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APPENDIX - 2.1

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APPENDIX - 2.2

MPCBCONSENT ORDER

MAHARASHTRA POLLUTION CONTROL BOARDTel: 24010437/24020781/24014701 -=- Kalpataru Point, 2n - 4 FloorFax: 24024068/24023515 Opp. Cine Planet Cinema,

! Website: http://mpcb.gov.in _iilI Near Sion Circle, Sion (E)l Ernail: [email protected] ' .• r,. Mumbai-400 022.

Red/M.S.I Date: IS /OP2014

Consent No: BO/ASTIRO-Pune/EIC No PN-21251-14/CC --4~~

Consent to Establish under Section 25 of the Water (Prevention & Controlof Pollution) Act, 1974 & under Section 21 of the Air (Preve~ion &Control of Pollution) Act, 1981 and Authorization I Rene~l ofAuthorization under Rule 5 of the Hazardous Wastes (Man \iJP~nt,Handling & Transboundry Movement) Rules 2008 .,<,,-

[To be referred as Water Act, Air Act and HW (M&H) Rule'

CONSENT is hereby granted toMIs. OC Specialities Pvt. Ltd.

,'"Plot No. E-18, MIDC Chinchohx,"Tal-Mohol, Dist- Soll!PUF".,

located in the area declared under the provisidqs dY;,,-~~eWater Act, Air act andAuthorization under the provisions of HW(M&H)~<ayjes and amendments theretosubject to the provisions of the Act and the'tmules""~nd the Orders that may be

~, -nmade further and subject to the following Jmd conditions:1. The Consent to establish ~\," fed for a period up to: Upto

commissioning of the unit QP-2..._~~~~:2;017.(Aprevious Cto E was granted ~on 27/04/2012 ) ~'\.' '(,.[ - )

.;f">"',,"\, "2. The Consent is valid for ,I"!!pufacture of - I .

I of7

Sodium Broli\fde,Or ;"",,-~,,Sodiumf.Bremide PowderZinc Hy,dfcoxye>rr", .Zi;c, {)xide 74

MTIM

232106

MTl1Vl

2. Di ~ Isopropyl Ethyl AminemIPEA)

18.18 MTIM

---1'0 -MTlM40

4. Phenetole5. Methyl-2-Chloro Phenyl Acetate 10.3 MTIM6. 4 Methoxy Phenvl Acetone 10 MTIM7. 2,3 Dichloro Pyridine 10 MTJM8. Para Hydroxy Benzoic acid 20 MT/M9. Para Hydrox Benzyl Alcohol 11.2 MTIM1O~ Paramethoxy Benzaldehyde or

para anisaldehyde24 M1'/M

11. Benzyldehyde Ortho SulphonicAcid Sodium Salt

24 MT/M

12. Benzyldehyde 2,4 Di SulphonicAcid

5

OC Specialities Pvt.Ltd, SRO Solapur VRlM/99240000

Sr. Product Na me l\Iaxi1H1IIII UOMNo. Quantity13. 2- Amino- 2 - Phenyl Butyric 6.5 MTIM

Acid14. Ortho Hydroxy Phenyl Acetic 15 MTIM

Acid15. 2 Coumaranone 12.4 MTIM16. Ortho CaynophenolJ 2- Hydroxy 10.12 MTIM

Benzonitril17. 3- Isochromanone 12 MTIM18. 2,6 Dichloro Benzoyl Chloride 2.2...1 MTIM19. Methy 1-2 -Dirnethy Iamino- 2- 10 MTIM

Phenyl Butyrate '-20. 2-Dirneth Iamino-z-Phenyl 3.01 MT;\::.

B-I."k'l!i1tl~_2L J3'iRkIDfiadle 3 ".~ Phthaifide 13

r2:~t P-Bromonisole / '4- Bromo Itt'5. ,~~'lWJ2IMtAnisole ~~

24. Para Bromo Phenetole / 4- 14.5 .f} \ MTIMs.....-',

.Bromop henetole

:25,. i.nt~nnediate - p. ~4W NITIMIhuiDtl,,-ardti'ofe

26.. 2.!i. ~ .•• .... • A-n..l V.7~ "MTIM~. ~ -~ .~yI ,,~?5 M1'IM- .•.-. Phenyl ~ I

Chllo'lcid'a ••28.. Indnlme _ '-~V 36.25 MTfM:29. Ethy[ Phenyl Glyoxalafe IUDK!." "

~ .•. 2$.42 MTIM30. t E h. ·1-l-H.-<f,.!"Ol'i; C~·el.ot..ex~~ ,- 33 T\1T/M

I Carboxylate ~~31. Ethyl.I.Hydroxy Cy."o. * ••. • 3a25 MT/l\1

Carboxvlate ,..",. -,32. 3· Chloro ,,~O 2 - ~ MTflvI

Hvdrazinyl -' .'B,y -IIUi\o.dUl~~" -

L SOOium ,....• .:25% 182..07 MTiM

2- Het..3IJK U Th.5l9 -X1T~1a. .,.-_.0.-_.-. - - . i -3f:a, 3OA2 ~ rIM

,,-......- 2 ~ hiS ._-I.. _ -rIM

:~~-1>10... 'lI!t.r .• .3' Benzoia.Acid.. -, A j, 1 1Mkn\stillation Residue of P-Xylene ~ ..,-:. 3.6 .~ ••..•••••..=1 ~7fVf

t . .•• Ammonium Chloride 36 MTIM

3. CONDITIONS UNDER WATER ACT:(i) The daily qua.ntity of trade effluent from the factor..,: hal! not exceed 20.0M:~.

_aailyql&aDlityofsewageefDuentfromth £actm 'b •.~U.not"'xceed 4.5M:l.ea~=

~ -- . - TIie:appJieant sbaIl proVide annprebeDSi' f.~·ea[-mt!n -.j remcmiSislmg 0 .~, seconduy~ IErtim.·' m-eawe~t a is warranted withrefureooe to ffiftnent qwility and ~ and. "iID'l:iHm~nwe same continuously.

(ill) Tr.ade :gmue.nt Di sposal: The treated! aillu:ent /Snall oe re.cycle to the maximumextend -& achieve zero discharge by providmg Double Effect Evaporator .In nocase. effluent shall lead outside industry premises.. . .

6;'''-a POI"", .'.~,.--..;~~."'r.,r "', ("I".

'---------- ~ihr~ ~.l,.g._\l_-------------ll:El )~< ( ) 0'L / ..••_ .. .-'-'"

OC Specialities P\<t.Lld. SRO Solapur l/R/M/99240000 20f7

I

(iv) Sewage Effluent Treatment: The applicant shall provide comprehensivetreatment system as is warranted with reference to influent quality and operateand maintain the same continuously so as to achieve the quality of treatedeffluent to the following standards(1) Suspended Solids Not to exceed 100 mg/l.(2) BOD 3 days 270 C. Not to exceed 100 mg/l.

(V) Sewage Effluent Disposal: The treated domestic effluent shall be soaked in asoak pit, which shall be got cleaned periodically. Overflow, if any, shall be used onland for gardening in own premises.

(vii) Non-Hazardous Solid Wastes:

(vi)

4. The applicant shall comply with the provisions of the ':Sat ,Control of Pollution) Cess Act, 1977 (to be referred'&~s\ sessamendment Rules, 2003 there under

~he;lda.H~w.ate_rcons.uID{ltionfor the following cate~~fu~ ~ as under:(i) Domestic purpose ... ~~(ii) Water gets Polluted & . ~."~",,~

Pollutants are Biodegradable ... ~~15CMD(iii) Water gets Polluted, Pollutants

are not Biodegradable & Toxic ...(iv) Industrial Cooling, spraying

in mine pits or boiler feed "(v) Gardening & Fire services

,•...... 0.00 CMD

10.0CMD2.00 CMD

The applicant shall reg "cons~mption in .the presc~~ '.(" :pJ.~Section 3 of the said Act.'\( -,

" "5. CONDITIONS U . .~&R ACT:(i) The appHe~e"'" olinstall a comprehensive control system consisting of

contrel eq ipments as is warranted with reference to generation ofo ~nd operate and maintain the same continuously so as to

.;;iIab.iI~i!the level of pollutants to the following standards:fU}'nH'nlr •• ituipment:

Air pollution control system of sufficient capacity shall beprovided to the limit emissions.

II, There shall not be any secondary (fugitive) emissions.'tan~~rlJ:sIf~BljE-Blj§.~iQI)Soj Air Pellutants.

(i) SPM/TPM Not to exceed 150 mgINm3(ii) S02 Not to exceed 155 Kg/day(iii) Acid mist Not to Exceed 35 mg/Nm3(iv) NH3 Not to Exceed 50 mg/Nm3(v) S02 (process) Not to Exceed 50 ppm

The applicant shall observe the following fuel pattern:-

to the Board the returns of waterpay the Cess as specified under

a.

(i)

81'. J\ln. '!\-PC' Of Fuel Quantitv1 Coal 15.5 MTlDav2 Biomass 30MTIDav3 Diesel 300 Lit IHr

.'

OC Specialities Pvt.Ltd. SRO Solapur URlM/99240000 30f7

The applicant shall erect the chimney(s) of the following specifications:-:-)1' Chim n«. .vtr:u hcrl To HC1:.;hr 111 .\P( 'SNu. \Itr,

Boiler 25.0(Common)

MDC1

2 Thermic Fluid HeaterStack3 D.G. Set 200 h,vA

Reactor- 1 4 H3 Scrubber4Reactor- 2 (HCL) Scrubber5

Scrubber6'Reactor- 4 'HN<h)7 ScrubberReactor - 5 (CO!)8 Scrubber

6.

b.

average.c. The industry shall take adequate measures for control of noise

lleye!>sfrom its o,wn sources within tile premises ~n respect of noise totess thaB 55 dB(A) ·du~ day t.ime .a:nd 45-·dB(A) -dll.'l.ring the nilg'k~tume., iD.a:v~ ~ ~ '!@e~ee,n() a.aa. to il0 p.m and :ni:ghttimelis reekeBlel.'ii ~eltweeoltl! p..m t6 6 a.m

\d.L IiIil:QlM,~ ~d.a ma1ke ef;f@ns 100);}\)riDg dawn noise level due to DGset, outeide indaetria! premises, within ambient norse requirementsby proper sitting and control measures.

e. Installation of DO Set must be strictly III compliance withrecommendations of DG Set manufacturer.

OC Specialities Pvt.Ltrl. SRO SoJapur URfM.J99240000 40f7

f. A proper routine and preventive maintenance procedure for DG setshould be set and followed in consultation with the DGmanufacturer which would help to prevent noise levels of DG setfrom deteriorating with use.

g; D.G. Set shall be operated only in case of power failure.h. The applicant should not cause any nuisance in the surrounding

area due to operation ofD.G. Set.7. CONDITIONS UNDER HAZARDOUS WASTE (MANAGEMENT, HANDLING &

TRANSBOUNDRY MOVEMENT) RULES, 2008:(i) The Industry shall handle hazardous wastes as specified below

-

Sr. 1\( 'I'ype Of Waste Quantity UOlVI DisposalMTID CHWTSDF0.30Cat.: 34.3- ETP Sludge,

DE

MTIM

1.

Salts2. Cat.: 28.1-

ResidueProcess 13.14

21.2Cat.: 20.3- DistillationResidue

3.

Treatment: - NIL(ii) The unithas to c&pIay and maintii·iii WE,a:lliJ~ online outside the

factory main gate in Marathi & Doth ona 6'x4' displayhoard in the manner and the rep e compliance along withphotograph shall be submitted t ffice & concerned RegionalOffice/ Sub Regional Office.

(iii) Whenever due to any acci .¥tI.-D ),pas leakage or other unforeseen actor even, such emissions ccu~..r··is apprehended to occur in excess ofstandards laid down, sucll information shall be forthwith Reportedto Collector, Dire tot)e of Industry. Safety and Health. PoliceStation, Fire B(1'g.aa~,lDi:rectorate of Health Services, Department ofExplosives, B0al" an' cal Body and the production process shouldbe stopped g all necessary safety measures. The industryshall ala o· or the emission and ensure that the emissions donot c. harm or nuisance in the surrounding. The industrysho . ~t estart the process without permission of the Board ando.I.J!l~~·l41·tutoryorganization as require under the law.

tlJjlr~~-c'Omply with folloWing additional conditions:LThe. ,shaIlmaintain good housekeeping and take adequate measures for

c~n.. . ollution from all sources so as not to cause nuisance to surroundingaite~ In-ll abitants.

II. T.he applicant shall bring minimum 33% of the available open land under green.~e:m.e1lime »lantiatl:oD.m.- Solid waste - The non hazardous solid waste aFising in the fa~t0ry premises,

- sweepings, etc., be disposed of scientifically so as not to cause any nuisance -/pollution. The applicant shall take necessary permissions from civic authorities fordisposal to dumping ground.

iv. The applicant shall provide for an alternate electric power source sufficient tooperate all pollution control facilities installed by he applicant to maintaincompliance with the terms and conditions of the consent. In the absence, theapplicant shall stop, reduce or otherwise, control production to abide by terms &conditions of this consent regarding pollution levels.

v. The applicant shall not change or alter quantity, quality, the rate of discharge,temperature or the mode of the effiuent / emissions or hazardous wastes or controlequipments provided for without previous written permission of the Board.

8,

50f7OC Specialities Pvt.Ltd. SRO Solapur URlM/99240000

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

vii. The applicant shall make an application for renewal of the consent at least 60 daysbefore the date of the expiry of the consent.

viii.The firm shall submit to this office, the 30th day of September every year, theEnvironmental Statement Report for the financial year ending 31"t March in theprescribed Form-Vas pre the provisions of rule 14 of the Environment (Protection)(Second Amendment) Rules, 1992.

ix. As inspection book shall be opened and made available to the Board's officersduring their visit to the applicant.

x, The applicant shall install a separate electric meter showing the consumption ofenergy for operation of domestic and industrial effluent treatment pla ts and airpollution control system. A register showing consumption of chemioals '~ed fortreatment shall be maintained.

xi. ~te drajnage system shall be provided for collection of ..,..-__ .zo-

.~$.,T~l~.~l~oles:shall he proVid~ at the-~~~ 9f , _ , _man~ni-eht iet"tIleasi't:$g ~~ tlQ~~NfiI-.em~i:(t.!f~Rb..',";.~:_·lljlt~~e ;Pip~a, /'sewers down- stream of the terminal manholes. No effluent s all find its way otherthan 111 designed and provided collection system.

xii, Ieither storm water nor discharge from other premises shall be allowed to mixwith the effluents from the factory,

9. This consent shall not be construed as .' exemption from obtainingnecessary No Objection Certificate fro~other Government agencies asmay deemed fit necessary.

before starting actual10.The applicant shall obtaicommercial Production.

11.This consent is issued as per the delegation of powers to HOD's videBoard Office Order No~3J.of 2013 dtd. 01/03/2013.V-

12.The applicant take any efIedive stepS towards implementationof the proj . ore obtaining Environmental Oearance as per EtADOtificati . and ame~ thereto & submit Bank Guarantee Rs.2 Iakh 15 days iD favor of Regieual 9fficer Pune valid up to3 :1.0&2;0, ;U:(i)wanls _plianc:e Qfthe same.

14.1f any non-compliance of the conditio-As of consent to Establish observed,the Board will initiate appropriate legal action including, revocation ofconsent and further action.

15. The Capital investment of the industry is Rs.5.14 Cr.. [1\

r.v ••~/iJ ~,01'i11'1,-I/pl(P. K Mirashe)

Assistant Secretary. (Technical)

\

,\

\

\

, I

60f7

I

,"

II

To,MIs OC Specialities Pvt Ltd.Plot No. E-18 , MIDC Chincholi ,Tal-Mohol , Dist- Solapur.

Copy to:RO, Pune /SRO,Solapur- They are directed to ensure the compliance of consentconditions.CAO/Cess BranchlMaster file.

