphono methyl Imino di acetic acid. The product is isolated by filtration wet

cake of PMIDA used for next stage.

Phosphono Methyl Imino acetic acid slurry is prepared by addition of ammonia solution and ammonia salt

of Phosphono methyl Imino di acetic acid is further oxidized by molecular oxygen to ammonia salt of

phosphono methyl Imino acetic acid. Followed by pH adjustment by HCl addition & followed by further

drying.

(13) 3,6 Di Chloro 2 Methoxy Benzoic acid (DICAMBA):

DICAMBA(2-Methoxy-3,6-dichloro benzoic acid) is manufactured starting from 2,5-dichloro aniline.In the

first step,2,5-dichloro aniline is diazotized in sulphuric acid medium with aqueous solution of sodium nitrite

at 5 – 6°C.The diazonium sulphate so formed is not isolated but decomposed by addition to hot water and

2,5-dichloro phenol so formed is isolated by steam distillation.The 2,5-dichlorophenol is then carbonated

by carbon dioxide to yield 2-hydroxy-3,6-dichloro benzoic acid.

First 2,5-dichloro phenol is treated with aqueous solution of potassium hydroxide to form potassium salt

which is dehydrated by addition of xylene and distillation of water as water-xylene azeotrope.The dry

potassium salt is then treated with carbon dioxide at 130 – 140°C in xylene solution under a pressure of 35

kg/cm2 .The potassium salt of acid formed is neutralized with hydrochloric acid to recover the benzoic acid

derivative. The unconverted phenol is recovered from xylene solution.In the last step,the 2-hydroxy-3,6-

dichloro benzoic acid is methylated with dimethyl sulphate and aqueous sodium hydroxide to give 2-

methoxy-3,6-dichloro benzoic acid (DICAMBA).The product is isolated after neutralization with aqueous

hydrochloric acid and extraction with solvent. Toluene extract is washed with water and the product is

recovered by distillation of toluene.

STAGE I : 2,5-Dichlorophenol Formation

Dichloroaniline is dissolved in 75-76% solution of sulphuric acid at 80°C and the salt is prepared.The cold

salt is treated with aqueous solution of sodium nitrite at 5-6°C to form the diazonium sulphate.The

diazonium sulphate is decomposed in hot water to yield 2,5-dichlorophenol which is separated by steam

distillation.

The spent sulphuric acid containing sodium sulphate is taken for recovery.The nitrogen gas liberated is

vented out.Total time cycle 18 hours.

STAGE II : 3,6-Dichloro Salicylic Acid formation

Dichlorophenol is treated with aqueous potassium hydroxide to form the potassium salt,which is

dehydrated by addition of xylene and removal of water azeotropically.The dried potassium salt is

suspended in xylene in an autoclave and carbon dioxide is passed at 140°C and a pressure of 35kg/cm2 is

maintained till the reaction is complete.A partial convertion(32%)is achieved and the unreacted



dichlorophenol is recovered and recycled.The potassium salt of the acid obtained is neutralized with

aqueous Hydrochloric acid.The solid obtained is diluted and washed with water and dried.

STAGE III : 3,6-Dichloro-2-Methoxy Benzoic Acid

3,6-Dichlorosalicylic acid is methylated at 100°C using water as solvent with dimethyl sulphate and sodium

hydroxide.The methylated acid is recovered by neutralization with aqueous hydrochloric acid.The product

is filtered and washed with water and the technical product DICAMBA obtained is dried.

(14) Pendimethlin Technical:

Step-1 Hydrogenation

Charge 4-nitro-3,4-xylidine ,diethyl ketone and catalyst in autoclave and purged hydrogen till complete

reaction. Then filter catalyst and recover excess diethyl ketone to obtained N-(1-ethyl propyl)-3,4-xylidine .

Step-2 Nitration

Prepare a mixture of water, nitric acid and sulphuric acid in reactor. Prepare a mixture of N-(1-ethyl

propyl)-3,4-xylidine with EDC solvent . add this solution in mixed acid at certain temperature, after

completion of addition digest reaction mass for 4 hrs. After completion of reaction mass separate spent

acid from bottom and wash organic mass with water and separate aqueous layer and neutralized and then

transfer to ETP.

Charge organic mass and add acetone and HCl (30%) and maintain for 6 hrs at 70°C after completion of

reaction neutralized excess HCl by NaHCO3 solution. Separate aqueous layer and wash organic mass with

water. Separate organic mass. Take organic mass for EDC recovery to obtain Pendimethalin.



CHEMICAL REACTION & MASS BALANCE

Cyper methric Acid Chloride:

Stage - 1

Cl

CCl4 CH2 CH CN CCl3 CH2 CH CN154 53 207

CTC Acrylonitrile Tetra Chloro Butyronitrile

Stage - 2

Cl Cl

CCl3 CH2 CH CN 2H2O + HCl CCl3 CH2 CH COOH NH4Cl207 18 36.5 226

53.5

Tetra Chloro Butyronitrile Water Hydrochloric

AcidTetra Chloro Butyric Acid

Ammonium Chloride

Stage - 3

Cl Cl

CCl3 CH2 CH COOH SOCl2 CCl3 CH2 CH COCl SO2 + HCl226 119 244.5 64 36.5

Tetra Chloro Butyric Acid Thyonil Chloride Tetra Chloro Butyric Acid Chloride Sulphur Di

oxide

Hydrochlor

ic Acid

Stage - 4

Cl Cl

H3C

CCl3 CH2 CH COCl C CH2 CCl3 CH2 C C O + HCl

H3C

H3C C CH2

H3C244.5 56

26436.5

Tetra Chloro Butyric Acid Chloride Isobutylene 2 - Chloro Cyclobutanone Derivat ive Hydrochloric

Acid

Preperation of Tetra Chloro Butyronitrile TBN

Preperation of Tetra Chloro Butyric Acid

Preperation of Tetra Chloro Butyric Acid Chloride

Preperation of 2 - Chloro Cyclobutanone Derivative



Stage - 5

Cl

CCl3 CH2 C C O CCl3 CH2 CH C O

H3C C CH2 H3C C CH Cl

H3C H3C

264 264

2 - Chloro Cyclobutanone Derivat ive 4 - Chloro Cyclobutanone Derivat ive

Stage -6

CCl3 CH2 CH C O + 2 NaO H CCl3 CH2 CH CH C OONa + NaCl

C

H3C C CH Cl H3C CH3

H3C

264 80 267.5 58.5

4 - Chloro Cyclobutanone Derivat ive Sodium Hydroxide Sodium Salt of Saturated Cypermethric Acid Sodium Chloride

Stage -7

CCl3 CH2 CH CH C OONa + NaOH CCl2 CH CH CH C OONa + NaCl

C C

H3C CH3 H3C CH3

267.5 40 23158.5

Sodium Salt of Saturated Cypermethric Acid Sodium Hydroxide Sodium Salt of Cypermethric Acid Sodium Chloride

Preperation of Sodium Salt of Saturated Cypermethric Acid

Preperation of Sodium Salt of Cypermethric Acid

Preperation of 4 - Chloro Cyclobutanone Derivative

Stage - 8

CCl2 CH CH CH C OONa + 1/2 H2SO4 CCl2 CH CH CH C OOH 1/2 Na2SO4

C C

H3C CH3 H3C CH371

231 49 209Sodium Sulphate

Sodium Salt of Cypermethric AcidSulphuric Acid

Sodium Salt of Cypermethric Acid

Stage - 9

CCl2 CH CH CH C OOH + SOCl2 CCl2 CH CH CH C OCl + SO2 + HCl

C C

H3C CH3 H3C CH3

209 119 227.5 64 36.5

Sodium Salt of Cypermethric Acid Thyonil Chloride Cypermethric Acid chloride Sulphur Di oxideHydrochloric

