ANNEXURE I PROPOSED TERMS OF...

M/s. Aarti Industries Limited (Organic Division), Vapi.

M/s.Jyoti Om Chemical Research Centre Pvt. Ltd., Ankleshwar. 11

ANNEXURE I

PROPOSED TERMS OF REFERENCE

As per standard ToR of organic manufacturing sector issued by MoEF&CC.

2 4 .0 M

W

I D

E

G

. I. D

. C

. R

O

A

D

2 0 .0 M W I D E G. I. D. C. R O A D

GEB-SUB

STATION

805

1

805

2

805

3

805

4

16,59

6.0

M

R

O

A

D

20

5

6.0

M

R

O

A

D

W A R E

H O U S E

(31.0 X 21.0)

6.0

M

R

O

A

D

CL2

STORAGE

YARD

(14.0X30.0)

2

4

.0

M

W

I D

E

G

. I. D

. C

. R

O

A

D

6 .0 M R O A D

R & D LAB. &

ENGG. STORE

(18.0X10.0)

OHC

ROOM

C

Y

C

L

E

S

T

A

N

D

(6

.0

X

4

3

.0

)

WATCH

MANCABIN

(3.6X6.0)

G

A

T

E

-I

CL2

STORAGE

YARD

(14.0X30.0)

OFFCIE &

CATEEN

(18.0X10.0)

WEIGH

BRIDGE

G A R D E N

G

A

T

E

-II

STORAGE

YARD

Q.A. LAB & INST.

(30.0X10.0)

ROOM

TANK

(6.0X10.0)

H T

YARD

(8.0X

13.0)

OCB

ROOM

(3.6X3.6)

(18.0X 11.5)

(18.0X 10.0)

3.4 D C N B

C O L U M N

( 14 X 20 )

(31.0 X 7.0)

6 .0 M R O A D

10.0

M

R

O

A

D

U T I L I T Y

B L D G .

(24.0X 28.0)

MCC

ROOM

(6.0X6.0)

ROOM

(6.0X6.0)

A C I D

S T O R A G E

Y A R D

(24.0 X 15.0)

MCB

PLANT(NEW)

(12.0X10.0)

STORAGE

(12.0X7.0)

H C L

STORAGE

(12.0X7.0)

U/G.

WATER

TANK

(12.5X12.5)

COOLING

TOWER

(5.0X12.5)

EFFLUMENT

TRATEMENT

PLANT

(20.0 X 44.7)

CR

PLANT

(8.0X23.50)

COOLING

TOWER

(5.0X12.5)

COOLING

TOWER

(5.0X12.5)

6.0

M

R

O

A

D

2,5DCNB

PLANT

(10.0X 24.0)

BN PLANT

(18.0X9.0)

CRYST.

(12.2X 16.0)

MCC

ROOM

CRYST.

COOLING

TOWER

(5.0X12.5)

CT

(18.0X 21.5)

6 .0 M R O A D

TANK-FARM

(12.25X28.0)

SOLID

WASTE

SUMP

(12.25X11.0)

FIRE

PUMP

(7.0X7.0)

F I R E

WATER

T A N K

(25.0X20.0)

CHILLING

PLANT

CT

SOLID

WASTE SHED

S

T.

T

A

N

K

SAFETY

CONCER

1

4

5

,6

17

9,4

RCC SLAB 2FL

MCB

PLANT

(EXP.)

(12.0X10.0)

ROOM

D C B PLANT

( 18.0 X 4.50 )

GRL

PLANT

ROOM

ROOM

STORAGE

YARD

(25.0X20.5)

TK-703

CAP.-100TON

TK-100A

CAP.-250TON

TK-738

CAP.-110TON

TK-708

CAP.-140TON

TK-529D

CAP.-130TON

TK-718

CAP.-95TON

TK-701

CAP.-160TON

TK-425

CAP.-830TON

TK-701

CAP.-160TON

TK-424

CAP.-140TON

TK-03

CAP.-60TON

TK-02

CAP.-120TON

CRYST.

(4.0X 16.0)

LIME

STORAGE

801,801/23

(ORGANIC DIVISION)

16

,6

14

0

GA

TE

GA

TE

4.00

6.50

MECHANICAL

STORE

10.77 X 11.77 Mtr.

ELECRICAL

STORE

OFFICE

3.77 X 3.85

INSTRUMENT

STORE

10.77 X 11.77

1.2

5 M

tr. W

ID

E P

AS

SA

GE

28

.3

5

11.35

4.00

18.00

28

.0

0

FABRICATION:-1

9.00 X 6.00 MTR

FABRICATION:-3

9.00 X 6.00 MTR

FABRICATION:-5

9.00 X 6.00 MTR

FABRICATION:-2

9.00 X 6.00 MTR

FABRICATION:-4

9.00 X 6.00 MTR

FABRICATION:-6

9.00 X 6.00 MTR

ELECTRICAL:-8

9.00 X 6.00 MTR

ELECTRICAL:-7

9.00 X 6.00 MTR

1.20 Mtr. plinth extention

PAINTING LOADING

PANNEL ROOM

UNLOADINGCONTRCTOR:-1

PAINTING

CONTRCTOR:-2

PAINTING

CONTRCTOR:-3

PAINTING

CONTRCTOR:-4

3.77X2.86 MTR

3.77X2.86 MTR

3.77X2.86 MTR 3.77X2.86 MTR 3.77X2.86 MTR

3.77X2.86 MTR

2.85

1,5

GA

TE

-II

5.00 Mtr. Wide Road

6.00 Mtr. Wide Road

8.0

0 M

tr. W

id

e R

oa

d

8.0

0 M

tr. W

id

e R

oa

d

2.0

0 M

tr. W

ID

E P

UM

PS

A

RE

A

FABRICATION

9.00 X 6.00 MTR

FABRICATION

9.00 X 6.00 MTR

8.0

0 M

tr. W

id

e R

oa

d

33,35

GA

TE

2,8

8

4,23

SPACE (FUTURE EXPANSION

(61.00X33.00Mtr)

EXPANSION TANKER PARKING AREA

(61.96X36.75Mtr)

UU

U

T

B

B

B

TOLET BLOCK

59

,9

6

2.0

0 M

tr. W

ID

E P

IP

ER

AC

K

2.0

0 M

tr. W

ID

E P

IP

ER

AC

K

2.90

2.90

3.20

2.40

2.40

5.45

2.90

2.50

2.40

2.40

1.80

1.80

1.80

3.60

2.30

3.00

2.50

2.50

19,49

HT.-1.50

FOUND.

(TYPE)

6.75Øx8ht

4.5Øx8ht

6.75Øx8ht

5.7Øx8ht

6.75Øx8ht

5.7Øx8ht

5.7Øx8ht

4.5Øx8ht

4.5Øx8ht

4.5Øx8ht

5.7Øx8ht

5.7Øx8ht

5.7Øx8ht

ONCB

DNCB

SPARE

MCB

MCB

MNCB

PPS BOTTOM

ONCB

4.5Øx8ht

PDCB

1.80

1.80

PNCB

PNCB

PNCB

DNCB

CABIN

TITLE -

DRN BY -CHKD. BY - APPRD. BY -

DRG.NO. -

REV. NO. -

M/S. AARTI INDUSTRIES LTD.PLOT NO.-801,801 / 23.,806,807G.I.D.C. THIRD PHASE VAPI.

SITE PLAN

SCALE -

WORK -SHOP

18.00 X 28.00

STORAGE TANKFARM

19.49 X 59.96

DESCRIPTIONSR.NO. L X D SQ.MUINTNO.

SECURITY GATE1 3.00 X 6.00 21.6012 6.00 X 43.00 258.002

STORAGE TANK -MCB3 19.00 X 17.00 331.503H.T YARD4 11.00 X 13.00 143.004

CYCLE STAND

(ORGANIC DIVISION)-801,801 / 23.