Received, Consent fee of-

OC Specialities Pvt.Ltd. SRO Solapur VRlM/99240000 7of7

APPENDIX - 2.3

LIST OF RAW MATERIALS &ITS SUPPLIERS

List of Raw Material for Proposed Unit1. Product: Sodium Bromide / Zinc Hydroxy / Zinc Oxide

Name of the Raw Material QuantityKg/ Batch

Zinc Bromide 70% 6000Sodium Hydroxide Flakes 1600Water 4800

2. Product: Di Isopropyl Ethylamine (DIPEA)


Di Isopropyl Amine 3030Sodium Hydroxide Flakes 1160Water 400Di Ethyl Sulphate 2100

3. Product: Anisole


Phenol 1900Dimethyl Sulphate 1780Sodium Hydroxide 970Water 1800

4. Product: Phenetole


Phenol 1700Sodium Hydroxide Flakes 930Diethyl Sulphate 2500Water 2700

5. Product: Methyl-2-Chloro Phenyl Acetate


2-Chloro Phenyl Acetic Acid 1000Methanol 500Sulphuric Acid 98% 50Sodium Carbonate 3Water 12

6. Product: 4 Methoxy Phenyl Acetone

Name of the Raw Material QuantityKg/Batch

Para Anisaldehyde 1000Methyl 2 Chloro Propionate 975Sodium Methoxide 440Water 1750Sodium Hydroxide 300Sulphuric Acid 400

62

7. Product: 2, 3 Dichloro Pyridine


3-Amino Pyridine 250HC130% 2900Hvdrocen Peroxide 50% 194Sodium Nitrate 194Water 2200Sodium Hydroxide Flakes 835Cupric Chloride Dihydrate 42Sulphuric Acid 42Iso Propyl Alcohol 75

8. Product: Para Hydroxy Benzaldehyde


Para Cresol 1080Air (Oxygen) 320Caustic Soda 65Hydrochloric Acid 30% 200Water 2000

9. Product: Para Hydroxy Benzyl Alcohol

Name of the Raw Material Quantity Kg/ Batch

Para Hydroxy Benzaldehyde 1220Toluene 2500Sodium Borohydride 325Methanol 300Caustic Soda 150Water 1000

10. Product: Paramethoxy Benzaldehyde or Para Anisaldehyde


Mixed Xylene 2550Para Hydroxy Benzaldehyde 1220Sodium Carbonate 780Dimethyl Sulphate 880Water 2850

11. Product: Benzaldehyde Ortho Sulphonic Acid Sodium Salt


Ortho Chloro benzaldehyde 900Sodium Sulphite 950Water 3000Hydrochloric Acid 30% 360Sodium Hydroxide Flakes 35

63

12. Product: Benzaldehyde 2, 4 - Di Sulphonic Acid


2,4 Dichloro Benzaldehyde 600Sodium Sulphite 930HCI 130Water 2205Sodium Hydroxide 5

13. Product: 2-Amino-2-Phenyl Butyric Acid


Propiophenone 550Methanol 700Ammonium Bi Carbonate 660Sodium Cyanide 225Acetic Acid 135Water 800Sodium Hydroxide 675Hydrochloric Acid 30% 2000

14. Product: Ortho Hydroxy Phenyl Acetic Acid


2-Chloro Phenyl Acetic Acid 1000Sodium Hydroxide 940Copper Sulphate 40HCI- 30% 2850Water 2200

15. Product: 2 Coumaranone


Ortho Hydroxy Phenyl Acetic Acid 750

16. Product: Ortho Caynophenol / 2 Hydroxy Benzonitrile


Salicylamide 620Mono Chlorobenzene 1650Thionyl Chloride 840

17. Product: 3-lsochromanone


Ortho Methyl Phenyl Acetic Acid 1000Monochloro Benzene 1500Catalyst 20Chlorine 408Water 2000Ammonia 25% 840Toluene 600

64

18. Product: 2, 6 Dichloro Benzoyl Chloride


2,6 Dichloro Benzaldehyde 900Nitric Acid 60% 1350Sodium Hydroxide Flakes 230HC130% 650Thionyl Chloride 1170i) Thionvl Chloride (Recovered) 500ii) Thionyl Chloride (Consumption) 670Water 650

19. Product: Methyl-2-Dimethylamino-2-Phenyl Butyrate


2-Amino-2-Phenyl Butyric Acid 1000Toluene 1800Dimethyl Sulphate 760Sodium Hydroxide Flakes 40Formic Acid 800Formaldehyde 37% 1100Water 1800

20. Product: 2-Dimethylamino-2-Phenyl Butanol


Methyl-2-Dimethylamine-2-Phenyl 550ButyrateToluene 720Vitride 70% in Toluene 1070Sodium Hydroxide Flakes 280Water 2000

21. Product: Pivalonitrile


Pivalic Acid 1020Ammonia 200

22. Product: Phthalide


Phathalic Anhydride 1600Methanol 6600Rany Nickel (Catalyst) 12.20Sodium Carbonate 35Hvdroqen 50Water 350

65

23. Product: P-Bromonisole / 4-Bromo Anisole


Anisole 1000HBr(48%) w/w 1625Hydrogen Peroxide (50%) w/w 750Water 500Sodium thiosulphate 25Water 500

24. Product: P-Bromonisole / 4-Bromo Anisole


Phenetole 1000hydrobromic Acid (48%)w/w 1450Hydrogen Peroxide (30%)w/w 1100Sodium thio-Sulphate Soln.(5%) w/w 525

25. Product: Intermediate - P- Bromoveratrole


Veratrole 1000Hydrobromic Acid (48%) 1300Hydrogen Peroxide (50%) 590Water 380Sodium Thiosulphate 25

66

LIST OF RAW MATETIALS SUPPLIERS

Sr. Name of Raw Material SuppliersNo.1. Zinc Bromide 70% Saltico Gmbtt , Germany2. Sodium Hydroxide Flakes GACl , Domestic3. Di Isopropyl Amine Arkema Peroxides India Private Limited,

France4. Di Ethyl Sulphate Industrial solvents, Ankleshwar

5. Phenol Hindustan Organics Chemicals6. Dimethyl Sulphate local Industrial solvent7. Sodium Hydroxide GACl8. 2-Chloro Phenyl Acetic Acid China9. Methanol Deepak Fertilizer, Taloia10. Sulphuric Acid 98% local commodities11. Sodium Carbonate local commodities12. Para Anisaldehyde Atul Ltd. or Inhouse13. Methyl 2 Chloro Propionate China14. Sodium Methoxide Alkali Metals Ltd.15. 3-Amino Pyridine China16. HC130% lanxes17. Hydrogen Peroxide 50% GACl,Dhej18. Sodium Nitrate Deepak Nitrite Baroda19. Iso Propyl Alcohol Deepak Fertilizers, Taloia20. Para Cresol Atul Ltd ; Atul21. Caustic Soda GACl22. Para Hydroxy Benzaldehyde Inhouse23. Toluene Imported / Hindustan Organics Chemicals/

Reliance24. Sodium Borohydride Rohm and Hass, Europe25. Mixed Xylene Reliance Ltd26. Para Hydroxy Benzaldehyde Inhouse27. Ortho Chloro benzaldehyde Imported china28. Sodium Sulphite Commodities29. 2,4 Dichloro Benzaldehyde Tessenderlo , Italy30. Propiophenone China31. Sodium Cyanide GACl,Dahej32. 2-Chloro Phenyl Acetic Acid China33. Ortho Hydroxy Phenyl Acetic Acid Inhouse34. Salicylamide Imported, China35. Mono Chlorobenzene Deepak Nitrite36. Thionyl Chloride lANXESS India, Naqda37. Ortho Methyl Phenyl Acetic Acid China38. Chlorine Andhra Suqars, Tanuku39. 2,6 Dichloro Benzaldehyde Tessenderelo , Italy40. Nitric Acid 60% Deepak41. 2-Amino-2-Phenyl Butyric Acid China42. Formic Acid GNCF43. Formaldehyde 37% local Commodities44. Methyl-2-Dimethylamine-2-Phenyl China

Butyrate45. Vitride 70% in Toluene Rohma Hass

67

Sr. Name of Raw Material SuppliersNo.46. Pivalic Acid China47. Ammonia Deepak48. Phathalic Anhydride Thirumallai49. Rany Nickel (Catalyst) Moranch50. Hydrogen GACl51. Anisole Inhouse - Phenol52. Phenetole Inhouse -Phenol53. Hydrobromic Acid (48%)w/w Solaris54. Veratrole Inhouse55. Sodium Thiosulphate local Commodities

68

APPENDIX - 2.4

MANUFACTURING PROCESS& MASS BALANCE

MANUFACTURING PROCESS

List of Raw Materials:

Sr. No. List of Raw Materials Batch Qty. (Kg)

1. Zinc Bromide 70% 6000 Kg = 42000 Kg (100%)

2. Caustic Soda 1600 Kg

3. Water 4800 Ltrs

A] REACTION:

ZnBr + 2 NaOH Zn (OH)2 + 2 NaBr

Zinc Bromide Caustic Soda Zinc Hydroxide Sodium Bromide M.W. = 224 M.W. = 2 X 40 M.W. = 99 M.W. = 224

= 80 = 208

B] BRIEF PROCESS:

Charge:

• 4800 Ltrs water, add under stirring.

• 1600 Kg Sodium Hydroxide Flakes stirred to dissolve completely.

Add:

6000 Kg Zinc Bromide Solution (70%) from top in 3 Hrs, stir well for 1 Hrs & centrifuged washed with 100 Ltrs water.

Output:

• Sodium Bromide 40 % solutions 9750 Kg.

• Zinc Hydroxide (wet Cake 30% moisture content) 2650 Kg.

1. SODIUM BROMIDE / ZINC HYDROXIDE / ZINC OXIDE

[Solid NaBr / NaBr Liquid 40%]

2. DI ISOPROPYL ETHYL AMINE [DIPEA]



1. DI Isopropyl Amine [DIPA] 3030 Kg

2. DI Ethyl Sulphate [DES] 2100 Kg

3. Caustic Soda Flakes (47%) 1160 Kg = 545 Kg on 100%

4. Water 400 Ltrs

A] REACTION:

C3H7 C3H7 2NH + (C2H5)2SO4 + NaOH 2N C2H5 + NaHSO4 + H2O C3H7

C3H7

B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

Charged Isopropyl Ethyl Amine & Diethyl Sulphate stirred well, then slowly added from the top caustic solution after completion of addition, heated for 3 Hrs. allow it to settle. Separate aqueous layer & organic layer. Organic layer is taken for recovery of DIPA & fractional distillation of DIPEA

Di Isopropyl Amine

M.W. = 2 X 101 = 202

Di Ethyl Sulphate

M.W. = 154

Caustic Soda M.W. = 40

Di Isopropyl Ethyl Amine

M.W. = 2X 129 = 258

Sodium Bi Sulphate

M.W.= 120

Water M.W.= 18

Caustic Soda Solution (47% 1160 Kg) (100% 545 Kg)

Water 400 Ltrs

Recovery of DIPA 570 Kg

Aqueous Layer 2940

Kg 150 Kg Pitch

Output 3030 Kg

Distillation Of

3750 kg organic layer

Ethylation

Di Isopropyl Amine (3030

Di Ethyl Sulphate (2100 Kg)

3. METHYL-2-CHLORO PHENYL ACETATE



1. 2-Chlorophenyl Acetic Acid 1000 Kg

2. Methanol 500 Kg

3. Sulphuric Acid (98%) 50 Kg

4. Sodium Carbonate 3 Kg Solution

12 Kg

5. Water

A] REACTION:

+ CH3OH B] BLOCK DIAGRAM:

CH2COOH

Cl

CH2COOH

Cl H2SO4

OCPA M.W. = 170.5

Methanol M.W = 32

Methyl-2-Chlorophenyl Acetate

M.W. = 184.5

Aqueous Layer 15 Kg

180 Kg

Waste Sulphuric Acid 165 Kg

Sulphuric Acid (98% 50 Kg)

Methanol 500 Kg

2-Chlorophenyl Acetic Acid 1000 Kg

Pitch 55 Kg

1030 Kg Pure

99.5%

Sodash Solution (15 Kg)

Methyl-2-Chlorophenyl Acetic Acid Distillation

Esterification

Methanol Recovered 300 Kg (Recycled)

4. 4-METHOXY PHENYL ACETONE

C] BRIEF PROCESS:

Charged Methanol, 2-Chlorophenyl Acetic Acid & Sulphuric Acid. Start heating, maintain reflux temperature for 4 Hrs. Start recovery of excess of Methanol which is recycled in the next batch. Allow it to settle. Separate aqueous Sulphuric Acid then add Sodium Carbonate solution to neutralize the mass, separate aqueous layer. Organic material taken for distillation.

•

List of Raw Material


1. 4-Methoxy Benzaldehyde / P-Anisaldehyde 1000

2. 2-Chloro Methyl Propionate 975

3. Sodium Methoxide (Powder) 440

4. Sulphuric Acid (98%) 400

5. Caustic Soda Flakes 300

6. Water 1750

A] REACTIONS:

CH + CH3 CH COOH3 + NaCl +CH3OH + NaOH + CH3OH

H3CO

CHO NaCOH3

Sodium Methoxide

M.W. = 122.5

H3CO

CH3 CH C COOH3

O

Para Anisaldehyde M.W. = 136

Methyl-2-Chloro Propionate

M.W. = 122.5

Epoxy Ester M.W. = 222

Sodium Chloride

M.W. = 58.5

Methanol M.W. = 32

1)

2)

Epoxy Ester M.W. = 222

H3CO

CH3 CH C COOH3

O

H3CO

CH3 CH C COONa

O


Glycidic Acid Sodium Salt M.W. = 230

Methanol M.W. = 32

2 + H2SO4 2 X + Na2SO4 2 X 2 X + CO2 B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

2-Chloromethyl Propionate is charged along with Para-Anisaldehyde under stirring. Reaction mass is cooled & Sodium Methoxide is charged lot-wise. After completion of addition stirred for 3-4 Hrs till reaction is completed. Add Caustic Soda solution & material is heated to reflux. Dilute sulphuric acid is added slowly till pH is 2. Reaction mass is maintained at reflux temperature till completion of reaction. Allow it to settle to remove aqueous layer. Organic layer is taken for distillation to get pure 4-Methoxy Phenyl Acetone.

3)

H3CO

CH3 CH C COONa

O

Glycidic Acid Sodium Salt

M.W. = 2x 230 = 460

H3CO

CH3 CH C COOH

O

Sulphuric Acid M.W. = 98

Glycidic Acid M.W. = 2 X 208 = 416

Sodium Sulphate M.W. = 142

4)

H3CO

CH3 CH C COOH

O

CH2 C CH3

O

H3CO

Glycidic Acid M.W. = 2 X 208 = 416

4- Methoxy Phenyl Acetate

M.W. = 2 X 164 = 328

Carbon Dioxide

M.W. = 44

Aqueous Layer 2827 Kg

Sodium Methoxide 440 Kg

2- Chloromethyl Propionate

975 Kg

Para Anisaldehyde 1000 Kg

Pitch 200 Kg

4-Methoxy Phenyl Acetate 1000 Kg

Pure 99%

Hydrolysis of Ester

Epoxidation

Distillation

Methanol 515 Kg

400 Kg 98% +

Decarboxylation & Separation of

Aqueous Layer

CO2 323 Kg

Dilute Sulphuric Acid (80%)

100 Ltrs Water Caustic Soda

300 Kg +

Water 1650 Ltrs

5. 2, 3-DICHLORO PYRIDINE

FOR STEP I & II


FOR STEP III


1. (35-37% w/w) Hydrochloric Acid 400

2. Sulphuric Acid 42

3. Cupric Chloride Dihydrate 42

4.

5.