Acid

Preperation of Cypermethric Acid

Preperation of Cypermethric Acid Chloride



(1) CYPERMETHRIC ACID CHLORIDE

Stage : 1TBN

Forcut : 380 Kgs, Acrylonitrile : 500 KgsCTC : 1550 KgsAcetonytrile : 22 KgsCatalyst : 10 Kgs, DEA-HCl : 11 KgsWater : 230 Kgs

Evaporation Loss : 22 KgsForcut Recovery : 380 KgsWaste Water to ETP : 328 Kgs

Stage : 2TBA

29% Ammonium chloride solution: 1753 KgsHCl 30% : 1800 Kgs

Water : 333 Kgs

Stage : 2ATBA Washing Waste water to ETP : 837 Kgs

Water : 281KgsWater from 2 CB : 610 Kgs

Stage : 3TBAC

DMF : 20 Kgs, TC: 1067 KgsWater for HCl : 763 kgsCaustic Lye 48% : 1495

Water for scrubber: 2989 Kgs

Distillation water recycle stage 2A : 286 KgsEvaporation Loss: 174 Kgs, 22.3% Na2SO3 : 5058 Kgs, 30% HCl recycle in stage 2 : 1090 KgsOrganic Residue : 68 Kgs

Stage : 42 CB

IB Recivered : 137 KgsEvaporation Loss: 300 KgsTEA + HCl + 764 C.S Lye : 1622 Kgsn-Hexane Recovery : 4840 KgsSoda wash Aq. : 610 Kgs

n-Hexane : 5140 KgsIB : 594 Kgs, TEA : 824 KgsWater for TEA HCl : 500 KgsSoda Ash : 5.0 KgsWater for Soda Ash : 505 Kgs

TEA Recovered : 824 Kgs

Aq. Mass to MEE : 1562 Kgs

Catalyst : 10 Kgs, TEA : 10 Kgsn-Hexane : 1000 Kgs

Caustic 100% : 971 KgsWater : 5141 Kgs

Stage : 5Na-CMA n-Hexane : 1405 Kgs

Sulphuric Acid : 1199 KgsWater : 514 Kgs

n-Hexane : 3000 Kgs

Stage : 6CMA

6889 (20%) Sodium Sulphate Soln. : 8519 KgsSent To MEE : 1630 Kgs

DMF : 10 Kgs, TC : 606 KgsCaustic Lye 48% : 849, Water for

Scrubber: 1697 Kgs, Water for HCl : 434 Kgs

Stage : 7CMAC

CMAC Distillation

n-Hexane Recovery : 2667 Kgs22.3% Na2SO3 Soln. : 2976 Kgs30% HCl recycle in stage 2 : 620 KgsEvaporation Loss : 333 Kgs

Organic residue : 45 Kgs

CMAC : 1000 Kgs



m-Phenoxy Benzaldehyde reaction chemistry

Stage-1 preparation of m-Bromo Benzaldehyde

CHO

Benzaldehydem.wt.=106

Br2/Cl2

EDCAlCl3

CHO

m.wt.=185

Br

m-Bromo benzaldehyde

Stage-2 preparation of acetal of m-bromo Benzaldehyde

CHO

m.wt.=185

Br

m-Bromo benzaldehyde

+ CH2OH

CH2OH

Mono ethylene glycolM.wt.=62

PTSA

Br

CH

O

O

CH2

CH2

acetal of m-BromoBenzaldehyde M.wt.=229

+ H2O

Stage-3 preparation of acetal of m- phenoxy Benzaldehyde

OH

Phenol M.wt.=94

+

Br

CH

O

O

CH2

CH2

acetal of m-BromoBenzaldehyde M.wt.=229

KOH

Toluene

CH

O

O

CH2

CH2

O

+ KBr

acetal of m-Phenoxy benzaldeyhe M.wt.= 242

+ H2O

CH

O

O

CH2

CH2

O

acetal of m-Phenoxy benzaldeyhe M.wt.= 242

Hydrolysis O

m-Phenoxy benzaldeyhe M.wt.= 198

CHO

+CH2OH

CH2OH

Mono ethylene glycolM.wt.=62

(2) M-PHENOXY BENZALDEHYDE



(2) M-PHENOXY BENZALDEHYDE

Preparation ofBromo

Benzaldelyde

Ethylene dichloride : 2.778 KgsAnhydrous AlCl3: 1.155 KgsBenzaldelyde : 0.7 KgsBromine : 0.578 KgsChlorine : 0.245 Kgs

HCl : 0.251 KgsBr2: 0.05 Kgs HCl Scrubber

Water : 0.904 Kgs

Dumping in chilled Water

FormicAcid : 0.025 KgsHCl (30%) : 0.121 KgsWater : 4.402 KgsWater for Washing : 1.10 KgsSodium thio sulphate : 0.011 Kgs

Reaction Mass : 5.155 Kgs

Aqueous Mass : 5.703 KgsWashing Aqueous Mass : 1.11

Organic Mass : 4.0 Kgs

Solvent Remove

EDC recover & recycle : 2.631 KgsCut-1 : 0.045 KgsResidue : 0.105 KgsLoss : 0.148 Kgs

25% HCl Solution : 1.205 Kgs

Preparation ofAcetyl of m- bromo

Benzaldelyde

m- bromo Benzaldelyde : 1.071 Kgs

Water : 0.104 KgsMEG recover & recycle : 0.415 KgsLoss : 0.006 Kgs

Ethylene glycol : 0.78 Kgs

Preparation ofm -Phenoxy

Benzaldelyde

Water : 0.111 KgsLoss : 0.02 KgsAqueous Mass : 2.083 Kgs

Phenol : 0.582 KgsKOH flakes : 0.384 KgsToluene : 1.448 KgsCuCl : 0.0055 KgsWater : 1.241 KgsC.S Lye : 0.02 Kgs


Hydrolysis

Reaction Mass : 2.793Kgs

H2SO4 5% Solution : 1.09 Kgs

Water : 1.090 KgsMEG recover & recycle : 0.345 Kgs

Layer Separation & Water WashingWater Washing : 0.451 KgsAqueous Mass : 0.44 KgsLoss : 0.012 Kgs

Organic Mass : 2.447 Kgs


Distillation

m- Phenoxy Benzaldelyde : 1.0 Kgs

Toluene recover & recycle : 1.375 KgsLoss : 0.019 KgsCut-1 recycle : 0.03 KgsResidue : 0.023 Kgs



