Exhibit 1 Location Map -...

Project: Manufacturing of Speciality Chemicals & Intermediates

Developer: M/s. Odessey Organics Pvt. Ltd.

EXHIBIT 1: LOCATION MAP OF PROJECT SITE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd.

Sr No.

EXHIBIT 2: MANUFACTURING PROCESS OF SPECIALITY CHEMICALS & INTERMEDIATES

GROUP 1 – DYES INTERMEDIATES (NITRO-AMINO PHENOL GROUP)

1) PRODUCTION OF – 2,4-DINITROCHLOROBENZENE FROM MONO CHLOROBENZENE

Particulars FOR 1.0 MT.FINISHED PRODUCT

1 Mono Chlorobenzene 0.565 MT

2 Sulfuric Acid (98%) 2.446 MT

3 Nitric Acid (99%) 0.7 MT

4 Finished Product 2,4-DNCB

1.0 MT

5 Yield 98.7%

6 Spent Sulfuric Acid 80% Generated

588.0

7 Total batches / Day 5.0 no. Batches

8 Total Working Days/ Months 26.0 no. Days

PROCESS DISCREPTION OF 2,4-DINITROCHLOROBENZENE MANUFACTURING - 1) Monochlorobenzene is nitrated in presence of excess of sulfuric acid as nitrating media &

fuming nitric acid as nitrating agent.

2) The first mono-nitration takes place at r.t or even at chill temperature.

3) However heating is required up to temperature 1150c to complete the dinitration of the chlorobenzene.

4) Once product is prepared at high temperature – layer seperation of product & sulfuric acid is to be done.

5) The fresh monochlorobenzene wash is given to sulfuric acid to remove any traces of nitric acid & organic compounds.

6) The 80% sulfuric acid is a bi-product from the process.

7) While 2, 4-Dinitrochlorobenzene with impurities like 2,5-/2,6 Dinitrochlorobenzene are the main product .

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 8) The water wash is given to this organic layer to remove any free acidity.

9) Then this organic layer is cooled & crystallized from “flakers”

10) The crystalline material is stored in a cool place in small containers.

11) This 2,4- Dinitrochlorobenzene is one of the important starting material for variety of dyes intermediates.

Reaction:

Process Flow Diagram

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 2) PRODUCTION OF: 2, 4-DINITROPHENOL FROM 2, 4-DINITROCHLOROBENZENE.

Sr. No Particulars 1.0 M.T FINISHED PRODUCT

(MT)

1 2,4-Dinitrochlorobenzene 1.126 MT

2 Caustic Lye (50%) 1.115 MT

3 Dil. Sulfuric Acid (30%) 1.892 MT

(Use of Own Spent Acid)

4 Water for Reaction & Product Wash

(Total)

18.92 KL

5 Finished Product Obtained 1.0 MT

6 Total Yield 98%

7 Total Salt Form During the Reaction 1.785 MT

8 Total % Concentration of Salts in

Reaction Water

9.5%

9 Total water effluent 19.0 KL

10 TOTAL BATCHES / DAY 5 NOS

11 TOTAL WORKING DAYS / MONTH 26 NOS.

PROCESS DISCREPTION OF 2, 4-DINITRO PHENOL MANUFACTURING:

1) 2,4-dinitro phenol is obtained by the alkaline hydrolysis of 2,4-dinitro Chlorobenzene.

2) 2,4-dinitrochlorobenzene is treated with 50% sodium hydroxide (50% caustic lye) at temperature 700c-1000c, in water, to produce the – sodium salt of 2,4-dinitrophenol.

3) This sodium salt on treatment with the – dil. Sulfuric acid (30%) gives the 2, 4-dinitrophenol.

4) This is to be filtered & given a fresh water wash to remove any traces of free acid & salts.

5) The product is to be suck dry under vacuum & store in plastic carboys in a cool & dry place.

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. Reaction:

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. Process Flow Diagram: 2, 4-dinitrophenol

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 3) PRODUCTION OF: PICRIC ACID FROM 2,4-DINITROPHENOL:

No Particulars 1.0 M.T FINISHED GOODS

BATCH

1 2,4-Dinitrophenol 0.820 MT

2 Sulfuric Acid 98% 3.952 MT

3 Nitric Acid 0.395 MT

4 ICE 4.099 MT (OPTIONAL)

5 Finished Product 1.0 MT

6 Total YielD 98%

7 Sulfuric Acid 80% Generate AS BI-PRODUCT

4.742 MT (SALE AS BI-PRODUCT)

8 Solvent for Spent acid Extraction 5.0 KL (100% RECYCLED)

9 Urea Require for Scrubber 20.0 KG

10 TOTAL BATCHES / DAY 5.0 NO

11 TOTAL WORKING DAYS / MONTH 26 NOS.

PROCESS DETAILS OF PICRIC ACID MANUFACTURING:

1) 2,4,6-trinitrophenol also commonly known as “picric acid” is obtained from the nitration of 2,4-dinitrophenol in presence of excess sulfuric acid as media.

2) concentrated nitric acid is used for the nitration

3) Process is to be carried out in controlled manner in between temperature 40-500c.

4) Once reaction gets completed – the product is to be filtered out from sulfuric acid in chilled condition.

5) The 80% sulfuric acid is obtained as the bi-product. it is to be sale in agro industries to manufacture the products like – alum, single super phosphates etc.

The product obtained is re-slurred in water & washed by fresh water.


Process Flow Diagram: PICRIC ACID

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 4) PRODUCTION OF: SODIUM PICRAMATE FROM PICRIC ACID

No Particulars 1.0 M.T FINISHED GOODS BATCH

1 Picric Acid 1.176 MT

2 Process Water 3.765 MT

3 Caustic Lye 50% 0.514 MT

4 NaSH (30%) as such 1.412 MT

5 Water for Washing 1.648

6 Finished Product 1000 MT

7 Total yield 88%

8 TOTAL EFFLUENT WATER 4.5 MT

9 Salts in the reaction water as Sodium Thio

Sulfate 3.0 MT

10 Total sludge Generation after Multiple

effect Evaporator 3.0 MT

11 TOTAL NO OF BATCHES / DAY 4 NO

12 TOTAL WORKING DAYS / MONTH 26 NO.S PROCESS DETAILS OF MANUFACTURING – SODIUM PICRAMATE.

1) Sodium picramate is manufactured by the sulfide reduction in an alkaline condition using the water as media.

2) First picric acid is taken in water & made slurry. Then added caustic lye slowely in to it so as to make the – sodium salt of picric acid.

3) Then over the period of 3 hrs the reducing agent – “sodium hydrogen sulphide” (nash) is added slowely & maintain.

4) Reaction color changes from yellow o dark brown, & sodium picramate starts to p.p.t. Out.

5) Then reaction mass is cooled & filtered on nutsch under vacuum.

6) The product is washed by fresh water so as to remove any salts & excess alkali.

7) Then product is suck dry under vacuum & taken out, placed in plastic carboys & stored in a cool & dry place.


Process Flow Diagram: SODIUM PICRAMATE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 5) PRODUCTION OF PICRAMIC ACID FROM SODIUM PICRAMATE:

No Particulars 1.0 MT FINISHED PRODUCT BATCH

1 Sodium Picramate 1.133 MT

2 Water FOR Sodium Picramate 0.667 KL

3 Sulfuric Acid 98% 0.616 MT

4 ICE 0.616 MT


6 Total Yield 98%

7 Water for Process Wash 2.0 KL

8 Caustic Lye (50%) for

Neutralization of Effluent

83.0 KG

9 Total Water Effluent 4.8 KL

10 Total salt Content of Effluent as –

Sodium Sulfate

1.094 MT

11 Total Batches /Day 2.0 NO

12 Total Working Days / Month 26 Nos.

PROCESS OF PREPERATION OF – PICRAMIC ACID.