OCB ROOM5A 3.60 X 7.20 25.925B 3.60 X 5.00 18.00

UPS ROOM5C 3.60 X 5.00 18.00OFFICE BLDG.6 40.00 X 10.00 400.00

MOTOR ROOM

STORAGE TANK & LAB. BLDG. 35.00 X 10.00 350.008 6.00 X 10.00 60.008

WEGIH BRIDGE9 3.50 X 20.00 70.009CL2 STORAGE YARD10 30.00 X 14.00 420.0010A

TANK AREA

10B11 24.00 X 15.00 360.0011

NCB-CN SECTION12 14.00 X 16.00 224.0012A5.00 X 14.00 70.0012B

ACID STORAGE YARD

13

18.60 X 22.35 415.714.50 X 18.00 81.00

UTILITY BLDG.15 24.00 X 28.00 672.0027.60 X 5.00 138.00

SULZER CRYSTILIZER16 18.00 X 15.50 279.0016TANKFARM AREA17 28.00 X 14.15 362.2017EXIST. MCB AREA18 12.00 X 32.50 390.0018A

16.00 X 32.50 520.0018B4.50 X 49.50 222.7518C

5

67 7

CL2 STORAGE YARD 30.00 X 14.00 420.00

OUTSIDE AREANCB-CR SECTION13A

13B OUTSIDE AREA18.00 X 16.00 288.00

5.00 X 18.00 90.0014 14A

14BNCB-COLUMN SECTIONOUTSIDE AREA

15A15B OUTSIDE AREA

OUTSIDE AREAOUTSIDE AREANEW MCB PLANT19 15.00 X 10.00 150.0019A

12.00 X 10.00 120.0019B EXTENSION MCB PLANTSTORAGE TANK20 28.00 X 7.00 196.0020U/G. WATER TANK21 12.50 X 12.50 156.2521ACOOLING TOWER AREA 12.50 X 10.60 132.5021BCOOLING TOWER AREA 27.60 X 11.00 303.6021CCRYSTILIZER SECTION-BN22 21.60 X 23.90 516.2422ACRYSTILIZER SECTION 21.95 X 23.90 524.6122B

TANKFARM AREA 5.00 X 47.60 238.0022D2,5 DNCB PLANT 10.80 X 23.90 258.1222C

E T PLANT23 23.94 X 44.70 1070.1223AOUTSIDE AREA 28.00 X 24.44 684.3223BCRYSTILIZER SECTION-DNCB24 8.00 X 28.00 224.0024DNCB OLD BLDG.25 13.50 X 13.50 182.2525A

DCB & BN PLANT25B

OUTSIDE AREA 31.50 X 10.94 344.6125C 18.00 X 21.50 387.00

DNCB COLUMN SECTION26 3.00 X 13.50 40.5026A26B 7.50 X 8.94 67.05DNCB COLUMN SECTION

STORAGE TANK -NCB27 25.00 X 20.50 512.5027A27B 15.50 X 24.94 386.57OUTSIDE AREA

OUTSIDE AREA 10.00 X 36.00 360.0027C27D 27.42 X 6.38 174.94OUTSIDE AREA

WARE HOUSE BLDG.28 31.00 X 21.00 651.0028A28B 31.00 X 7.00 217.00OUTSIDE AREA

FIRE WATER TANK29 25.00 X 20.00 500.0029A29B 7.00 X 7.00 49.00FIRE PUMPSHOUSE

WOM COOLING TOWER AREA30 7.00 X 9.90 69.3030

25D

DNCB OLD BLDG. 18.00 X 8.00 144.00

SECURITY GATE AND OHC1 4.00 X 7.50 30.0012 3.00 X 33.00 99.002

STORAGE TANKFARM3 19.49 X 59.96 1168.6234 18.00 X 28.00 504.004

CYCLE STAND

WORK SHOP11.35 X 34.68 393.62

70.0070.00

6.30 X 26.30 165.69

STORE AND BLDG.

39.80 X 36.75 1462.65827.92 X 22.15

2013.00

8

5

7 7

WEGIH BRIDGEWEGIH BRIDGE

20.00 X 3.5020.00 X 3.50

DRIVER BLDG.TANKER PAKING AREA

5

6 6A6B

9 9 SPARE FOR FUTURE EXPANSION

6.3

3

11.35 X 34.68

GREEN BELTOPEN AREA

TOTAL BULT UP AREA9605.22

13604.57

25913.65

OHC

CYCLE

STAND

PLOT AREA 806,807 - 17948.00SQ.M

AREA STATEMENT--

PLOT AREA ORGANIC DIVISION - 27529.00SQ.M

MISTRY

COOLING TOWER

(9.0X15.0)

ROOM

(6.0X6.0)

H C L

STORAGE

(12.0X5.0)

MCC

ROOM

(6.0X6.0)

MASS

COOLER-4

MASS

COOLER-3

MASS

COOLER-2

MASS

COOLER-1

PROPOSED

CHLORI-

NATION

(EXISTING)

CHLORI-

NATION

4,5

8

5

MASS

COOLER-2

MASS

COOLER-1

MASS

COOLER-3

VAPORIZER

CL2

SCRUBBER

NCB-CR

SECTION

(18.0X16.0)

NCB-CN

SECTION

(14.0X16.0)

NCB-COL.

SECTION

(20.0X16.0)

C R

(6.0X6.0)

SULZER

C R

(18.0X11.0)

TANK AREA

COOLING

TOWER

(5.0X5.0)

3200Ø COL.

REMOVEL PLANT

(6.10X

6.1)

6,1

6,112,4

P I P E R A C K (4.60M WIDTH)

1100Ø

COLUMN

(3.50X3.50)

COOLING

TOWER

(5.0X5.0)

PLOT

NO.-806,807

EXIST.GREEN BLET

ELECT.

BLDG.

(10.0X4.50)

H Y YARD

(7.0X5.0)

WATCH

MANCABIN

PROPOSED

WEIGH BRIDGE

PROPOSED

WEIGH BRIDGE

DISPATCH

OFFICE

7.56

12.00

3.50

3.50

12.00

3.00

3.00

2.50

38

,5

7

6,35

6.50 Mtr. Wide Road

TRUCK DRIVER

AMINTY BLDG.

6.30X22.30Mtr16.00

6.30

6.00

175,84

128,2

61,96

39.8092

20

123,55

EXIST.GREEN BLET

EX

IS

T.G

RE

EN

B

LE

T

PR

OP

OS

ED

G

RE

EN

B

LE

T

PROPOSED GREEN BLET

7

49,72

20

PR

OP

OS

ED

G

RE

EN

B

LE

T

4.0

43.50

5.50

PR

OP

OS

ED

G

RE

EN

B

LE

T

EX

IS

T.G

RE

EN

B

LE

T

167.0

36.7397

618.4361.00 X 33.00

PLOT NO.-806,807

TOTAL PLOT AREA - 45477.00SQ.M

6,94



ANNEXURE III

LIST OF DIRECTORS WITH ADDRESS

SR. NO.

NAME OF DIRECTOR

DESIGNATION ADDRESS TELEPHONE NO.

1.

Shri. Rajendra V Gogri

Chairman & Managing Director

1401, Antriksh, Murar Road, Mulund (West), Mumbai -400080

022-67976666

2.

Shri. Rashesh C Gogri

ViceChairman Managing Director

601, Antriksh, Murar Road, Mulund (West), Mumbai -400080

022-67976666

3. Shri. Parimal H Desai

Whole -time Director A-1403, 14th floor, Runwal heights, LBS marg, Mulund (West), Mumbai-400080

022-67976666

4. Shri. Manoj M Chheda

Whole -time Director Dunhill Villa Co. Op. Hsg-Soc.Ltd, esant Road, Santracruz (West), Mumbai -400054

022-67976666

5. Shri. Kirit R Mehta Whole -time Director 10, Pushpendra Mansion, Phirojshah Mehta Road, Santracruz (West), Mumbai-400054

0260-2400366

6. Smt. Hetal Gogri Gala

Whole -time Director 558-B, Gopal Sadan, Block No.801, 8th floor, Jamshed Road, Matunga (East)Mumbai 400019

022-67976666

7. Shri. Renil R Gogri Whole -time Director 1401, Antriksh, Murar Road, Mulund (West), Mumbai -400080

022-67976666



ANNEXURE IV

LIST OF PRODUCTS AND THEIR PRODUCTION CAPACITY

Sr. No.

