exhibit 1. location map of project...

Project: Manufacturing of Aroma Chemicals

Developer: M/s Raigad Petroleum Limited.

EXHIBIT 1. LOCATION MAP OF PROJECT SITE

Project: Manufacturing of Aroma Chemicals Developer: Raigad Petroleum limited

BENZYL SALICYLATE

No Description 01 IUPAC NAME Benzyl 2‐hydroxybenzoate

02 MT/Month 300 MT 0 MT/Annum 3600 MT

Chemistry:

Process:

Benzyl chloride undergoes esterification with Salicylic acid in presence of Triethylamine to give Benzyl salicylate crude which passed through resin to get colorless crude followed by distillation to give Benzyl salicylate product.

Material Balance:

No Input Qty per MT Qty Output Qty Per MT Qty 01

Benzyl chloride 701 Aq.Triethylamine hydrochloride solution (23-30%) 2844

02 Salicylic acid 787 Effluent 524 03 Triethyl amine 616 Crude weight 1233 04 Water for quenching 1984 Total 4601 05 Water for neutralization 513 Total 4601

Resin process: No Input Qty per MT Qty Output Qty Per MT Qty 01 Benzyl salicylate crude 1233 Benzyl salicylate 1232.8 02 Resin 2.74 Resin 2.74 03 Sodium Hydroxide solution 2515 Sodium Hydroxide solution 2515.2 Total 3750.74 Total 3750.74


Distillation:

Recovery of Triethylamine:

No Input Qty per MT Qty Output Qty Per MT Qty 01 TEA+HCl solution (23-

30%) 2844 Rec TEA 56202 Sodium hydroxide 277 Effluent 2559 Total 3121 Total 3121

Resin washing 1st washing with methanol

No Input Qty per MT Qty Output Qty Per MT Qty 01 Methanol 6.85 Methanol 6.85 Total 6.85 Total 6.85

Methanol recovery


Methanol 6.85

Methanol recovered 6.66 Bottom mass 0.05 Loss 0.13 Total 6.85 Total 6.85

2nd washing with Hexane

No Input Qty per MT Qty Output Qty Per MT Qty 01 Hexane 17.11 Methanol 17.11 Total 17.11 Total 17.11

Hexane recovery


Hexane 17.11Hexane recovered 16.72

Bottom mass 0.05

No Input Qty per MT Qty Output Qty Per MT Qty

Crude of Benzyl Salicylate 1232.8

Column Tops 98.8Benzyl Salicylate 1000Bottom mass 109Loss 25Total 1232.8

Total 1232.8


Loss 0.34 Total 17.11 Total 17.11

01.MANUFACTURING PROCESS FLOW DIAGRAM OF PRODUCTION OF BENZYL SALICYLATE


CAMEK

S. No Description Details

1 IUPAC NAME --------- 2 CAS No 65113-99-7 3 MT/Month 6.5 MT 4 MT/Annum 78 MT

Chemical Reactions:

Stage 1

Material Balance:

Stage 1

S.No Input Qty per MT Qty Output Qty Per MT Qty 01 A-Campholenic

aldehyde 1142Recovered mixture of MEK & Methanol 7783

02 MEK 856 Potassium acetate solution 225103 Methanol 7477 Effluent 358404 Soda ash 11 Crude 145005 Salt 57 Total 1506806 Acetic acid 274 07 KOH 228 08 Water for quenching 1712 09 Water 3311 Total 15068

Distillation:


Manufacturing Process:

A-Campholenic aldehyde undergoes aldol condensation with MEK in presence of base and

Methanol as solvent to give CAMEK crude which is subjected to give CAMEK mains.