Sodium Hydroxide Flakes Water

835

1570 A] REACTIONS:

STEP- I CHLORINATION OF 3-AMINO PYRIDINE:

+ HCl + H2O2 + 2H2O N N

STEP- II DIAZOTISATION OF 3-AMINO-2-CHLOROPYRIDINE:

+ NaNO2 + + 2H2O + NaCl N N


1. 3-Amino Pyridine 250

2. Hydrochloric Acid [35-37% w/w] 2500

3. Hydrogen Peroxide [50% w/w] 194

4.

5.

Sodium Nitrite [NaNO2] Water

194

420 6. Water 1750

31 % soln

40% w/w

NH2 NH2

Cl

3-Aminopyridine M.W. = 94.12

Hydrochloric Acid

(35-37%) M.W. = 36.5

Hydrogen Peroxide

(50% w/w) M.W. = 34

3-Amino-2- Chloropyridine M.W. = 128.56

Water M.W. = 18

NH2

Cl

N NCl

Cl

Sodium Nitrite

M.W. = 69

3-Amino-2- Chloropyridine M.W. = 128.56

2HCl

0-5°C

Diazonium Salt Water

M.W. = 18 Sodium Chloride

M.W. = 58.5

B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

� STEP – I CHLORINATION OF 3-AMINO PYRIDINE:

3-Amino Pyridine is treated with Hydrochloric Acid [35% - 37% w/w] and Hydrogen Peroxide [50% w/w].

� STEP – II DIAZOSATION OF 3-AMINO-2-CHLOROPYRIDINE:

3-Amino-2-Chloropyridine formed in above step is treated with Sodium Nitrite solution. Diazonium Salt formed.

� STEP – III DECOMPOSITION OF DIAZONIUM SALT INTO 2, 3

DICHLOROPYRIDINE

Diazonium Salt is further reacted with previously heated solution of salt and acid. The evolved Nitrogen gas is scrubbed. On addition of (40% w/w) caustic solution to adjust pH 7-7.5 pass stream and product 2, 3-dichloropyridine starts distillating out along with steam water.


1. Para Cresol 1080

2. Air (Oxygen) 320 3. Caustic Soda 65 4. Water 2000 5. Hydrochloric Acid 30% 200

Hydrochloric Acid (30%)

400 Kg

Decomposition of Diazonium Salt

Sulphuric Acid

(80%)

Cupric Chloride 42 Kg

Caustic Soda 835 Kg

Mother Liquor 125 Kg for IPA recovery IPA recovered 50 Kg Bottom Discarded 75 Kg

Isopropyl Alcohol 75 Kg

Crystallization of 2, 3-

Dichloro-pyridine 300 Kg

Aqueous Effluent 4408 Kg

2, 3-Dichloropyridine wet 320 Kg

+ Water 1875 Ltrs.

(Recycled)

2, 3-Dichloropyridine

250 Kg Dry

Steam Distillation

Hydrogen Peroxide (50%) 194 Kg

3-Amino Pyridine 250 Kg

Hydrochloric Acid (30%) 2500 Kg

Chlorination

210 Kg Water +

NaNO2 194 Kg

Diazotisation

420 Kg Water

N2 gas 74 Kg

Water 1570 Kg


400 Kg

Decomposition of Diazonium Salt

Sulphuric Acid

(80%)

Cupric Chloride 42 Kg

Caustic Soda 835 Kg

A] REACTION:

Para + Air [2(O)] P-Hydroxy + P-Hydroxy + Water Cresol Benzaldehyde Benzoic Acid B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

Para Cresol along with catalyst and water is fed continuously to the oxidation reactor and air is passed at desired temperature. After maintaining period, material is continuously withdrawn from the oxidation reactor at fixed interval. The material is further treated with dilute Caustic Soda Solution to remove p-Hydroxy Benzoic Acid. The slurry is fed to centrifuge washed & dried to get p-Hydroxy Benzaldehyde. The alkali aqueous layer is neutralized with Hydrochloride acid 30% and precipitated p-Hydroxy Benzoic Acid is centrifuged, washed & dried.

Aqueous effluent 2165 Kg

Water

500 Kg

P-Hydroxy Benzaldehyde

1000 kg

Centrifuging 1300 Kg

Drying

Water 1500 Kg

Caustic Soda 5 Kg

Alkali

Treatment Oxygen (Air) 320 Kg

Para Cresol 1080 Kg

Oxidation

Aqueous Layer for P-Hydroxy Benzoic

Acid Recovery

Acidification by HCl 30% 200 kg

P - Hydroxy Benzoic Acid

200 kg

6. 2-AMINO-2-PHENYL BUTYRIC ACID


A] REACTIONS:

1)

+ NaCN + 2NH4HCO3 + NaHCO3 + NH4OH + H2O

2)

+ NaOH + 2H2O + NH4HCO3

3)

+ HCl + NaCl


Moles Per Mole

1. Propiophenone 550 Kg = 4.10 1

2. Methanol 700 Kg

3. Ammonium Bicarbonate 660 Kg = 8.35 2.036

4. Sodium Cyanide 225 Kg = 4.59 1.12

5. Acetic Acid 135 Kg = 2.25 0.55

6. Water 800 Kg + 1725 kg

7. Sodium Hydroxide Flakes 675 Kg = 16.87 4.11

8. Hydrochloric Acid (30% w/w) 2000 Kg 600 Kg (100 %)

= 16.44 4.00

O II C – C2H5

HN O C C O

C2H5 C NH

Propiophenol M.W. = 134

Sodium Cyanide

M.W. = 49

Ammonium Bicarbonate

M.W. = 2 X 79 = 158

5-Phenyl-5- Ethyl Hydention

M.W. = 204

Sodium Bicarbonate M.W. = 84

Ammonium Hydroxide M.W. = 34

Water M.W. = 18

HN O C C O

C2H5 C NH

5-Phenyl-5- Ethyl Hydention

M.W. = 204


Water M.W. = 2X 18 = 36

Sodium Salt 9, 2- Amino- 2- Phenyl

Butyric Acid M.W. = 201

Ammonium Bicarbonate M.W. = 79

COONa C2H5 C NH2

COONa C2H5 C NH2

Sodium Salt 9, 2- Amino- 2- Phenyl

Butyric Acid M.W. = 201

COOH C2H5 C NH2

Hydrochloric Acid M.W. = 36.5

2-Amino -2- Phenyl Butyric Acid M.W. = 179

Sodium Chloride M.W. = 58.5

B] BLOCK DIAGRAM:

STAGE – II

C] BRIEF PROCESS:

Charge in to autoclave, Propiophenone, Methanol, Ammonium Bicarbonate, Sodium Cyanide, Water. Close the autoclave. Heat to get desire temperature & pressure. After completion of reaction, material is acidified to adjust pH 7.0 then centrifuged to get 5-Phenyl-5-Ethyl Hydention. It is further treated in autoclave with Caustic Soda solution. It is further neutralized with 30% HCl to adjust pH 7.0 to 7.5. It is then centrifuged washed with water, dried to get 2-Amino-2-Phenyl Butyric Acid.

Drying 800 Kg

2 –Amino, 2- Phenyl Butyric Acid

Centrifuging

Neutralization

7.0

HCl 30% 2000 Kg

Water 200 Ltrs

Aqueous Layer

4600 Kg

Water Vapour 150 Kg

650 Kg Dry 2 –Amino, 2- Phenyl

Butyric Acid

Caustic Soda 675 Kg

1000 Kg 5-Phenyl -5-Ethyl Hydention

Autoclave

Aqueous Layer

2070 Kg

Centrifuging

Water 300 Ltrs

Ammonium Bicarbonate 660Kg

Propiophenone 550 Kg

Neutralization

7.75

Acetic Acid 135 Kg

Sodium Cyanide 225 Kg

Water 500 Ltrs

Autoclave

Water 1525 Kg

7. ORTHO HYDROXYL PHENYL ACETIC ACID /

2-HYDROXY PHENYL ACETIC ACID


A] REACTIONS:

1)

+ 3NaOH + NaCl + 2H2O 2)

+ 2 HCl + 2NaCl

3)

NaOH + HCl NaCl + H2O


1. 2-Chloro Phenyl Acetic Acid 1000

2. Caustic Soda Flakes 940

3. Copper Sulphate.7H2O 40

4. Hydrochloric Acid (30% w/w) 2850

5. Water 2200

CH2COOH

Cl

CH2COONa

ONa

Ortho Chloro Phenyl Acetic

Acid

Caustic Soda M.W. = 3 X 40 = 120

Sodium Salt of 2-Hydroxy Phenyl

Acetic Acid M.W. = 196

Sodium Chloride

M.W. = 58.5

Water M.W. = 2 X 18 = 36

CH2COONa

ONa

CH2COONa

ONa

Sodium Salt of 2-Hydroxy Phenyl

Acetic Acid M.W. = 196

Hydrochloric Acid

M.W. = 2X 36.5 = 73

2-Hydroxy phenyl Acetic Acid M.W. = 152

Sodium Chloride

M.W. = 2 X 58.5 = 117

Hydrochloric Acid

M.W. = 36.5

Sodium Chloride

M.W. = 58.5

Water M.W. = 18


B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

In autoclave charge water, caustic Soda flakes, Copper Sulphate.7H2O and Orthochloro Phenyl Acetic Acid and heated till desire pressure is reached.

Reaction temperature is maintain till completion of reaction. Autoclave is cooled and material transferred to neutralization tank. The hydrochloric Acid is added till pH 6.5 to 7.0 and allowed to settle. The bottom Copper sludge is separated. The material is further neutralized to pH 2. It is then cooled to 200C.It is then cooled to 200C. It is centrifuged, washed with water, dried to get

Drying Wet cake 900 Kg

Water 200 Kg

Aqueous Layer

6070 Kg

Centrifuging

HCL 30% 650 Kg

IInd

Neutralize Solution

pH 2.0

Copper Sulphate.7H2O 40 Kg

Caustic Soda Flakes 940 Kg

2 chlorophenyl Acetic Acid 1000 Kg

Autoclave Pressure 14-16 Kg


2200 Kg

Ist Neutralize Solution

6.5 to 7.0 Water 2000 Ltrs

750 Kg 2-Hydroxy Phenyl Acetic Acid

Water Vapour 150 Kg

8. 2-COUMARANONE


A] REACTION:

+ 2 + H2O B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

Ortho Hydroxy Phenyl Acetic Acid is charged into reactor and heated to 150° C to distilled out water of reaction. Vacuum is applied and crude 2-Coumanone is distilled to get pure 2-Coumanone

Sr. No. List of Raw Material Batch Qty. (Kg)

1. Ortho Hydroxy Phenyl Acetic Acid 750

CH2COOH

OH CH2 C O O

2-Hydroxy Phenyl Acetic Acid M.W. = 152

2-Coumaranone M.W. = 134

Water M.W. = 18

Ortho Hydroxy Phenyl Acetic Acid 750 Kg

100 Kg water Vapour

30 Kg Pitch

620 Kg 2-Coumaranone

Distillation of

Crude 2-Coumaranone

Dehydration

9. 3- ISO CHROMANONE


A] REACTIONS:

1)

+ Cl2 + HCl 2)

+ NH4OH + NH4Cl


1. Ortho Methyl Phenyl Acetic Acid 1000

2. Mono Chlorobenzene 1500

3. Catalyst 20

4. Chlorine 408

5. Ammonia 840

6. Water 2000

7. Toluene 600

CH3

CH2OOH

CH2 Cl

CH2OOH

Ortho-methyl Phenyl Acetic Acid

M.W. = 150

Chlorine M.W. = 71

2- Chloromethyl Phenyl Acetic Acid

M.W. = 184.5

Hydrochloric Acid

M.W. = 36.5

CH2 Cl

CH2OOH CH2 O C O CH2

2- Chloromethyl Phenyl Acetic Acid

M.W. = 184.5

Ammonia

3- Iso Chromanone M.W. = 148

Ammonium Chloride

M.W. = 53.5

B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

Charge into glass lined reactor 2-Methyl Phenyl Acetic Acid, Mono Chlorobenzene and Catalyst .chlorine is pass at 900C till desire conversion is obtained. The evolved hydrochloric acid is scrubbed in to water. After completion of reaction nitrogen is purged to remove HCl from the system. Material is cooled to 250C and ammonia solution is added till pH 6.5 -7. After reaching pH 6.5 -7 organic layer is separated & washed with water, unreacted 2-Methyl Phenyl Acetic Acid is recovered by acidification of aqueous layer. Organic layer is distilled to recovered MCB. The bottom left material 3-IC is distilled under high Vaccum and further crystallized in Toluene. Toluene is recovered from mother liquor by distillation.

Toluene (550 Kg) Toluene recovered (400 Kg)

Crude 3-IC (25 Kg)

600 Kg 3-Iso Chromanone

99.5

Centrifuging &

Drying

Crystallization

625 Kg

Toluene 600 Kg

Pitch 60 Kg

3- Iso Chromanone

Distillation

MCB (Recovered) 1300 Kg

MCB Recovery by Distillation

Cyclisation pH 6.8-7.0

840 Kg Ammonia (25%)

Water 2000 Kg

Chlorine 408 Kg

Mono Chloro Benzene 1500 Kg

Ortho methyl phenyl Acetic Acid 1000 Kg

Chlorination


210 Kg

Catalyst 20 Kg

N2

Aqueous effluent 3298 Kg

10. 2, 6- DICHLORO BENZOYL CHLORIDE


A] REACTIONS:

1)

+ HNO3 + HNO2 2)

+ NaOH + H2O 3)

+ HCl + NaCl

4)

+ SOCl2 + SO2 + HCl

Sr. No. List of Raw materials Batch Qty. (Kg)

1. 2,6 Dichloro Benzaldehyde 900 2. Nitric Acid 60% 1350 3. Sodium Hydroxide Flakes 230 4. HCl 30% 650 5.

Thionyl Chloride 1170

Thionyl Chloride (Recovered) 500 Thionyl Chloride (Consumption) 670

6. Water 650

CHO

Cl Cl

COOH

Cl Cl

2, 6 Dichloro Benzaldehyde

M.W. = 175

Nitric Acid M.W. = 63

2, 6 Dichlorobenzoic Acid

M.W. = 191

Nitrous Acid

COOH

Cl Cl

COONa

Cl Cl


M.W. = 63

Sodium Hydroxide M.W. = 40

2, 6 Dichlorobenzoic Acid Sodium Salt

M.W. = 213

Water M.W. = 18

COONa

Cl Cl

COOH

Cl Cl

2, 6 Dichlorobenzoic Acid Sodium Salt

M.W. = 213

Hydrochloric Acid M.W. = 40


M.W. = 191

Sodium Chloride M.W. = 58.5

COOH

Cl Cl

COOH

Cl Cl


M.W. = 191

Thionyl Chloride

M.W. = 119

2, 6 Dichlorobenzoyl Chloride

M.W. = 209.5

Sulphur Dioxide

M.W. = 64

Hydrochloric Acid

M.W. = 36.5

B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

� STEP – I : OXIDATION OF 2,6 DICHLORO BENZALDEHYDE

2, 6 Dichloro Benzaldehyde is treated with nitric acid 60%.The evolved nitric acid is Scrubbed into caustic soda solution to get sodium nitrite solution which is sold in the market. The 2, 6 Dichloro Benzoic acid formed is cooled & centrifuged. It is further neutralized with caustic soda solution, clarified and neutralized with Hydrochloric acid 30%. The Precipitated 2, 6 Dichloro Benzoic acid is centrifuge, washed with water & dried.

� Step – II

The dry 2, 6 Dichloro Benzoic acid is further treated with Thionyl Chloride. The

evolved gas of Sulphur Dioxide is scrubbed in to caustic soda solution and Hydrogen Chloride gas is scrubbed in to water scrubber. After completion of reaction excess Thionyl Chloride is distilled & recycled and bottom material is Vaccum distilled to get pure 2, 6 Dichloro Benzoyl Chloride.