(3) ACEPHATE

P

S

NH2

OCH3

OCH3

O,O-Dimethyl phosphoroamido thioate M.F.=C2H8NO2PSM.wt.= 141

DMS P

O

NH2

SCH3

OCH3

O,S-Dimethyl phosphoroamido thioate M.F.=C2H8NO2PSM.wt.= 141

P

O

NH2

SCH3

OCH3

O,S-Dimethyl phosphoroamido thioate M.F.=C2H8NO2PSM.wt.= 141

+ (CH3CO)2

Isomerisation

H2SO4

Acetylation

acetic anhydride M.F.=C4H6O3M.wt=102

O P

O

CH3CONH

SCH3

OCH3

acephate M.F.=C4H10NO3PS

M.wt.=183

+ CH3COOH acetic acid

M.F.=C2H4O2M.wt.=60

CH3COOH acetic acid

M.F.=C2H4O2M.wt.=60

+ NH4OH Ammonium HydroxideM.F.=NH4OHM.wt.=35

CH3COONH4Ammonium acetateM.F.=C2H7O2NM.wt.=77

+ H2OWaterM.F.=H2OM.wt.=18



DEHYDRATION, ISOMERIZATION &

ACETYLATION

HYDROLYSIS & NEUTRALIZATION

MDC: 1.3 kgsDMPAT: 1.18 kgsAC2O: 0.96 kgsDMS: 0.12 kgsH2SO4: 0.04 kgs

(3) ACEPHATE

Water: 1.24 kgsAmmonia: 0.22 kgs

MDC loss: 0.003 kgsMDC recovered: 0.650 kgs

EXTRACTIONMDC : 9.646 kgsMDC loss: 0.102 kgsAq. ML to incinerator: 2.51 kgs

ATMOSPHERIC DISTILLATIONMDC loss: 0.19 kgsMDC recovery: 8.210 kgs

VACCUM DISTILLATIONMDC loss: 0.214 kgsMDC Recovery: 1.497 kgs

CRYSTALLIZATIONEthyl Acetate: 1.461

FILTERATION EA RecoveryEA loss: 0.293 kgsResidue: 0.330 kgsEA Recovered: 1.076 kgs

DRYING EA loss: 0.092

ACEPHATE: 1.0



Stage-1 Bromination of Cypermethric acid

Stage-2 Dehydrohalogenation & Acidification

Stage -3 Esterification

Stage-4 Acidification

C l2 C = C H -C H -C (C H 3 )2

C H C O O H

C y p e rm e th ric a c id M .F .= C 8 H 1 0 O 2 C l2M .w t.= 2 0 9

+

H B r M .F .= H B rM .w t.= 8 1

H B r

+3

2 H C l

H y d ro c h lo r ic a c idM .F .= H C lM .w t.= 3 6 .5

B r2 H C -C H -C H -C (C H 3 )2

C H C O O H

T rib ro m o C y p e rm e th ric a c id M .F .= C 8 H 1 1 O 2 B r3M .w t.= 3 7 9

B r

B r2 H C -C H -C H -C (C H 3 )2

C H C O O H

T rib ro m o C y p e rm e th ric a c id M .F .= C 8 H 1 1 O 2 B r3M .w t.= 3 7 9

2 N a O H D e h y d ro h a lo g e n a tio n

B r2 C = C H -C H -C (C H 3 )2

C H C O O H

D ib ro m o C y p e rm e th ric a c id M .F .= C 8 H 1 0 O 2 B r2M .w t.= 2 9 8

+

B r

+ H 2 S O 4

N a 2 S O 4 + 2 H 2 O + H B r

s o d iu m s u lp h a te

M .w t.= 1 4 2 M .w t= 1 8 M .w t.= 8 1

w a te r h y d ro b ro m ic a c id

B r 2 C = C H - C H - C ( C H 3 ) 2

C H C O O H

D i b r o m o C y p e r m e t h r i c a c i d M . F . = C 8 H 1 0 O 2 B r 2M . w t . = 2 9 8

+ C H 3 O H

M e t h a n o lM . F . = C H 3 O HM . w t . = 3 2

H 2 S O 4

B r 2 C = C H - C H - C ( C H 3 ) 2

C H C O O C H 3

D i b r o m o C y p e r m e t h r i c e s t e rM . F . = C 9 H 1 2 O 2 B r 2M . w t . = 3 1 2

+ H 2 O

B r 2 C = C H - C H - C ( C H 3 ) 2

C H C O O C H 3

D i b r o m o c y p e r m e t h r i c e s t e rM . F . = C 9 H 1 2 O 2 B r 2M . w t . = 3 1 2

+ N a O H

B r 2 C = C H - C H - C ( C H 3 ) 2

C H C O O N a

S o d i u m s a l t o f D i b r o m oc y p e r m e t h r i c a c i dM . F . = C 8 H 9 O 2 B r 2 N aM . w t . = 3 2 0

+ C H 3 O H

H y d r o l y s i s

B r 2 C = C H - C H - C ( C H 3 ) 2

C H C O O H

D i b r o m o c y p e r m e t h r i c a c i dM . F . = C 8 H 1 0 O 2 B r 2M . w t . = 2 9 8

+ N a C l

M . w t . = 5 8 . 5

(4) DELTA METHRIN



Stage-5 Chlorination

Stage-6 crude deltamethrin

Stage-7 Epimerization & purification

B r2 C = C H -C H -C (C H 3 )2

C H C O O H

D ib ro m o C y p e rm e th ric a c idM .F .= C 8 H 1 0 O 2 B r2M .w t.= 2 9 8

+S O C l2

T h io n y l c h lo rid eM .F .= S O C l2M .w t.= 1 1 9

B r2 C = C H -C H -C (C H 3 )2

C H C O C l

D ib ro m o C y p e rm e th ric a c id c h lo rid eM .F .= C 8 H 9 O B r2 C lM .w t.= 3 1 6 .5

+ S O 2 + H C l

B r2 C = C H -C H -C (C H 3 )2

C H C O C l

D ib ro m o c y p e rm e th r ic a c idc h lo r id eM .F .= C 8 H 9 O B r2 C lM .w t .= 3 1 6 .5

+ OC H O

OC H C N O O C -C H -C (C H 3 )2

C H -C H = C B r2D e lta m e th r inM .F .= C 2 2 H 1 9 N O 3 B r2M .w t .= 5 0 5

m -P h e n o x y B e n z a ld e h y d e M .F .= C 1 3 H 1 0 O 2M .w t.= 1 9 8

+

+N a C l

OC H C N O O C - C H - C ( C H 3 ) 2

C H - C H = C B r 2

R S - D e l t a m e t h r i nM . F . = C 2 2 H 1 9 N O 3 B r 2M . w t . = 5 0 5

c a t a l y s t

OC O O C - C H - C ( C H 3 ) 2

C H - C H = C B r 2

S D e l t a m e t h r i nM . F . = C 2 2 H 1 9 N O 3 B r 2M . w t . = 5 0 5

E p i m e r i s a t i o n

H

C N



Preparation of RR-Cypermethrin acid

(Stage : 1)

(Isomer Seperation)

Reaction mass : 14.042

RR-Cypermethric acidComplex breaking

15% aq. Soln. of catalyst recover & recycle: 5.848 kgs

Loss: 0.005 kgs

Methylene Dichloride : 2.510 kgsHCl (30%): 0.398 kgsWater: 3.116 kgs

Organic mass : 4.01

Brominationof

BenzeneBromination of

RR-Cypermethric acid (stage : 2)

HBr gas : 2.148 kgsAlCl3: 0.868 kgsMDC: 3.186 kgs

Benzene : 2.68 kgs

FeCl3: 0.044 kgsBromine: 4.836 kgs Loss:0.045 kgs

HBr scrub in NaOH for bromine recovery: 0.15 kgs

Bromination mass washing

HCl (30%) : 1.42 kgs

Water: 3.72 kgs

Acid water washing(Stage : 3)

Water: .1.2 kgsHCl (30%): 0.172 kgsWash water: 1.2 kgs

Aq. Mass to ETP: 1.45

(4) DELTA METHRIN

Esterification (Stage : 4)

MDC : 2.0 kgsMethanol: 0.5 kgsSulphuric acid: 0.528 kgs

Sodium Bi Carbonate: 0.052 kgsWater: 2.0 kgs

Residue : 0.2 kgsMDC recovery: 4.181 kgsMDC loss: 0.319 kgs

Aq. Mass: 4.002 kgs

Ester Hydrolysis (Stage : 5)