02 .MANUFACTURING PROCESS FLOW DIAGRAM OF PRODUCTION OF CAMEK

Geranyl Nitrile

S.No Input Qty per MT

Qty Output Qty Per MT Qty

1 CAMEK Crude 1450

Column Tops 244 CAMEK 1000 Column bottom mass 169 Distillation loss 37 Total 1450

Total 1450


S. No Description Details 1 IUPAC NAME 3,7-dimethylocta-2,6-dienenitrile 2 CAS No 5146-66-7 3 MT/Month 5 MT 4 MT/Annum 60 MT

Chemical Reactions:

Stage 1

CHO

(NH2OH)2.H2SO4 Na2CO3N

OH

Na2SO4 CO2 3H2O22

Citral Hydroxyl Ammonium SulphateCital Oxime SodiumSulphate

C10H16OMol. Wt.: 152.23

H8N2O6SMol. Wt.: 164.14

CNa2O3Mol. Wt.: 105.99

C9H16NO•••

Mol. Wt.: 154.23

Na2O4SMol. Wt.: 142.04

CO2Mol. Wt.: 44.01

Stage 2

NOH

Cital Oxime

OO

O

Acetic anhydride

N

O

OH

C10H15NMol. Wt.: 149.23

C2H4O2Mol. Wt.: 60.05

C10H17NOMol. Wt.: 167.25

2

Geranyl Nitrile Acetic acid

C4H6O3Mol. Wt.: 102.09

Material Balance Stage 1

S.No Input Qty per MT Qty Output Qty Per MT Qty

01 Citral 1079 Sodium sulphate/Ammonium Sulphate solution (18-28 %)

2412

02 Hydroxyl amine sulphate

629 Effluent 3097

03 Soda ash/Ammonia

629 Carbon dioxide 130

04 Sodium chloride 40 Citral Oxime Crude 1235

05 Water for quenching

1439

06 Water for washing 3058 Total 6874 Total 6874

Stage 2

S. No Input Qty per MT Qty Output Qty Per MT Qty


01 Citral oxime crude 1235 25% Acetic acid 1937

02 Acetic anhydride 635 Effluent 1082

03 Water 1175 Geranyl Nitrile Crude 1112

04 Soda ash 7

05 Water 1079

Total 4131 Total 4131 Distillation:

03.MANUFACTURING PROCESS FLOW DIAGRAM OF PRODUCTION OF GERANYL NITRILE

S. No Input Qty per MT Qty Output Qty Per MT Qty

1 Geranyl Nitrile Crude 1112

Column Tops 18 Geranyl nitrile Product 1000 Column bottom mass 75 Distillation loss 19 Total 1112

Total 1112


PRIONYL


No Description 01 IUPAC NAME Methyl 2,4-dihydroxy-3,6-dimethylbenzoate 02 MT/Month 30 MT 0 MT/Annum 360MT

Chemistry: Stage 1A

Stage 1B

Stage 2

Stage 3

Process: Stage1A & B :


Propionyl chloride reacts with Propene gas in presence of Aluminium chloride catalyst gives Chloro –Hexanone which undergoes dechlorination ( in Stage 1B) in presence of Triethanolamine gives crude 4-Hexen-3-one and subjected to distillation to give 4-Hexen-3-one.

Stage 2

4-hexen-3-one reacts with Dimethyl malonate in presence of base gives Methyl 3,6 –dimethyl-2,4 dioxocyclohexanecarboxylate (DIONE).

Stage 3:

Methyl 3,6 –dimethyl-2,4 dioxocyclohexanecarboxylate (DIONE) undergoes aromatization by chlorinationa and dehydrochlorination with Sulphuryl chloride followed by recrystallisation gives Prionyl (Methyl 2,4-dihydroxy-3,6-dimethylbenzoate.

Stage 1A

Material Balance:

No Input Qty per MT Qty Output Qty Per MT Qty 01 Ethylene dichloride 15731 Water - AlCl3 soln (30-38%) 1501602 Aluminium chloride 3972 Effluent 3253403 Propionyl chloride 2622 Crude weight 1918704 Propene 2105 Total 6673705 Soda ash 199 06 Water for quenching 103228 07 Water for washing 31780 08 Total 66737

Stage 1B

Material Balance:

No Input Qty per MT Qty Output Qty Per MT Qty 01 Stage 1 crude 19187 Water+ TEA (29 to 33%) 1688202 Triethanolamine 3972 Effluent 1251303 Ethelene Dichloride 1589 Crude weight 1918704 Water for TEA 11917 Total 4858205 Water 11917 06 Total 48582

Distillation:

No Input Qty per MT Qty Output Qty Per MT Qty 19187 Recovered EDC 15651


Stage 2 Material Balance:

No Input Qty per MT Qty Output Qty Per MT Qty 01 4-Hexen-3-one 1271 Methanol recovered 389802