HCl 215 Kg

Distillation

SO2 390 Kg

2, 6 DCBA 950 Kg

Drying 950 Kg

Water 30 Kg

1505 Kg Aqueous to ETP

Centrifuging 2, 6 DCBA wet cake 980 Kg

Water 150 Kg

Thionyl Chloride

Pitch 190 Kg

Thionyl Chloride 500 Kg

Recycled

Pure 2, 6

Dichloro Benzoyl Chloride

Caustic Soda 230 Kg

Acidification pH 6.5-7.0

Water 500 Kg

1030 Kg Nitric Acid 48% Recycled

Neutralization 2, 6 DCBA

980 Kg

HCl 30% 650 Kg

2, 6 Dichlorobenzaldehyde

900 Kg

Centrifuging

Nitrous acid 240 Kg

Nitric Acid 60% w/w 1350 Kg

Oxidation

11. METHYL – 2 – DIMETHYL AMINO – 2 – PHENYL BUTYRATE

A] REACTIONS:

1)

+ (CH3)2SO4 + H2SO4 2)

+ HCOOH + CH2O + CO2 + H2O

Sr.

No.

List of Raw Materials Batch Qty. (Kg)

Moles Per Mole

1. 2-Amino-2-Phenyl Butyric Acid 1000 = 5.586 1

2. Toluene 1800

3. Dimethyl Sulphate 760 = 6.03 1.079

4. Sodium Hydroxide Flakes 40 = 1.0

5. Formic Acid 800 = 14.78 2.646

6. Formaldehyde 37% w/w 407 Kg 100% 1100 = 13.56 2.427

7. Water 1800

COOH

NH2 C C2H5

COOCH3

NHCH3 C C2H5

2-Amino - 2 – Phenyl Butyric

Acid M.W. = 179

Dimethyl Sulphate

M.W. = 126

Methyl -2 – Mono Methyl Amine-2-Phenyl Butyrate

M.W. = 207

Sulphuric Acid M.W. = 98

COOCH3

NHCH3 C C2H5

COOCH3

N(CH3)2 C C2H5

Methyl -2 – Mono Methyl Amine-2-Phenyl Butyrate

M.W. = 207

Formic Acid

M.W. = 46

Formaldehyde M.W. = 30

Methyl-2-Dimethyl Amino – 2 –

Phenyl Butyrate M.W. = 221

Carbon Dioxide

M.W. = 44

Water M.W. = 18

Toluene

B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

In a reactor, Toluene, 2-Amino-2-Phenyl Butyric Acid and Dimethyl Sulphate is charged.

After completation of reaction. Water is added. Organic layer is separated and neutralized with caustic soda solution to pH 7 to 7.5.Organic layer is mixed with Formaldehyde solution 37 %,formic acid 85% and reflux till completation of reaction. Aqueous layer is separated and washed with water and neutralized with Caustic soda solution. Toluene is recovered by distillation and recycled. The Bottom material is Vaccum distilled. Pitch is drained.

Aqueous Effluent 1600 Kg

NaOH 10 Kg Water 300 Kg 2-Amino-2-Phenyl

Butyric Acid 1000kg

Vaccum Distillation

Pitch 40 Kg

1000 Kg Methyl-2-Dimethyl Amino-2-Phenyl

Butyrate

Toluene 1600 Kg Recycled

Toluene 1800 Kg

Esterification & Methylation

Dimethyl Sulphate 760 Kg

Caustic Soda 30 Kg

Methylation

Water 1500 Kg

Neutralization pH 7-7.5

Formaldehyde 37% 1100 Kg

Aqueous Layer

2370 Kg

Formic Acid 800 Kg

CO2 490 kg

12. 2- DIMETHYL AMINO – 2 – PHENYL BUTANOL


A] REACTION:

B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

In a S.S. reactor, toluene is charged along with Methyl-2-Dimethylamine-2-Phenyl Butyrate. Vitride 70% is added from the top slowly. After completion of addition reaction is maintain till completion. The effluent of Vitride is decomposed by addition of Caustic soda solution. The organic layer is separated. Toluene is recovered by distillation and Product is drained from the bottom.


1. Methyl-2-Dimethylamine-2-Phenyl Butyrate

550

2. Toluene 720 3. Toluene (R) 870 4. Vitride 70% in Toluene Vitride 750 + Toluene 320

=1070 5. Sodium Hydroxide Flakes 280 6. Water 2000

COOCH3

N(CH3)2 C C2H5

CH2OH

N(CH3)2 C C2H5

7% Vitride

Methyl-2-Dimethyl Amino-2-Phenyl

Butyrate

2-Dimethyl Amino-2-Phenyl Butanol

Toluene (R) 870 Kg recycled

2-(Dimethyl Amino)-2-Phenyl Butanol 430 Kg

Toluene Recover

Sodium Hydroxide 280 Kg

Aqueous Layer

3150 Kg

Toluene 720 Kg

Methyl-2-Dimethyl Amino-2-Phenyl Butyrate 550 Kg

Vitride 70% 1070 Kg

Water 2000 Kg

Reduction

13. 4 – BROMO ANISOLE


A] REACTION:

+ HBr + H2O2 + 2 H2O

B] BLOCK DIAGRAM:

Sodium thiosulphate solution 10 kg water vapor 525 kg

Anisole 1000 kg Hydrobromic Acid 48% 1625 kg Hydrogen Peroxide 30% 1250 kg 2030 kg 550 kg 160 kg filter


1. Anisole 100

2. HBr 1625 3. Hydrogen Peroxide 50%

750 Mixed to get 30% w/w

1250 Kg 500 4. Water

5. Sodium Thiosulphate

25 Soln. 525 Kg 500 6. Water

OCH3

Bromination

Crude P. Bromo

Anisole 1845 Kg

Distillation of 1820 kg Crude P.

Bromo Anisole

Br

OCH3

Anisole M.W. = 108

Hydrobromic Acid

M.W. = 81

Hydrogen Peroxide

M.W. = 34

P. Bromo Anisole

M.W = 187

Water M.W = 2 X 18

= 36

14. 4 - BROMOPHENETOLE

C] BRIEF PROCESS:

In the glass lined reactor anisole and Hydrobromic Acid (48%) is charged. The materials are cooled to 50C and then add slowly Hydrogen peroxide (30%) solution. Reaction is exothermic. Chilling is required. Temperature is controlled between 10-120C throughout the addition of Hydrogen peroxide solution after completion of reaction. Material is stirred at 10-150C for 1 hr check completion of reaction. conversion repeated is above 99%. If it is less then stirred 1 hr more. After completion of reaction material allowed to settle. Separate out bottom organic material for aqueous layer. Organic material recharged and washed with 5% sodium Thiosulphate solution till colour changes to light yellow. Material is allowed to settle. separate Organic layer for aqueous layer and taken for Vacuum distillation to get pure form.


A] REACTION:

+ HBr + H2O2 + 2H2O


1. Phenetole 1000 2. Hydrobromic Acid (HBr) [48%

w/w] 1450 = 696 Kg (100%)

3. Hydrogen Peroxide (H2O2) [50% w/w]

670 = 335 Kg (100%) 30% soln. 430 4. Water

5. Sodium Thiosulphate 25 6. Water 500

OC2H5

Br

OC2H5

Phenetole M.W. = 122.17

Hydrobromic Acid

M.W. = 81

Hydrogen Peroxide

M.W. = 34

Para – Bromo Phenetole

M.W. = 201.06

Water M.W. = 2 X 18

= 36

B] BLOCK DIAGRAM:

C] BRIEF PROCESS:

In a glass lined reactor, Phenetole and Hydrobromic acid (48 %) are charged. The material is cooled to 50C and then add slowly Hydrogen Peroxide (30 % w/w) solution. Reaction is exothermic. Chilling is required. Temperature controlled between 10-120C throughout the addition of Hydrogen peroxide solution. After completion of reaction material is stirred at 10-150C for 1 hr. Check completion of reaction. Conversion expected is above 99%. If it is less than that stirred 1hr more. After completion of reaction material is allowed to settle. separate out bottom organic material from aqueous layer. Organic material is recharged and washed with 5% w/w sodium thiosulphate solution. Till colour changes to light yellow material is allowed to settle. Separate organic layer from aqueous layer and taken for vacuum distillation to get pured form.

List of Raw materials:

Sr.

No.

Name of Raw Material Batch quantity

in Kg

1 2,4-Dichloro benzyl chloride 2000 2 Triethyl amine 20

3 Sodium cyanide 500 4 Water 4844

5 Toluene 1000 6 Sodium Hydroxide 486

7 Conc. HCl 1800 9 Thionyl chloride 944

1450 Kg P – Bromophenetole Pure 99%

Hydrogen Peroxide 30% w/w) 1100 Kg

Phenetole 1000 Kg

2, 4 – Dibromophenetole Pure 175 Kg

22 Kg Pitch

Distillation of 2, 4- Dibromo

Phenetole

2, 4- Dibromo Phenetole

197 kg

Crude P - Bromo – Phenetole 1657 Kg

10 Kg Water Vapour

Hydrobromic Acid (48% w/w) 1450 Kg

Sodium thiosulphate solution (5% w/w) 525 Kg

550 Kg Aqueous effluent

Bromination

Crude P - Bromo – Phenetole 1682 Kg

1868 Kg Aqueous effluent

15. 2, 4 – DICHLORO PHENYL ACETYL CHLORIDE

A] REACTIONS:

Stage I: Cyanation

Cl

Cl

Cl

2,4-Dichloro benzyl chloride,MW=195.5

+ NaCN

sodium cyanide,MW=49

Cl

Cl

CN

(2,4-dichlorophenyl)acetonitrile,MW=186

+ NaCl

Sodium Chloride,MW=58.5

Toluene

water,TEA

Stage II: Hydrolysis

Cl

Cl

CN

(2,4-dichlorophenyl)acetonitrile,MW=186

NaOH,Toluene

Cl

Cl

COONa

(2,4-dichlorophenyl)acetic acid sodium salt,MW=227

+ NH3

Ammonia,MW=17

HCl

Cl

Cl

COOH

(2,4-dichlorophenyl)acetic acid,MW =205

+ NaCl

Sodium Chloride,MW =58.5

Stage III: Chlorination

Cl

Cl

COOH

(2,4-dichlorophenyl)acetic acid,MW=205

+ HCl(g)

Hydrochloric acid,MW=36.5

SOCl2

Cl

Cl

COCl

(2,4-dichlorophenyl)acetyl chloride,MW=223.5

+ SO2(g)

Sulfur dioxide,MW=64

B] FLOW CHART:

Stage I :Cyanation

4)Sodium cyanide solution(500 kg in 2000 kg water)

1)Toluene(1000 Kg)

2)2,4-dichloor benzyl chloride(2000 Kg)

3)Triethyl amine(20 Kg) 5)Sodium Hypoch

(10% 100 Kg)

6)recovered toluene(950 Kg)

7)Pitch(150 kg)

Cyanation

Organic layer Aqueous waste

contains excess sodium

cyanide

Aqueous waste after

hypo treatment (2620

kg)

Organic layer

Crude

Pure Stage I (1800 kg)

Stage II (Hydrolysis)

1)Water(1944 Kg) 4)Ammonia gas(157 Kg)

2)Sodium Hydroxide(486 Kg)

3)Stage I(1800 Kg)

5)HCl(1800 Kg)

6)Water washing(900 Kg) 7)Waste aqueous

layer(5183 Kg)

Stage III (chlorination)

1)Thionyl chloride (944 Kg) 3)Sulfur dioxide gas(496

kg)

2)Stage II(1590 Kg) 4)HCl gas(283 Kg)

5)Pitch (165 Kg)

Hydrolysis

Isolation

Filtration

Stage II(1590 kg)

Chlorination

Distillation

Crude

Pure (1590 Kg)

C] BRIEF PROCESS:

Stage I : Cyanation

2,4 dichloro benzyl chloride is coverted into cyanide by using sodium cyanide and toluene as a solvent and triethyl amine as a base.The product is isolate by layer separation.The organic layer is distilled out to recover toluene followed by fractional distillation gives pure product stage I as (2,4-dichlorolphenyl)acetonitrile.The aqueous layer contains extra sodium cyanide is destroyed by using sodium hypochlorite as a oxidizing agent.

Stage II : Hydrolysis

Stage I is hydrolyzed to acid using sodium hydroxide as a hydrolyzing agent.The product is

isolated by acidifying with hydrochloric acid and it is isolated by filtration followed by water

washing gives wet product which on drying gives stage II as a 2,4-dichloro phenyl acetic

acid.

Stage III: Chlorination:

Stage II i.e 2,4-dichloro phenyl acetic acid is converted into acid chloride using thionyl

chloride as a chlorinating agent.the liberated and hydrochloric acid gas is scrubbed into

water and sulphur dioxide gas into alkali scrubber which converts into sodium sulfite .The

product is isolated by fractional distillation gives pure product as 2,4-dichloro phenyl acetyl

chloride.


Sr.

No.


in Kg

1 P-xylene 1500 2 p-formaldehyde 1110 3 Conc. HCl 6095 4 Sodium carbonate 44 5 water 3669 6 Zinc Chloride 45 7 Sodium cyanide 470 9 Sodium Hydroxide 439

A] REACTIONS:

Stage I: Chloromethylation

CH3

CH3

p-Xylene,MW=106

+ HCHO

n

p-formaldehyde,MW=30

+ HCl

CH3

CH3

Cl

2-(chloromethyl)-1,4-dimethylbenzene,MW=154.6

+ H2O

water,MW=18

Stage II : Cyanation

CH3

CH3

Cl

2-(chloromethyl)-1,4-dimethylbenzene,MW=154.6

+ NaCN

Sodium cyanide,MW=49

CH3

CH3

CN

(2,5-dimethylphenyl)acetonitrile,MW=145

H2O,Toluene

+ NaCl


16. 2,5 – DIMETHYL PHENYL ACETYL CHLORIDE

Stage III: Hydrolysis

CH3

CH3

CN

(2,5-dimethylphenyl)acetonitrile,MW=145

NaOH,H2O

CH3

CH3

COONa

(2,5-dimethylphenyl)acetic acid sodium,MW=186

+ NH3

Ammonia,MW=17

HCl,MW=36.5,Toluene

CH3

CH3

COOH

(2,5-dimethylphenyl)acetic acid,MW=164

+ NaCl


Stage IV: Chlorination

CH3

CH3

COOH

(2,5-dimethylphenyl)acetic acid,MW=164

SOCl2

CH3

CH3

COCl

+ HCl

Hydrochloric acid,MW=36.5(2,5-dimethylphenyl)acetyl chloride,MW=182.6

+ SO2(g)

Sulfur dioxide,MW=64

B] FLOW CHART:

Stage I : Chloromethylation

4)Zinc chloride(45 Kg)

1)p-Xylene(1500 kg)

2)Conc. HCl(4665 Kg)

3)p-Formaldehyde(1110 Kg)

5)Sodium carbonate(30 kg) 7)waste aqueous layer

6)Water(300 Kg) 5630 kg

8)Recovered xylene

450 kg

9)Pitch

145 kg

1425 kg

Condensation

Isolation

Organic layer

Crude stage I

Pure stage I


4)Sodium cyanide solution(470 Kg in 1425 Kg water)

1)Toluene(712 kg)

2)Stage I(1425 Kg)

3)Sodium carbonate (14 kg) 5)Sodium Hypochlorite

(10 %, 300 Kg)

6)recovered toluene(676 Kg)

7)Pitch(150 Kg)

1254 Kg

Cyanation

Organic layer Aqueous waste

contains excess sodium

cyanide

Aqueous waste after

hypo treatment

Organic layer

Crude

Pure Stage II

Stage III : Hydrolysis

1)Water(1317 Kg) 4)Ammonia gas

2)Sodium Hydroxide(439 Kg) 125 Kg

3)stage II(1254 Kg)

5)HCl(1430 Kg)

7) Waste aqueous layer

3688 kg

1254 Kg

Isolation

Filtration

Wet stage III Drying

Dried stage III

Hydrolysis

Stage IV : Chlorination

1)Thionyl chloride(953 Kg)

2)Stage III(1254 Kg)

5)Pitch(140 Kg)

C] BRIEF PROCESS:

Stage I : Chloromethylation

P-xylene is chloromethylated using p-formaldehyde and concentrated hydrochloric acid and zinc

chloride as a catalyst.The product is isolated by separating organic layer, followed by sodium

carbonate washing to remove excess acidity.The organic layer is distilled out to remove p-xylene

followed by fractional distillation gives pure product stage I as 2-(chloromethyl)-1,4-dimethylbenzene


Stage I 2-(chloromethyl)-1,4-dimethylbenzene is coverted into cyanide by suing sodium cyanide and

toluene as a solvent.The product is isolate by layer separation.The organic layer is distilled out to recover toluene followed by fractional distillation gives pure product stage II as (2,5-dimethylphenyl)acetonitrile

Stage III : Hydrolysis

Stage II is hydrolyzed to acid using sodium hydroxide as a hydrolyzing agent.The product is isolated

by acidifying with hydrochloric acid and it is isolated by filtration followed by water washing gives

wet product which on drying gives stage III as a 2,4-dimethyl phenyl acetic acid.