Methanol : 0.5 kgsCaustic flakes: 0.435 kgsWater: 1.0 kgs

Aq. Mass : 2.063 kgs

AcidificationToluene : 3.84 kgsHCl: 1.32 kgs

Aq. Mass : 1.36

Chlorination & Degassing (Stage : 6)

Thionyl Chloride : 0.455 kgsDMF: 0.004 kgs

0.244 SO2

0.34 HCl1.593 C.S Lye 22%

0.420 Water

SO2 Scrubber

0.466 30% HCl Solution

Crude Deltamethrin &

Washing

(Stage : 7)

m- Phenoxy Benzaldehyde : 0.6 kgsWater: 1.0 kgsSoda ash: 0.05 kgs

Sodium cyanide: 0.258 kgsTEBA: 0.05 kgsWater: 1.5 kgsAcetic acid: 0.005 kgsHypo wash: 0.2 kgsToluene: 2.5 kgs

1.5 aq. Mass contain NaCN1.8 kgs : Aq. mass

Detoxification 2.3 kgs aq. Soln.

TolueneRecovery

6.14 Toluene Recovery0.2 kgs loss

Epimerisation&

Purification of Deltamethrin(Stage : 8)

4.53 IPA recover0.105 kgs: TEA recover0.045 kgs: TEA loss0.008 Hyflow + Carbon0.25 kgs: DM ML0.19 IPA loss

Iso propyl alcohol : 4.75 kgsTEA: 0.15 kgsActivated carbon: 0.004 kgsHyflow supercell:: 0.004 kgs

1.0 Kg Deltamethrin Technical

Sodium Sulphite (22%)1.837

0.8 (10%) NaOCl solution

Recovery of SS-CMA&

Ephedrine Hydrochloride

Layer Separation

Aqueous Mass 14.11 kgsMDC: 8.31 kgsHCl (30%): 2.01 kgs

PROCESS FLOW DIAGRAM OF SS-CMA & EPHEDRINE HYDEOCHLORIDE

Acidification

Aqueous Mass to ETP : 12.61

Water : 3.0 kgsHCl (30%):0.3 kgs

Organic Mass : 11.815

3.83 16% Aqueous solution of Cat-V recycle

MDC Recovery &ChlorinationThionyl Chloride : 1.84

3.3 Kg SS Cypermethric Acid Chloride1.315 Water

SO2 Scrubber

1.88 30% HCl Solution

5.84 C.S Lye (23%)

7.98 MDC Recovery0.291: loss

0.099 SO2 Gas0.564 HCl gas

6.83 (22%) sodium sulphite

Hot Filtration & washing

Loss: 0.048 kgsAq. Mass for Cypermethric acid& Catalyst recovery: 14.543 kgs

Hot water washing: 3.975 kgsMDC: 0.413 kgs

Wet cake RR CMA complex: 3.839

DehydrationMethylene di Chloride recover: 1.29 kgsLoss: 0.005 kgs

Crude Bromo Benzene: 5.412

Washing

HBr: 2.148

Aq. Mass for Bromine recovery: 1.64 kgsAq. Mass to ETP: 1.064 kgs

Water: 2.5 kgsSodium Thio Sulphate: 0.05 kgs

Crude Bromo Benzene: 5.258

Distillation

Residue: 0.448

Loss: 0.05 kgsBromo Benzene: 4.40 kgsBenzene recycle: 0.360 kgs

Organic mass : 2.67


Loss:0.030 kgs

Aq. Mass contains HCl & HBr for Bromine recovery: 6.15 kgs


Organic mass : 7.145

Dehydro halogination

Water: .4.09 kgsCaustic flakes: 0.186 kgsCaustic lye (47%): 0.258 kgs

Loss: 0.226 kgsMDC recover: 4.675 kgs:


Acidification & layer SeparationMDC: 1.910 kgs

H2SO4: 0.295 kgs

Aq. Mass: 5.858 kgsLoss: 0.025 kgs

Organic mass 3.100

Washing & layer SeparationWater: .0.725 kgs Aq. Mass: 0.77 kgsLoss: 0.005 kgs

Organic mass 3.05

MDC RecoveryMethanol: 0.455 kgs

MDC recovered: 1.610MDC + traces of methanol: 0.209 kgsLoss: 0.021 kgsMDC recover: 1.610 kgs

Organic mass 1.665

Esterification

Reaction mass 1.971

Sulphuric acid: 0.131 kgsMethanol: 0.175 kgs

Water : 2.752 kgsCaustic soda: 0.509 kgsCypermethric acid: 2.87 kgs

15% Aq. Soln of CAT-V: 7.964 kgs



Stage - 1

O

CCl2 CH2 CH CH COCl OHC NaCN

CH3C CH3

227.5 198 49

Cypermethric Acid chlorideM eta Phenoxy Benzaldehyde Sodium Cyanide

Catalyst

O CN O

CCl2 CH2 CH CH C O CH NaCl

CH3C CH3

416 58.5

Cypermethrin Sodium Chloride

Stage - 2

O CN O

CCl2 CH2 CH CH C O CH

C

H3C CH3

416

Cypermethrin

Epimerisation

O

CCl2 CH2 CH CH C O CH CN

C

H3C CH3

416

Alphamethrin

O

(5) ALPHA CYPERMETHRIN



Detoxification of Cyanide by Hypo

NaCN NaOCl NaOCN NaCl

49 74.5 65 58.5

Sodium Cyanide Sodium Hypo Chloride Sodium Cynate Sodium Chloride

2 NaOCN 3 NaOCl NaCl N2 NaHCO3

65 74.5 58.5 28 84

Sodium Cynate Sodium Hypo Chloride Sodium Chloride Nitrogen Sodium Bicarbonate

STAGE: ICYPER REACTION

STAGE: 2 WASHING

Sodium Cyanide: 230 kgsWater: 1065 kgsCatalyst: 20 kgsSoda ash: 20 kgsCMAC: 900 kgsMPB: 720 kgsN- Hexane: 2780 kgs

(5) ALPHA CYPERMETHRIN

Water: 1500 kgs

Cyanide layer: 1443 kgs

STAGE: 3 WASHINGWater: 2000 kgs

loss: 20 kgsWaste water: 1512 kgs

STAGE: 4, HEXANE RECOVERYHexane loss: 71 kgsHexane recovery: 2669 kgs

EPIMERIZATIONTri Ethyl Amine: 644 kgsN- hexane: 4992 kgsEvaporation loss: 228 kgsWaste Water: 2766 kgs

FILTERATION Cyper ML: 400 kgs

DRYING

ALPHA CYPER METHRIN: 1000 KGS

Sodium Hypo Chlorite: 1500 kgs

Waste water: 2943 kgs

loss: 20 kgsWaste water: 2000 kgs

Tri ethyl Amine: 700 kgsWater: 2630 kgsN- Hexane: 5200 kgs



Cl2C=CH-CH-C(CH3)2

CHCOCl

2,2,Dichloro vinyl-2,2-dimethyl cyclopropanecarboxylic acid chlorideM.F.=C8H9OCl3M.wt.=227.5