Dimethyl malonate 1638Water (Sod.Sul( 5-8% )& MEOH(4-6%) 13588

03 Sodium Methoxide 960 Effluent 494204 Methanol 4266 DIONE Product 166705 Water for quenching 8898 Total 2409506 30 % Sulphuric acid 2825 07 Water for washing 4237 08 Total 24095

Stage 3 Material Balance:

No Input Qty per MT Qty Output Qty Per MT Qty 01 Dione 1667 DMF+Acid for neutralisation 1300002 DMF 3333 Effluent 1700003 Sulphuryl chloride 1333 Prionyl Crude 133304 Water for quenching 8333 Total 3133305 Water for washing 16667 Total 31333

No Input Qty per MT Qty Output Qty Per MT Qty 01 Prionyl Crude 1333 Charcoal recovered 2702 Methanol 4862 Aqueous Methanol Solution 3104203 Activated Charcoal 27 Effluent 450004 Water for quenching 26810 Prionyl product 100005 Water for washing 4167 Total 36568 Total 36568

Column Tops 556Product 1271Column Bottom mass 1390

Distillation Loss 319 Total

19187 Total 19187


04 .MANUFACTURING PROCESS FLOW DIAGRAM OF PRODUCTION OF PRIONYL


Aldehyde C11

No Description 01 IUPAC NAME 10- Undecen-1-al 02 CAS No 112-45-8 02 MT/Month 25 MT 0 MT/Annum 300 MT

Chemistry:

Process:

Undecylenic acid undergoes decarboxylation at high temperature with Formic acid & Methanol in presence of Catalyst MC gives Undeylenic aldehyde (Aldehyde C11) Crude along with Carbon

dioxide gas and water. Washing Crude followed by distillation gives Aldehyde C11 Products

Material Balance:

No Input Qty per MT Qty Output Qty Per MT Qty 01 Undecyleneic acid 1805 Carbon dioxide (CO2) gas 41502 Formic acid 1221 Water 23503 Methanol 828 Crude 276804 Paraffin 711 Bottom mass from reaction 104605 Catalyst MC 120 Loss 22106 Total 4685 Total 4685

Washing

No Input Qty per MT Qty Output Qty Per MT Qty 01 Crude 2768 Crude weight after wash 179102 Soda ash 17 effluent 279903 Salt 86 Total 459004 Water 1719 05 Total 4590


Distillation:

05 .MANUFACTURING PROCESS FLOW DIAGRAM OF PRODUCTION OF


Crude weight 1791

Column Tops 146Product 1000.00Column Bottom mass 556Distillation Loss 89

Total 1791 Total

1791


MPO

No Description 01 IUPAC NAME 3-Methylpent-3-en-2-one 02 CAS No 565-62-8 02 Proposed MT/Month 225 MT 0 Existing MT/Month 100

Chemistry:

Process: Methyl ethyl ketone reacts with Acetaldehyde in presence acid gives 3-methylpent-3-en-2-one (MPO) with water followed by neutralization with caustic solution to give MPO crude. Distillation of MPO crude gives MPO mains.

Material Balance:

No Input Qty per MT Qty Output Qty Per MT Qty 01 Methyl ethyl ketone 2815 MPO Crude 317602 Acetaldehyde 626 Sodium Sulphate solution 95703 Sulphuric acid 290 Total 413304 Caustic lye 402 Total 4133

Distillation:


Crude weight 3176

MEK recovered 1702MPO 1000Column Bottom mass 413Distillation Loss 61

Total 3176


06 .MANUFACTURING PROCESS FLOW DIAGRAM OF PRODUCTION OF MPO

OR MPO by Resin Process:

Methyl ethyl ketone reacts with Acetaldehyde mixture passed through resin gives gives 3-methylpent-3-en-2-one (MPO) crude. Distillation of MPO crude gives MPO mains.

Material Balance:

No Input Qty per MT Qty in Kg

Output Qty Per MT Qty in Kg

01 Methyl ethyl ketone 1891 MPO Crude 252102 Acetaldehyde 630 Resin for disposable 303 Resin 3 Total 2524 Total 2524

Note: Resin quantity in the column is deposable for every MT of Product.