Name of Product Existing quantity in MT/Month as per CCA AWH-50294

Proposed quantity in MT/Month

Total quantity after expansion in MT/Month

1 Para Nitro Chloro Benzene(PNCB) 5000

3900 9000 (Either/Or)

2 Ortho Nitro Chloro Benzene(ONCB)

3 Meta Nitro Chloro Benzene(MNCB) 100

4 2,5 Dichloro Nitro Benzene(2,5 DCNB) 400 0

1500 (Either/Or)

5 3,4 Di Chloro Nitro Benzene(3,4 DCNB) 600

6 2,3 DiChloro Nitro Benzene (2,3 DCNB) 100

7 2,4 DiChloro Nitro Benzene(2,4DCNB) 400

8 2,6 Di Chloro Nitro Benzene (2,6DCNB) 0

9 2,3,4 TrichloroNitro Benzene (2,3,4 TCNB) 0

10 2,4,5 TrichloroNitro Benzene (2,4,5 TCNB) 0

11 2,4 Dichloro 3 Fluoro Nitro Benzene 0

12 2,4 DiNitro Chloro Benzene 200 1300 1500

(Either/Or)

13 Mono Chloro Benzene(MCB) 3800

3000

8000* (Either/Or)

14 Ortho Dichloro Benzene(ODCB) 500

15 Para Dichloro Benzene(PDCB) 500 16 Meta Dichloro Benzene(MDCB) 0 17 1,2,4 Tri Chloro Benzene(1,2,4 TCB)

200 18 1,2,3 Tri ChloroBenzene(1,2,3 TCB) 19 TCAN 0

20 Ortho Anisidine 30 0 30

21 Para AniSidine 20 0 20

22 Dichloro Aniline 50 0 50

23 2,5 DiChloro Aniline 35 0 35

24 3,4 DiChloro Aniline 15 0 15

25 Ortho Chloro Aniline 10 0 10

26 PPDA 25 0 25

27 OPDA 225 0 225

28 OCPNA/PCONA 100 0 100 29 ONA/PNA 150 0 150



33 ONCB Para Sulphonic Acid 25 0 25

34 3,3 DiChloro Benzedine Sulphate 10 0 10 35 Dilute Sulphuric Acid 1441 0 1441

Total 13936 8200 22136

By-Product

1. Sulphuric Acid 70% 3627 3027 6654

2. Hydrochloric Acid 30% 6165 7038 13203

3. Thio liquor 136.5 0 136.5

Total 9928.5 10065 19993.5 *NOTE: As such either/or any product will be 8000 MT/MONTH, but 1, 2, 4 TCB, 1, 2, 3 TCB, TCAN not more than 3000MT/Month)

LIST OF RAW MATERIALS

(Existing quantity as per CCA Order No. AWH-50294)

Sr. No.

Name of Products

Name of Raw materials CAS No. Raw Material Consumption in MT/Month

1. PNCB/ONCB Chloro Benzene 108-90-7 3614.58 Nitric Acid 7697-37-5 2416.43 Sulphuric Acid 7664-93-9 1913.01 Spent Acid 7664-93-9 5436.97 Total 13380.99

2. MNCB Chloro Benzene 108-90-7 72.29 Nitric Acid 7697-37-5 48.33 Sulphuric Acid 7664-93-9 38.26 Spent acid 7664-93-9 108.74 Total 267.62

3.

2:5 DCNB

2,5 Dichloro Benzene 89-61-2 353.08 Conc. Nitric Acid 7697-37-5 156.15 Sulphuric Acid 7664-93-9 130.77 Spent acid 7664-93-9 571.97 Total 1211.97

4.

3:4 DCNB

2,5 Dichloro Benzene 89-61-2 529.62 Conc. Nitric Acid 7697-37-5 234.23 Sulphuric Acid 7664-93-9 196.15 Spent acid 7664-93-9 857.96



Sr. No.

Name of Products


Total 1817.96 5.

2:3 DCNB


6.

2:4 DCNB


7.

2,4 Dinitro Chloro Benzene

PNCB 100-00-5 155.60 98% Conc. Nitric Acid 7697-37-5 68.00 98% Conc. Sulphuric Acid 7664-93-9 59.20

Recovered spent acid 7664-93-9 44.56 Total 327.36

8.

Mono Chloro Benzene

Fresh benzene 71-43-2 2634.87 Recovered benzene 71-43-2 3222.21 Chlorine 782-50-5 2397.20 Total 8254.28

9.

Ortho Dichloro Benzene


10.

Para Dichloro Benzene


11.

1,2,4/1,2,3 Trichloro Benzene

ODCB 95-50-1 86.56 Recovered Ortho Di-Chloro Benzene

95-50-1 302.91

Chlorine 782-50-5 236.31 Total 625.79

12.

Ortho Anisidine

Ortho Anisole 91-23-6 37.32 Hydrogen 1333-74-0 1.53



Sr. No.

Name of Products


Rec. 30% OA Crude 91-23-6 9.00 Total 47.85

13.

Para Anisidine

Para Anisole 91-23-6 24.88 Hydrogen 1333-74-0 1.02 Rec. 30% OA Crude 91-23-6 6.00 Total 31.90

14.

Dichloro Aniline

Mixture of 2,5DCNB & 2,6 DCNB

89-61-2 59.63

Hydrogen 1333-74-0 1.94 Fresh Solvent 0.43 Recovered solvent 37.90 Total 99.90

15.

2,5 Di Chloro Aniline


89-61-2 41.74

Hydrogen 1333-74-0 1.36 Fresh Solvent -- 0.30 Recovered solvent -- 26.53 Total 69.93

16.



89-61-2 17.89

Hydrogen 1333-74-0 0.58 Fresh Solvent 0.13 Recovered solvent -- 11.37 Total -- 29.97

17.

Ortho Chloro Aniline

OCNB 100-00-5 12.37 Hydrogen 1333-74-0 0.47 Fresh Solvent -- 0.31 Recovered solvent -- 7.32 Total 20.47

18.

PPDA

ONA 65996-98-7

31.90

Caustic 1310-73-2 18.50 Sulphur 7704-34-9 14.80 Total 65.20

19. OPDA ONA 65996-98- 287.10



Sr. No.

Name of Products


7 Caustic 1310-73-2 166.50 Sulphur 7704-34-9 133.20 Total 586.80

20.

OCPNA/PCONA

3:4DCNB/2:5DCNB 611-06-3 115.20 Anhydrous Ammonia 7664-41-7 12.70 Ammonia Solution (32%) 7664-41-7 252.30

Total 380.20

21.

ONA/PNA

ONCB/ PNCB 88-73-3 172.80 Anhydrous Ammonia 7664-41-7 19.05 Ammonia Solution (32%) 7664-41-7 378.45 Total 570.30

22.

ONCB Para Sulfonic Acid

MCBPSA 23.80 H2SO4 7664-93-9 23.80 HNO3 7697-37-5 10.20 KCl Mix 7447-40-7 7.63 NaCl 7647-14-5 17.73 Total 83.14

23.

3:3 Dichloro Benzdine Sulphate

ONCB 88-73-3 18.52

Dichlone 117-80-6 0.11

Emulsifier 107-98-2 0.04

Caustic Lye 48% 1310-73-2 2.82

Hydrogen 1333-74-0 0.60

Fresh Toluene 108-88-3 0.65

Recovered Toluene 108-88-3 20.89

HCl 3% Mixture 57.62 Spent Acid 62% 7664-93-9 36.63 Thiourea -- 0.10

Total - 137.98 Total 31977.76



Raw Material Consumption of proposed Product:

Sr. No.

Name of Product


1. PNCB/ONCB Chloro Benzene 108-90-7 4630.41 Nitric Acid 7697-37-5 2618.31 Sulphuric Acid 7664-93-9 2076.59 Spent acid 7664-93-9 3869.43 Total 13194.75

2. MNCB Chloro Benzene 108-90-7 50.02 Nitric Acid 7697-37-5 28.28 Sulphuric Acid 7664-93-9 22.43 Spent acid 7664-93-9 41.80 Total 142.54

3.