+ OCH2OH

OCH2OOC-CH-C(CH3)2

CH-CH=CCl2

PermethrinM.F.=C21H20O3Cl2M.wt.=391

m-Phenoxy Benzalalcohol M.F.=C13H12O2M.wt.=200

+ HCl

(6) PERMETHRIN

(6) PERMETHRIN

Stage - 1REACTION &

WASHING

CMAC : 620 KgsMPBAL: 520 KgsWater : 1250 KgsPotassium Carbonate : 15 Kgs

Water : 233 Kgs

PERMETHRIN: 1000 KGS

Distilled Water : 45 Kgs

HCL gas to Scrubber: 100 kgs

HCl 30% : 333 Kgs

Stage - 2DE- HYDRATION

Waste Water : 1260 Kgs

CRUDE PERMETHRIN:

1045 KGS



Cl3-C-(O)Cl

Trichloro acetyl chloride

+ CH2=CHCN

acrylonitrile N

ClCl

Cl OH

2-Hydroxy -3,5,6-trichloro

pyridine

+ HCl

N

ClCl

Cl OH

2-Hydroxy -3,5,6-trichloro

pyridine

+ NaOH + (C2H5O)2P(S)Cl

DETCN

ClCl

Cl O

Chlorpyriphos

+ NaCl

P(S)(C2H5O)2

(7) CHLORPYRIFOS



HTCP FORMATION

TCAC: 1436 kgsACN: 521 kgsCatalyst: 7 kgs

Solvent: 2200 kgs

Na- HTCP PREPARATION

TCAC: 186 kgsSolvent: 2200 kgsACN: 21 kgsLoss: 120 kgsResidue: 182 kgs

(7) CHLORPYRIFOS

Water : 2600 KgsCaustic lye: 1890 kgs

DISTILLATION

HCl gas: 139 kgs

FILTERATIONLoss: 100 kgsML: 4027 kgs

SLURRY PREPARATIONWater : 1670 Kgs

TOXIFICATION

EDC: 4018 kgsSalt: 25 kgsCatalyst: 8 kgsCaustic lye: 25 kgsDETC: 643 kgs FILTERATION

Loss: 100 kgsResidue: 36 kgs

SEPARATION ML to Incinerator: 2952 kgs

EDC RECOVERY Loss: 198 kgsEDC recovered: 3818 kgs

CHLORPYRIPHOS: 1000 KGS



CH3

N

S

C NHNH2

2-Hydrogeno-4-Methyl Benzothiazole M.F.= C8H9SN3M.wt.=179

+ HCOOH

Formic acid M.F.=CH2O2M.Wt.=46

CH3

N

S

C

Tricyclazole M.F.= C9H7SN3M.wt.=189

CH

N

N + 2H2O

(8) TRICYCLOZOLE

REACTOR

WATER DUMPING

4-HMBT : 1.0 kgsFormic acid: 0.760 kgs

FILTERATION & WASHING

Water : 6.660 kgsCaustic (20%) Solution: 0.406 kgs

Reaction Mass : 1.760 kgs

DRYING

TRI-CYCLOZOLE : 1.0 KGS

Evaporation Loss: 0.510 kgs

Reaction Mass : 8.826 kgs

Water : 2.0 kgs

Wet cake : 1.510 kgs

(8) TRICYCLOZOLE

Loss: 0.1 kgsAq. ML: 9.216 kgs



Stage-1 preparation of Oxirane

2,4-dichloro valerophenone 2-Butyl-(2,4-Dichloro phenyl) Oxirane

M.F.=C11H12Cl2O M.F.=C12H14Cl2O

M.wt.=231 M.wt.=245

Stage-2

Preparation of Hexaconazole

Cl

Cl

C

O

(CH3)2S/(CH3)2SO4

(CH3)2S/

/KOH

Cl

Cl

C

O

K2SO4+H2O

C

Cl

Cl

+

K2CO3

2-Butyl-2-[2,4 Dichloro Phenyl] OxiraneM.F.=C12H14Cl2OM.wt.=245

O

1,2,4-Triazole M.F.=C2H3N3M.wt.=69

Hexaconazole M.F.=C14H17Cl2ON3M.wt.=314

Cl

Cl

C

OH

CH2

N

N

N

(CH2)3CH3

N

N N

(9) HEXACONAZOLE



(9) HEXACONAZOLE

PREPRATION OF OXIRANE

2,4 Di Chloro Valerophenone: 950 kgsDMS: 1577 kgsWater: 81 kgsDMSO4: 836 kgsKOH: 913 kgs

Recovered DMS: 1262 kgsLoss: 275 kgs

WATERDUMPING

at 65-70 0C

Water: 5712 kgsAqueous mass: 1193 kgsLoss: 5 kgs

FILTERATION & LAYERSEPARATION

Aq. Mass: 7500 kgsLoss: 35 kgs

PREPARATION OF HEXACONAZOLEDMF: 3488 kgsAnhydrous K2CO3: 82 kgs1,2,4 Triazole: 327 kgs

FILTERATION K2CO3 Wet cake: 95 kgsLoss: 30 kgs

DMF RECOVERY DMF recovered: 3138 kgsLoss: 170 kgs

CRYSTALIZATIONMethanol: 985 kgsMethanol for washing: 140 kgs

Mother liquor: 1526 kgsLoss: 60 kgs

HEXACONAZOLE TECHNICAL: 1000 KGS



Cl

Cl

C CH3

O

2,4-Dichloro acetophenone M.F.:-C8H6OCl2M.wt.:-189

+

OH

OH

CH3

1,2-PentanediolM.F.:-C5H12O2M.wt.:-104

Toluene

Cl

Cl

C CH3

O O

CH2CH2CH3

1,3-Dioxolane-2-(2,4-Dichloro phenyl)-2-Methyl-4-n-PropylM.F.:-C13H16Cl2O2M.wt.:-275

+ H2O

M.F:-H2OM.wt.:-18

Cl

Cl

C CH3

O O

CH2CH2CH3

1,3-Dioxolane-2-(2,4-Dichloro phenyl)-2- Methyl-4-n-PropylM.F.:-C13H16Cl2O2M.wt.:-275

+ Br2

Bromine M.F.:-Br2M.wt.:-160

CH2Cl2

Cl

Cl

C CH2Br

O O

CH2CH2CH3

1,3-Dioxolane-2-(2,4-Dichloro phenyl)-2-bromo Methyl-4-n-PropylM.F.:-C13H15Cl2O2BrM.wt.:-354

+ Br

M.F.:-HBrM.wt.:-81

H

(10) PROPIOCONAZOLE



Cl

Cl

C CH2Br

O O

CH2CH2CH3

1,3-Dioxolane-2-(2,4-Dichloro phenyl)-2-Bromo methyl-4-n-PropylM.F.:-C13H15Cl2O2BrM.wt.:-354

+

N

N

N

1,2,4-Triazole M.F.:- C2H3N3M.wt.:-69

H

DMF

KOH

Cl

Cl

C

O O

CH2CH2CH3

N

N

N

CH2

PropiconazoleM.F.:-C15H17Cl2N3O2M.wt.:-342

+ KBr

potassium bromideM.F.:-KBrM.wt.:- 119

+ H2O

M.F.:-H2OM.wt.:-18

+

Potassium hydroxideM.F.= KOHM.wt.=56



(10) PROPIOCONAZOLE

PREPRATION OF 1,3DIOXOLANE -2-(2,4DICHLORO PHENYL)-2-

METHYL-4-n PROPYL

1,2 Propane diol: 560 kgsToluene: 1326 kgs2,4 Di Chloro Aceto Phenone: 926 kgs

Water: 88 kgsLoss: 5 kgs

WASHING

10% Sodium Carbonate: 500 kgsWater: 500 kgs

Aqueous mass: 1193 kgsLoss: 5 kgs

BROMINATIONBromine: 716 kgs HBr: 300 kgs scrub in water (1200 kgs)