Distillation:

MANUFACTURING PROCESS FLOW DIAGRAM OF PRODUCTION OF



Crude weight 2521

Water 174MEK recovered 964MPO 1000Column Bottom mass 333

Distillation Loss 50 Total 2521


DNEI

S. No Description Details 1 IUPAC NAME 2 CAS No ------ 3 MT/Month 1.25 MT 4 MT/Annum 15 MT

Chemical Reactions:

Stage 1A

Stage 1B

Stage 2


Material Balance

Stage 1A



01 Citronellal 1676 Aq Acetic acid (25-30%) 356902 Acetic anhydride 2220 Effluent 521903 Triethylamine 1099 CAL Diacetate Crude 612804 Sodium acetate 168 Total 1491605 Toluene 3352 06 soda ash 25 07 Water for quenching 1341 08 Water for washing 5027 09 Salt 8 Total 14916

Stage 1B


01 CAL Diacetate crude 6128 Phosphoric acid recovered 44902

Ortho Phosphoric acid 419Acetic acid solution (50-60%) 3519

03 Soda ash 25 DCC crude 474104 Sodium chloride 168 Effluent 758305 water for Hydrolysis 2011 Total 1629206 water for neutralization 7541 Total 16292

Distillation:

S.No

Input Qty per MT


1 DCC crude 4741

Recovered Toluene 3187 Column Tops 164 DCC Mains 1076 Column bottom mass 198 Distillation loss 116

Total 4741 Total 4741


Stage 2:


01 DCC mains 1076 Recovered MPK 210902 MPK 2676 Sodium acetate solution 136403 Sodium Methoxide 108 Effluent 217504 Acetic acid 110 DNEI Crude 154205 Sodium chloride 48 Total 719006 Water for quenching 1103

07 Water for neutralization 2069

Total 7190

Distillation:

Manufacturing Process:

Stage 1A: Citronellal reacts with acetic anhydride in presence of Triethyl amine and Toluene as solvent gives Citronellyl Diacetate crude

Stage1B: Citronellyl diacetate undergoes cyclisation in presence of Phosphoric acid followed by hydrolysis gives acetic acid and Dihydrocyclocitral crude which on distillation gives Dihydrocyclocitral product

Stage 2:

Dihydrocyclocitral product undergoes condensation with MPK in presence of base catalyst gives DNEI crude which subjected to distillation gives DNEI mains.



DNEI crude 1542

Column Tops 292DNEI Mains 1000Column Bottom mass 219Distillation loss 31Total 1542

Total 1542


Geranyl Acetate/Neryl Acetate/Linalyl Acetate

S. No Description Details 1 IUPAC NAME 3,7-Dimethyl-2,6-octadien-1-yl acetate,

3,7-Dimethyl-1,6-octadien-3-yl acetate 2 CAS No 105-87-3,141-12-8,115-95-7 3 MT/Month 200 MT/M 4 MT/Annum 2400 MT/M

Chemical Reaction:

Process:

Dry Hydrochloric acid generated by using 35 % Hydrochloric acid with Sulphuric acid. Myrcene reacts with Dry Hydrochloric acid gives Mixture of Geranyl Chloride(GCl),Neryl chloride (NCl) and Linalyl chloride (LCl) followed by esterification with Sodium Acetate gives Mixture of Geranyl acetate(GA),Neryl acetate(NA) & Linalyl acetate (LA) crude which subjected to distillation gives mixture of ester followed by separation gives Geranyl acetate,Neryl acetate and Linalyl acetate products.


Material Balance: Dry Hydrochloric acid:



01 Hydrochloric acid (30-35%) 1936 Dry Hydrochloric acid 228

02 Sulphuric acid 797 Dil Sulphuric acid (70 %) 2505 Total 2733 Total 2733

Hydrochlorination:



01 Myrcene 830 Effluent 86402 Cuprous chloride 3 Mixture of GCl+NCl+LCl 105203 PTC 13 Total 191604 Dry Hydrochloric acid 228 05 Sodium Carbonate 6 06 Water 237 07 Sodium Hydroxide 6 08 Water 593 Total 1916

Esterification:



01 Mixture of GCl+NCl+LCl 1052 Sodium Chloride solution 963

02 Sodium acetate 516 Effluent 214903 Water 593 Mixture of GA+NA+LA 118404 Water for neutralisation 2135 Total 4296 Total 4296


