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APPENDIX - 2.1
PLOT LAYOUT PLAN
I-o:::;)a~Q..J<Zo~<to:::;)aw~CI)wao~:::;).<z<>enaUJo:::;)Qoa=Q.
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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)
Name of the Raw Material QuantityKg/ Batch
Di Isopropyl Amine 3030Sodium Hydroxide Flakes 1160Water 400Di Ethyl Sulphate 2100
3. Product: Anisole
Name of the Raw Material QuantityKg/ Batch
Phenol 1900Dimethyl Sulphate 1780Sodium Hydroxide 970Water 1800
4. Product: Phenetole
Name of the Raw Material QuantityKg/ Batch
Phenol 1700Sodium Hydroxide Flakes 930Diethyl Sulphate 2500Water 2700
5. Product: Methyl-2-Chloro Phenyl Acetate
Name of the Raw Material QuantityKg/ Batch
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
Name of the Raw Material QuantityKg/ Batch
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
Name of the Raw Material QuantityKg/ Batch
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
Name of the Raw Material QuantityKg/ Batch
Mixed Xylene 2550Para Hydroxy Benzaldehyde 1220Sodium Carbonate 780Dimethyl Sulphate 880Water 2850
11. Product: Benzaldehyde Ortho Sulphonic Acid Sodium Salt
Name of the Raw Material QuantityKg/ Batch
Ortho Chloro benzaldehyde 900Sodium Sulphite 950Water 3000Hydrochloric Acid 30% 360Sodium Hydroxide Flakes 35
63
12. Product: Benzaldehyde 2, 4 - Di Sulphonic Acid
Name of the Raw Material QuantityKg/ Batch
2,4 Dichloro Benzaldehyde 600Sodium Sulphite 930HCI 130Water 2205Sodium Hydroxide 5
13. Product: 2-Amino-2-Phenyl Butyric Acid
Name of the Raw Material QuantityKg/ Batch
Propiophenone 550Methanol 700Ammonium Bi Carbonate 660Sodium Cyanide 225Acetic Acid 135Water 800Sodium Hydroxide 675Hydrochloric Acid 30% 2000
14. Product: Ortho Hydroxy Phenyl Acetic Acid
Name of the Raw Material QuantityKg/ Batch
2-Chloro Phenyl Acetic Acid 1000Sodium Hydroxide 940Copper Sulphate 40HCI- 30% 2850Water 2200
15. Product: 2 Coumaranone
Name of the Raw Material QuantityKg/ Batch
Ortho Hydroxy Phenyl Acetic Acid 750
16. Product: Ortho Caynophenol / 2 Hydroxy Benzonitrile
Name of the Raw Material QuantityKg/ Batch
Salicylamide 620Mono Chlorobenzene 1650Thionyl Chloride 840
17. Product: 3-lsochromanone
Name of the Raw Material QuantityKg/ Batch
Ortho Methyl Phenyl Acetic Acid 1000Monochloro Benzene 1500Catalyst 20Chlorine 408Water 2000Ammonia 25% 840Toluene 600
64
18. Product: 2, 6 Dichloro Benzoyl Chloride
Name of the Raw Material QuantityKg/ Batch
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
Name of the Raw Material QuantityKg/ Batch
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
Name of the Raw Material QuantityKg/ Batch
Methyl-2-Dimethylamine-2-Phenyl 550ButyrateToluene 720Vitride 70% in Toluene 1070Sodium Hydroxide Flakes 280Water 2000
21. Product: Pivalonitrile
Name of the Raw Material QuantityKg/ Batch
Pivalic Acid 1020Ammonia 200
22. Product: Phthalide
Name of the Raw Material QuantityKg/ Batch
Phathalic Anhydride 1600Methanol 6600Rany Nickel (Catalyst) 12.20Sodium Carbonate 35Hvdroqen 50Water 350
65
23. Product: P-Bromonisole / 4-Bromo Anisole
Name of the Raw Material QuantityKg/ Batch
Anisole 1000HBr(48%) w/w 1625Hydrogen Peroxide (50%) w/w 750Water 500Sodium thiosulphate 25Water 500
24. Product: P-Bromonisole / 4-Bromo Anisole
Name of the Raw Material QuantityKg/ Batch
Phenetole 1000hydrobromic Acid (48%)w/w 1450Hydrogen Peroxide (30%)w/w 1100Sodium thio-Sulphate Soln.(5%) w/w 525
25. Product: Intermediate - P- Bromoveratrole
Name of the Raw Material QuantityKg/ Batch
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]
List of Raw Materials:
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
List of Raw Materials:
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
Caustic Soda M.W. = 40
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
List of Raw Materials:
FOR STEP III
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
Sr. No. List of Raw Materials Batch Qty. (Kg)
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.