2:5 DCNB

2,5 Di chloro Benzene 89-61-2 88.27 Conc. Nitric Acid 7697-37-5 39.04 Sulphuric Acid 7664-93-9 32.69 Spent acid 7664-93-9 142.99 Total 302.99

4.

3:4 DCNB


5.

2:3 DCNB


6.

2:4 DCNB


7.

2,4 Di nitro Chloro Benzene

PNCB 100-00-5 700.20 98% Conc. Nitric Acid 7697-37-5 306.00 98% Conc. Sulphuric Acid

7664-93-9 266.40



Sr. No.

Name of Product



8.

2,6 Di nitro Chloro Benzene

PNCB 100-00-5 15.56 98% Conc. Nitric Acid 7697-37-5 6.80 98% Conc. Sulphuric Acid

7664-93-9 5.92


9.

2,3,4 Tri chloro Nitro Benzene (2,3,4 TCNB)

1,2,4/1,2,3 TCB 87-61-6 201.86 Nitric Acid 7697-37-5 70.11 Sulphuric Acid 7664-93-9 81.21 Spent Acid 7664-93-9 38.82 Soda Ash 1.94 Total 393.94

10.

2,4,5 Tri chloroNitro Benzene (2,4,5 TCNB)

1,2,4/1,2,3 TCB 87-61-6 20.19 Nitric Acid 7697-37-5 7.01 Sulphuric Acid 7664-93-9 8.12 Spent Acid 7664-93-9 3.88 Soda Ash 497-19-8 0.19 Total 39.39

11.

Crude TCNB

1,2,4/1,2,3 TCB 87-61-6 141.30 Nitric Acid 7697-37-5 49.08 Sulphuric Acid 7664-93-9 56.85 Spent Acid 7664-93-9 27.17 Soda Ash 497-19-8 1.36 Total 275.76

12.

2,4 Di chloro 3 fluoro Benzene

1,2,4/1,2,3 TCB 87-61-6 79.73

Nitric Acid 7697-37-5 32.01 Sulphuric Acid 7664-93-9 38.41 Soda Ash 497-19-8 0.33 Total 150.49

13.

Crude DCNB

2,5 Di chloro Benzene 89-61-2 132.40 Conc. Nitric Acid 7697-37-5 58.56 Sulphuric Acid 7664-93-9 49.04



Sr. No.

Name of Product


Spent acid 7664-93-9 214.49 Total 454.49

14.

Mono Chloro Benzene


15.

Ortho Di chloro Benzene


16.

Para Di chloro Benzene


17.

1,2,4/1,2,3 Tri chloro Benzene

ODCB 95-50-1 302.97 Recovered Ortho Di-Chloro Benzene

95-50-1 1060.19

Chlorine 782-50-5 827.09 Total 2190.25

18.

TCAN

Aniline 62-53-3 47.54 MCB 108-90-7 0.23 Rec. MCB 108-90-7 138.46 HCl gas 7647-01-0 18.62 Chlorine 7782-50-5 108.77 NaOH 1310-73-2 6.38 Total 320.00

19.

Ortho Anisidine

Ortho Anisole 91-23-6 37.32 Hydrogen 1333-74-0 1.53 Rec. 30% OA Crude 91-23-6 9.00 Total 47.85

20.

Para Anisidine

Para Anisole 91-23-6 24.88 Hydrogen 1333-74-0 1.02 Rec. 30% OA Crude 91-23-6 6.00 Total 31.90



Sr. No.

Name of Product


21.

Di chloro Aniline


89-61-2 59.63

Hydrogen 1333-74-0 1.94 Fresh Solvent -- 0.43 Recovered solvent -- 37.90 Total 99.90

22.



89-61-2 41.74

Hydrogen 1333-74-0 1.36

Fresh Solvent -- 0.30 Recovered solvent -- 26.53 Total 69.93

23.



89-61-2 17.89

Hydrogen 1333-74-0 0.58 Fresh Solvent 0.13 Recovered solvent -- 11.37 Total -- 29.97

24.

Ortho Chloro Aniline

OCNB 100-00-5 12.37 Hydrogen 1333-74-0 0.47 Fresh Solvent -- 0.31 Recovered solvent -- 7.32 Total 20.47

25.

PPDA

ONA 65996-98-7 31.90 Caustic 1310-73-2 18.50 Sulphur 7704-34-9 14.80 Total 65.20

26. OPDA

ONA 65996-98-7 287.10 Caustic 1310-73-2 166.50 Sulphur 7704-34-9 133.20 Total 586.80

27.

OCPNA/PCONA

3:4DCNB/2:5DCNB 611-06-3 115.20 Anhydrous Ammonia 7664-41-7 12.70 Ammonia Solution (32%)

7664-41-7 252.30



Sr. No.

Name of Product


Total 380.20

27.

ONA/PNA

ONCB/ PNCB 88-73-3 172.80 Anhydrous Ammonia 7664-41-7 19.05 Ammonia Solution (32%)

7664-41-7 378.45

Total 570.30

28.

ONCB Para Sulfonic Acid

MCBPSA 23.80 H2SO4 7664-93-9 23.80 HNO3 7697-37-5 10.20 KCl Mix 7447-40-7 7.63 NaCl 7647-14-5 17.73 Total 83.14

29.

3:3 Di chloro Benzdine Sulphate

ONCB 88-73-3 18.52 Di chlone 117-80-6 0.11 Emulsifier 107-98-2 0.04 Caustic Lye 48% 1310-73-2 2.82 Hydrogen 1333-74-0 0.60 Fresh Toluene 108-88-3 0.65 Recovered Toluene 108-88-3 20.89 HCl 3% Mixture 57.62 Spent Acid 62% 7664-93-9 36.63 Thiourea -- 0.10 Total -- 137.98 Total -- 27642.95



ANNEXURE V

BRIEF PROCESS DESCRIPTION

1. PARA NITRO CHLORO BENZENE (PNCB)/ORTHO NITRO CHLORO BENZENE (ONCB)/ META NITRO CHLORO BENZENE(MNCB):

Manufacturing Process:

Mixed acid containing concentrated nitric acid and concentrated sulphuric acid is reacted with Chloro benzene to produce Para nitro Chloro benzene. The reaction gets completed in series of Nitrator with cooling coils and jackets. Reaction is followed by spent acid separation, washing by water, drying to get Para nitro Chloro benzene

Chemical reaction:

PNCB

ONCB



MNCB

Material balance:

Input Kg Kg Output

Chloro Benzene (Fresh) 1795

Nitric Acid 1200Sulphuric Acid 950 6645 Reaction Mass

Spent Acid 2700Total 6645 6645 Total

2645 Reaction MassReaction Mass 6645 2700 Spent Acid

1300 Spent AcidTotal 6645 6645 Total

Reaction Mass 2645Washing Water 100 2745 Reaction Mass

Total 2745 2745 Total

190 EffluentReaction Mass 2745 2555 Reaction Mass


10 Water LossReaction Mass 2555 2545 Reaction Mass


2503 MNCBReaction Mass 2545 42 Residue


Drying

Distillation

Reaction

Separator

Washing-1

Separator



2. 2, 5 /3, 4 / 2, 3/2, 4/2,6 DICHLORO NITRO BENZENE & CRUDE DCNB


Mixed acid containing concentrated nitric acid and concentrated sulphuric acid is reacted with 2, 5 Di Chloro benzene to produce 2,5 Di Chloro nitro benzene . The reaction gets completed in series of Nitrators with cooling coils and jackets. Reaction is followed by spent acid separation, washing by water, drying to get a 2,5 Di Chloro nitro benzene.

3, 4 Di Chloro benzene is used to produce 3, 4 Di Chloro Nitro benzene.