1) This is the simple acidification process. Nothing else.

2) The sodium picramate is taken in a water & made slurry. Then added a 1:1 sulfuric acid in it slowely over a period of 1 hr, so as to adjust the ph 4.0 on ph paper.

3) Then it is to be maintain for 2 hrs & filter on nutsch under vacuum.

4) Product is to be given water wash so as to remove any excess acid & salts.


Process Flow Diagram: PICRAMIC ACID

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 6) PRODUCTION OF: 4-NITRO-2-AMINO PHENOL FROM 2,4DINITROCHLOROBENZENE

No Particulars 1.0 MT FINISHED GOODS BATCH

1 2,4-DNCB 1.563 MT

2 Water for Process 20.48 KL


4 Dil. HCL Acid (30%) 0.77 MT

5 Lime (Real) 0.5 MT

6 Sulphur Powder 0.370 MT

7 Na SH (30%) 2.004 MT

8 Sodium Chloride 4.652 MT

9 Dil. HCL Acid (30%) 3.3 MT


11 Total Yield % 84.3 %

12 Total Water for Product Washing NIL

13 Total Effluent Generate per Batch 22.7 KL

14 Total Salt Content of Effluent as Sodium

Chloride

5.610 MT

15 Total no. of Batches / day 2 NO

16 Total Working Days / month 26 NO PROCESS FOR THE PREPERATION OF – 2-AMINO-4-NITRO PHENOL (4-NAP)

1) The 4-nap is a very important dyes intermediate. Various types of dyes can be prepared from the same. 4-nap is prepared by the sulfide reduction of 2,4-dinitrochlorobenzene in alkaline condition.

2) At first – the calcium poly sulfide is prepared by heating- quick lime, sulfur & sodium hydrogen sulfide togather in small quantity of water.

3) The 2,4-d.n.c.b. Is taken in hot water & caustic lye is added over a period of time so as to prepare the sodium salt of – 2,4-dinitrophenol.

4) Then maintaining the temperature between 80-900c, above freshly prepared calcium polysulfide solutions is added slowly in it.

5) After completion of reduction reaction the ph of reaction mass is adjusted to acidic range (4 to 4.5) by means of dil. Sulfuric acid.

6) The product – 4-nap is p.p.t. Out.


7) Then cooling is applied & the product is filtered on nutsch under vacuum. No further water wash is required.

Reaction:


Process Flow Diagram: 4-NITRO-2-AMINO PHENOL

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 7) PRODUCTION OF: 2,4-DINITRO SEC. BUTYL PHENOL FROM SEC. BUTYL PHENOL

No Particulars 1.0 MT FINISHED GOODS BATCH

1 Sec. Butyl Phenol 0.652 MT

2 Conc. Nitric Acid (70%) 0.952 MT

2a Methylene Di Chloride 0.652 MT

3 Iso Propyl Alcohol 52 KGS

4 Water 0.220 KL

5 Water for Distillation 0.50 KL

6 Urea 2.5 KG

7 Methanol 0.440 KL

8 ETHYL BENZENE 0.500 KL


10 Process Effluent 0.652 KL

11 Solid Waste NIL

12 Methanol Loss (5%) 25 LIT

13 MDC Loss (5%) 50 LIT

14 Hydrogen Peroxide 25.0 KG

15 TOTAL BATCHES / DAY 4 BATCHES

16 TOTAL WORKING DAYS / MONTH 26 DAYS PROCESS FOR THE PREPERATION OF: 2-SEC BUTYL PHENOL

1) This is a completely green process – as instead of any mineral acid catalyst & solvent are used for the nitration which both are completely re-usable for many times.

2) 2-secondary butyl phenol is to be taken in e.d.c as a media & added a solid catalyst in it.

3) Then slowely added – concentrated nitric acid at temperature 60 to 750c

4) After completion of reaction – the catalyst is filtered off & recycle for next batch,

5) Solvent is distilled off & recovered.

6) The product is given a alkaline water wash to remove any traces of free nitric acid & stored in a drums.


Process Flow Diagram: 2, 4-DINITRO SEC. BUTYL PHENOL

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 8) PRODUCTION OF: 6-N-AMINE-DINITROPHENOL FROM -2, 4-DINITROCHLOROBENZENE.

NO PARTICULARS 1.0 MT FINISHED GOODS BATCH

1 2,4- DINITROCHLOROBENZENE 0.933 MT

2 WATER 5.6 MT

3 CAUSTIC LYE (50%) 0.780 MT

3 ORGANIC AMINE 0.282 MT

4 DIL. SPENT ACID FOR ETP 0.156 MT

5 YIELD OF FINISHED PRODUCT 1.0 MT

6 TOTAL YIELD (%) 96%

7 SALTS IN EFFLUENT 0.830 MT

8 TOTAL EFFLUENT GENERATED INCLUDING

PLANT WASH & REACTION WATER

7.780 KL

9 TOTAL NO. OF BATCHES / DAY 1 NO

10 TOTAL WORKING DAYS / MONTH 26 NO

PROCESS DETAILS OF THE PREPARATION OF: N-ALKYL AMINO DINITROPHENYL

1) It is the simpliest condensation process.

2) The 2,4-dinitrochlorobenzene is first converted in its sodium salt by means of sodium hydroxide in water.

3) Then slowely added alkyl amine in it (ex.- n-ethyl amine).

4) Then the reaction is maintained at reflux for 3-4 hrs.

5) Product p.p.t out after cooling.

6) Use of – different alkyl amine – produce different molecules. These are used as dyes intermediate to produce various colour sheds.

Reaction:


Process Flow Diagram

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 9) PRODUCTION OF:4-NITRO ORTHO XYLENE FROM ORTHO XYLENE:

NO PARTICULARS 1.0 M.T FINISHED GOODS PLANT BATCH

1 ORTHO XYLENE 0.750 MT

2 ETHYLENE DI CHLORIDE (RDC) 1.5 MT

3 FUMING NITRIC ACID 0.500 MT

4 ACETIC ANHYDRIDE 0.675 MT

5 CATALYST 75 KG

6 FINISHED PRODUCT 1.0 MT

7 YIELDS % 95%

7A WATER FOR PRODUCT WASHING 0.375 KL

8 WATER FOR DISTILLITION 0.130 KL

9 ACETIC ACID AS BI-PRODUCT 0.815 MT

10 LIME TO NEUTRAL NITRIC ACID 82.0 KG

11 GYPSUM FORM 98.0 KG

12 COPPER OXIDE AS BI-PRODUCT 0.500 MT

13 ACTIVATED CHARCOAL REQUIRED 10.0 KG

14 TOTAL WATER AS EFFLUENT 0.716 KL

15 TOTAL NO. OF BATCHES / DAY 3.0 NOS

16 TOTAL WORKING DAYS / MONTH 26 NOS

PROCESS BRIEF OF – 2-NITRO-4-CHLOROSULFON CHLOROBENZENE.

1) This is a chlorosulfonation process carried out in (e.d.c) as a solvent.

2) The reaction is exothermic & hence continuous cooling is required.

3) The – hydrochloric acid gas –gets out during the reaction which is to be scrubbed in to – hcl gas scrubber effectively. It generate dil. Hcl as a bi-product.

4) After completion of reaction – layer seperation to be done. Gives 80% sulfuric acid as an bi-product & e.d.c + product layer.

5) This e.d.c layer is to be washed by alkaline water to remove any traces of acid.

6) Distillition of e.d.c – gives the product.


Process Flow Diagram: 4-NITRO ORTHO XYLENE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 10) PRODUCTION OF: 2-NITRO-4-CHLOROSULFONIC ACID FROM 2-NITRO CHLOROBENZENE.