Stage IV : Chlorination:

Stage III i.e 2,4-dimethyl phenyl acetic acid is converted into acid chloride using thionyl chloride as a

chlorinating agent.the liberated sulphur dioxide gas and hydrochloric acid gas is scrubbed into

scrubber. The product is isolated by fractional distillation gives pure product as 2,5-dimethyl phenyl

acetyl chloride.

Distillation

Crude

Pure

Packing

1300 kg

3)Sulfur dioxide(489

Kg)

NaOH scrubber

Sodium sulfite

HCl(275 Kg)

Chlorination


Sr.

No.


in Kg

1 2-chloro phenyl ethyl amine 2000

2 Ethanolamine 2800

3 Xylene 2800

4 Sodium Hydroxide 515

A] REACTION:

Cl

NH2

2-(2-chlorophenyl)ethanamine,MW=155.5

+ OH

NH2

Ethanolamine,MW=61

NH

2,3-dihydro-1H-indole,MW=119

OH

NH2 .HCl

Ethanolamine hydrochloride,MW=97.5

+ NaOH

sodium Hydroxide,MW=40

OH

NH2

Ethanolamine,MW=61

+ NaCl

Sodium chloride,MW=58.5

+ H2O

water,MW=18

CH4

17. INDOLINE

B] FLOW CHART:

3)Xylene(2800 Kg)

1) Ethanolamine(2800 Kg)

2)2-chloro phenylethylamine Sodium Hydroxide(515 kg)

(2000 kg)

Pitch(81 kg)

Recovered Xylene(2660 kg)

Fractional distillation

C] BRIEF PROCESS:

Brief Process:2-chloro phenyl ethylamine is cyclised to 3-indoline by using ethanolamie as a base.

The product is isolated by extraction in xylene followed by solvent distillation gives crude product

which on fractional distillation gives pure product. The by-product ethanolamine hydrochloride is

basified with sodium hydroxide liberates free base which is used in the next reaction.

Upper Organic Layer

Crude

Pure(1450 kg)

95% of theory

Bottom layer

Recovered

ethanolamine

2750 kg

Liquid aqueous waste

(421 Kg)

Cyclization


Sr.

No.


in Kg

1 Mandelonitrile(MN) 1320 Kg

2 Ethyl alcohol 912 kg

3 Hydrochloric acid gas 362 Kg

4 Wtaer for reaction 357 Kg

5 Toluene 660 Kg

6 Water for dissolution 660

A] REACTION:

H OH

CN

Mandelonitrile,MW=133

+Ethyl alcohol,water

Toluene

H OH

COOC2H5

Ethyl Mandalate,MW=180

NaOCl ,MW=74.5

O

O

OC2H5

Ethyl phenyl glyoxalate,MW=178

+ NH4Cl

Ammonium chloride,MW=53.5

HCl(g)

Hydrochloric acid,MW=36.5

+NaCl

Sodium chloride,MW=58.5

+H2O

Water,MW=18

18. ETHYL PHENYL GLYOXALATE (EPG)

B] FLOW CHART:

4)Hydrochloric acid gas(362 Kg)

1)Ethyl alcohol(912 kg) 5)recovered ethyl alcohol

2)Mandelonitrile(1320 Kg) (406 Kg)

3)Water(357 Kg)

6)Toluene(660 Kg)

7)water(660 kg) 8)Waste water(660 Kg)

Toluene (660 Kg) 9) Ammonium chloride

(534 Kg) for sell

10) Sodium hypochlorite(8000 kg) 11) Waste water (8824

Kg)

12)recoverd toluene

(627 Kg)

13)Pitch(83 Kg)

C] BRIEF PROCESS:

Mandelonitrile is reacted with hydrochloric acid and water and hydrolyzed to acid which is in-situ

esterfied with etyla alcohol to give ethyl mandalate. The excess ethyl alcohol is distilled out and re-

used in the next batchs. After that water and toluene is added ,water layer is separated which

contains ammonium chloride. Organic layer contains product is oxidized with sodium hypochlorite.

The organic layer is separated followed by tolune distillation gives crude ethyl phenyl glyoxalate

which on fractional distillation gives pure ethyl phenyl glyoxalate.

Organic Layer

Oxidation

Organic layer

distillation

Crude EPG

Pure EPG

1137 Kg

Organic Layer


Sr.

No.


in Kg

1 1-hydroxy cyclohexane carbonitrile 1000

2 Hydrochloric acid gas 292

3 Ethyl alcohol 736

4 Water for reaction 288

5 Toluene 500

6 Water for washing 500

A] REACTION:

NC OH

1-hydroxycyclohexanecarbonitrile,MW=125

HCl,C2H5OH

EtOOC OH

ethyl 1-hydroxycyclohexanecarboxylate,MW=172

+ H2O + NH4Cl

water,MW=18 ammonium chloride,MW=53.5

water,Toluene

19. ETHYL-1-HYDROXY CYCLOHEXANE CARBOXYLATE

B] FLOW CHART:

4)1-hydroxy cyclopentane carbonitrile(1000 Kg)


2Hydrochloric acid (292 Kg) (332 Kg)

3)Water(288 Kg)

6)Toluene(500 Kg) 8)Waste water(644 Kg)

7)water(500 kg) 9) Ammonium chloride

(428 Kg) for sell

10)Recovered toluene

(475 kg)

11)Pitch( 117Kg)

C] BRIEF PROCESS:

1-hydroxy cyclohexane carbonitrile is hydrolyzed with hydrochloric acid and esterifies with ethanol

in-situ gives desired product. The formed product is isolated by adding water followed by toluene

extraction. The aqueous layer is separated contains ammonium chloride and organic layer contains

product. The solvent is distilled out gives crude product which on fractional distillation gives ethyl-1-

hydroxy cyclohexane carboxylate.

Organic Layer

Organic layer distillation

Crude

Pure ethyl-1-hydroxy-

cyclohexane carboxylate

1320 Kg

Hydrolysis and

Esterification


Sr.

No.


in Kg

1 1-hydroxy cyclopentane carbonitrile 1000 Kg

2 Hydrochloric acid gas 329 kg

3 Ethyl alcohol 829 kg

4 Water for reaction 320 Kg

5 Toluene 500 Kg

6 Water for washing 500

A] REACTION:

HCl,C2H

5OH

+ H2O + NH4Cl

water,MW =18 ammonium chloride,MW =53.5

NC OH

1-hydroxycyclopentanecarbonitrile,MW =111

Toluene

OHEtOOC

ethyl 1-hydroxycyclopentanecarboxylate,MW -158

20. ETHYL-1-HYDROXY CYCLOPENTANE CARBOXYLATE

B] FLOW CHART:

4)1-hydroxy cyclopentane carbonitrile(1000 Kg)


2Hydrochloric acid (329 Kg)

3)Water(320 Kg) (375 Kg)

6)Toluene(500 Kg) 8)Waste water(662 Kg)

7)water(500 kg) 9) Amonium chloride (482

Kg) for sell

9)Recovered toluene

10) Recovered toluene

(475 Kg)

C] BRIEF PROCESS:

1-hydroxy cyclopentane carbonitrile is hydrolyzed with hydrochloric acid and esterifies with ethanol

in-situ gives desired product. The formed product is isolated by adding water followed by toluene

extraction. The aqueous layer is separated contains ammonium chloride and organic layer contains

product. The solvent is distilled out gives crude product which on fractional distillation gives ethyl-1-

hydroxy cyclopentane carboxylate.

Organic Layer

Organic layer

distillation

Crude

Pure ethyl-1-hydroxy-

cyclopentane carboxylate

1410 Kg

Hydrolysis and

Esterification

11)Pitch( 74Kg)


Sr.

No.


in Kg

1 2,3-Dichloro pyridine 2000 Kg

2 Hydrazine hydrate (60% aqueous

solution)

3587 Kg

3 n- butanol 5000 Kg

4 Potassium carbonate 1840

A] REACTION:

N Cl

Cl

2,3-dichloropyridine,MW=296

2 +2 NH2NH

2

Hydrazine ,MW=64

+ K2CO

3

Potassium carbonate,MW=138

n-Butanol

N

Cl

NHNH2

3-chloro-2-hydrazinylpyridine,MW=287

2+ 2KCl

Potassium Chloride,MW=149

+ CO2

Carbon Dioxide,MW=44

+ H2O

Water,MW=18

21. 3-CHLORO-2-HYDRAZINYL PYRIDINE

B] FLOW CHART:

3)Potassium carbonate(1840 Kg) 4)Hydrazine hydrate

1) n-Butanol (4000 Kg) (3587 Kg)

2)2,3-Dichloro pyridine CO2 gas (600 Kg)

(2000 kg)

Cooling,Filtration

5)n-butanol(1000 kg)

Layer separation

Aqueous layer (5127 Kg)

to ETP

C] BRIEF PROCESS:

2, 3-Dichloro pyridine is reacted with hydrazine hydrate in presence of potassium carbonate

as a neutralizing agent and n-butanol as a solvent. The product is precipitated out during

course of reaction is isolated by filtration followed by n-butanol washing gives final product 3-

chloro-2-hydrazinyl pyridine as a solid. The biphasic mother liquor is separated by layer

separation method. Aqueous layer is sent to ETP for treatment and organic layer is taken for

n-butanol distillation and recovered n-butanol is re-used for next batch. The remaining pitch

after n-butanol distillation is sent for incineration.

Wet Weight

Drying

Dry weight (1800 kg)

Mother Liquor

Organic layer

distillation

Recovered n-

butanol(4850Kg)

For re-use

SSR

Pitch (50 Kg)

Incineration

MASS BALANCE DETAILS W.R.T EACH PRODUCT TO BE MANUFACTURED

UNDER PROPOSED FINE CHEMICAL INTERMEDIATES

MANUFACTURING UNIT

1. Product: Sodium Bromide / Zinc Hydroxy / Zinc Oxide

• Product: Sodium Bromide Sol. 40%= 390 MT/Month

Sodium Bromide Powder = 232 MT/Month

Kg per Batch: 9750

Stage: 1 Batches Per Month: 40

Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Zinc Bromide 70%

6000

Sodium Hydroxide Flakes

1600

Water 4800 Sodium Bromide 40% Solution

9750

Zinc Hydroxide 30%

2650

Total 12400 0 0 0 0 12400

Stage : 2

Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in kg

/ Batch

Liquid

Effluent in

kg / batch

Solid

Waste in

kg / batch

Emissions

in kg /

batch

Output

in kg /

batch

Zinc Hydroxide 2650 Zinc Oxide 800 1850

Total 2650 0 0 0 800 1850

Stage: 3

Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in kg

/ Batch

Liquid

Effluent in

kg / batch

Solid

Waste in

kg / batch

Emissions

in kg /

batch

Output

in kg /

batch

Sodium Bromide Solid

9750 3950 5800

Total 9750 3950 0 0 0 5800

• Product: Zinc Hydroxy = 106 MT/Month

Kg per Batch: 2650


Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Zinc Bromide 6000 Sodium Hydroxide Flakes

1600

Water 4800

Sodium Bromide 40% Solution

9750

Zinc Hydroxide 30%

2650

Total 12400 0 0 0 0 12400

Stage: 2

Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in kg

/ Batch

Liquid

Effluent in

kg / batch

Solid

Waste in

kg / batch

Emissions

in kg /

batch

Output

in kg /

batch

Zinc Hydroxide 2650 Zinc Oxide 800 1850

Total 2650 0 0 0 800 1850

• Product: Zinc Oxide= 74 MT/Month

Kg per Batch: 1850


Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Zinc Bromide 6000 Sodium Hydroxide Flakes

1600

Water 4800 Sodium Bromide 40% Solution

9750

Zinc Hydroxide 30%

2650

Total 12400 0 0 0 0 12400

Stage: 2

Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in kg

/ Batch

Liquid

Effluent in

kg / batch

Solid

Waste in

kg / batch

Emissions

in kg /

batch

Output

in kg /

batch

Zinc Hydroxide 2650 0 Zinc Oxide 800 1850

Total 2650 0 0 0 800 1850

2. Product: Di Isopropyl Ethylamine (DIPEA) = 18.18 MT/Month

Kg per Batch: 3030


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Di Isopropylamine 3030 570 150 Sodium Hydroxide (47%)

1160

Water 400 2940

Di Ethyl Sulphate 2100 Di Isopropyl Ethylamine (DIPEA)

3030

Total 6690 570 2940 150 0 3030

3. Product: Methyl-2-Chloro Phenyl Acetate = 10.3 MT/Month

Kg per Batch: 1030


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2-Chloro Phenyl Acetic Acid

1000 55

Methanol 500 300

Sulphuric Acid 98% 50

Sodium Carbonate 3

Water 12 180

Methyl-2-Chloro Phenyl Acetate

1030

Total 1565 300 180 55 0 1030

4. Product; 4 Methoxy Phenyl Acetone= 10 MT/Month

Kg per Batch: 1000


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Para Anisaldehyde 1000 200

Methyl 2 Chloro Propionate

975 CO2 – 323

Sodium Methoxide 440 Methanol – 515

Water 1750 2827

Sodium Hydroxide 300

Sulphuric Acid 400

4 Methoxy Phenol Acetone

1000

Total 4865 0 2827 200 838 1000

5. Product: 2,3 Dichloro Pyridine= 10 MT/Month

Kg per Batch: 250


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

3-Amino Pyridine 250 75 N2-74

HCl 30% 2900 Hydrogen Peroxide 50%

194

Sodium Nitrate 194

Water 2200 1875


835

Cupric Chloride Dihydrate

42

Sulphuric Acid 42

Iso Propyl Alcohol 75 50

Liquid Waste 4408

2,3 Dichloro Pyridine 250

Total 6732 1925 4408 75 74 250

6. Product: 2-Amino-2-Phenyl Butyric Acid= 6.5 MT/Month

Kg per Batch: 650


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Propiophenone 550

Methanol 700

Ammonium Bi Carbonate

660

Sodium Cyanide 225

Acetic Acid 135

Water 800 2070

5 Phenyl-5-Ethyl Hydantoin

1000

Total 3070 0 2070 0 0 1000

Stage: 2

Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

5-Phenyl-5-Ethyl Hydantoin

1000

Sodium Hydroxide 675 Water vapour -

150

Water 1725 4600

Hydrochloric Acid 30%

2000

2-Amino-2-Phenyl Butyric Acid

650

Total 5400 0 4600 0 150 650

7. Product: Ortho Hydroxy Phenyl Acetic Acid = 15 MT/Month

Kg per Batch: 750


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2-Chloro Phenyl Acetic Acid

1000 60

Sodium Hydroxide 940

Copper Sulphate 40

HCl – 30% 2850

Water 2200 6070 150

OHPAA 750

Total 7030 0 6070 60 150 750

8. Product: 2 Coumaranone = 12.4 MT/Month

Kg per Batch: 620


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Ortho Hydroxy Phenyl Acetic Acid