Chemical reaction:

2, 5 DCNB

3, 4 DCNB

H2O

Water

+

3,4- DichloroNitro Benzene

Cl

NO2

+ HNO3 + H2SO4

Nitric Acid

Sulphuric Acid

Cl

3,4 - Dichloro Benzene

Cl

Cl



2, 3 DCNB

2, 4 DCNB



Material Balance:

3. 2, 4DI NITRO CHLORO BENZENE:


Mixed acid containing concentrated nitric acid and concentrated sulphuric acid is reacted with Para Nitro Chloro Benzene to produce 2, 4 Di Nitro Chloro Benzene. The reaction gets completed in series of Nitrators with cooling coils and jackets. Reaction is followed by spent acid separation, washing by water, drying to get a 2, 4 Di Nitro Chloro Benzene.

Input Kg Kg Output

2,5 Dichloro Benzene 918

Conc. Nitic Acid 406Sulphuric Acid 340 3164 Reaction Mass

Spent Acid 1500Total 3164 3164 Total

1115 Crude DCNB

Reaction Mass 3164

1500 Spent Acid (Recycle in next batch)

549 Spent AcidTotal 3164 3164 Total

Crude DCNB 1115Water 110 1225 Reaction MassTotal 1225 1225 Total

175 Water to ETPReaction Mass 1225 1050 DCNB


210 Reaction Mass DCNB 1050 840 2,5 DCNB


Reaction Mass 210 200 2,5 DCNB10 Residue

Total 210 210 Total

Distillation

Nitration

Seperation

Washing

Seperation

Crystalizer



Chemical reaction:

Material Balance:

Cl

NO2

+ HNO3 H2SO4

NO2

ClNO2

+ 2H2O+

P-Nitro Chloro Benzene

Nitric Acid Sulphuric Acid Dinitro Chloro Benzene

Water

INPUT KG KG OUTPUT

Para Nitro Chloro Benzene 194598% Conc. Nitric Acid 850 4092 Reaction Mass

98% Conc. Sulphuric Acid 740Recovered Spent acid 557


1285 Mixed Acid

Reaction Mass 4092557 Spent acid resued in

next batchWater 250 2500 DNCB CrudeTotal 4342 4342 Total

DNCB Crude 2500Water 250 2750 Reaction MassTotal 2750 2750 Total

Reaction Mass 2750 2500 DNCB Crude250 Waste water


Nitration

Seperation

Washing

Seperation



4. 2,3,4/2,4,5 TRI CHLORO NIRTO BENZENE & CRUDE TCNB:


1,2,3/1,2,4 Tri Chloro Benzene is subjected to nitration reaction using nitric acid along with sulphuric acid as dehydrating agent to yield 2,3,4/2,4,5 TRI CHLORO NIRTO BENZENE & CRUDE TCNB.

Chemical reaction:



Material Balance:

5. 2,4 DI CHLORO 3 FLUORO NITRO BENZENE


2,6 Dichloro Flouro Benzene is subjected to nitration reaction using nitric acid along-with sulphuric acid as dehydrating agent to yield 2,4 DI CHLORO 3 FLUORO NITRO BENZENE

Chemical reaction:

C6H3Cl2F + HNO3 = C6H2Cl2FNO2 + H2O

165 63 210 18

Input Kg Kg Output1,2,4/1,2,3 TCB 2600Nitric Acid 903 5049 Reaction massSulphuric Acid 1046Spent Acid 500


3244 Organic LayerReaction mass 5049 1305 Spent Acid

500 Spent Acid For Next BatchTotal 5049 Total

Organic Layer 3244Water 480 3224 TCNB wetSoda Ash 25 525 Water to ETP


TCNB wet 3224 3220 2,3,4/2,4,5TCNB4 Loss in air


Nitrator

Seperator

Washing

Dryer



Material Balance:

6. MONO CHLORO BENZENE


The chlorine in the gaseous form is reacted with benzene to form mono Chloro benzene in the chlorinator reactor, reaction is followed by benzene recovery.

Chemical reaction:

Input Kg Kg Output26DCFB 6000Nitric Acid 2409 11299 Reaction massSulphuric Acid 2890Spent Acid


7659 Organic LayerReaction mass 11299 3640 Spent Acid

Spent Acid For Next Batch

Total 11299 Total

Organic Layer 7659Water 800 7525 DCFNBSoda Ash 25 959 Water to ETP


Nitrator

Seperator

Washing



Material Balance:

Input Kg Output Kg

Fresh benzene 1929

Chlorination

Recovered benzene 2359 HCl 902

Chlorine 1755 Reaction mass 5141

Total 6043

Total 6043

Reaction mass 5141

Distillation

Recovered Benzene 2359

MCB 2782

Total 5141 Total 5141

HCl 902 HCl

Scrubber

HCl loss 28

Water 1774 HCl solution(30%) 2648


7. ORTHO DICHLORO BENZENE AND PARA DICHLORO BENZENE


The chlorine in the gaseous form is reacted with mono chloro benzene to formOrthodichloro

benzene and Para Dichloro Benzenein the chlorinator reactor, reaction is followed by benzene

recovery.



Chemical Reaction:

ODCB

PDCB

Material Balance:

Input Kg Output Kg

Fresh benzene 1338

Chlorination

Recovered benzene 2359 HCl 1252

Chlorine 2436 Reaction mass 4881




Reaction mass 4881 Distillation Recovered Benzene 2359

DCB Crude 2522


HCl 1252 HCl Scrubber

HCl loss 20

Water 2460 HCl solution(30%) 3692


Crude DCB 2522

Crystalizer

P-DCB pure 1250

Crude DCB 1272


Crude DCB 1272

Fractionation O-DCB 1250

Residue 22

Total 1272

1272

MM/s.Jyoti Om

8. 1,

Manufac

The chlo

chlorinat

separatio

pure prod

Chemica

m Chemical

,2,3-TRI CHL

cturing Pro

rine in the g

tor; Reactio

on of crude tr

duct.

al Reaction:

M

Research C

LORO BENZ

cess:

gaseous form

n is follow

ri chloro ben

:

M/s. Aarti I

Centre Pvt. L

ZENE AND 1

m is reacted w

wed by ben

nzene. Crude

Industries L

Ltd., Anklesh

1,2,4- TRI CH

with either b

nzene or Or

e product is t

Limited (O

hwar.

HLORO BEN

benzene or o

rtho di chl

then subject

Organic Div

NZENE

ortho di chlor

loro benzen

ted to Flash D

ision), Vap

ro benzene i

ne recovery

Distillation t

pi.

36

in the

then

to get



Material Balance:

Input Kg Output Kg

Ortho DiChloro Benzene

2229

Recovered Ortho DiChloroBenzene

7800

Chlorination

HCl 3128

Chlorine 6085 Reaction ma 12986


Benzene recovery Recovered 7800

Reaction mass 12986 Mix products 5186


Distillation 124 TCB 3700

Mix products 5186 Reaction ma 1486


Reaction mass 1486 Distillation 123 TCB 1450

Residue 36


HCl 3128 HCl Scrubber HCl loss 28

Water 6294 30% HCl 9394




9. ORTHO ANISIDINE /PARA ANISIDINE


Here ortho anisole is reacted in an autoclave reactor with hydrogen gas in presence of metal

powder catalyst to produce orthoanisidine. The reaction is followed by layer separation and

solvent recovery.

For production of paraAnisidinesame above manufacturing process is applied by taking para

Anisole instead of ortho Anisole.

Chemical Reaction:

Ortho Anisidine

Para Anisidine

Hydrogen

NO2

Ortho Anisole

+ 3 H2

Catalyst

NH2

2 H2O

Water

+

Ortho Anisidine

O CH3O CH3

O CH3O CH3 Para Anisidine

+

Water

2 H2O

NH2

Catalyst3 H2+

Para Anisole

NO2

Hydrogen



MATERIAL BALANCE

10. 3, 4 DICHLORO ANILINE /2, 5 DICHLORO ANILINE


Here 3,4dichloro nitrobenzene is reacted in an autoclave reactor with hydrogen gas in presence

of metal powder catalyst to produce 3,4 di-chloro aniline . The reaction mixture contains solvent.