NO PARTICULARS 1.0 M.T FINISHED GOODS BATCH

1 2- NITRO CHLOROBENZENE 0.632 MT

2 ETHYLENE DI CHLORIDE 2.53 MT

3 CHLOROSULFONC ACID 1.18 MT

4 DIL. HCl GENERATED 0.400 KL

5 80% SULFURIC ACID GENERATED 0.632 MT

6 WATER FOR PRODUCT WASHING 2.10 KL


8 % YIELD 98%

9 TOTAL EFFLUENT WATER GENERATE 2.10 KL

10 NO. OF BATCHES PER DAY. 1 NO

11 TOTAL WORKING DAYS/ MONTH 26 NOS.

PROCESS BRIEF TO PREPARE 2-NITRO-4-SULFONAMIDE CHLOROBENZENE:

1) This is the pressure ammonolysis of chlorine group attached with a sulfonic acid group at 4-position.

2) The “chlorine” is replaced by “amino” group, & bi-product form is – hydrochloric acid which is continuously neutralized by excess of ammonia in suit.

3) After completion of – ammonolysis – the excess ammonia is neutralized by adding the dil sulfuric acid.

4) At ph – 4 to 4.5 the product p.p.t. Out from reaction water.

5) Then the product is filtered in nutsch, given a fress water wash to remove any free acidity & suck dry under vacuum,

Reaction:


Process Flow Diagram: 2-NITRO-4-CHLOROSULFONIC ACID


11) PRODUCTION OF: 2-NITRO-4-CHLORO SULFONAMIDE CHLOROBENZENE

NO. PARTICULARS 1.0 M.T FINISHED PRODUCT BATCH

1 2-NITRO-4-CHLOROSULFONIC

CHLOROBENZENE

1.257 MT

2 PROCESS WATER 7.632 KL

3 20% AQ. AMMONIA SOLN 1.0 KL


5 YIELD % 85%

6 DIL.SULFURIC ACID FOR EFFLUENT

NEUTRALIZATION

0.132 MT

7 TOATAL NO OF BATCHES / DAY 1 NO.

8 WATER FOR PRODUCT WASHING 2.105 MT

9 PROCESS EFFLUENT / DAY 10.63 KL

10 SALT IN PROCESS WATER AS

AMMONIUM CHLORIDR

0.176 MT

PROCESS BRIEF:

1) This product is prepared by – hydrolysis of : “2-nitro-4-chlorosulfonamide chlorobenzene” ---- followed by the sulfide reduction in suit.

2) The : 2-nitro-4-chlorosulfonamide chlorobenzene, water as media & 50% caustic lye are heated togather for 3-4 hrs at 1000c,

3) When hydrolysis of the chlorine group is complete – the reaction mass is cooled to 600c & the sulfide solution of – sodium sulfide is introduced slowely over a period of 2 hrs.

4) When the reduction reaction is completed it is cooled up to 200c– & the excess alkali is neutralised by addition of dil. Sulfuric acid.

5) When ph : 4 to 4.5 achieve the end product starts to p.p.t. Out.

6) End product is to be filterd on nutsch & washed by the fresh water. Then it is to be suck dry under vacuum & stored in a plastic carboys, in a cool & dry place.


Process Flow Diagram: 2-NITRO-4-CHLORO SULFONAMIDE CHLOROBENZENE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 12) PRODUCTION OF: 2-AMINOPHENYL-4-CHLORO SULFONAMIDE

NO PARTICULARS 1.0 M.T FINISHED PRODUCT BATCH

1 2-Nitro-4-Sulfonamide

Chlorobenzene.

1.326 MT

2 Water for Process 7.96 KL

3 50% Caustic Lye 1.124 MT

4 Sodium Sulfate (Na2S) 0.658 MT

5 Water for dilution of Sodium Sulfate 1.534 MT

6 50% dil. Sulfuric Acid 0.513 MT


8 Yield % 95%

9 Water for Product Washing 2.966 KL

10 Total effluent water / batch 13.61 KL

11 Salt contain of the process water as

Sodium Chloride & Sodium Sulfate

4.085 MT

12 TOTAL NO. OF BATCHES / DAY 1 NO

13 TOTAL NO OF DAYS / MONTH 26 NO.

PROCESS BRIEF OF – MONO NITRO ORTHO XYLENE:

1) Ortho xylene is to be nitrated in acetic acid as a media & dil. Nitric acid in present of a heterogenious catalyst at an elivated temperature – 60 to 700c

2) This is a single step nitration reaction.

3) After completion of reaction the catalyst is filtered off & reused for next reaction – product layer gets separate from acetic acid.

4) Product is given a wash of alkaline water to remove all tracess of free acid.

5) While – dil. Acetic acid is to be send for concentration so as to reuse it completely.

6) As no- hazardous effluent generate it is a completely green process.


Process Flow Diagram: 2-AMINOPHENYL-4-CHLORO SULFONAMIDE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 13) PRODUCTION OF: MONO CHLOROBENZENE FROM BENZENE BY CHLORINATION

Sr No. Particulars FOR 1.0 MT.FINISHED PRODUCT

1 Benzene 0.867 MT

2 Chlorine Gas 0.788 MT

3 Ferric Chloride 0.1 MT

4 Finished Product

Monochlorobenzene

1.0 MT

5 Yield 80.0%

6 Hydrochloric Acid 30%

Generated

588.0

7 Bi-Product – Dichlorobenzene

Generated

0.250 MT (20%)

8 Total batches / Day 1.0 no. Batches

Reaction:



GROUP 2 – BULK DRUG INTERMEDIATES & BULK DRUGS (A.P.I). 1) PRODUCTION OF: 2-METHOXY NAPHTHALENE FROM BETA NAPHTHOL

No Particulars 1.0 M.T FINISHED PRODUCT PLANT BATCH

1 Beta Naphthol 1.029 MT

2 Water 2.573 KL


4 Dimethyl Sulfate 1.072 MT

5 Dil Sulfuric Acid (50%) 1.400 MT

6 Methylene Di Chloride 0.309 MT

7 Beta Naphthol Recovered 0.103 MT

8 Finished Product Obtained 1.0 MT

9 Organic Sludge Obtained 18.00 KG

10 Total No of Batches 4 NOS

11 Total Salts as Sodium Sulfate 54.0 KG

12 Total Water as Effluent 3.43 KL

13 Total NO OF DAYS/MONTH 26 NO.S

PROCESS BRIEF:

1) The beta –naphthol is first dissolved in alkaline water containing excess quantity of caustic lye.

2) In this clear solution the dimethyl sulfate is added slowely in period of 20-30 min.

3) Then the reaction mass is boiled for 1.5 hrs so as to complete the reaction.

4) The product gets p.p.t. Out after cooling of reaction mass.

5) It is filtered in nutsch & given a water wash to it.

Reaction:

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. Process Flow Diagram: 2-METHOXY NAPHTHALENE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 2) PRODUCTION OF: 2-ACETYL-6-METHOXY NAPHTHALENE FROM 2-METHOXY NAPHTHALENE.

No. Particulars 1.0 M.T FINISHED GOODS PLANT BATCH 1 NEROLINE 0.878 MT 2 M.D.C. 5.277 MT 3 Zinc Chloride 0.928 MT 4 Acetic Anhydride 0.622 MT 5 Ice Water 3.666 MT 6 Nitrobenzene 0.225 MT 7 Methanol 1.755 MT 8 Finished Product 1.0 MT 9 Yield (%) 90% 10 Bi-Product 0.112 MT 11 Effluent Water 5.650 KL 12 Dil Acetic Acid Generate 0.750 MT 13 Caustic Required for ETP 0.112 MT 14 TOTAL NO OF BATCHES / DAY 2 NO 15 TOTAL NO OF DAYS/MONTH 30 DAYS

PROCESS BRIEF This is an “Acetylation process”. regioselective acetylation of 2-methoxy naphthalene gives its– 6-acetyl derivative. it is used as pharma intermediate

1) The 2-methoxy naphthalene is treated with acetic anhydride at moderate temperature in presence of – benign catalyst.