750 30 Water Vapour –

100

2 Coumaranone 620 Total 750 0 0 30 100 620

9. Product: 3-Isochromanone= 12 MT/Month

Kg per Batch: 600


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Ortho Methyl Phenyl Acetic Acid

1000 100 60 HCl – 210

Monochloro Benzene 1500 1300 200

Catalyst 20

Chlorine 408

Water 2000 3298

Ammonia 25% 840

Toluene 600 400 200

3-Isochromanone 600

Total 6368 1800 3298 60 610 600

Stage: 2

Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Hydrochloric Acid Gas 210 Water 490

Hydrochloric Acid 30%

700

Total 700 0 0 0 0 700

10. Product: 2,6 Dichloro Benzoyl Chloride = 22.1 MT/Month

Kg per Batch: 850


Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2,6 Dichloro Benzaldehyde

900 1505 190

Nitric Acid 60% 1350 1030 240


230

HCl 30% 650

Thionyl Chloride 1170 500 HCl – 215 SO2 –390

Water 650 30

2,6 Dichloro Benzoyl Chloride

850

Total 4950 1530 1505 190 875 850

Stage : 2

Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent

in kg /

batch

Solid

Waste in

kg / batch

Emissions

in kg /

batch

Output in kg /

batch

Nitrous acid 240 Sodium nitrite

30% soln. Caustic soda 205

water 725 Total 1170 1170 Kg

Hcl 215 HCl 30% w/w Soln. Water 500

Total 715 715

Sulpher dioxide 390 Sodium Sulphite 25 % w/w soln. Sodium

Hydroxide Flakes 490 Water 2195

Total 3075 3075 Grand Total 4960 0 0 0 0 4960

11. Product: Methyl-2-Dimethylamino-2-Phenyl Butyrate= 10 MT/Month

Kg per Batch: 1000


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2-Amino-2-Phenyl Butyric Acid

1000 3970 40 CO2 – 490

Toluene 1800 1600 200

Dimethyl Sulphate 760


40

Formic Acid 800

Formaldehyde 37% 1100

Water 1800

Methyl-2-Dimethylamino-2-Phenyl Butyrate

1000

Total 7300 1600 3970 40 690 1000

12. Product: 2-Dimethylamino-2-Phenyl Butanol = 3.01 MT/Month

Kg per Batch: 430


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Methyl-2-Dimethylamine-2-Phenyl Butyrate

550 3150 170

Toluene 720 870

Vitride 70% 1070


280

Water 2000

2-Dimethylamino-2-Phenyl Butanol

430

Total 4620 870 3150 0 170 430

13. Product: P-Bromonisole / 4-Bromo Anisole =16.5 MT/Month

Kg per Batch: 1650


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Anisole 1000 2030 160 Water vapor- 10

HBr(48%) w/w 1625 550

Hydrogen Peroxide (50%) w/w

750

Water 500

Sodium thiosulphate 25

Water 500

P- Bromonisole 1650

Total 4400 0 2580 160 10 1650

14. Product: Para Bromo Phenetole / 4-Bromophenetole=14.5 MT/Month

Kg per Batch: 1450


Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Phenetole 1000 1868 Water Vapor - 10

hydrobromic Acid (48%)w/w

1450 550

Hydrogen Peroxide (30%)w/w

1100

Sodium thio-Sulphate Soln.(5%) w/w

525

P- Bromo phenetole 1450

2,4 Dibromophenetrol (crude)

197

Total 4075 0 2418 0 0 1647

Stage: 2

Name Of The Raw

Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2,4 Dibromophenetole (crude)

197 22

2,4 Dibromophenetole (Pured)

175

Total 197 0 0 22 0 175

15. Product: 2,4- Dicloro Phenyl Acetyl

Kg per Batch: 2000

Stage I: Cyanation Batches per

month:25

Name Of The

Raw Material

Input

qty. in

kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid

Waste in

kg / batch

By-

product

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2,4-Dichloro benzyl chloride

2000

Triethyl amine 20

Sodium cyanide 500 Water for sodium cyanide dissolution

2000 2620 150 kg pitch

Toluene 1000 950 Total 5520 950 2620 150 1800

Stage II: Hydrolysis

Name Of The

Raw Material

Input

qty. in

kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid

Waste in

kg / batch

By-

product

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Stage I Product 1800 157

Sodium Hydroxide

486

Water for sodium hydroxide dissoltion

1944 2483

Conc. HCl 1800 1800

Water for washing

900 900

Total 6930 5183 157 1590

Stage III: Chlorination

Name Of The

Raw Material

Input

qty. in

kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

By-

product

Gaseous

Emissions

in kg /

batch

Outp

ut in

kg /

batch

Stage II Product 1590 283

Thionyl Chloride 944 496

Total 2534 165 pitch 779 1590

16. 2,5-Dimethyl Phenyl Acetyl Chloride

Kg per Batch: 2000

Stage I: Chloromethylation Batches per month:25

Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg

/ Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

By-

product

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

P-xylene 1500 450 145 pitch

p-formaldehyde 1110 780

Conc. HCl 4665 4800 Zinc Chloride 45 50

Sodium carbonate

30

water 300

Total 7650 450 5630 145 1425

Stage II: Cyanation

Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid

Waste in kg

/ batch

By-

product

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Stage I Product 1425

Sodium cyanide 470 Water for sodium cyanide dissolution

1425

Toluene 712 676 1966

Sodium carbonate

14

Total 4046 676 1966 150 pitch 1254

Stage III: Hydrolysis

Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

By-

product

Gaseous

Emissio

ns in kg /

batch

Output

in kg /

batch

Stage II Product

1254 125

Sodium Hydroxide

439

Water for sodium hydroxide dissoltion

1317 1631

Conc. HCl 1430 1430

Water for washing

627 627

Total 5067 3688 125 1254

Stage IV: Chlorination

Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

By-

product

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

Stage III Product

1254 275

Thionyl chloride 950 489

Total 2204 764 140 pitch 1300

17. Indoline

Kg per Batch: 2000

Batches per month: 25

Name Of The Raw

Material

Input

qty. in

kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2-chloro phenyl ethyl amine

2000 81

Ethanolamine 2800 2750 50 Xylene 2800 2660 140

Sodium Hydroxide 515 984 Total 8115 5410 1174 81 1450

18. Ethyl Phenyl Glyoxalate (Epg)

Kg per Batch: 1320


Name Of The Raw

Material

Input

qty. in

kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in

kg / batch

Solid

Waste in

kg / batch

By-

product

Gaseou

s

Emissio

ns in kg

/ batch

Output

in kg /

batch

Mandelonitrile(MN) 1320 kg 534 kg

Ethyl alcohol 912 kg 406 kg

HCl (gas) 362 Kg Water 357 kg

Water for dissolution 660 kg 660 kg

Toluene 660 Kg 627 kg

Sodium hypochlorite(10% assay)

8000 kg 8824 83 kg pitch

Total 12271 1033 9484 83 534 1137

19. Ethyl-1-Hydroxy Cyclohexane Carboxylate

Kg per Batch: 1000


Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in

kg /

Batch

Liquid

Effluent in kg

/ batch

Solid

Waste in kg

/ batch

By-

product

Gaseous

Emissio

ns in kg /

batch

Output

in kg /

batch

1-hydroxy

cyclohexane

carbonitrile

1000 117 kg pitch 428

Hydrochloric

acid gas 292

Ethyl alcohol 736 332 water 288 Toluene 500 475 Water for

washing 500 644

Total 3316 807 644 117 428 1320

20. Ethyl-1-Hydroxy Cyclopentane Carboxylate

Kg per Batch: 1000


Name Of The

Raw Material

Input qty.

in kg /

Batch

Recycle

qty. in kg

/ Batch

Liquid

Effluent in

kg / batch

Solid

Waste in kg

/ batch

By-

product

Gaseous

Emission

s in kg /

batch

Output

in kg /

batch

1-hydroxy cyclopentane

carbonitrile

1000 74 Kg pitch 482

Hydrochloric acid

gas 329

Ethyl alcohol 829 375 Water for reaction 320 Toluene 500 475 Wtaer for washing 500 662

Total 3478 850 662 74 kg pitch 482 1410

21. 3-Chloro-2-Hydrazinyl Pyridine

Kg per Batch: 2000


Name Of The Raw

Material

Input

qty. in

kg /

Batch

Recycle

qty. in kg /

Batch

Liquid

Effluent in

kg / batch

Solid Waste

in kg / batch

Gaseous

Emissions

in kg /

batch

Output

in kg /

batch

2,3-Dichloro

pyridine 2000 600 Kg

CO2 Hydrazine

hydrate(60% aqueous

solution)

3587 5127

n-butanol 5000 4850 50 kg pitch Potassium carbonate 1840 Total 12427 4850 5127 50 600 1800

APPENDIX - 2.5

WATER BUDGET&

WATER PERMISSION LETTER

MAHARASHTRA JNDUSTRJAL DEVELOPMENT CORPORATIONHeAD ,; "Udyog Sarthi", Mahakali Caves Road,

_ro ••,u ..•_ •• (1;;') u .......-b __: _"""ora nQ1: OrientHouse.5 Floor.

Alii anaban Stree • Billard Estate. Fort. Mumbai • 38. II~ ~ ~ IITe e. : 2_7 0027/~21~n"3 'Fax: \I).a) 2.l:11H 1'567

T••••• ::>~a1~'>47 1=,.,,:(020) 2261~1b> /m.VTT. /~ /£~Y'5, ,

~ ~ '\fflPr 'J:f"q.f fc}-~ W7JCft~ :-~&.'<J9/.(t)9~

~,/~ '{rrl:q'tl"r~rn-:rfC;t~e.:H-~\Ji:-::Tur, fsr.,

~W.t-q<: ~,~il161131~dlR'ICh aBr,~ '{il<.'1lct~·

~ : ~til611 ofldlfTl45 /$r..~ ~.t-q~ .. '1 oo\11l;Suf)ilI 31'T'Cf)R :(~ Bbft. ~ '10 Bbft. cmfur3rnT Ch'l!Jicsllcill:i

~ :- 'I) ~ \31i ~ <lRT f(;tf%JIJI 'Q?I' ~ o'd/OQ,/-:(,Oq-:(,

:() <IT ChlllTC1l1l"l1 'Q?I'~ '1~q<: ~ q'1/qO/~oq~:3) ~ \31i ~ <lRT f(;tf%JI<'l q?I' ~ O~/qq/:(Oq:(

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~ ~,qq,19oo/- lITCffit w. :(:(Q,~~ ~ oQ,/qq/:(Oq:( 3FCnT \N ~~,

'{i~C11l!\'< II i't) Ch~ 1fXUTT~ 3lffi". ~ ~ '1 +j;""'lllJ1C1 q') '<1'<'"1r~ I 1RiR 'fl'lGX

~~.

~ ChCiSfClJil:i ~ cn'l, 311QUli'ti ~~. t-q~ ~il1Jl 3f)WfTICh ai?r Rir. ttlC1Il!\'<

~ -:(,~ fB-."41. CRiM ~0 "41."41. Clli (1I-41~ 3ft til fTl45 -;::roo\ill '5 un Cfi'<1'<H IROllJ) c>13ltt

q ~rJl1;H1'{ 3llQuri'<"l ~ ~ ~ ~. ~ 3lTQUf \N ~ ttlC1Il!\'< ~

~ ~ ~ ~ ~o ttr."41. Clllfll4l 'icihlll;SOn ~Olll=cf1 'CZI'CI'X{!l1' Cfi,<cflc>1.

'iCiS\Jil;sof)'<"lIJt C1IlIU"~ 'til~C'll \RT.+ftcx-, ~, ~, qm;q, m ~ ~C'lllcn'<"lrJt

3'lIQulifl ~ ~ ~. \J'f'{' ~ 'Q'N Cfi'l!Ic:rlllill ~ ~ :(00 fTr.+ft. ClJI'<"lltil

3lN."t'fi."t'fi. $ ~ ~ ~ Qlulllift $ clChlcft ~. ~ X1&IT

311Qorixi Qlolllill G'{' ~. ~~.'dO ~RI£1sft 3lIChI,{C11 ~. ~ ~ GI'&C"lIr*H

~.~~.:('1 uRl£l4) f$crr C'll1~C6ill Utlf(;tl:i 3i'ltM~ICfi G'{' 3lICfiI,{C11 ~. ~ 4lUlll't)

q ~ mrcn ~ 1RiR '<"lgCh14 q:mc)- tt fcj.:Rft .

WATER BUDGET

FOR

THE PROPOSED FINE CHEMICAL INTERMEDIATES MANUFACTURING UNIT

BY

“OC SPECIALITIES PVT. LTD.”, PLOT NO E-18, CHINCHOLI MIDC,

SOLAPUR, MAHARASHTRA.

Daily Water Consumption

45 M3/Day

[18 # M3/Day + 27$* M3/Day]

* Cooling Water8 M3/ Day

Process 17 M3/ Day

Cooling Blow Down

1 M3/Day

The effluent generated @ 24.5 M3/Day would be

treated in a separate Effluent Treatment Plant (ETP)

followed by Double evaporator system.

Treated separately in Septic Tank followed by soak pits.

Domestic 5 M3/ Day

Effluent Generated 4.5 M3/Day

Boiler Blow Down

1 M3 /Day

* Boiler Feed8 M3/ Day

Effluent Generated 20 M3/ Day

* Washing& Lab

3 M3/Day

Gardening 2 M3/ Day

Effluent Generated 2.5 M3/Day

Note: # MIDC Water Source, * Use of the condensate water from the DEE and

$ Rain water

1. WATER CONSUMPTION

The manufacturing set-up to be provided on site shall be to take up only four products

daily. As per the market demand four products shall be manufactured from list of

twenty one products. While calculating the daily Water Consumption, the four products

which require higher water quantity have been considered from the product list. The

same are as follows-

Table No.: 1

Water Consumption Aspect Considered for the Products requiring Maximum

Utilization

Sr. No. Name of the product Water Consumption

(M3/Day)

1. Sodium Bromide / Zinc Hydroxy / Zinc oxide

6.4

2. 2,3 Dichloro Pyridine 2.9

3. 2,6 Dichloro Benzoyl Chloride 3.5 4. Ethyl Phenyl Glyoxalate (EPG) 4.03

Total 16.83 say 17

The daily water requirement in the industry for various operations and processes has

been shown in the following Table-

Table No.: 2

Water Consumption

Sr. No. Description Water Consumption (M

3/Day)

1. Domestic # 5 ($4 + #1)

2. Industrial a. Processing #17

b. Washing *3c. Cooling *8d. Boiler Feed *8e. Scrubber *2

Industrial Total 38

(#17 + *21) 3. Other (Gardening) 2

Grand Total 45

(#18 + *$27) Note: # MIDC Water Source.

* Use of the condensate water from the DEE.

$ Rain Water

Hence, the total water requirement for proposed project would be 45 M3/Day. Out of

which 27 M3/Day shall be condensate water from DEE and rainwater whereas 18

M3/Day would be taken from MIDC water supply scheme.

2. INDUSTRIAL EFFLUENT:

Industrial effluents mainly comprises of effluents from process, laboratory, washing,

cooling and boiler blow downs etc.

The manufacturing set-up to be provided on site shall be to take up only four products

daily. As per the market demand four products shall be manufactured from list of

twenty four products. While calculating the daily Effluent Generation quantities, four

products which generate higher effluent quantity have been considered from the

product list. This has been done to design the effluent treatment facility for worse

scenario. The same are as follows-

Table No. 3

Waste Water Aspect Considered for the Products having Maximum Potential

for Pollution

Sr.

No.

Name of the product Effluent Generation

(M3/Day)

1. 2,3 Dichloro Pyridine 5.8 2. Ortho hydroxyl phenyl acetic acid 4.0 3. 3 - Isochromanone 2.1 4. Ethyl Phenyl Glyoxalate (EPG) 7.9

Total 19.8 say 20

The total effluent generated from various operations and processes in proposed project shall be to the tune of 24.5 M3/Day. Details of same are given in following table-

Table No.: 2.9

Effluent Generation

Sr.