The reaction is followed by solvent recovery and layer separation. Crude product is then

subjected to flash distillation to get the pure product.

For production of 2,5dichloro anilinesame above manufacturing process is applied by taking

2,5dichloro nitrobenzene instead of,4 di-chloro nitrobenzene.

Chemical Reaction:

3, 4 DCA

Input Kg Kg Output

Ortho Anisole 5355Hydrogen 220 10 Hydrogen loss

30% Ortho Anisole Crude as Solvent 1291

6856 Reaction Mass


1260 WaterReaction Mass 6856

129130% Ortho Anisole Crude as Solvent

4305 Ortho Anisidine Total 6856 6856 Total

Hydrogenation

Phase seperation and distillation

3,4 Dichloro Aniline

+

Water

2 H2O

NH2

Cl

Catalyst3 H2

Cl

+

3,4 DichloroNitro Benzene

NO2

Cl Cl

Hydrogen



2,5 DCA

Material Balance:

Input Kg Kg Output 2,5 DCNB 14000

Reaction

Hydrogen 456

20 Hydrogen Loss Fresh Solvent 100

10 Solvent Loss

Recovered Solvent

8900

23426 Reaction mass


Solvent recovery

8 Solvent Loss Reaction mass 23426 8900

Solvent Recovery

14518 Reaction mass

Total 23426

23426 Total

Phase seperator

2718 Effluent to ETP Reaction mass 14518 11800 Crude(DCA)


Distillation

11740 2,5 DCA Crude 11800 60 Water to ETP Total 11800 11800 Total

Cl

2,5 Dichloro Aniline

NH2Cl

+

Cl 2,5 Dichloro Nitro Benzene

Hydrogen

NO2

3 H2Catalyst

Cl

2 H2O

Water

+



11. DICHLORO ANILINE


Here Dichloro nitrobenzene is reacted in an autoclave reactor with hydrogen gas in presence of

metal powder catalyst to produce Dichloro aniline. The reaction mixture contains solvent. The

reaction is followed by solvent recovery and layer separation. Crude product is then subjected to

flash distillation to get the pure product.

Chemical Reaction:



Material Balance:

Input Kg Kg Output 2,5 DCNB 14000

Reaction

Hydrogen 456

20 Hydrogen Loss Fresh Solvent 100

10 Solvent Loss

Recovered Solvent

8900

23426 Reaction mass


Solvent recovery

8 Solvent Loss Reaction mass 23426 8900

Solvent Recovery

14518 Reaction mass

Total 23426

23426 Total

Phase seperator

2718 Effluent to ETP Reaction mass 14518 11800 Crude(DCA) Total 14518 14518 Total

Distillation

11740 2,5 DCA Crude 11800 60 Water to ETP Total 11800 11800 Total

12. ORTHO CHLORO ANILINE


Here OrthoChloro Nitrobenzene is reacted in an autoclave reactor with hydrogen gas in presence

of metal powder catalyst to produce Ortho chloro aniline. The reaction mixture contains solvent.

The reaction is followed by solvent recovery and layer separation.



Chemical Reaction:

Material Balance:

Input Kg Kg Output

OCNB 7294Hydrogen 279 3 Hydrogen Loss

Fresh Solvent 180 90 Solvent LossSolvent 4320 11980 Reactionmass


90 Solvent LossReactionmass 11980 4320 Solvent Recovery

7570 ReactionmassTotal 11980 11980 Total

1672 Effluent to ETPReactionmass 7570 5898 OCA

Total 7570 7570 TotalPhase seperator

Reaction

Solvent recovery



12. ORTHO CHLORO PARA NITRO ANILINE /PARA CHLORO ORTHO NITRO ANILINE


3,4 Di Chloro Nitro Benzene, recycled liquor Ammonia & anhydrous Ammonia are taken

together in an autoclave for manufacturing of Ortho Chloro Para Nitro Aniline. Desired

temperature and pressure maintain are 15 to 16 hours to complete then reaction. When reaction is

over &excess of Ammonia is blown off through vent valve and scrubber in water to from 32%

w/w Ammonia solution.

Same above manufacturing process is applied by taking 2,5 Di Chloro Nitro Benzene instead of

3,4 Di Chloro Nitro Benzene for manufacturing of Para Chloro Ortho Nitro Aniline.

Chemical Reaction: OCPNA

PCONA

MM/s.Jyoti Om

Material

13. O

Manufac

Para Nitr

in an au

maintain

Ammoni

solution.

Same a

Benzenei

m Chemical

l Balance:

ORTHO NITR

cturing Pro

ro Chloro Be

utoclave for

are 15 to

a is blown

above man

insteadofPar

M

Research C

RO ANILINE

cess:

enzene, recy

manufactur

16 hours to

off through

nufacturing

ra Nitro Chlo

M/s. Aarti I

Centre Pvt. L

E /PARA NITR

ycled liquor A

ring of Para

o complete

vent valve

process

oro Benzene

Industries L

Ltd., Anklesh

RO ANILINE

Ammonia &

a Nitro Ani

then reactio

and scrubbe

is applied

efor producti

Limited (O

hwar.

E

& anhydrous

iline. Desire

on. When r

er in water t

d by taki

ion of Ortho

Organic Div

Ammonia a

ed temperatu

reaction is o

to from 32%

ing Ortho

o Nitro Anilin

ision), Vap

are taken tog

ure and pre

over &exce

% w/w Amm

Nitro C

ne.

pi.

45

gether

essure

ess of

monia

Chloro



Chemical Reaction:

PNA

ONA

MM/s.Jyoti Om

MATER

14. O

Manufac

Molten O

mixer to

Same abo

Aniline f

m Chemical

RIAL BALA

ORTHO PHEN

cturing Pro

Ortho Nitro A

yield OrthoP

ove manufac

for productio

M

Research C

ANCE

NYLENE DI

cess:

Aniline goes

PhenyleneD

cturing proce

on of Para Ph

M/s. Aarti I

Centre Pvt. L

AMINE /PA

s to reduction

iAmine.

ess is applie

henylene Dia

Industries L

Ltd., Anklesh

ARA PHENYL

n vessel whe

ed by taking

amine.

Limited (O

hwar.

LENE DIAM

ere caustic +

Para Nitro A

Organic Div

MINE

+ sulfur solut

Aniline inste

ision), Vap

tion is fed fr

ead ofOrtho

pi.

47

rom

Nitro



Chemical Reaction:

OPDA

PPDA



Material Balance:

15. 3,3 DI CHLORO BENZDINE SULPHATE


Manufacturing of DCBS mainly consist of two steps that is Hydrogenation of Ortho Nitro Chloro

Benzene and Rearrangement.

First 1-Chloro-2-nitro Benzene is hydrogenated in presence of NaOH, Dichlone&catalystto get

1,2-Bis(2-Chloro Phenyl) Hydrazine. Then this reaction mass is reacted with H2SO4 and produce

DCBS.

Input Kg Kg Output

ONA 319 37 O2

Caustic 185 615 Reaction mass

Sulphur 148

Total 652 652 Total

Reaction mass 615 179 Filtrate136 thio300 Reaction mass

Total 615 615 Total

250 Pure PPDA

Crude PPDA 300 50 Loss in air

Total 300 300 Total

Reduction

Cooling &

filtration

Flaking & drying



CHEMICAL REACTION



MATERIAL BALANCE

Input Kg Kg Output

ONCB 1.8521Dichlone 0.0111Emulsifier 0.0044Caustic Lye 48% 0.2815DM water 0.2519Hydrogen 0.06 4.6144 Reaction massFresh Toluene 0.0646Recovered Toluene 2.0888Total 4.6144 4.6144 Total

0.8956 Aqueous layer To ETP

Filter ML 4.6144 3.7188 Hydro TolueneTotal 4.6144 4.6144 Total

1.1737 Real Hydrazo

HCl 3% 5.7622 4.3957Hydro Toluene for rearrangement

Hydro Toluene 3.7188 3.9116 TO ETPTotal 9.481 9.481 Total

Hydro Toluene 4.3957Real Hydrazo 1.1737Spent Acid 62% 3.663Thiourea 0.0103 11.1541 Reaction massHot water 1.9114Total 11.1541 11.1541 Total

Reaction mass 11.1541 3.1939 Toluene for Distillation

7.9602 DCBS massTotal 11.1541 11.1541 Total

DCBS mass 7.9602 6.0406 Spent acid 1.9196 DCBS Wet cake

Total 7.9602 7.9602 Total

DCBS Wet cake 1.9196 1 DCBS Real0.9196 Loss in Air


Toluene for 3.1939 2.0888 Recovered toluene0.15 Loss

0.9551 ResidueTotal 3.1939 3.1939 Total

Drying

Toluene recovery

Hydrogenation

Layer Seperation

Decomposition

Rearrangement

Layer Seperation

Filtration



16. ORTHO NITRO CHLORO BENZENE PARA SULPHONIC ACID


Mixed acid containing concentrated nitric acid and concentrated sulphuric acid is reacted with

MCB- to produceONCB-PSA. The reaction gets completed in nitrators Reaction is followed by

salting,filtration and decanting to get a ONCB-PSA .