WASHING10% Sodium Carbonate: 500 kgsWater: 500 kgs

Aqueous mass: 1215 kgsLoss: 5 kgs

TOLUENERECOVERY

Toluene recovery: 1259 kgsLoss: 53 kgs

PREPARATION OFPROPICONAZOLE

DMF: 3520 kgs1,2,4 Triazole: 372 kgsKOH: 332 kgs

Water: 97 kgsKBr: 472 kgs

DMSO RECOVERYDMF recovered: 3380 kgsLoss: 140 kgs

WASHINGToluene: 2125 kgsWater: 1600 kgs Aqueous mass: 1820 kgs

DISTILLATIONToluene Recover: 2040 kgsLoss: 85 kgs1st cut Recycle: 250 kgsResidue: 70 kgsPROPICONAZOLE TECHNICAL:

1000 KGS



2CS2 + NH2CH2 NH2CH2 + 2NaOH + 4H2O NaSC(S)NHCH2CH2NH(S)CSNa.6H2O

carbon disulphide

152

Ethylene Diamine

60

Sodium Hydroxide Water

80 72

Disodium salt of Ethylene bis dithio

carbamate hexahydrate (DBH)

365

NaSC(S)NHCH2CH2NH(S)CSNa.6H2O

Disodium salt of Ethylene bis dithio

carbamate hexahydrate (DBH)

332

+ MnSO4[SC(S) NHCH2CH2NH(S)CSMn] x

Manganese sulphate

151

Mananese salt of ethylene bis dithio carbamate

265.3

+ Na2SO4 + 6H2O

Sodium sulphate Water

142 108

[SC(S) NHCH2CH2NH(S)CSMn] x

Mananese salt of ethylene bis dithio carbamate

265.3

+ ZnSO4

Zinc sulphate

161

[SC(S)NHCH2NH(S)CSMn]x . (Zn) y

MANCOZEB

271

(11) MANCOZEB



(11) MANCOZEB

Sodium Salt Formation

EDA : 206 KgsWater : 166 KgsNaOH(48%) : 580 KgsWater : 340 KgsCS2: 572 kgs

Stripping CS2 Recycle : 54 Kgs

WashingWater : 28 Kgs

MancozebSalt

Formation

MnSO4 : 90 KgsWater : 518 Kgs

MnSO4 (27%) : 1816 Kgs

ZnSO4 (32%) : 21 Kgs

Washing &

Filtration

Water : 680 KgsCond. Recycled from RVD : 124 KgsWater : 804 Kgs

Effluent To MEE : 4500 Kgs

Homonization

Water : 229 KgsZnSO4 (32%) : 145 Kgs

SLS : 33 KgsHMT : 20 Kgs

Drying Loss : 694 KgsCond. Recycled : 124 Kgs

MANCOZEB : 1000 Kgs



P CH2 N

OHO

HO

CH2COOH

CH2COOH

PMIDA M.F=C5H10PO7N

M.wt.=227

+ 1/2 O2catalyst

+NH3P CH2 NH

OHO

HOCH2COOH

Glyphosate M.F.=C3H8O5NPM.wt.=169

Reaction chemistry

C2H4OH Catalyst CH2COONa

HN + 2NaOH HN +4H2

C2H4OH CH2COONa

DEA DSIDA

O

CH2COONa HO CH2COOH

NH + PCl3 +HCHO +3H2O P CH2N

CH2COONa HO CH2COOH

DSIDA PMIDA + NaCl + H2O

(12) GLYPHOSATE



DSIDAPreparation

PMIDA Preparation

Adjustment of pH

ANF

DEA : 0.908 kgsNaOH (4%): 1.531 kgsWater: 1.288 kgsCatalyst: 0.182 kgs

HCHO (37%) : 0.782 kgs PCl3: 1.48 kgsHCl: (30%): 0.9 kgs

0.050 kgs to Scrubber

NaOH (47%) :1.388 kgs

Water : 1.6 kgs 7.159 (ML to MEE )

Slurry Preparation

Carbon : 0.157 kgsWater: 1.0 kgsLiq. Ammonia (20%): 0.708 kgs

OxidationOxygen : 0.3 kgs CO2 : 0.150 kgs

ANF

pH Adjustment & CrystallizationHCl (30%) : 1.1 kgs

CentrifugeWater : 0.4 kgs

SFD

4.351 kgs (ML to Incinerator)

Evaporation Loss : 0.295 kgs

Glyphosate Technical (95%) : 1 MT

(12) GLYPHOSATE

H2 gas : 0.38 kgs



2,5-dichloro aniline

NH2

Cl

Cl

+ 2NaNO2 + 2H2SO4

N=NHSO 4

Cl

Cl

OH

Cl

Cl

+ Na2SO4 + N2 + H2SO4

sodium nitrite sulphuric acid

-H2O

Diazonium sulphate 2,5-Dichloro Phenol

OH

Cl

Cl

OK

Cl

Cl

OK

Cl

Cl

OH

Cl

Cl

COOK

OH

Cl

Cl

COOH

KOH -H2O CO

2Aq.HCl

2,5-Dichloro Phenol Aq.Potassium salt Dry potassium salt 3,6-Dichlorosalicylic acid

OH

Cl

Cl

COOH

OCH3

Cl

Cl

COONa

OCH3

Cl

Cl

COOH

(CH3)2SO

4

NaOH+ NaCH3SO4 + NaCl

Aq.HCl

3,6-Dichlorosalicylic acid 3,6-Dichloro-2-Methoxy benzoic acid

(13) DICAMBA (3,6 DI CHLORO 2 METHOXY BENZOIC ACID)

DCP FORMATION REACTOR

3,6 DCSA FORMATION REACTOR

DICAMBA FORMATION

2,5 DCA: 3390 kgsSodium Nitrite: 1460 kgsSulphuric acid (98%) : 7840 kgsWater: 8450 kgsSulphamic acid: 100 kgs

2,5 DCP: 3180 kgsPotassium Chloride: 1080 kgsWater: 740 kgsXylene ®: 10930 kgsXylene (F): 630 kgsCarbon dioxide: 1700 kgsHydro Chloric acid (30%): 2350 kgs

3,6 Di Chloro Salicylic acid: 1680 kgsRecovered 2,5 DCP: 1830 kgsRecovered Xylene: 10930 kgs

Xylene loss: 630 kgsWaste water: 4100 kgsKCl Powder: 288 kgsWater vapour: 1152 kgs

3,6 Di Chloro Salicylic acid: 1680 kgsSodium Hydroxide: 1660 kgsWater: 6470 kgsDi Methyl Sulphate: 3660 kgsHCL (30%): 990 kgs

DICAMBA: 1000 KGS

Sodium methyl sulphate: 3900 kgsWaste water: 9014 kgsSodium chloride: 470 kgsOrganic impurities: 76 kgs

(13) DICAMBA (3,6 DI CHLORO 2 METHOXY BENZOIC ACID)

2:5 Di Chloro Phenol: 3180 kgsSpent Sulphuric acid: 8240 kgsSodium Sulphate: 5640 kgsWaste water: 3660 kgsNitrogen gas: 520 kgs



Stage-1 Hydrogenation

Stage-2 nitration

CH3

CH3

NO2

4-nitro-O-xylene M.wt.=151

+ C

C2H5

C2H5

O

Diethyl Ketone M.wt.=86

CH3

CH3

NHCH

C2H5

C2H5

N-(1-Ethyl Propyl)-3,4-Xylidine M.wt.=191

Catalyst

Hydrogen+ 3H2O

CH3

CH3

NHCH

C2H5

C2H5

N-(1-Ethyl Propyl)-3,4-Xylidine M.wt.=191

(HNO3+ H2SO4)