2) After completion of reaction water is added to break the excess of acetic anhydride in to acetic acid. & product p.p.t. out.

3) The product is filtered on nutsch & washed by water to remove all traces of free acid.

4) Further the product is purified & crystallized using suitable solvent.

Reaction:


Process Flow Diagram: 2-ACETYL-6-METHOXY NAPHTHALENE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 3) PRODUCTION OF: 3-NITRO ACETOPHENONE FROM ACETOPHENONE

No s Particulars 1.0 M.T FINISHED GOODS PLANT BATCH 1 ACETOPHENONE 1.25 MT 2 Sulfuric Acid (98%) 1.562 MT 3 Sulfuric Acid (98%) 1.208 MT 4 Nitric Acid (72%) 1.090 MT 5 Crude Product 1.719 MT 6 M.D.C. 3.430 MT 7 METHANOL 2.083 MT 8 Pure Product 1.0 MT 9 Bi-Product 0.718 MT 10 No. of Batches 3 NOS 11 Total yield of Pure Pro 58 % 12 Total yield of bi product 42% 13 Water during distillation 0.420 KL 14 Sulfuric Acid (80%) Generated 16.5 MT

BRIEF PRODUCTION PROCESS OF : 3-NITRO ACETOPHENONE

1) Acetophenone is nitrated – at chilled condition ( -50c to -100c) in excess of sulfuric acid as an nitrating media & concentrated nitric acid.

2) In the chilled sulfonated acetophenone- chilled nitrating mixture is added slowely over a period of 3-4 hrs. & further maintainance of 3-4 hrs at chilled condition.

3) After completion of the reaction – the solvent (e.d.c) is added to the reaction mass so as to extract all organic mass. Then solvent is recovered by distillition gives the end product.

4) This end product is re-crystallized in methanol to eliminate all other impurities specially : 2-nitro-acetophenone (obtained as an bi-product)

5) 80% sulfuric acid obtained as an bi-product to be sale

Reaction:


Process Flow Diagram: 3-NITRO ACETOPHENONE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 4) PRODUCTION OF: 3-AMINO ACETOPHENONE FROM 3-NITRO ACETOPHENONE.

No Particulars 1.0 mole Lab Batch (Gms)

1 Nitro Acetophenone 1.250 MT

2 Water 1.706 KL

3 NaSH (30 %) soln 3.113 MT


5 Yield % 99 %

6 Product Washing 2.5 KL

7 Total Effluent Generated 6.10 KL

8 Total Salt Content of Effluent 2.0 MT

9 TOTAL NO. OF BATCHED / DAY 1 NO.

10 TOTAL WORKING DAYS/ MONTH 26 NOS PROCESS BRIEF OF 3-AMINO PHENOL:

1) It is a simple sulfide reduction of 3-nitro acetophenone using water as media.

2) It is carried out by – slow & control addition of nash – at 600c, in the solution of water + 3-nitro acetophenone.

3) Further the reaction is to be maintaining at boiling condition for 2-3 hrs.

4) After cooling the reaction mass – product gets separate. To be filtered off & washed by water to wipe out any excess nash present.

Reaction:

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. Process Flow Diagram: 3-AMINO ACETOPHENONE


5) PRODUCTION OF: 3-HYDROXY ACETOPHENONE FROM 3-AMINO ACETOPHENONE

No Particulars 1.0 M.T FINISHED GOODS PLANT BATCH

1 3-Amino Acetophenone 1.250 MT

2 Sulfuric Acid (98%) 1.250 MT

3 Ice Water for Sulfuric Acid 2.860 MT

4 Sodium Nitrite 0.680 MT

5 Water for Sodium Nitrite 2.042 MT

6 Water for Hydrolysis 5.520 MT

7 Charcoal (5%) 63.0 KG

8 Hi-Flow 10.0 KG

9 Total Finished Product 1.0 MT

10 Total Yield % 79.5 %

12 Water Wash to Product &

Machinery

1.250 KL

11 Effluent Water Generated / Batch 12.70 KL

12 Total no. of Batches / Day 1 NO.

13 Salt Content of Effluent as Sodium

Sulfate

4.0 MT

14 Total Organic Waste of the

Process / Day:

0.666 MT

BRIEF PROCESS OF: 3-HYDROXY ACETOPHENONE.

1) This is a diazotization of – 3-amino acetophenone followed by – acid hydrolysis.

2) Initially – 3-amino acetophenone is dissolved in 50% sulfuric acid in & added sodium nitrite solution drop wise in chilled condition.

3) The process is maintain till the complete 3-amino group get di-azotize.

4) After this – excess water is added & heated slowely to boil.

5) The product is boil up to 1 hr till complete hydrolysis of di-azo compound.

6) Cooling to 100c – the end product p.p.t. Out from the reaction mass,

7) It is to be filtered on nutsch & washed with fresh water to remove all free acid.


8) Further the end product is purified & recryatallized from suitable solvent.

Reaction:

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. Process Flow Diagram: 3-HYDROXY ACETOPHENONE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 6) PRODUCTION OF: 3-ACETOXY ACETOPHENONE FROM 3-HYDROXY ACETOPHENONE.

No Particular 1.0 M.T FINISHED GOODS PLANT BATCH

1 3-Hydroxy Acetophenone 0.800 MT

2 Water for reaction 2.4 KL


4 ACETIC ANHYDRIDE 0.665 MT


6 TOTAL YIELD % 96%

7 WATER FOR WASHING OF

PRODUCT + MACHINERY

2.0 KL

8 TOTAL EFFLUENT GENERATED 4.640 KL

9 TOTAL SALT CONTENT OF THE

EFFLUENT AS SODIUM ACETATE

0.920 MT

10 TOTAL NO. OF BATCHES / DYA 1 NO

11 TOTAL NO. OF DAYS WORKING 8 DAYS ONLY

BRIEF OF THE PROCESS OF: 3-ACETOXY ACETOPHENONE:

1) It is a simple acetylation of the “hydroxy” group of : 3-hydroxy acetophenone using the acetic anhydride in alkaline media.

2) The “naoh” in water – makes the sodium salt of – 3-hydroxy acetophenone, it reacts rapidly with “acetic anhydride” to produce the end product.

3) The product immediately p.p.t. Out from the reaction mass.

4) Product is to be filtered & wash with water to remove any free acid & salts.

5) The salt – sodium acetate form as a bi-product in the process have a good commertial value.

Reaction:


Process Flow Diagram: 3-ACETOXY ACETOPHENONE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 7) PRODUCTION OF: CRUDE 3-AMINO SALICYCLIC ACID FROM 3-AMINO PHENOL


1 3-AMINO PHENOL 0.917 MT

2 WATER 2.186 MT

3 POTASSIUM CARBONATE 0.734 MT

4 CARBON DI OXIDE 0.400 MT

5 SULFURIC ACID 0.500 MT

6 ICE 0.500 MT


YIELD % 77.7%

8 WATER FOR PRODUCT WASH 2.0 KL

9 3-AMINO PHENOL RECOVERY 0.185 MT

% RECOVERY 20%

10 WATER FOR MACHINERY WASH 0.5 KL

11 TOTAL PROCESS EFFLUENT 5.876 KL

12 TOTAL NO. OF BATCHED / DAY 3 NO

14 TOTAL SALT CONTENT OF EFFLUENT

AS POTASSIUM SULFATE

1.762 MT

15 TOTAL DAYS OF WORKING 26 NOS. BRIEF OF PROCESS OF: PREPERATION OF – 4-AMNIO SALICYCLIC ACID (CRUDE)

1) This is a carbonolysis of – 3-amino phenol under pressure & elivated temperature in alkaline & aqueous media.