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
Hydrochloric Acid (30%)
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
List of Raw Materials:
A] REACTIONS:
1)
+ NaCN + 2NH4HCO3 + NaHCO3 + NH4OH + H2O
2)
+ NaOH + 2H2O + NH4HCO3
3)
+ HCl + NaCl
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
Caustic Soda M.W. = 40
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
List of Raw Materials:
A] REACTIONS:
1)
+ 3NaOH + NaCl + 2H2O 2)
+ 2 HCl + 2NaCl
3)
NaOH + HCl NaCl + H2O
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
Caustic Soda M.W. = 40
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
Hydrochloric Acid (30%)
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
List of Raw Materials:
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
List of Raw Materials:
A] REACTIONS:
1)
+ Cl2 + HCl 2)
+ NH4OH + NH4Cl
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
Hydrochloric Acid (30%)
210 Kg
Catalyst 20 Kg
N2
Aqueous effluent 3298 Kg
10. 2, 6- DICHLORO BENZOYL CHLORIDE
List of Raw Materials:
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
2, 6 Dichlorobenzoic Acid
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
2, 6 Dichlorobenzoic Acid
M.W. = 191
Sodium Chloride M.W. = 58.5
COOH
Cl Cl
COOH
Cl Cl
2, 6 Dichlorobenzoic Acid
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
List of Raw Materials:
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.
Sr. No. List of Raw Materials Batch Qty. (Kg)
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
List of Raw Materials:
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
Sr. No. List of Raw Materials Batch Qty. (Kg)
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.
List of Raw Materials:
A] REACTION:
+ HBr + H2O2 + 2H2O
Sr. No. List of Raw Materials Batch Qty. (Kg)
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.
List of Raw materials:
Sr.
No.
Name of Raw Material Batch quantity
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
Sodium Chloride,MW=58.5
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
Sodium Chloride,MW=58.5
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
Stage II : Cyanation
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 II : Cyanation
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
List of Raw materials:
Sr.
No.
Name of Raw Material Batch quantity
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
List of Raw materials:
Sr.
No.
Name of Raw Material Batch quantity
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
List of Raw materials:
Sr.
No.
Name of Raw Material Batch quantity
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)
1)Ethyl alcohol(736 kg) 5)recovered ethyl alcohol
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
List of Raw materials:
Sr.
No.
Name of Raw Material Batch quantity
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)
1)Ethyl alcohol(829 kg) 5)recovered ethyl alcohol
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)
List of Raw materials:
Sr.
No.
Name of Raw Material Batch quantity
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
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 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
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 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
Stage: 1 Batches Per Month: 6
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
Stage: 1 Batches Per Month: 10
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
Stage: 1 Batches Per Month: 10
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
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
3-Amino Pyridine 250 75 N2-74
HCl 30% 2900 Hydrogen Peroxide 50%
194
Sodium Nitrate 194
Water 2200 1875
Sodium Hydroxide Flakes
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
Stage: 1 Batches Per Month: 10
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
Stage: 1 Batches Per Month: 20
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
Stage: 1 Batches Per Month: 20
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
Stage: 1 Batches Per Month: 20
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
Stage: 1 Batches Per Month: 26
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
Sodium Hydroxide Flakes
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
Stage: 1 Batches Per Month: 10
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
Sodium Hydroxide Flakes
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
Stage: 1 Batches Per Month: 7
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
Sodium Hydroxide Flakes
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
Stage: 1 Batches Per Month: 10
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
Stage: 1 Batches Per Month: 10
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
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
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
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
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
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
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
Batches per month: 20
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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'{i~C11l!\'< II i't) Ch~ 1fXUTT~ 3lffi". ~ ~ '1 +j;""'lllJ1C1 q') '<1'<'"1r~ I 1RiR 'fl'lGX
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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
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F. I ••
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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
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(If', liZ , 1UAM4) __ lIII..l I( MAAHO(D ., cUlln.
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(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
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Ga~ Area!'\. H. Arcs
G~tt j\ r-e:l~o. H. Ares:
_______ ._ • __ • __ •.•••• _ ~_ ••• , /'0 ••• _ •••• "_ •• -
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-- - - ..• ]. - -
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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
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86- 5. 28-0, 1.19 " 1 .si-o-
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'88, 7". 14'.0 124/1
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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'{)
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'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
•
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. , ~14¢!i4~') lffic(. ',-
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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
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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.