Chemical Reaction:

Material Balance:

Input Kg Kg Output

MCBPSA 1.047H2SO4 1.047 2.5426 Nitro massHNO3 0.4486


Nitro mass 2.5426 6.5926 Reaction massWater 4.05Total 6.5926 6.5926 Total

Reaction mass 6.5926KCl Mix 0.3355 7.7082 Reaction massNaCl 0.7801Total 7.7082 7.7082 Total

1.8882 RetenateReaction mass 7.7082 5.82 Filter ML to ETPTotal 7.7082 7.7082 Total

1 W/c of ONCBPSA

Retenate 1.8882 0.8882 Decanted ML to ETP


DUMPING VESSEL

SALTING VESSEL

NITRATION

FILTRATION

DECANTING



17. 2,4,6 TRICHLORO ANILINE


Here Aniline is reacted HCl gas in presence of solvent to produce Aniline Hydrochloride. The

chlorine in the gaseous form is reacted with Aniline hydrochloride to form 2,4,6 Tri Chloro

Aniline. The reaction is followed by washing and solvent recovery.

CHEMICAL REACTION



Material Balance:

Input Kg Output Kg

Aniline 0.618MCB 0.003Recovered MCB 1.8

HCl gas 0.242HCl to scrubber

0.68

Chlorine 1.414 Reaction mass 3.397Total 4.077 Total 4.077

Reaction mass 3.397 Waste water 0.37NaOH 0.083 Organic layer 3.11Total 3.48 Total 3.48

Distilled MCB 1.8

Organic layer 3.11Distilled 2,4,6 TCA

1.3

Residue 0.01Total 3.11 Total 3.11

HCl 0.68 HCl 0.07Water 1.24 HCl(30%) 1.85Total 1.92 Total 1.92

Condensation

Washing

Distillation

HCl Recovery



ANNEXURE VI

DETAILS OF WATER CONSUMPTION

Sr.No. Purpose Existing fresh Water consumption in KL/day

Proposed fresh Water Consumption in KL/Day

Total fresh water consumption (KL/day)

A Domestic 55 0 55 B Industrial 1) Cooling 334 150 484

2)Process 146 263 409 3) Washing 10 0 10 Total (B) 490 413 903 Total (A+B) 545 413 958

DETAILS OF WASTE WATER GENERATION

Sr.No. Purpose Existing Waste water generation in KL/day

Proposed Waste water generation in KL/Day

Total wastewater generation in KL/day

A Domestic 50 0 50 B Industrial

1)Cooling 79 41 120 2)Process 61 81 142 3) Washing 10 0 10

Total (B) 150 122 272 Total (A+B) 200 122 322

Note: Our group company M/s. Aarti Industries Limited (Alchemie Organic Division) having discharge of 90 KLD and M/s. Aarti Industries Limited (Amine Division) having discharge of 55 KLD are in the process of achieving zero liquid discharge,already an EC is granted which will reduce the load of CETP.



WATER BALANCE DIAGRAM (AS PER CCA NO.AWH-50294)

Washing 10 KL/Day

Domestic 55 KL/Day

Cooling 334 KL/Day

Industrial 490 KL/Day

Total Water Consumption 545 KL/Day

Effluent from Process

61 KL/Day Cooling Blow down 79 KL/Day

Sewage 50 KL/Day

Loss 255KL/Day

Effluent Treatment Plant 150 KL/Day

Treated effluent is sent to C.E.T.P. of M/s. Vapi Green Enviro Ltd. For

further treatment & for final disposal 150 KL/Day

STP 50 KL/Day

Washing 10 KL/Day

Water coming from reaction

27 KLD

Water along with HCland H2SO4

112 KL/Day

Process 173(146+27)



WATER BALANCE DIAGRAM (PROPOSED EXPANSION)

Washing 10 KL/Day

Domestic 55 KL/Day

Cooling 484 KL/Day

Industrial 903KL/Day

Total Water Consumption 958 KL/Day

Cooling Blow down 120 KL/Day

Sewage 50KL/Day

Washing 10 KL/Day

Process 436(409+27) KL/Day

Polishing System 272 KL/Day

STP 50KL/Day

Treated effluent will be sent to C.E.T.P. of M/s. Vapi Green Enviro Ltd. For further treatment &

for final disposal

Water coming from reaction

27 KLD

Water with HCl 308 KL/Day

Water from acid concentration 42 KL/Day

Effluent from Process

100 KL/Day Primary Treatment

162 KL/Day ETP

110 KL/Day

M/s.

D

.Jyoti Om Chem

DETAILS OF T

mical Research

TREATMENT

Centre Pvt. Ltd

T SCHEME AN

d., Ankleshwar.

ND DISPOSAL

M/s. Aa

L

arti Industries

s Limited (Org

58

ganic Division)

ANNEX

), Vapi.

XURE-VII



ETP Process Description:

Brief Description of Effluent Treatment Plant:

The treatment process consists of

Physico - Chemical treatment of effluent.

ii)Bio-logical treatment of Physico -Chemical treated aqueous effluents diluted with domestic

effluent. General waste water & sewage is given anaerobic treatment in the septic tank to reduce

organic load & suspended particles before giving it bio-logical treatment.

Bio-logical Treatment

Physico - Chemically treated aqueous effluent, domestic effluent and non-process effluent are

combined and subject to bio-logical oxidation. General waste combined with the recycled

effluent from sludge dewatering and rain water in dykes area is collected in combined collection

sump. All the above streams are combined and equalized with the help of aeration in equalized

tank to obtain same organics load all times and partly reduction in COD/BOD. The equalized

effluent is pumped in to the primary treatment tank where sludge (settled) is collected in solar

dry bed and over flow collected in aeration tank. Activated sludge treatment as per extended

aeration process is carried out in aeration basin thereby reducing soluble BOD to desired treated

effluent quality. Oxygen is supplied to the aeration tank through fixed, mechanical surface

aerator. Effluent from aeration tank enters in to the secondary classifier where the produced bio-

sludge settles allowing classified supernatant to over flow to carbon filter and sand filter. After

tertiary treatment, treated effluent is discharged to CETP pipeline through continuous sampler.

Settled sludge from secondary clarifier scrapped out in to the solar dry bed. Most of the settled

sludge in clarifier is recycled back to the aeration tank to maintain the desired MLSS/MLVSS

concentration in the aeration tank.