2) Excess potassium carbonate is used so as to maintain the ph of reaction mass alkaline through out the reaction.

3) The reaction is carried out at 1200c, with cabon di oxide gas.

4) The potassium salt of salicyclic acid form is to be – p.p.t by dil. Acid.

Reaction:


Process Flow Diagram: 3-AMINO SALICYCLIC ACID

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 8) PRODUCTION OF: PURE SODIUM P- AMINO SALICYLIC ACID

NO. PARTICULAR 1.0 M.T FINISHED GOODS PLANT BATCHES.

1 CRUDE PAS ACID 1.103 MT

2 WATER 1.103 MT

3 CAUSTIC FLEX 0.294 MT

4 WATER FOR CAUSTIC FLEX 0.294 KL

5 ACTIVATED CHARCOAL 56.0 KG

6 HI-FLOW SSUPER CELL 60.0 KG

7 TOTAL ETHANOL 1.123 MT


9 % YIELD. 79%

10 TOTAL PAS RECOVERY 0.220 MT

11 TOTAL WATER EFFLUENT 2.18 KL

12 SULFURIC ACID 0.706 MT

13 ICE 0.706 MT

14 TOTAL NO OF BATCHES / DAY 2 NOS

16 TOTAL SALT CONTENT OF EFFLUENT

AS SODIUM SULFATE

1.126 MT

17 TOTAL WORKING DAYS / MONTH 26 DAYS

BRIEF OF PROCESS –

1) It is a purification of crude salicyclic acid so as to achieve u.s.p. Grade.

2) In appropriate quantity – sodium salt of crude product is prepared & dissolved at high temperature. Then treated with activated carbon to litch out all impurities.

3) This mass is filtered through – hi-flow super cell then from micro filter.

4) Then pure product is p.p.t. By chilling the reaction mass up to 00c


Process Flow Diagram: PURE SODIUM P- AMINO SALICYLIC ACID


Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 9) PRODUCTION OF: 3-AP.-4-CARBOXAMIDE HEMISULPHATE FROM CYANOACETAMIDE

NO. PARTICULARS 1.0 M.T FINISHED GOODS PLANT BATCH

1 CYANOACETAMIDE 0.588 MT

2 TRIETHYL ORTHO FORMATE 1.251 MT

3 MORPHOLINE 0.771 MT

4 ISO PROPYL ALCOHOL 0.276 MT

5 HYDRAZINE HYDRATE 0.316 MT

6 WATER 4.133 MT

7 SULFURIC ACID (98%) 0.323 MT

8 ICE 0.323 MT

9 CRUDE PRODUCT 1.005 MT

10 WATER 0.745 KL

11 AQUEOUS AMMONIA 20% 0.338 MT

12 ACTIVATED CHARCOAL 70.0 KG

13 HI-FLOW SUPERCELL 60.0 KG

14 DIL. SULFURIC ACID 0.387 MT

15 FINISHED PURE PRODUCT 1.0 MT

17 ETHYL ALCOHOL RECOVERY AS

BI-PRODUCT

0.250 MT

18 TOTAL WATER EFFLUENT / BATCH 7.5 KL

19 NO. OF BATCHES / DAY 1 NO

20 TOTAL SALT CONTENT OF

EFFLUENT AS AMMONIUM

SULFATE

1.401 MT

BRIEF OF PROCESS:

1. Cyanoacetaide, triethyl ortho formate, morpholine & iso propyl alcohol, are reflux

togather for the condensation. Ethanol is generated as a bi product.

2. This condenstae product is added in the mixture of – 50% sulfuric acid & hydrazine

hydrate is added slowely, & boil for the completion of reaction. After it, the product is

isolated by quinching it in to ice water. Product is filtered off, centrifuge & given a fresh

water wash to remove all free acid.


Process Flow Diagram: 3-AP.-4-CARBOXAMIDE HEMISULPHATE


Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 10) PRODUCTION OF: ALLOPURINOL FROM: 4-CARBOXAMIDE HEMISULPHATE.

NO PARTICULARS 1.0 M.T FINISHED PRODUCT PLANT BATCH

1 HEMISULPHATE 1.618 MT

2 FORMAMIDE 4.737 MT

3 FORMAMIDE RECOVERY 2.842 MT

4 METHANOL FOR WASHING 1.0 KL


5A % YIELD 80%

6 TOTAL WATER EFFLUENT NIL


8 TOTAL NO OF WORKING DAYS /

MONTH

10 NO


1) This is a condensation process between – hemisulphate & formamide.

2) This is carried out at reflux temperature in formamide as a solvent, after the completion of reaction, excess solvent is distilled off & product is filtered.

3) Product is washed by the fresh water & dried in oven.

Reaction:


Process Flow Diagram: ALLOPURINOL

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 11) PRODUCTION OF: C.P.A DERIVATIVE OF Q-ACID FROM : 2,4-D.C.F.A

NO. PARTICULARS 1.0 M.T FINISHED GOODS PLANT BATCH

1 2,4-DICHLORO-5-FLUORO

ACETOPHENONE

0.693 MT

2 DIMETHYL CARBONATE 1.386 MT

3 SODIUM METHOXIDE 0.201 MT

4 TOLUENE 1.386 MT

5 DIMETHYL SULFATE 0.473 MT

6 DIMETHYL FORMAMIDE 0.274 MT

7 WATER 0.347 KL

8 GLACIAL ACETIC ACID 0.101 MT

9 SODIUM SULFATE ANHYDROUS 20.0 KG

10 CYCLOPROPYL AMINE 0.181 MT


12 YIELD % 90%

13 ORGANIC RESIDUE 0.114 MT

14 SODIUM METHYL SULFATE SALTS AS BI-

PRODUCT

0.502 MT

15 ETHYL ACETATE 2.0 KL

16 ETHYL ACETATE RECOVERY 100%

17 TOLUENE RECOVERY 100 %

18 DIMETHYL CARBONATE RECOVERY 1.030 MT (95%)

19 DIMETHYL CARBONATE CONSUMED AS

REACTANT

0.302 MT

20 METHANOL RECOVERED 0.214 MT

21 TOTAL NO OF BATCHES / DAY 5 NOS * 30 WORKING DAYS.

BRIEF OF PROCESS: 1. It is a single step process where 3 condensation reactions are carried one after another

in suit.

2. First – 2,4-dcfa is condensed with the dimethyl carbonate in presence of strong base like

– sodium methoxide in toluene as solvent. After the completion of the reaction –

dimethyl formamide dimethyl sulfate adduct is added followed by – cyclopropyl amine.

3. After chilling – the end product – “c.p.a. Derivative of acetophenone” is precipitated.


Process Flow Diagram: C.P.A DERIVATIVE

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 12) PRODUCTION OF: CIPROFLOXACIN Q ACID – FROM C.P.A. DERIVATIVE.


1 C.P.A DERIVATIVE PURE 1.191 MT

2 TOLUENE 4.765 KL


4 WATER 1.866 KL

5 TOLUENE RECOVERY 4.765 KL (100%)

6 FRESH WATER 2.654 KL


8 30% DIL HCl 0.847 KL

9 50% CAUSTIL LYE FOR PROCESS WATER

NEUTRALIZATION

0.270 MT

10 DIMETHYL FORMAMIDE 2.86 KL


12 YIELD % 99.0 %

13 DIMETHYL FORMAMIDE RECOVERY 2.86 KL (100%)


15 PROCESS EFFLUENT 6.67 KL

16 SALTS CONTENT OF EFFLUENT AS SODIUM

CHLORIDE

56 KG

17 TOTAL NO. OF WORKING DAYS / MONTH 30 DAYS


1) C.p.a derivative is condensed with sodium hydroxide in anhydrous condition & followed by hydrolysis of ester group in to carboxylic acid group.