Distillation:

Separation of GA,NA & LA



Crude weight 1184

Column tops 74Mixture of GA+NA+LA 1000Column Bottom mass 89Distillation Loss 21

Total 1184



Mixture of GA+NA+LA

1000

Column tops 8GA 552NA 339LA 94

Column Bottom mass 4

Distillation Loss 3

Total 1000


Geranyl Alcohol/Neryl Alcohol/Linalyl Alcohol

Chemical Reaction:

O

O

C12H20O2

MW:196.29

Geranyl Acetate

O

O

O

O

C12H20O2

MW:196.29

Nerayl Acetate Linalyl acetate

NaOHOH

C10H18OMW:154.25

Geraniol

OH

OH

C10H18OMW:154.25

Nerol Linalool

Na+O

O-

Sodium Acetate

C2H3NaO2

MW:82.03C10H18O

MW:154.25

C12H20O2

MW:196.29

NaOHMW:40.00

Sodium Hydroxide

Process:

Dry Hydrochloric acid generated by using 35 % Hydrochloric acid with Sulphuric acid. Myrcene reacts with Dry Hydrochloric acid gives Mixture of Geranyl Chloride(GCl),Neryl chloride (NCl) and Linalyl chloride (LCl) followed by esterification with Sodium Acetate & Hydrolysis with Sodium hydroxide gives Mixture of Geranyl alcohol(GOL),Neryl alcohol(NOL) & Linalool (LOL) crude which subjected to distillation gives mixture of alcohols followed by separation gives Geranyl alcohol,Nerol and Linalool products.


Material Balance:

Dry Hydrochloric acid:



01 Hydrochloric acid (30-35%) 1167 Dry Hydrochloric acid 333

02 Sulphuric acid 2833 Dil Sulphuric acid (70 %) 3667 Total 4000 Total 4000

Hydrochlorination:



01 Myrcene 1215 Effluent 1090.502 Cuprous chloride 4.5 Mixture of GCl+NCl+LCl 1540.003 PTC 18 Total 2630.504 Dry Hydrochloric acid 333 05 Sodium Carbonate 9 06 Water 608 07 Sodium Hydroxide 9 08 Water 434 Total 2630.5

Esterification:



01 Mixture of GCl+NCl+LCl 1540 Sodium Chloride solution 1497

02 Sodium acetate 755 Effluent 149603 Water 955 Mixture of GA+NA+LA 173304 Water for neutralisation 1476 Total 4726 Total 4726


Distillation:

Hydrolysis:



01 Mixture of GA+NA+LA 1464 Sodium acetate solution 122502 Sodium Hydroxide 321 Effluent 1479 Water 608 Mixture of GOL+NOL+LOL 1165 Water for neutralization 1476 Total 3869 Total 3869

Distillation:

Separation of GOL+NOL+LOL


No Input Qty per MT Qty in Kg Output Qty Per MT Qty in Kg

Crude weight 1733

Column tops 108Mixture of GA+NA+LA 1464Column Bottom mass 130Distillation Loss 31

Total 1733


Crude weight 1165

Column tops 66Mixture of GOL+NOL+LOL 1000Column Bottom mass 76Distillation Loss 23

Total 1165


Mixture of GOL+NOL+LOL

1000

Column tops 12GOL 566NOL 306LOL 94

Column Bottom mass 14

Distillation Loss 8

Total 1000


Phenyl ethyl alcohol Capacity 20.0 MTPM

Sl.No Description 1 IUPAC NAME 2-Phenyl ethanol 2 CAS No 60-12-8 4 Proposed MT/Month 20 MT

Chemical Reaction:

Chemistry: Stage 1:

Stage2:

Stage 3:

Process:

Styrene undergoes Epoxidation with Chlorohydrin gives Styrene chlorohydrin crude , which subjected to react to Sodium Hydroxide solution gives Styrene Epoxide crude & Sodium chloride Aqueous solution, Styrene oxide undergoes hydrogenation by using Hydrogen pressure and presence of catalyst. The product mass is filtered by Nitrogen pressure to remove spent catalyst .The


filtrate, Phenyl ethyl alcohol (PEA) crude is distilled to obtain pure Phenyl ethyl alcohol which is packed and sold in the market.