No.

Description Effluent Generation

(M3/Day)

1. Domestic 4.5

2. Industrial a. Processing 20 b. Lab & Washing 2.5 c. Cooling Blow Down 1 d. Boiler Blow Down 1 e. Scrubber 0 Industrial Total 24.5

Total (1 & 2) 29 Grand Total 29

Table No. 2.10

Water Balance w.r.t Proposed Activity

Sr. No

Category Water

Consumption (M3/Day)

Losses Effluent

Generations (M3/Day)

Disposal

1. Domestic #5

($4 + #1) 0.5 4.5

Septic tank followed by soak pits

2. Industrial

Processing #17 - 20 The effluent shall be treated in ETP comprising of Double Effective Evaporator thereby achieving Zero Discharge.

Cooling *8 4 1

Boiler *8 4 1 Scrubber *2 -- -- Lab & Washing *3 0.5 2.5 Industrial Total 38

(#17 + *21) 5.5 24.5

3. Gardening # 2 2 -

Total 45

(#18 + $*27) - -

Note: # MIDC Water Source.

* Use of the condensate water from the DEE.

$ Rain water

The entire trade effluent generated would be treated in a full-fledged Effluent Treatment Plant (ETP) to be provided in industrial premises. The ETP shall comprise of various unit operations and processes such as Bar Screen, Equalization cum Aeration Tank, Lamella Clarifier, Sand Filter, Carbon Filter and Sludge Drying Beds as well as Double Effect Evaporation (DEE) System. Installation of DEE for evaporating the trade effluent generated from the proposed activities would result in ‘ZERO DISCHARGE’ of effluent. The condensate water to the tune of 23 M3/Day shall be recycled for cooling & boiler feed make up water as well as for washing thereby reducing raw water demand.

Further, the salts left over after evaporation in DEE & Sludge from Clarifier would be bagged for dispatch to ‘Common Hazardous Waste Treatment Storage and Disposal Facility (CHWTSDF)’. Industry has procured membership of CHWTSDF

APPENDIX - 2.6

ETP DETAILS&

P& I DIAGRAM

i

AI 81 ..CI 0• ;5 + JII; -

-0m!~ r

Ia..0L.&J,:2• •mljl -

l~ilIli:l~i cizd!ll ~ r=e= I.1U.1l~ c>

'. ~_I _r -.a'i '-~ ~W& .3:.. ., .. ....£.@ .d--~ .Ff1~~_-Itll! ST.••'IlC - - ovtIlI'\.OW I'll'[ l.IC

W!1!1t WIE1U ~a I CIY[Jnow I'll'[ tMt 1r~UI @§~

::-,sr.uJC-1iIIDD .~

~2

2

.~

r< >-~

'7~

II r)1{(in -0 H~ -o,~~~SV r I

~

+ 9J \Iir PYW OOSIMG DCrSING l\.lIoc;( lUI C1LIIl WAlII TAHIC rEED I'\aoIP SoUCl run CAnQM run~ e e IWX11all. ••• 1000 UT _ I leI lIW '_ X tIS' ••••li NOTt:- iN: Sl.U0G£ lEI) TO I[ lUlU' NEAll Ii) @ I eIIlIl e 0.II' SCIIml E<MLATION TAHIC N'RQXIWArt I W£TER AVlAl

I. •••••10 "-'WgU! AIllAllOII I COlJ..E:CnOtl UI«

IID:3WX3W

~'ilie FOR ST~PINGSR.NO DESCRJPTIOH I NO.

=Si EQUIPMENT j§i;::MMId 1 BAR SCREEN 12 AlRATOR BlOWER PUMP 1.&F 1 r-1 3 EFFLUENT TRANSFER PUMP SP 0 J-t.1 1 14 FLOCUlATOR ISTATIC MIXER 25 . LAMaLA PLATE SEPRATOR 1

CUENT:-8 FL TER FEED FUdP SP 1 tiM 1OC SPECIALITIES PVT. LTD.I 7 PRESSURE GAUGE ... 1

8 ACTIVATED SAND FILTER 1&- x as- 1 SOLAPUR9 AC11VATED CARSON FD..TER 16" X 65' 1•i 10 DOSING TANK PUMP 2 TITLE ;- P & I DIAGRAM FOR11 CLEAR WATER TANK -{

EFFLUENT TREATMENT PLANTI Z5 !tI3/DAY

f~ Q,tJE BY SIGN S.41-m&aDRAWM 07.07.12 GANESH -at<ED 07.07.12 JHII ..4N.4NDl SPBCULrI'1I!S & 8.ERYICJ!,S PY1'LID.

Ii AP?R£D 07.07.12 SANl<HE ........••....'L.~{=-.~.....--.-..-SCALE:- HTS PROJ. :I: IiWl£ FROt.l pwc. SIZE ORDER NO. DW~1 REV,

A3-EQP-Ol RONO. REVISIONS ~ C~ APPR. DIIJE owe. HO. ~OAAWING - A3 NO.AI 81 cl 0

134

APPENDIX - 2.7

DRAWING OFDOUBLE EFFECTIVE

EVAPORATOR

12 1 11 1 10{) 1 if 1 8 1 '7 1 5 1 5 ~ <J 1• S 1..•. ,

F. I ••

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Q <=:=#r<"0:1 E

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(e=.;;z~(• ;-,',f- j~ g,

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r-- r-~ 8- I.~I

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~Ii=:::;:

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~ '-.-II T.11 T if .l\ IJ ::K IJ ~ DI 4~r..&( .n.;; r---\ •...-------- --------- - -~

~ t~ j§ fBl f~ ~ n-~J P-1el ~ ~ ~ ~I itt-~I ~

1: · -

- ••••••• NrR" mm., ----- --- -~--.1M r-_ " 1- I~ •• <>~- --- 1IL_ ••• 8!:!.~~p£ IJd.GE iii .•...•-.-_. E-- - - ..-...•.- -,--- - - O~- - _ ,...CJ.,4 - - --v , - - 111 •.•-T_ -- - -- _ ,,... - - --- - - - -- •• PReCESS F\..OW ~..., -,----- - ,... - '" .- sfi;- -.~ - - _nF'CR DOU8.! ~ ~-_.---- --- - - - i'= :: --- ----- ------ - - I.K

~ -- U& -.:1 •. 11 EVAl'OAAroR ~~- - ~....". .,.. ~:- ...••....,.~

'"' I ~leU

':' DBOJro: e/ ~ I a::s-a. [!DI£IrnI1 " 1 ::: 1 J_1= I 11 1 H 1 9 1 8 7 f :'J '2 1

APPENDIX - 2.8

BOILER DRAWING

APPENDIX - 2.9

EEFICACY LETTERFORMDC

FROM SUPPLIER

rt;lL&J-

Elite Thermal Engineers Pvt. Ltd.An ISO· 01: 2008 Certified CompanyMum Office : 314. Jayagandha AMex.e. Ram Man.rtl Road, Opp. Dr_Parao pe's Eye He pltal Thane ).Pm - 400 602. - 91-22-2533 1807 (3 Unes) • Fax • 91-22-2533 3069. Em I: AIH.lllan. lltath«rmal. 1\

Pune OffIce : Samruddhl Enclave. OffIce No B. 3C & 3D, rst Floot. Near MlJktangaoSchool. Plot No 22S. No. 46, CTC No.3925. Parvatl, Pune· 009. 020-2421946Bl71. Fa 020-2 21947• Email: sal••. punltt.th.nnalJnW()f1(s : Gal No. 558, Village WIng, Post Sh rwaI, Tal. Khandala, Dls Salara - 12801

. 91-2 69-284290 191-9226681306. Fax: 91-2169-284295. Email t factory@elltelhennaUn

Reference No.: ETEPLlMKTG/2014-15/TO/335 Date io" May 2014.

To,M/S.OC SPECIALITIES PVT.L TD.Plot NO. E-18, MIDC, Chincholi,Tal: Mohol, Dist. Solapur. Mah.

To Whom It May Concern:

THIS IS TO INFORM YOU THAT WE HAVE OFFERED A 3 MTPH CAPACITY STEAMBOILER USING COAL I AGROWASTE BRIQUETTE AS FEEDSTOCK, TO OCSPECIALITIES PVT. LTD. FOR THEIR UPCOMING PLANT AT CHINCHOLI MIDC,SOLAPUR.

KINDLY NOTE THAT OUR DESIGN OF MULTI-CYCLONE DUST COLLECTOR (MDC) ISADEQUATE TO CONTROL THE AIR EMISSION NORMS SET BY MAHARASHTRAPOLLUTION CONTROL BOARD AND CONTROL THE EMISSION OF FLY ASH I DUSTPARTICLES TO ATMOSPHERE LESS THAN PRESCRIBED LIMIT OF MAX. 150 mg/nm3

•

SINCE THIS IS A RELATIVLY SMALL BOILER, THERE IS NO NECESSITY TO INSTALLELECTROSTATIC PRECIPATOR (ESP) TO CONTROL AIR EMISSIONS, ASMUL TICYCLONE DUST COLLECTOR WILL BE ADEQUATE TO DO THE SAME.

WE HAVE DONE SEVERAL INSTALLATIONS OF BOILERS OF SIMILAR CAPACITY WITHMDC IN VARIOUS INDUSTRIES ACROSS INDIA AND HAVE NEVER FACED ANY ISSUESWITH THE PERFORMANCE OF THE MDC.

Yours faithfully,For ELITE THERMAL ENGINEERS PVT. LTD.~e.~~~S~G.M Sales & Marketing)

3TPH ( F & A 1000C) capacity Boiler

1. Heat Input required = 3000x540 = 20,76,923 kcal/hr

0.78

2. Fuel - Imported Coal

3. Fuel calorific value = 5200 kcal/kg

4. Fuel consumption = 21,60,000 = 399 kg/hr

5,200

5. Fuel to Air Ratio = 1 : 15

6. Flue gas generated = 399x15 + 399

= 6384 kgs/hr

7. Flue gas flow at inlet of = 6384

Multi cyclone 0.675 ( ∆ t 2500 C flue gas density = 0.675 kg/m3)

= 9457 m3/hr

8. No of cyclone - 3 Nos

9. The flow rate through each cyclone = 9457

3

= 3152 m3/hr

10. Inlet Area of cyclone (350mm x 175mm) = 0.06 m2

11. Inlet Velocity at cyclone/sec. = 3152

0.06x3600

= 14.59 m/sec This is as per standard International norms.

12. Ash Distribution in Boiler plant

Ash % in imported coal is 6%

Hence Ash generated/hr = 399 x 6% = 23.94 kg/hr

13. Ash Distribution is as below

a) 50% Ash collected in Boiler = 23.94 x 50% = 11.97 kg/hr

b) 25% Ash collected in APH = 23.94x 25% = 5.985 kg/hr

c) Remaining 25% Ash carried over = 23.94 x25% = 5.985 kg/hr

to Cyclone separator

Total flue gas quantity = 6384 kg/hr

14. Ash collected in cyclone separator considering 85% efficiency of cyclone separator

= 5.985 x 0.85

= 5.08725 kg/hr

15. Remaining Ash in flue gas = 5.985 – 5.08725

= 0.8977 kg/hr

Hence SPM level in the flue gas = 0.8977

6384

= 140.62 PPM

6 Lac kcal/hr Thermic Fluid Heater

1. Heat Input required = 600000 = 769230 kcal/hr

0.78

2. Fuel - Imported Coal

3. Fuel calorific value = 5200 kcal/kg

4. Fuel consumption = 769230 = 147.9 kg/hr

5,200

5. Fuel to Air Ratio = 1 : 15

6. Flue gas generated = 147.9 + 147.9

= 2366 kgs/hr

7. Flue gas flow at inlet of = 2366

Multi cyclone 0.675 ( ∆ t 2500 C flue gas density = 0.675 Kg/m

3)

= 3505 m3/hr

8. No of cyclone - 3 Nos

9. The flow rate through each cyclone = 3505

3

= 1168 m3/hr

10. Inlet Area of cyclone (200mm x 100mm) = 0.02 m2

11. Inlet Velocity at cyclone/sec. = 1168

0.02x3600

= 16.22 m/sec This is as per standard International norms.

12. Ash Distribution in Boiler plant

Ash % in imported coal is 6%

Hence Ash generated/hr = 147.9 x 6% = 8.874 kg/hr

14. Ash Distribution is as below

a) 50% Ash collected in Furnance = 8.874 x 50% = 4.437 kg/hr

b) 25% Ash collected in APH = 8.874 x 25% =2.218 kg/hr

c) Remaining 25% Ash carried over = 8.874 x25% = 2.218 kg/hr

to Cyclone separator

15. Total flue gas quantity = 2366 kg/hr

16. Ash collected in cyclone separator considering 85% efficiency of cyclone separator

= 2.218 x 0.85

= 1.8853 kg/hr

16. Remaining Ash in flue gas = 2.218 –1.8853

= 0.3327 kg/hr

Hence SPM level in the flue gas = 0.3327

2366

= 140.61 PPM

APPENDIX - 2.10

LIST OF COAL SUPPLIER

LIST OF COAL SUPPLIERS

SR. SUPPLIERSNO.

1. SAIBABA LOGISTICS303,B, Suraj Appt.Krishna Nagar,Opp. Simhadri HospitalVisakhapatnam - 539 002.

2. MIS. NISHA INFRASTRUCTURE6, Sheela Smruti,Tejpal Scheme Rd # 3,Vile Parle (E),Mumbai- 400057

3. MIS. GANDHAR COALS & MINES1001, 10TH Floor, Unique Towers,Near Poonam Heights,S.V. Road, Goregaon ( W ),MUMBAI - 400062.

4. PAS STEELS PVT. LTD.107 B, Vaibhav Indusrial Estate,Saki Vihar Road, Powai,Mumbai 400 072.

5. GUPTA COAL INDIA LTD.'B' wing ih floor Shri Ram TowersKingsway Sadar

Nagpur - 01Maharashtra India.

6. BHATIA GLOBAL TRADING LTD.Corporate Office: " BCC HOUSE :,8/5, Manoramaganj,Navratan Bagh Main Road,INDORE - 452 001. ( MP )

DRAWING OF SCRUBBER

DETAILS OF SCRUBBERS

No.Attached to

Process PlantDia. Height

Scrubbing

Media

Mode of Disposal of

Scrubbed Material

1. SO2 0.5 M 3 M Water &

Caustic

soda

Sodium Sulphite Soln.

25% is produced as a

byproduct.

2. CO2, NH3 0.5 M 3 M Water From scrubbing CO2 gas

soda water is formed.

3. NH 0.5 M 3 M Water Ammonia is reused in3. NH3 0.5 M 3 M Water Ammonia is reused in

process

4. HNO2 0.5 M 3 M Water &

Caustic

soda

Sodium Nitrite 30% Soln.

is produced as by

product

5. HCl 0.6 M 6 M Water HCl Acid 30% is produced

as a byproduct

A~"MONIA/NITROAS/NITBfC ACIOSCRU89~R TA K 3 ~L

WI H C LUMN

DAT 29/111/201 ,

HORIZON!, L TANI{

,

!

DII'IICII CONDmoH I'IIOCUI •••• IIImCIlIIH

nUll) HANOLm HCL QAIJ+HZO+ta. COOlN) WATf"

OPfltA1IHO PIlUSUtI('I(O/cJ • •

DaIOH Pfl£5SOftf J.r. J.r.TUT I'ft£SiURf (MWD.)DIJlIAnotI O.

6.0 &.0

OPfltATlHO TfW(ftAnMf DC • •ClfilON lfWfltAlUM 180 tlO

NUIoI8ElI Of PASSU 10.&"I.'.

SUIV"ACE MfA ••2 J 2.M

WfIGHT flM'1Y 200 (N'PIlOlC.)KG.