2) After completion of reaction – product is precipated by adding concentrated sulfuric acid in it very slowely.

3) The product is chilled & filtered of. Fresh water washing is given to remove all free acid.

4) Further the product is re-crystallized in suitable solvents like – alcohol


Process Flow Diagram: CIPROFLOXACIN Q ACID

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 13) PRODUCTION OF: CIPROFLOXACIN BASE FROM Q-ACID

NO. PARTICULARS 1.0 MT FINISHED GOODS PLANT BATCH

1 Q ACID 1.0 MT

2 D.M.S.O. 5.0 KL

3 AN. PIPERAZINE 0.800 MT

4 PURIFIED WATER 6.0 KL

5 ACETIC ACID GLACIAL 1.50 MT

6 ACTIVATED CHARCOAL 50 KG

7 HI-FLOW POWDER 30 KG

8 25% AQ. AMMONIA SOLN 2.00 MT

9 PURIFIED WATER FOR

WASHING

2.025 KL


11 YIELD % 84.5%

12 TTAL D.M.S.O. RECOVERY 4.90 KL (99%)

13 TOTAL PROCESS WATER AS

EFFLUENT

9.60KL

14 SALTS IN THE PROCESS WATER

AS AMMONIUM ACETATE

1.332 MT

15 PIPERAZINE RECOVERY 0.400 MT

16 M.D.C. LOSS 50 KG

17 TOTAL BATCHES / DAY 2 NO * 26 WORKING DAYS

Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. BRIEF OF PROCESS:

1) Q-acid is condensed with the anhydrous piperazine in n-butanol as a solvent at reflux temperaure. After complection of reacion solvent is completely distilled off.

2) To the residue added water + acetic acid at high temperature & make a clear solution of acetate salt of product. Added activated carbon & filter it to remove all impurities.

3) To this clear filtrate added aqueous ammonia so as to precipitate the end product.

Reaction:


Process Flow Diagram: CIPROFLOXACIN BASE


Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit - 2 Developer: M/s. Odyssey Organics Pvt. Ltd. 14) PRODUCTION OF: CIPROFLOXACIN HYDROCHLORIDE SALT – BASED ON 1.0 MT

CIPROFLOXACIN BASE.

NO PARTICULARS 1.0 MT CIPROFLOXACIN BASE CONVERSION PLANT

BATCH

1 CIPROFLOXACIN BASE 1.0 MT

2 METHANOL 4.0 KL

3 PURE HCl IN IPA. 30% SOLN 0.400 KL

3A 98% SULFURIC ACID FOR HCL 0.900 MT

4 METHANOL FOR PRODUCT

WASHING

1.00 KL


6 YIELD % 99%

7 METHANOL RECOVERY 100%

8 P-Toluene Sulfonic Acid 56 KG

9 Purified Water 60 lit

10 Aqueous Ammonia 1.0 kg

11 CIPROFLOXACIN BASE

RECOVERY OBTAINED

9.0 KGS

12 75% SPENT SULFURIC ACID

FORM

1.2 MT

13 TOTAL NO. OF BATCHES / DAY 1 NO.

14 TOTAL NO .OF WORKING

DAYS

26 NOS.


1) It is the simple acidification process in solvent so as to prepare a salt of ciprofloxacin base.

2) Ciprofloxacin base is taken in equal quantity solvent as methanol – to this slurry at chill temperature added slowely equi molar amount of aqueous hydrochloric acid.

3) The precipated end product is filtered off & given a wash of fresh methanol.

4) The product is dried & stored in appropriate facility.


Process Flow Diagram: CIPROFLOXACIN HYDROCHLORIDE SALT

Project: Manufacturing of Speciality Chemicals & Intermediates Developer: M/s. Odyssey Organics Pvt. Ltd.

EXHIBIT 3: WATER BALANCE DIGRAM

Sock Pit & Septic Tank

Domestic Use 9.0 KLD

(2.5 + 6.5) KLD

17.5.

Total Water Requirement 468 KLD

[Existing 52 KLD+ Proposed 416 KLD

Industrial Use 454 KLD

(49+405) KLD

Gardening 5.0 KLD

(0.5 + 4.5) KLD

Boiler 113 KLD

Disposal at MSWL

Inorganic salts as Sludge from MEE

Process 272 KLD

Acid Dilution 30 KLD

Multiple Effect Evaporator

250 KLD

ETP 255 KLD

170

Evaporation Loss 7.5 KLD

Cooling Tower 25 KLD

Gas Quenching 12 KLD

Sell to other Industries as dilute Acid

5.4 KLD

Condensed Water (90%)

225 KLD

Activated Charcoal

Bed

Recycle & Reuse for Process

85


AT PRESENT ODYSSEY ORGANICS HANDLES 3 MAIN EFFLUENT STREAMS –

EXHIBIT 4: ETP DETAILS

SECOND IS REDUCTION STREAM AS BELOW:

SPENT SULFURIC ACID

NITRATION PROCESS

STORAGE TANKS

100 % SALE AS BI-PRODUCT

NEUTRALIZATION STORAGE TANKS

MULTIPLE EFFECT EVAPORATOR

(1000 KG / HR)

CONDENSE WATER STORAGE

RECYCLE SLUDGE

M.S.W.L

REDUCTION STREAM


THE THIRD IS - HYDROLYSIS STREAM IS AS BELOW.

In the below diagram:

A & B– Collection & Primary Treatment Tanks (Neutralization & Hydrogen Peroxide Mixing).

C - Primary Clarifier to settle the Solids,

D – Secondary Tank (aeration)

E – Secondary Clarifier,

V- “V” – Shaped Notch for Sample collection & Discharge to C.E.T.P

HYDROLYSIS STREAM

STORAGE TANKS 1

A B

C

D E

TO C.E.T.P. V


Project: Manufacturing of Speciality Chemicals & Intermediates Exhibit ‐ 5


EXHIBIT 5: LAYOUT PLAN FOR PROPOSED PROJECT

A. Layout Plan of Plot no. 36 & 37



B. Layout Plan of Plot no.39



EXHIBIT 6: MANAGEMENT OF HAZARDOUS WASTE DISPOSAL

Sr.

No

.

Hazardous

Waste

Category

No.

Quantity (MT/Month) Source of

Generation

Stora

ge Disposal

E P T

1 Used Oil 5.1 30 150 180 Plant

Maintenance Drum

Selling to

registered

Refiner

2 ETP Sludge 26.2 2 13 15 ETP Bag

M.S.W.L.

for Land

Fill or

Incineratio

n

3

Solid

Sludge

from MEE

34.4 10 1720 1730 MEE Bag

M.S.W.L.

for Land

Fill or

Incineratio

n

4 Organic

Residue 28.1 Nil 25 25 Process Bag M.S.W.L.