Material Balance:

Stage 1 No Input Qty per MT Qty Output Qty Per MT Qty 01 Styrene 1330 Effluent 3671 02 Hydrogen peroxide 50%

1277 SCH Crude weight

1862 03 Water for process 1330 Total 5533 04 30% Hydrochloric acid 1596 Total 5533

Stage 2 No Input Qty per MT Qty Output Qty Per MT Qty 01 SCH Crude weight

1862 Aq.layer frm Rxn (18-20 % NaCl) 4272

02 NaOH 878 Crude weight 3429 03 EDC 1995 Total 7701 04 Water for reaction 2128 05 30% HCl for neutralization 838 Total 7701

Distillation:


Crude 3429

EDC recovered 1953 First Cut 68 Styrene epoxide Mains 1131

Final Cut 208

Distillation Loss 69



Stage 3:-

No Input Qty per MT Qty Output Qty Per MT Qty 01 Styrene epoxide 1131 Hydrogen loss 4 02 Catalyst 2 Catalyst recovered 2 03 Hydrogen 23 PEA Crude 1264 04 Methanol 113 Total 1270 05 Base 1 Total 1270

Solvent Recovery:

Hydrolysis:

No Input Qty per MT Qty Output Qty Per MT Qty 01 PEA Sol free 1155 Effluent 492 02 Water 452 PEA Crude 1138 03 Sodium Hydroxide 23 Total 1630 Total 1630

Distillation:


Crude 1264 Methanol recovered 109 PEA Sol Free 1155



PEA Crude 1138

Water 5 First Cut 61 PEA 1000

Final Cut 49

Distillation Loss 23 Total 1138 Total 1138


OR PHENYL ETHYL METHYL ETHER (PEME)

No Description 01 IUPAC NAME 2-methoxy ethyl benzene 02 CAS No 3558-60-9 03 MT/Month 20 MT 04 MT/Annum 240 MT

Chemistry:

Process: Stage1: Phenyl ethyl alcohol reacts with methanol in presence of catalyst gives PEME crude, The crude subjected to methanol recovery followed by Distillation gives Phenyl ethyl methyl ether (PEME).

Material Balance: Stage 1 No Input Qty per MT Qty Output Qty Per MT Qty 01 Phenyl ethyl alcohol 1068 Methanol recovered 2345 02 Methanol 2671 Effluent 2169 03 MSA 5 PEME crude 1329 04 Water 2099 Total 5843 Total 5843

Distillation:


PEME Crude 1329

First Cut 131 PEME product 1000 Final cut 170 Distillation loss 28



OR Alpha-Pinene epoxide – Capacity 20 MTPM

S. No Description Details 1 IUPAC NAME Pinene epoxide 2 CAS No 1686-14-2 3 MT/Month 20 MT 4 MT/Annum 240 MT

Chemical Reactions Stage 1

A-Pinene

C10H16Mol. Wt.: 136.23

H2O2

O

Hydrogen Peroxide A-Pinene Epoxide

C10H16OMol. Wt.: 152.23

Material Balance: Stage 1

S.No Input Qty per MT Qty Output Qty Per MT Qty 01

alpha pinene 1017

Effluent 1249 02

Hydrogen peroxide (50%) 679 A-Pinene epoxide

crude 1174 03 Catalyst ST 66 Total 2423 04 Phenyl phosphonic acid 16 05 PTC 81 06 Catalyst PBS 25 07 Sodium sulphate

anhydrous 25 08 Water quenching 102 09 water for washing 407 10 Salt 5 Total 2423


Distillation:



1 A-Pinene epoxide crude 1174

Recovered A-Pinene 58 A-Pinene epoxide Mains 1000 Column Bottom mass 98 Loss 18 Total 1174

Total 1174


OR

Alpha-Campholenic aldehyde – Capacity 20 MTPM

S. No Description Details 1 IUPAC NAME 1-(2,2,3-trimethyl-1-cyclopent-3-enyl)ethanone 2 CAS No 4501-58-0 , 42370-35-4 3 MT/Month 20 MT 4 MT/Annum 240 MT