WfIOHT fUlL Of WATlJt 2ao (N'PROlC.)

-- N. -.ATIIID I:DJlN.crtDN •• "rIC.••• •• • HOlD ••• CIlt HlII .111 (1lfP ., NllCUI_1I

UMHte

IG •• ••••• 4HOlD" •• CIltPGI ••.• c_V WAIl M1IO lUI"

III.., •• 4 HOlD " •• CIlt •••••.• (Ilfr I>__ 0UftD

'101)1M •• • HOlD " •• CIlt PGI II •.• (on ., ••••• _ 0UftD

III •• • HOlD ".1 CIlt PGI lalLI (1lIr I)___ lUI"

III 10,.,....,

• HOlD " •• CIlt PCO II •.• (on I)____ 0Uft.D

IfP '/2. """.f. IIIJMC( Ill( DIlolIl

III I/J' •.•.••.r, tIJMel __

~l-II I:. AU. 0IYfJ4SI0HI NfL •• iMI.

2> rOl.ll"f1l[1II' Of_ OH _oW( NlUo ~5 ..5> CMJI AU.. '1lU~ t; 1_4> ~ ~ 'MItt fUHOU IAII1' II: f1I1ID_ -.n; 1I01I~

(If', liZ , 1UAM4) __ lIII..l I( MAAHO(D ., cUlln.

I> _ CQl\,. OT '-1: __ PO ••••• COlOUlll lIIU. If. AHtJI •. CIlt ML 0 .•. "MIl.

(10 10 10 ~ on.)I> DClM./,.Nff ~Ii NlC ElCOUIIAoUY Cl'..III ..-om .J> lHf fllUlPl.lfHT IHOUt.O II[ CNlJH[D A' [M1'- IXNI. 0MlI II ,"'" NO.1 •

I> tN8I'fCllllH lit 1- aJrNl / SO(5

I> • _(0 TOI( ,IU.fO UP Wi Cl.J(NrL

...,.....

,.,.VIEr 'ROil 'r"-'r

....,..,.-I---"~~:r-i=~d tsO'"fIlWAl rAWNO fllW Alloal[RI-'=+--+':;;::'-f~a~ TfH-'" ••:ww.u •••• (,ware'11IIII

CHWTSDF MEMBERSHIP

LETTER

ENVIRO POWER LTD

This is to certify that: IL:... ~:":""';';:'..::!C.IiI~=~I.A.I!;~~...&..lI~=

Address: . a ' "_Chi c, I a . aha' - ._S,.' '~413255. is a Valid member of CHWTSDF (As per MOU with MIDC &MPCBJ at Plot No. P-56, Ranjangaon MIDC, Taluka - Shirur, Pune - 412220.

Membership No. : MEPL/CP0023

Membership Period: 21 AUGUST 2012 to 20 AUGUST 2017.

For Maharashtra Enviro Power Ltd.

Authorized

5M3

p,_ L(Com mon Hazard ou s Waste Treatrnent, Storage an d Dis posa I FaciliM

APPENDIX - 1.1

MIDC NOTIFICATION

.•. _'lit _ .••.~.• _ ...•.~' ' . ....:.__ .. n ~-,----

( "'... - ~;l\..

I • uat'It..,.•••••l'~( .•

----.--- ~ ..-Area . Gat

H. Arcs NIJ.An.":!

H, Arcs.__ .- ......•.__ ., -_ . " .

. 3(:'1 II 84-0 79. 10'T>~.;, Us 2 pt. 14 75-0 :,.10 j 5 40,07'2 10 75'0 81 2 3-0i3 n 57'0 82 2 39-0j.4 7 J5'0 B3 2 3·0.75/ S 2 ~J5'O 84- .., 34-0~..•, ": 1 75·0 8S 4 30-f)1. ' _..,~..,' 3 53-0 80 4 65-0! ..I ,'-11

it)' 1 ~ 0 S 1-0 a7 ...• 43'-00

76 ... 2 ]8·0 tS 14 1'j'(1

77 2 9"'0 ~Q l~ t 3'0'?~ 3 6?'(J"- - _.- -.. .- •.. __ ..--.- ~~.-_ ...._.., - - '" -"-"""'.

Ga~ Area!'\. H. Arcs

G~tt j\ r-e:l~o. H. Ares:

_______ ._ • __ • __ •.•••• _ ~_ ••• , /'0 ••• _ •••• "_ •• -

- .--~- ---,-...:..--,.,.., --- .- ..•.~ ~

20c,: pL. '")('in .

. .;.}7 pt.. -- .•.

5 QO.()()2 I;l21-4 ~~ 14 .:

26 soc~ 7d·~,

12 3'2'0

-- - - ..• ]. - -

- ...• - P'!

- If,'HI' ,/,Pfrs-:.-t tv: (he East by--Gnt Nos. !4,1 5. J 9. 20. 25. 56, 62. 64 pt.. 65 pl ..•

fl(~ rr.. 07 pt., 68 pt., 70 pr., 90. Q2. 94, 95. 98. 104. l05. "'06. of villagrK~"ndi. -" J

On the West by-Oat Nos. 52,,14'8' pt., ISS, J56•. 151. (58. )83..1~I is\!. J90. 230 pt., 231 Pt.1 233 pt ... of -<jiUage Cbincholi, and Bo,undZl1

l~f Village Sawleshawar.d" the North by-Boundav of Villaaes Darfal and Akole,

I. .• ow~ ,.~. '0" fir S'ltith by-Gat Nos. 1 pt. 4 ft .. 6. 8. 10 pt.. ~I pt .. 12 'fK-.

fJ pt.. 1\.~ ~ pt:, 2~ pt., 25 pt., 28 pt. 29 .pt., J2, 37. 70 pf .. 71 p!.72 pt., . d 73 pt.. of Village Chincholi and Pune-Solanur Nntion~1H· L.. N' J'l •

I~\;\\'a :. O. 7.i :l!

'ByQrdct and in' the name of· the Governor 0f Me harashtra, .:M, D~.SARV!.' .•..."r.AR-

-oe~.... omcer.

.. .•

•

,Area. Gat.

H.. ~ . _ . No,

75' '3 84-0 lOff 1 ~1),76 o 41-{) 109 '0 '39-071. 0 .41-0. no.·. ' 0 ' 43<0

.·78 0 51-0· III .. . 1, SQ-G

1P 7 49{) jJ2-: - I' 44-0

... ,80 9 68,0 lIS 1 35~O

81 0 25-0 1'14 2 12{)

82 1 23·0 115 l' '42»0.

&3 1 15'0 116/1 0 4S{)

84 1 14-0 .116/2 Q 45-0

.,.85/1 0 4-0 117' .2 .17-0

8511. . 1 49-0 -llS 0 ,31-(/

86- 5. 28-0, 1.19 " 1 .si-o-

.81 2 1.1-0 -120 . . . 4 _23>0

'88, 7". 14'.0 124/1

,3 48-0

89 ; 3 67'(} 125 '0 241).

90 4 14·0. 126{1 2 99-{)

91 2 SS-O 126/'" , -2' 0-0

92· 4 61-{) 127 4 .62.0. ss 3 51>0 .• , 12$/.1 ,1 60'0i 94, 2 691> l28ff),

,1 .83{)'

95 10 "88-0 128/3 . 4 4S'{)

5-96/1 13 90,0' ]29/1 1l. S(rO~!,'96/2 . ~ "\ 2 200 129/211, " ',1 14-0

.'~,:'97/t .~~ :(- '4S~O - 129/2/2 1 14-(J

'97/2 I ~' 2''' 7'0 >--"---:.12912./13 " .1. '.1400

M\-'~'" ..," ,

·t 129'lgl4r ..

.13i)'91/3 '2 . 7,0 } 1. ' ..[ r .93 .1 ~, 9'·48-0 129/21-S 1 ' 14-0

99 f~\ 3,64'0· '" l29-fZIl5 ' ; 1 .: 14';(}

, 100 3 ·S-O 129/211 1 14-0

lOl 1 89-0 130 s 14-{)

102 4 35'0 131 ·s 94~O'

103 "4"~"'5£1;3 -..~::'........, 13'2 .4 93{)1, 133": '"7"

104 2 .g-{) . :'··5~~54·O.105 5 81N) 134 7 51-{)

106/1 . 0 38{1 lil5· 14. 40'{)

106/2 -0 34-0· 135 0 24~O

106/3 0' 3s.o. 137 7 45{)

JO~/4 . 0 33-<J1~ 4 . 50'\}139 ...•. S{)f

101 0 84~Q 140 11 7~

¥~ ~ . i{tt~l~ ~ ~~, if ~~ l'~(./~ ~ .~ ;.\~O . [~~"!:l• take effect in the area mentioned'.in the Schedule annexed hereto. and.. declares the said area as industrial area under clause (g) of section 2 ,Q! tb~said Act. '. ,

, .The said area is more clearly defined in red in ·the maps deposited in. tho

Offi~ of the Chief Executive Officer" Mabarashtra InduStrial DevelopntentCorporation. Bombay 400 093,. and the. Special .Land .-Acquisi.tion Offieer,Solapur Division. Solapur, Dis' let Solapur, and is bounded by the: .~"as indicated in the said Schedule.' ~

, Schedule ..District Solapur, taluka Mohol, vil~ge Ch~holL

- ------~-- ~----------~---H. AtC$10 33-1.2 61-Q

10 5l-t7 '61'

10 93"93 75'e

- 4 94/ •'1 20"8- 34·.6 80-'6 44-0

13 1:7·trJ·1 9-04 - 11-t1 89-$

3 46"G4 81-9:3 '63-04 20,0

. .12 42--.5 2S·.{

6tH}166·~·4 11·lJ3 59'0. :3 9(}{):9 39-0

11 0-08 97'0

GatNo.

I pt.4 pc59

10 pt.II pt.12 pt.

-- 13 pt.14IS16222 pt I to 325 pt.262728 p.29 pt.· J .38 l! .. ~\39! 1+:i '~L!O l ,~;

4 lA/I;4'; /V43 .~.\ i..

I, 44454647

49

Area

H.Ar~s? 36·0'5 92-03 2-02 9;-06· 56-01 80·01 92-0'1 92-02 40'02 19.02 28-0.4 60-03 40-07 16-01 '97-0:? 29<lo 80-0o 80-0

14 2-0.IS 37-{)

-9 56'0'IS 44-03 61{}4 10-05 77'0

12 61{J-3 ~S:O3 85'0·,5 - ~O.O .5 19·0

GatNo.

so51/151/2,",........5354/1f_54/2•54/,35556-57585-96061.; 62636465666~68/1.'68i26970 pr.il pt72 pt73.pt.74

4

•

fll!H'" -tI'IlA .(t.ihr,'~-~~ "~.t/.~:,,,~ :t\,.fGi~lfr~J ~r '3'ff""<~f~J lf1"ar rr.I~~. . ;~ .

•.• II _ L • . ......•....

_=-1*. - .. ' ...~.wn:

~ .•~

~.1·!!~~''¥:!i

!>£ ~(t 0'\ ~ ..,

<: ,,'f.;,)

-... ._-.....,........ • 1 ••••:il •••••••• "I. - .....-'_._. __ .-- •• 14 ---1 - ..'-...- -.--, ,

~=tit+H· ..•...;..0 _

. ~a~.~~<f.ig1~1~::: IJ. ~ i l; rT~\'1 ,~ "J

~ Ct-L\} ~ c ~~

~tI~.-_1fm ..F'q"-wf'1~ lrG ~<:-',~Jl¥~ q., 9~l,;" <t~~u9lt,1J, 1~G~~~~, ~L¥l ~?f(,J 1~;OJ- ~~ •.~ q~1~~~q., ~.l~1'1 9' l.t~.

. , ~14¢!i4~') lffic(. ',-

~~R·4n{'&Z ~ ~~.~.~~~_4;~~Nifr~;N. -~~-m.-., q'j

,. .•••. .&

. 9'~ q.: 1,~ q"'s 1iJJ ~~' cr.}... .•.~~I ~VJ ,,-~ ({oJ iJ<t 'i-I. I"~

,,~fct;~~.I

;rt{r~~.f '<Gf-.t'rw: - <;Cii?t·r ~·qrFf~l~ q' ~Dql~}

qr. if. U(ttC,rr:~~l! . '~'- .• ". ~,.. 4.' •...~ s,;b '. ~fQT~~ arrtr'fl; <:r.to" -, 1

. I'~; -~. " .

Ill!'USTRIES, ENERGY AND' LABOUR DEPARTL'YIENT'> antralaya, Bombay 400 032, 'dated the 12th May 1988

MlsJL\.RJ.S·h 'RA lNOUSTRtAL DEYELOPMENT ACT, 196J., 229

fNo .. IDC+ 218(/(10514)"'IND~!4.-ln exercise of powers eonferred ,bysub-section (3) of section I of ·tile Maharashtra Industrial DevelopmentA.c~ 1961 (Mah, rre of 1962) the <1overnment of Maharasbtra liereby appoints17fh May 1988 to be the date from which Chapter VI of the said Act shaH+~.;:: .. 'J I ij; • _ 'm" .; __••••

\Tl11' ~r<~-~,

; r

:q~l~q m~f~~~~, i; ;.:~, t\~':'j~itt<,~J, ~{; -1I(, 9 0 r·~'~~l~<..;(

INDUSTRJEs: ENERG Y A..~D l:ABOlJR {)EPART~1ENT. Muntralaya, Bombay 40i>v32. dated 13th May 1988

1tJ.f{AR.ASHTI{A :,,<;)L'S d::'iAL DE\ :-1Ol'Ml.:Nl Al'T/ 196 II

No...rec. 2!~3f{4gSG)YIND.i4.--Iu exercise of powers conferred by Sub-&cUm (3) of Section 1 of the Mah:JjJ~hl:a Industrial Development Act. 1!.!61.(Mah. Tn l)( ;962). tit·.; Gcvcm.n 'n' o~ ;1I!:ih::f~S'htra hereby appoints 27th May1988. to be the date from which Chapter VI of the'-snid Act shall take Clil.!Clin the area mentioned in the Schedule annexed hereto and declares the saidArea as industrial area under clause (g)o[ section 2 of the said Act.

The said Area is more clearly defined in red in the maps deposited in theoffices of the Chief Executive Officer, Mnharashtra : Industrial DevelopmentEorporation. Bombay 400 093~ and the Special Land Acquisition Officer.Auraagabad, District Aurangabad; and is bounded by the areas as indicatedin tbe said .schcdule. e- .

"SCHI!DVLEDistrict Aurangabad, t~Juk;a .Atlrangatx'ld;: village WnIQdgaon.-- -' .,-~.-.-.--.- .._ ... _---_ ..... -... "~ ---

Oat No. AreaAres

Gat No. ArcaAres

...._-- -----e! pt. 02·() 69 pt. 01·0

,J" -.-----.--.- -- - - - -_._.-I .

B-owtdtUies. :

Orr the Nortli by'.-Part of.Gat Nos. 70. 71~16. 77.18.CJr. the SOfith.~.~p~rt of Gal,N~s. 70. 11, 76. 17~78 ~nd 8I.On {he East b. .~oundary of village Nakashtra wadi.On tlu: lVestry. -Aurn~i$.d-Ahm.dnagar Road.

. 1 'i! •

District ~ranga.bad, taluka Aurangabad, village Patoda.:--'-r-- -- --.-.- -'.. -_._._".- ,.-.-.

Gat No. AreaAres

- ....~------16' pt.

_. ,' •.._-,.-- ...__ ..- ..._-- ...• -._._ .. -"--."---'---07'0

;J~s:On lhe North by.-Part of Gat Nos. 18, 19. 20, 21 and 26.On .he S~)u'h by.-Part of Gat No~. 18. 19. 20 and 22.On the East by.~Bou(]dary of village Valadgnqn,0,. the West bj.-Boundary of village Valadgeon.

plot layout planenvironmentclearance.nic.in/writereaddata/online/...sr. product name l\iaxi1h1iiii...

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