Nitration

CH3

CH3

NHCH

C2H5

C2H5

PendimethalinM.wt.=281

NO2

NO2

(14) PENDIMETHLIN



(14) PENDIMETHLIN

Preparation of N-(1-ethyl Propyl)

3,4-xylidine

Hydrogen Gas : 55 KgsDiethyl Ketone : 883 Kgs4-Nitro-O-Xylene : 620 KgsCatalyst-1 : 0.248

Filtration &

Layer Separation

Reaction Mass: 1558.248 Kgs

Castalyst recover : 0.248 KgsLoss : 10 KgsAqueous mass : 222 kgs

Reaction Mass 1326 Kgs

Solvent Recovery Recover Diethyl Ketone: 536 KgsLoss : 30 Kgs

Preparation of

Pendimethalin

N-(1-ethly propyl)-3,4-xylidine : 760 Kgs

Ethylene dichloride: 1390 KgsWater: 453 KgsNitric acid (60%) : 1121 KgsSulphuric acid (98%) : 801 Kgs

Layer Separation &

Water Washing

Spent Acid : 2000 KgsAqueous mass : 1094 KgsLoss : 45 Kgs

Reaction mass : 4525 Kgs

Water : 1000 Kgs

Organic mass : 2386 Kgs

De nitrosation of

Pendimethalin

Diethyl Ketone : 20 KgsHCl(30%) : 575 Kgs

Reaction mass : 2981 Kgs

pH adjustment & layerSeparation & water washing

5% NaHCO3 solution : 3500 KgsWater for washing : 1400 Kgs

Reaction mass : 2286Kgs

Solvent RecoveryUnder vacuum

Recover Ethylenedichloride : 1158 KgsLoss : 128 Kgs

Pendimethalin (92%) : 1000 Kgs



ANNEXURE-3

Quantity of waste to be generated (liquid and solid) & scheme for their Management/disposal.

Quantity of Waste Water (liquid waste) generation and its management :

Sr. No. Particulars Water Consumption, M3/day Effluent Generation, M3/day

1.0 Domestic 15.0 12.0

2.0 Processing & product washing

208.9 291.7

3.0 Floor, container, equipment Washing

10.0 10.0

4.0 Cooling Tower 400.0 75.0

5.0 Boiler 215.0 25.0

6.0 Scrubber 10.0 10.0

7.0 Gardening 15.0 0

8.0 Total 873.9 423.7

9.0 Total Industrial 843.9 411.7

10.0 Treatment in RO Plant

- 120.0

11.0 RO Rejection - 20.0

12.0 Treatment in MEE - 282.7

13.0 Treatment in SBT - 258.5

14.0 Recycled to process from RO permeate

100.0 -

15.0 Treatment in incinerator

- 9.0

16.0 Net Fresh water 773.9 -

17.0 Net Discharge 258.9

Total fresh water requirement will be 774 m3/day which is met through GIDC water supply.

Total Industrial wastewater generation will be 412 m3/day. Out of which about 283 m3/day of high

TDS & high COD of effluent generated from the process will be collected separately, neutralized,

filtered & finally taken to solvent stripper & MEE. Average 9 m3/day of high COD & high ammonia

effluent will be collected, neutralized, filtered and incinerated in proposed incineration system.

Balance 120 m3/day of normal effluent from cooling tower, boiler blow down, floor/container



washing and scrubber will be collected separately and sent to RO system. Thus 239 m3/day of

condensate from MEE/ATFD and 20 m3/day of effluent from RO rejection; total 259 m3/day will be

treated in catalytic advance oxidation followed by soil bio reactor and finally discharge into effluent

drainage line to Arabian Sea. 100 m3/day of RO permeate will be recycled back to the process.

Domestic Waste water (12 m3/day) will be disposed by septic tank & soak pit.

CHARACTERISTICS OF STREAMWISE UNTREATED EFFLUENT

No Parameters Concentrated

effluent (High

COD/NH3-N)

Concentrated

effluent

(High TDS)

Combined

Normal

effluent

to RO

Total

effluent to

ETP (RO

rejection +

MEE

condensate)

Treated

effluent

EPA norms

1 pH 4-5 4-5 6.0-7.0 6-8 7.5 6.5-8.5

2 Color pt. Co 500 200 100 150-200 50 <100

3 TDS mgl 8% 15-18% 1000-1200 2000-3000 2000-3000 -

4 S/S mgl 150-200 300-400 100 100-120 70-80 <100

5 Oil/grease

mgl 1.3 2-3 2.0 1-2 0.5-1.0 <10

6 BOD mgl 5000 3000 200-250 1200-1500 70-80 <100

7 COD mgl 2,00,000 25000-30000 1000-1200 4000-5000 200-250 <250

8 NH3-N mgl 4000-5000 40-50 5-6 10-15 10-12 <50

9

Phenolic

compound

mgl

0.6 2-3 0.5 1-2 0.16 <1

10 Sulphide mgl 5-6 3-4 1-2 ND ND <2

11 Hydraulic

load, m3/day 9.0 282.7 120 258.5 258.5

12 Mode of

treatment Incineration MEE RO ETP - -

Based on the above criteria incineration system, solvent stripper followed by MEE, Reverse Osmosis &

Effluent Treatment Plant having under mentioned specification is required to install.



(A) DETAILS OF PROPOSED INCINERATION SYSTEM FOR HIGH COD/NH3 EFFLUENT

Effluent Quantity: 9 m3/day

Design Criteria: 20 m3/day

Sr. No. Particulars Details

1.0 Capacity of Incinerator 1000 kgs / hr effluent

1.2 Process Thermal destruction of organic matter by heat transfer

1.3 Design Temperature 1200oC

1.4 Operation temperature in primary chamber

850oC

1.5 Applied HP 21 HP

1.6 Control Manual with digital temperature digital indicator

1.7 Fuel consumption 300 kgs/hr (LDO/FO)

2.0 Primary Combustion chamber

2.1 Material of construction MS

2.2 Installation Vertical Fired, Circular Refractory lined

2.3 Lining Inside portion of chamber duly lined with fire bricks and fire insulation bricks

2.4 Maintenance & Ash Door 01 no each

2.5 Combustion Burner Low air pressure burner, manually operated (01 nos.)

2.6 Operating Temperature 8500C

Liquid Spray Nozzle Air atomized, external mix (02 Nos.)