Chemical Reactions Stage 1

O

A-Pinene Epoxide

C10H16OMol. Wt.: 152.23

Zinc Bromide CHO

C10H16OMol. Wt.: 152.23

A-Campholenic aldehyde

Stage 1

S.No Input Qty per MT Qty Output Qty Per MT Qty 1 A-Pinene

epoxide 1137 Zinc bromide solution (15-18%) 133

2 Toluene 2274 Effluent 209 3

Zinc bromide 23 A-Campholenic aldehyde crude 3410

4 Water 318 Total 3752 Total 3752


Distillation



1 A-Campholenic aldehyde crude 3410

Recovered Toluene 2205 Column Tops 84 A-Campholenic aldehyde 1000 Column Bottom mass 86 Loss 35 Total 3410

Total 3410


Developer: M/s.Raigad Petroleum Ltd.

S.No

EXHIBIT 4. WATER BALANCE DIAGRAM FOR PROPOSED PROJECT

TYPE OF USE WATER CONSUMPTION

KL/DAY

WASTE WATER

GENERATION

KL/DAY

E P T E P T

1 Domestic 5.0 35.0 40.0 3.0 25 28

2 Gardening 0 15.0 15.0 0.0 0.0 0.0

3 Industry

A Process 14.0 200.0 214.0 10.0 177.92 187.92

B Boiler /Cooling 20 243.8 263.8 2.0 15.86 17.86

Total Industrial 34 443.8 477.8 12 193.78 205.78

Total (1+2+3) 39 493.8 532.8 15 218.78 233.78


Developer: M/s.Raigad Petroleum Ltd.


Developer: M/s Raigad Petroleum Limited.

EXHIBIT 4. FLOW DIAGRAM 0f ETP


Developer: M/s. Raigad Petroleum Limited.

S. No.

EXHIBIT 5. HAZARDOUS WASTE GENERATION & MANAGEMENT

Particulars Category No. Existing Proposed Total Qty Disposal

1

Chemical

Sludge from

Waste Water

Treatment

34.3 90 KG

/M 11.91 MT/M 12.0 MT/M CHWTSDF

2 Distillation

Residue 20.3 50 MT/M 3.12 MT/M 53.12 MT/M

Sale to PCB

registered Party

3 Discarded

Containers 33.3

15

Nos/M

Carbouys/Dr

ums/IBCs200

Nos/M

Carbouys/

Drums/IBCs

215 Nos/M

Sale to PCB

registered Party

4 Lead Acid

Batteries

Batteries

Rules, 2002 Nil 08 Nos /A 08 Nos /A

Sale to

Authorised Party

5

Waste or residue

containing oil

(Oil soaked

gaskets and

cotton waste)

5.2 Nil 100 kg/M 100kg/M CHWTSDF

6 e-Waste E- waste

Rules, 2011 Nil 30 kg/M 30 kg/M

Sale to

Authorised Party

7 Resin

- 0.92 MT/M 0.92 MT/M CHWTSDF

8 Spent

oil/Waste oil 5.1 - 450 Kg/M 450 Kg/M

Sale to

Authorised party



Sr.N

EXHIBIT 6. DETAIL OF STACK & FUELS

Details

Capacity Stack Ht. Fuel/Fuel

consumption Stack Dia(mm)

Stack gas

temp(˚C)

Existin

g

Prop

osed

Existin

g

Propos

ed

Existin

g

Propose

d

Existin

g

Propose

d

Existin

g

Propo

sed

1. Boiler

1.6 TPH

(F.O.

based)

--- 16 m ---

F.O.

based,

1000

Lit/day

F.O.

based,

1000

Lit/day

or Biofuel

1000

Lit/day

300

mm --- 140 ---

2. Boiler

2 TPH

(Coal

based)

10

TPH

(Coa

l

base

d)

21 m 32 m

Coal

based

5.8 TPD

Coal

based

30 TPD

300

bottom/t

op ID in

mm)

1500/900

140 160

3. Therm

opack ---

6 lac

KCal --- 30 m ---

3.624

TPD --- 550 --

4. DG set 250

KVA

750

KVA 5 m 11 m

100

lit/hr 250 lit/hr 150 200 200 200



EXHIBIT 7. CONSENT TO OPERATE

exhibit 1. location map of project...

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