Details of ETP

Sr. No. Treatment Unit Dimension of ETP (in

meter) MOC

Existing ETP Equipments

1. Oil & grease tank 8 kl MS

2. Equalizer Tank -1 150 KL RCC

3. Equalizer Tank -2 150 kl RCC

4. Flash mixture -2 0.500 kl RCC

5. Poly dosing tank 0.458 kl RCC

6. Primary Clarifier 80 KL RCC

7. Bio-Reactor 400 KL RCC

8. Secondary Clarifier 120 KL RCC

9. Secondary sludge tank 5 kl MS

10. Polishing tank-1 3.7 kl RCC

11. Polishing tank-2 3.7 kl rcc

12. Activated Carbon Column --- MS

13. Multigrade sand filter ---- ms

14. Raw Water Tank 5 KL HDPE

15. Final Outlet Tank 1 KL RCC 16. Neutralizer - 1 12 KL MSTL

17. Neutralizer - 2 6 KL HDPE

18. Neutralizer - 3 4 KL SS

19. Lime Preparation Tank - 1 10 KL RCC

20. Lime Preparation Tank - 2 10 KL RCC

21. Filter Press --- ---- Proposed ETP Equipments

1. Flash mixture-1 2.5 kl SS 2. Flocculator 2.5 kl MS 3. PAC dosing tank 0.527 kl MS 4. Final Outlet Tank 5 KL HDPE 5. Neutralizer 4 15KL MS 6. Memebrane Filter Press



ANNEXURE VIII

DETAILS OF ELECTRICITY AND FUEL CONSUMPTION

Sr. No.

Name Requirement Source

Existing as per CCA AWH-50294

Proposed Total

1 Diesel 225 lit/hr 350 lit/hr 575lit/hr Local market

2 Energy - Electricity

2500KVA 1000KVA 3500KVA DGVCL

DETAILS OF FLUE GAS EMISSIONS

Sr. No.

Stack Attached To Stack Height in Meter

Fuel APCM Type of Emission

Permissible Limit

Existing as per CCA (AWH-50294) 1. D.G.set

(1 no. 625 KVA) 11 Diesel None PM

SO2

NOX

150mg/ Nm3 100 ppm 50ppm

2. D.G.set (1 no. 750 KVA)

11 Diesel None PM SO2

NOX


Proposed

1. D.G.set (1 no. 1100KVA)


NOX


2. Thermo pack 100000KCal


NOX




DETAILS OF PROCESS EMISSION

Sr. No.

Stack attached to Stack Height in Meter

APCM Parameter Permissible Limit

Existing as per CCA (AWH-50294) 1. Chlorinator for MCB

plant 18 Two stage

water scrubber+Caustic scrubber

HCl Cl2

20 mg/Nm3 9 mg/Nm3

2. Nitrator of NCB plant 12 Two Stage Caustic scrubber

NOX 25 mg/Nm3

Proposed 1. Connected to HCl

storage tank 11 Water

scrubber+Caustic scrubber

HCl

2. Connected to GLV NCB 11 Caustic scrubber

NOX 25 mg/Nm3

3. Spent acid Concentration plant

11 Caustic scrubber

4. Batch Nitration plant 11 Caustic scrubber

5. DNCB Plant 11 Water scrubber followed by Caustic scrubber



ANNEXURE IX

DETAILS OF HAZARDOUS WASTE GENERATION & DISPOSAL

Sr.No.

Name of Waste (Category)

Existing Quantity

Proposed Quantity

Total Quantity

Mode of disposal

1. ETP waste (34.3)

75 T/month 110 MT/Month

185 MT/Month

Collection, Storage, Transportation, disposal to TSDF developed by VGEL, Vapi

2. Distillation Residue (26.1)

120 T/month 441 MT/Month

561 MT/Month

Collection, Storage, Transportation, disposal to CHWIF at SEPPL for incineration.

3. Spent carbon (35.3)

1 T/Month +0.00 1 T/Month Collection, Storage, Transportation disposal to CHWIF at SEPPL.

4. Discarded Material (plastic bags, Drums)(33.3)

What so ever -- What so ever

Collection, Storage, Transportation disposal entire quantity reuse to filling sludge and drums for filling finished products

5. UsedOil(5.1) 200 Lit/year 800 Lit/year

1000 Lit/year

Collection, Storage, Transportation disposal by reuse in plant & machinery for lubricating purpose.

6. Insulation waste

2.0 T/Month 5 T/Month 7 MT/Month

Collection, Storage, Transportation and disposal to TSDF, Vapi

7. a. Dil. H2SO4 b. Dil. H2SO4

21600 T/year 7500 T/year

+0.00 21600 T/year 7500 T/year

M/s. Aarti Industries (Alchemie organic Div.) M/s. Apex Pharma Chem Pvt. Ltd. Reception/collection/ Storage/ Reuse/

User

Typewritten Text

ANNEXURE-X CCA BEFORE 2006

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Typewritten Text

ANNEXURE-XI MEMBERSHIP CERTIFICATE

Vapi Wasir. 5r i:.ii1uent t\{a-nagement Cc. Lir.l.

Registered Office : VIA House, Plot No.135, GIDC VAPI 396 195, Guiarat" INDIATel.: (0260) 2428950 o Telefax : (0260) 2429950 c WEBSITE : www.ceq)vapi.com

E-mail : [email protected], [email protected]

Ref. No.CETP_Memb.Cern/ 1/ 2005_06 / 9073 March 8, 2006

MEMBERSHIP CONFTRMATION CETTTIFICATE

This is to certify that M/s. Aarti Industries Limited, Plot No. \U/n,

Phase II, G.I.D.C. Yapi 396 195, is a Member of Cornmon Effluent Treatment

Plant. The Membership No. is 1.

This certificate is issued at the specific request of the above party.

For Vapi & Effluent Management Co. Ltd.

Shyam S. DevadigaHead - Finance

D:Certy-CETP CertysD/tcT

COMMON EFFLUENT TREATMENT PLANT :"CETP", N. H. No.8, Near Darnanganga Bridge, GIDC, VAPI396195. Tel.: (0260) 2432950Telefax Z4g49Z9

. COMMON SOLID WASTE PLANT:"CSWP", Plot 4807 etc. Phase IV, GIDC, VAPI 396195. Tel.: (0260) 2427 0,2435186

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l::

Vapi !\',r'.li: <k Efilueni Management L' i 'l

ReeisteredOffice:VlAHouse,PlotNo'135,GIDC,VAPI395195'GujaraiINDIA'-i?fr toiool zze950 r Telefax : (0260) 24?]9950 IWEBSITE : www'cetPvapi com'

i-mail:admin@cetPvaPi'com,vwemcl-ad1@sanchamet'in

WtrFRef. No.CSWP-M emb.Ceft1/37 /9074

This is to certifY that

G.I.D.C., YaPi396195, is the

Membership No is: 31.

F:Certy-CSWP Certy

March 8, 2006

M/s. Aarti Industries Limited, Plot NO' 80L/23'

member of Common Solid Waste Project Site' The

This certi{icate is issued at the specific request of the above Party'

Emlfft-e & Erfluent Management co' Ltd'

\ / " / .tr*vSHYAMS.DEVADIGAHead - Finance

COMMON EFFLUENT TREATMENT PLANT :

"CETP", N. H. No.8, Near Darnanganga Bridge, CIDC, VAPI 396 195 TeI : (0260) 2432950 Telefax : 2434929

COMMON SOLID WASTE PLANT :,,CSWp... plot 4807 etc. Phase IV, GIDC VAPI 396 195. Tel.: (0260\ 2427950' 2435786


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Snunaskrnn Errvino Pnojecrs Fvr. Lrd. .Q.'':'jiT: ::il:::'::::,:::::Tili::ff:::11' ffiPh.: +91-261-295't248,2it46181, 6452205 Fax : +91-26,1.2354068 E-mait : [email protected] ,.o,ffi".,,n"u

CertificateCertificate No3 CSA027

To Whomsoever it may concern

This is to certify that

AARTI INDUSTRIES LI1\4ITEDORGANIC DIVISION

PLOT NO _ 801/23PHASE - III

GIDC - VAPI

VALSAD

is a valid member oJ-

tNvtRa

Date of issae

Date of expiruion

Place of issue

Pvr. l-rd.

for rntegrated common Ha4,ardous waste Management .I,-acirity,

This membership is vatid for a period of

5 Years

i I1/05/2010

i I0/05/2015

1 Surat

For,Saurashtra Enviro

STJBJECT TO SURAT JURISDICTION

site : R s No 415, 417 & 418, vllage : Juna Katariya' B/h. cail Pump station, samakhiyati - Randhanpur Highway, Tatutu , gt ".h.iiililixu-il1


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