5 Process

Waste 26.1 12 1738 1750 Process Bag

M.S.W.L.

for Land

Fill or

Incineratio

n

6

Discarded

Bags &

Container

33.3 1200 6000 7200 Production

Section

Store

into

SWSA

Selling to

registered

reuser/rec

yclers

't ::MAHARASHTRA POLLUTION CONTROL BOAR.D

| :2402078U24OLO437. cr : 24024068.k*'a:

.,,hRp//mpcb.mah.nii. inI e-mail: [email protected]

and conditions;

Red/ SSIi...u''it No. Fo/ Ro.Raigad/ pcl-l/ EIC-428-06/E/ cc- 2\ (

KALPATARU POINT, 3'd & 4th itoor,Opp. Clneplanet, Near Sion Circle,Sion (East). MUMBAI : 400 0 t2

Date; I t/ 3/2006

upto commissioning of the unit'.:

*

-r

.TFTItml'Fw

I''P

r\c

I

consenttoEstab|ishundersection25oftheWate.r(Preventlon&contlo|;i;;il;il;; j;"i, 1974 & under section 21 of theair (Prevention & control

ii p"i[ir""i A;t, 1981 anj euttroriz.ation l.--Renewal of Authorization

;;i"t i;iJ s oi tne Hazardous ' wastes (Management & Handling)

i,li"j is89 and Amendment Aules' [to be referred as Water Act' Air Act

and HW(M&H) Rules respectivelyl'

CONSENT is hereby granted 1o

M/s' OdYsseY Organlcs Pvt' Ltd'-

' Plot Ho' e' f-6, 37-' MIDC M"h"d'-' ' '''t ' '

Dist' Raigad' - , ., ,, ,.,

|ocated in the area declared under the provisions.of the,WaterlAct,]Air act and Authorization

i-'iiiiinli pii"il.* oi lrw(r'ltaH) iuies ino amendments,theretors-ubject t9 tlr'e provisions ot the

;il.;iii; i;E uno ttr*'Oto"it that may be made further and subject to the following terms

l

a

I 3., CONDITIONS UNDER WATER ACT :

(i)

(iil

(iii)

The daili quantity of trade effluent from the factory shall not exceed 2O'O M3

' t d5'oM3'The daily quanti{ of sewage effluent from the factory shall fiot excee

.lTrade Etfluent :

i;;;il;;i : The applicant shall provide compiehensive treatment system

;"*Gtfi6""f pti*ary I s""onoury and/or tertiary. treatT"n! ?: I warranted with

iuiui"..,i lo inttueniquality and operate and mdintaln lho .same continuously so

"-" io1.n-ieu" tnu quatity oi the treated effluent to the Jollowing standards :

1\ ^!r Between 55 to 90z{ Susoenoed Solios Not to exceed 100 mgil'

3i ddn 3days 27 Deg c Not to exceed 100 mg/l

4i coD Not to exceed - 250 mg/l

si oir & Grease Not to exceed 10 mg/l .

6i iotat-OissotveO Sotios Not to exceed 2100 mg/l

7\ q,,r^h,r6c Not to exceed 1000 mg/|.

;i ffi;l;;; Not to exceed 600 ms/l '

;j. v" soo-irt Not to exceed 60% mg/l

t":_

eia1

Text Box

Exhibit 7: Consent to Establishment

shall prpviore gg.l4prahqnsiveto infludnt q$ality affl bperateachieve thg qlality of treatedso as t0

T.reatnent Qisqos?l

(viii) gther conditiona I

0. CONDITION$ UNPER AIR ACT :

The applicant shall install a ogmprehonslvg control syBtgm con€istlng ot aQntrol

eouioliints as is warrantEd with referonce to generathn a{ emlo€ion and operateario haintain the same continusu$ly $0 as to achieve thg lsvel of poll$tants tq the

fallqwing standards :

Qar)trel EqrJipmont : Scrubber 9f adequatg capacity shall be provid€d to limit

the emissions.

Standads for'Fmlssisns af Air Follqtants :

(i) SPMITFM(ii) soaNot to exoeedNol to excesd

150 mg/Nr.rr83,6 Kg/DEy.

(ii)

(ii0

(lv)

The appllcant ehall ob-ssrve the following fuel Battern :'

r!" Brd'slr€ $t8*fl^n

The applicant shall brect the thinrney(s) of the lgllowlng oBectficauqn8 :'Sr.No. cli{tev ?ttached !q ft"eigltt !0 !SlS.I Bbliei 11.0

The appli€Ent€.hat! piovide ports in the chimney/(s) and facilities such as ladder'ptatfoim etc. for monitoring the air emissions and the same shall be open forinspection toland for use of the Board's Staff. The chimney(g) vents attached to

uarious sorrces of emission shall be designated hy numbers. sqch as S-1, s-2,

etc. and these shall be painted/ displayed to facilltat€ ldentification.

:,(vD

:

emissiong and

(iD

(iii) storage,

7

s.

o

. i 5i!:;: 'sd/-

1,,, "a;t,{D.E.,BoralkarfMember Secretary

Principal Scientlflc Officer 'TO;Mls.. Odyss€y Organics Pvt. Ltd.Plot Ne, F- 36, 37, MIDC Mahad,0ist. Ralgad.Copy to:1) RO- Raigad / $RO- Mahad / CAO/ Cess Branch / Master file.2) Chief Accounts Otficer, I\4PCB, Mumbai

Received Consent fee of - Amount D.D.No.I{s.1,500f 24626

Date Drawn ofi2110612006 Mahad Co-op Urban

N{AIIAIi.ASIITIIAPhone : 4A10437 AA207 81

t4037 124 t403527 3

3. CONDITIONS(i) The:daily quantity

POLLUTION

24044532t4024068 14023516 nAH.AMsi{rRA

enquiry@mpcb gov. inhtl p://nr D(b. g01,.ir)

CONTROL I}OARDKaloataru Point, 3rd & 4th floor,l\4atunga Scherne Road No.8, Opp.Planet Clnema, Near Sion Circle, SionMumbai - 400 022

Sion-CineaFlFax :

Email :

Visit At : ffi\wwIled.tS.S.I DTte: 1l1ll3Con.se,nt No: IIO/ASTIIIIC. No-RD-2S 2 2-i J/IVG: n - O 7 S7 C

Consent to Operatc under Section 26 of the Water (prevention & Controlof Pollution) Act, 1974 & undcr Scction 2l of the Air (prevention &Control of Pollution) Act, 1981 and Authorization / Renerval ofAuthorization rrnder Rulc 5 of thc Hazard<lus Wastes (M:rnagen-reDt,Ilandling & 1'ransboundry Movement) R ules 200g['lo be referred as Water Act, Air Act and HW (M&H) Rules respeciively].

CONSENT is hereby granted to r: r, ",- '

Odyssey Organics Pvt Ltd, .:. .

Plol No-B-36/3 7. MIDC Mahact,Dist-Raigad. -402309Maharashtra, India

located in the ar.ea declared under the provisions of the Water Act, AirAuthorization under the provisions of HlV(M&H) Rules and amendmentssubject to the provisions of the Act and the Rules and the Orders thatmade furthel and subject to the following terms and conditions:

.1. The Consent to Operate is granted for a period up to:

?. The Consent is valid for tlle manufacture of-

act andtheretomay be

Sr.No- Products Maximr.rm Qr"rantit5'

tr'r Sodium Picramati:,.. 10.0 MTAII,€\ 4-Chloro-2-Amino Phenol (4 CAP) 12.0 MT/Mo. 5-Nit lo-2-Amino Phenol (5 NAPr 12.0 MT/M

BY PRODUCTt/1 Dilute Sulphuric Acid 100.0 MT/\4

}ltrotzor4'.

&

UNDER WATT]R ACT:of trade effluent from the factory shall not exceed 20.0M8.

(ir) The daily quantity of sewage elIluent from the factory shall not exceed b.0Mr.

tr$SR O/l\,1ahad/ l/Ri Si+4580000

eia1

Pencil

eia1

Text Box

Exhibit 8: Consent to Operate

(iii) Trade Effluent :

Tr-eatment: The applicant shall provide complehensive trealnr,,,;,,consisting of primary / secondary and/or tertiary treatment as is wii .:. i,, i .. ;

referencetoinfluentqualityandoperateandmaintainthesamecaJr.;rii.,,.:.as to achieve the quality ofthe treated effluent to the followine stand:l .i. r

t PH Between 6.5 to S.ir100 mg/t.2 Suspended Solids ot to exceed

3 BOD 3 davs 27 des.0 Not to exceed 100 m4 COD Not to exceed 250 m5 oil & Grease Not to exceed 10 rn6 Total Dissolved SoIids Not to exceed 21007 Phenolic Compounds Not to exceed 2.08 Sulnhates Not to exceed II Chlorides Not to exceed10 % Sodium Not to exceed .' 600/o rr

v) Trade Effluent Disposal: The treated effluent shallback into process to the maximum extent and remainin

lel:iated and rcr.rdispose of to CE

(l .r.rsed

ETP.oacK lnto process f,o tne maxtmum extent and remallrng shall cllspose of tiThere shall not be any discharge of effluent outside the industry premises.