3.0 Secondary Combustion Chamber

3.1 Material of Construction Mild Steel

3.2 Installation Vertical Fired, Circular Refractory lined

3.3 Lining Inside portion of chamber duly lined with fire bricks and fire insulation bricks

3.4 Maintenance & Ash Door 01 no each

3.5 Combustion Burner low air pressure burner, manually operated (01 nos.)

3.6 Operating Temperature 1200 0C

3.7 ID Fan 01 No., 7000-8000 cfm

3.8 Holding Tank 16000 liters

4.0 Type of Ventury Scrubber Pressure Shower

4.1 Throat Diameter 1140 mm x 1500 x 3300 tower

4.2 Height 7000 mm bottom discharge, 500 mm dia

5.0 Stack Conical Base, Guy Support, 30 m height 500 mm dia.

5.1 Measuring Equipment Waste Water meter, Fuel meter, Power meter

5.2 Sampling Port 100 mm dia



(B) DETAILS OF PROPOSED SOLVENT STRIPPER FOLLOWED BY MEE & ATFD FOR HIGH TDS EFFLUENT:

Effluent Quantity: 282.7 m3/day

Design criteria: 300 m3/day

Sr. No. Particulars Capacity in M3 MOC

1 Oil/Grease trap 0.5 M3 MS/Epoxy

2 Collection cum 150 M3 RCC/TL

3 Lime dosing tank 6 M3 HDPE

4 Neutralization tank 20 m3 RCC/TL

4 Solvent stripper 300 KLD SS 316

5 MEE Calndria:I 300 KLD Ti-clad

6 MEE Calndria:II

7 MEE Calndria:III

8 Agitated Thin Film Dryer (ATFD) 40 TPD SS 316

9 Final holding tank for water from MEE condensate & ATFD

200 M3 RCC



© DETAILS OF PROPOSED REVERSE OSMOSIS PLANT FOR NORMAL EFFLUENT

Effluent quantity: 120 m3/day


Sr. No. Particulars Capacity in M3 MOC

1 Collection tank 125 RCC/TL

2 pH Correction tank 25 M3 RCC/TL

3 RO Plant 7 m3/hr SS/PP/FRP/Membrane

(D) DETAILS OF PROPOSED EFFLUENT TREATMENT PLANT FOR RO REJECTION & MEE CONDENSATE

EFFLUENT

Effluent Quantity: 259 m3/day


Sr.

No

Name of the unit Capacity MOC

1 Collection cum equalization tank with air

sparger

150 RCC/TL

2 Neutralization tank with Air sparger 150 RCC/TL

3 Chemical dosing tank 5 HDPE

4 Catalytic AOS system and Soil Biological

Treatment

275 RCC

5 Final treated effluent holding tank 275 RCC



FLOW DIAGRAM OF EFFLUENT TREATMENT PROCESS

Total effluent : 411.7 M3/Day

Processing: 208.9 Cooling: 400 Boiler: 215 Washing: 10 Scrubber: 10

291.7 75 25 10 10

Holding tank: 258.5 M3/Day

RO Plant: 120 RO Permeate: 100 Recycle

RO Rejection: 20Collection tank

Neutralization tank

Filtration

Holding tank

MEE Condensate from MEE

Salt to TSDF

High COD/NH3: 9.0 High TDS + Normal: 282.7

Collection tank

Neutralization tank

Filtration

Holding tank

Incinerator

ATFD: 82.5 Filtrate

238.5

SBT: I

Treated effluent pipe line

Arabian Sea

Treated effluent holding tank

Catalytic Advance Oxidation system

SBT:II SBT: III SBT: IV

Incineration ash

Solvent Stripper



ANNEXURE: 4

Quantity of Solid Waste generation and its management

No Type of waste Category Qty. MT/ Anum

Treatment Disposal

1 ETP waste) 34.3 13700

Dried, packed in bags

Dispose off into TSDF, BEIL,

Ankleshwar & Detox, Dahej

2 Salt from MEE 34.3 14040 Dried, packed in bags

Dispose off into TSDF, BEIL,

Ankleshwar & Detox, Dahej

3 Used Oil 5.1 0.2 Packed in carboys Incinerated into own

Incineration system

4 Discarded containers 33.3 5.0 De-contaminated, stored

Sell to authorized

recycler





7 Used rubber hand gloves/pipes etc


Incinerated into own

Incineration system

Note: We will apply for membership of M/S BEIL, Ankleshwar, Detox Dahej, M/S RSPL for the

disposal of hazardous waste.



ANNEXURE-5

Topographical map



Annexure-6

PLOT ALLOTMENT LETTER ISSUED BY THE GIDC



ANNEXURE-7

A schematic representation of the feasibility drawing



ANNEXURE-8

Details of flue gas/process gas emission & its control measures

Sr. No. Particulars Details

1.0 Capacity of steam boiler 15 TPH x 2 nos.

1.1 Fuel used Coal

1.2 Consumption 16000 kgs/hr

1.3 APC provided Separate MDC & ESP

1.4 Height of chimney 55 meters common

2.0 Capacity of Incinerator 1000 kgs/hr liquid

2.1 Fuel used LDO/FO

2.2 Consumption 300 kgs/hr

2.3 APC Ventury scrubber

2.4 Chimney 21 meter

3.0 Capacity of D G set 1000 KVA x 3 nos.

3.1 Fuel used HSD

3.2 Consumption 360 lits/hr

3.3 APC Exhaust

3.4 Height 11 meters

4.0 Stack attached to Reaction vessel

4.1 APC Two stage alkali scrubber x 4 Nos.

4.2 Height of vent 11 meters

4.3 Pollutants SO2< 40 mg/Nm3 NOx: < 25 mg/Nm3

HCl: < 20 mg/Nm3 NH3: < 175 mg/Nm3

Br2< 5 mg/Nm3



DETAILS OF AIR POLLUTION CONTROL SYSTEM ATTACHED TO EACH COAL/LIGNITE FIRED BOILER Boiler : 30000 kg of steam/hour Coal/lignite consumption : 16000 kgs/hr Calorific value : 4200 kcal/kg Inlet to dust collector : 280°C Stack temp : 180°C Diameter of chimney : 750mm Flue Gas Volume : 6107Am3/hr I.D. Fan : 15254 m3/hr Stack diameter : 850Ømm Stack height provided : 55 meters Efficiency : Thermal Efficiency of Boiler 82±2% 1.0 Air Pollution control System: Multi Cyclone Dust Collector (Grit Arrestor) Cyclone tube diameter : 1100 Ø mm Height of tube : 660 mm No of tubes : 1no Dia of tubes : 587Ø mm Dimensions : 3175lX1215WX1215Ht Collection efficiency : 60-70% (over 40micron) Expected outlet dust load : 150 < mg/nm3 at out let of bag filter Inlet Dust load : 25-40 gms/nm3 Density : 600kg/ m3 Fines : (< 1 mm) 2.0 Air Pollution control System: Electro static Precipitator ESP model : SC-11-16-24(G) (3x9.125) 1.2 P Design volume : 60588 Am3/hr Design Temperature : 1500C Maximum Inlet Dust Load : 13.01 Gm/ Nm3

Outlet Emission : 50 Mgm/ Nm3

Moisture in Gas : 15.83% V/V Collection area : 1399 m2

Specific collection area : 83.1 m2/m3/s No of gas passages : 11 Velocity through ESP : 0.49 M/s No of fields : 3 Migration velocity : 5.37 Cm/s Residence time : 16.9 Sec Dust collection efficiency : 98.8% Expected emission : PM: < 50 mg/Nm3 : SOx: < 100 ppm : NOx: < 50 ppm



DETAILS OF TWO STAGE SCRUBBING SYSTEM

Sr. No. Name of the unit Size

1 Height of Scrubber (Packed column) 3 meter

2 Size of Scrubber 600 mm dia

3 MOC of Scrubber MS Graphite

4 Type of Packing Paul /ring 1

5 Height of Packing 2.5 meters

6 Height of Scrubber (Falling Film) 2.5 meters

7 Size of Scrubber 400 mm dia

8 MOC of Scrubber MS graphite lined

9 Size of Vacuum catch pot 630 lits

10 MOC of Scrubber MS graphite lined

11 Capacity of water circulation tank 15 KL

12 MOC Tank MS FRP

13 Capacity of water circulation Pump 6 m3/hr

14 Size of ventury 200 kgs/hr

15 MOC of condenser PP/FRP

16 Size of condenser 20 m2

17 MOC of condenser MS

18 Size of caustic circulation tank 15 KL

19 Capacity of circulation pump 54 m3/hr

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