Non-Hazard

(i) Domestic purpose(ii) Watel gets Polluted &

Pollutants are Biodegradable ...(iii) Water gets Polluted, ?oilutants

are not Biodegradable & Toxic ...(jv) Jndustria I Cool i n g. spraying

in miue pits or boiler feed.llhe applicant shall regrrlar\' submit

consumption' in the prescribed formSection 3 o{ th,e. said Act.

Wastes:

ons: Industry should monitor effluent quality regularly.

... 7 .0 cMD

3O.O CMD

O.OO CMD

8.OO CMDto the Board the returns of waterpay the Cess as specified under

4., The. applicant shall comply with the provisions of the Water (prevention &Control of Pollution] Cess Act, 1977 (to be. referred as Cess Act) and. alnendment Rules, 2003 there underThe daiiy water consumption for'the following categories is as under:

SRO/Mahad/l/RrS/445 80000

{CY$"

5. CONDITIONS UNDER AIR ACT:(t Tlie applicant shall install a comprehensive control system

consisting of control equipments as is waEanted with reference togenelation of emission and operate and maintain the samecontinuously so as to achieve the level of pollutants to the followinesta ndards:

a. Control Equipment:Industry shall provide dust collector/scr.r-rbber of sufficient caDacitv

to contrcl the emissions.

b. Standards for Stack Emissions:

1 SPM/TPM Not to exceed 150 me/Nm32 SOz Not to exceed 3.6 Ks/dav3 SOz (Process) Not to exceed 50::'i irp \,i4 Acid Mist/HCL Not to exceed €.5 ', ppm

(i) The licant shall otrserve the foll<-r

(iii) it:J'Jlh" "hl-.r"y/(s) and facilities such as ladder,

and the same shall be open for

be designated by numbers such as S-1, S-2, etc. andto facilitate identification.

(iv) The industry :e adequate measures for control of noise levels from its own

Lan /b dlJ(A) durrng day time and Z0 dB(A) during night time. Dayin between 6 a.m. and 10 p.m. and night time is reckoned between

various sources of ethese shall be pai

time is

(vi) Oth nditions:1) The industry should not cause any nuisance in surrounding area.2) The industry should rnonitor stack emissions and ambient air quality regularly.

SRO/Mahad/l/R/S/44580000

i"' r i' "'(ii) The applicant shall erect the chimney(s) oTthg following

! i,llio)

6. CONDTTIONS UNDER HAZARDOUS WASTE (MANAGEMENT, HANDLINGTRANSBOUNDRY MOVEMENT) RULES, 2OO8:

(i) The Industry shall handle hazardous wastes as specified below.

2.

Treatment: - NILTr'e authorization is hereby granted to operate a facility for collection, storage,

transport & disposal of hazardous waste.

The industry should comply with the Hazardous Waste (N{&H) Rules,.2003.

Whenever due to any accide(t or other unforeseen act or even, slch emissio- -

occur or is apprehended to occr.rr in excess of standards laid down, sr' '

information shall be forthwith Reported to Board, concerned Police Statio!,

i'i

D.

office of Directorate of Health Services, Department of E.xplosives, Inspectoratr,of Factories and Local Body. In case of failure of pollqtio4 cgnirol equipments,the produclion process connected to il shall be stopped.The unit has to display and maintain the data online 6rttside tbe factory main

(i')1.

gate in Marathi & English boLh on a 6'x4' in the manner and thesubmitted to this officereport of the compliance along with p

& concerned Regional Office/ Sub

c. It shall be ensured that theof strictly in accordance with the H

liis handled, managed & disposedWasl-e (Manage men | & Handling)

Rules, 1989 as amended on 2003'qnil shown & submitted to the Board as &when asked for.

ii, The applicantcoverage/

sweeprngs, of scientifically so as not to cause any nuisance / pollution.The take necessa* permissions from civic authorities for disposal todump

Lt shall provide fo'.. an alternate electric power source suffrcient to operatecontrol facilitibs installed by he applicant to maintain compliance with the

d conditions of the conseit. 'In the absence, the applicant shall stop, reduce orcontrol production to abide by terms & conditions of this consent regardingrir. . r. qlrrcrwlsc, uuuu

"r'.',,.,.pollution levels.v.'', ihe applicant shall not chaDg6 or alter quantity, quality, the rate of dischatge,

temperature or the mode of the effluent / emissions or hazardous wastes or controlequipments provided for without previous written permission of the Board.

vi. The applicant shall provide facility for collection of environmental samples and

samples of trade and sewage effluents, air emissions and hazardous wastes to theBoard staff at the terminal. or designated points and shall pay to the Board for theservices rendered in this behalll

vii. The applicant shall make an application forbefore the date of the expilT of the consent.

renewal of the consent at least 60 days

iii. Solid waste

minimum 33% of the available open

hazardous solid waste arising in the

land under green

factory premises,

of September every year, theyear ending 31* March in theof the Environment (Protection)

viii:The film shall submit to this office, the 30th davEnvironmental Statement Report for the financial

' prescribed Form-V as pre the provisions of rule 14(Second Amendment) Ru1es, 1992.

26.2 Chemical sludge from wastewater treatlrrent

SRO,&{ahad/VR /S/44580000

xl,

IX.

Copy for inforrnation to:-Regio na I Officel MPCB RaigadSub-Regional Officer MPCB, MahadChief Account Officer MPCB Mumbai.

xii. Neither storm water nor dischar.ge from other premises shall be allowed to mix withthe effluents flom the factory

8. If CETP does not work lbr achieving standards & problem ofpollution occurs, industry shall voluntarily stop the production ortotal effluent shall be reused.

9. Tlre consent slrould not be construed as any exemption fromobtaining necessary NOC from other Govt, agcncies as may deemcdfit necessa ry.

10. The industry shall also cornply with the Irrdustii specific standardsnotified under Environrnent Protectiol Aq*a '

t,l- ,:].

11. The overall production quantities shall not exceed the consentedlimits and there shall not be any iiitieaie in pollution load.

12. The iridustry shall comply with the Resta.rt direction conditionsvide letter dtd-L4l0bl20l2 .foi .*trich B.G of Rs.b0, 000/- has beenobtained.

13. Capital investment of the industry is Rs. 1.71 lakh. A^ffi ffi,,,

As inspection book shall be opened and made availaltle to the Board's officels dulinetheir visit Io lhp apllicanl.The applicant shall install a sepalate elcctric meter showing the consulnption ofenelgyfor opelation of domestic and industrial efflLrent tr.eatment plants and air pollutioncontrol system. A register showing consumptjon of chemicals used for tr.eatment shallbe maintained.Separate drainage system shall be provided for collection of trade and sewaeeef{luents. Terminal manholes shall be provided at the end of collection svstem u.iiharlangeme[t for rneasuring tire flow. No effluent shall be aclmitteci in ihe nipes /servers down- stream of the terminal manholes. No effluent shali find its wav othelthan in designed and plovided collection System.

(P.K.Mirashe)Assistant Secretary (Technical)

Received Consent fee of -

S RO/Mahad/l/R/S/44580000

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