FORM-I. M/s. SRF LIMITED

FORM-I for PROPOSED EXPANSION OF SPECIALTY CHEMICALS, PESTICIDE, FLUORO CHEMICALS & CAPTIVE POWER PLANT IN EXISTING UNIT of M/s. SRF LIMITED Plot No. D-2/1, Village: Suva, GIDC Phase II, Dahej, Taluka: Vagra, District: Bharuch (Gujarat) Prepared By: NABL Accredited Testing Laboratory ISO 9001:2008 Certified Company Aqua-Air Environmental Engineers P. Ltd. 403, Centre Point, Nr. Kadiwala School, Ring Road, Surat - 395002 1

(I) Basic Information Sr. Item No. APPENDIX I FORM 1 Details 1. Name of the Project/s SRF Limited 2. S.No. in the Schedule 5(f), 5(b), 4(d) & 1(d) 3. Proposed capacity/area/length/tonnage Proposed Capacity: to be handled/command area/lease area/number of wells to be drilled Specialty Chemical & Fluoro Chemicals Products: 5,86,677 MTPA Pesticide: 500 MTPA Total Proposed Capacity : 5,86,677 MTPA + 500 MTPA = 5,87,177 MTPA Captive Power Plant: 75 MW No bore well to be drilled within the premises. 4. New/Expansion/Modernization Expansion 5. Existing capacity/area etc. Existing capacity: Specialty Chemicals & Fluoro Chemicals Products: 1,75,000 MTPA Captive Power Plant: 25 MW Existing Plot Area: 11, 81,776.35 sq.m. 6. Category of project i.e. A or B A 7. Does it attract the general condition? If N.A. yes, please specify. 8. Does it attract the specific condition? If N.A. yes, please specify. 9. Location Plot/Survey/Khasra No. Plot No. D-2/1 Village Village: Suva, GIDC Phase II, Dahej Tehsil Vagra District Bharuch State Gujarat 10. Nearest railway station/airport along with Nearest Railway Station : Bharuch: 39 kms distance in kms. Nearest Airport: Baroda: 90 kms 11. Nearest Town, city, District Headquarters Nearest town: Bharuch : 39 kms, along with distance in kms. 12. Village Panchayats, Zilla Parishad, Municipal corporation, Local body (Complete postal addresses with telephone nos. to be given) 13. Name of the applicant SRF Limited Nearest District Head quarter: Bharuch : 39 kms Village: Suva, Tal: Vagra, Dist: Bharuch, Gujarat. 2

14. Registered address Plot No. D-2/1, Village: Suva, GIDC Phase II, Dahej, Taluka: Vagra, District: Bharuch (Gujarat) 15. Address for correspondence: SRF Limited Plot No. D-2/1, Village: Suva, GIDC Phase II, Dahej, Taluka: Vagra, District: Bharuch (Gujarat) Name Mr. Dhananjay Ranade Designation (Owner/Partner/CEO) Senior Vice President & Head of Works Address Plot No. D-2/1, Village: Suva, GIDC Phase II, Dahej, Taluka: Vagra, District: Bharuch (Gujarat) Pin Code 392130 E-Mail dhananjay.ranade@srf.com Telephone No. 02641-289201 / 202 Mobile No. +919824780404 Fax No. - 16. Details of Alternative Sites examined, if No any location of these sites should be shown on a toposheet. 17. Interlinked Projects No 18. Whether separate application of Not applicable interlinked project has been submitted? 19. If Yes, date of submission Not applicable 20. If no., reason Not applicable 21. Whether the proposal involves Not applicable, as the project is located in notified industrial approval/clearance under: If yes, details estate. of the same and their status to be given. (a) The Forest (Conservation) Act, 1980? (b) The Wildlife (Protection) Act, 1972? (c) The C.R.Z Notification, 1991? 22. Whether there is any Government No order/policy relevant/relating to the site? 23. Forest land involved (hectares) No 24. Whether there is any litigation pending No against the project and/or land in which the project is propose to be set up? (a) Name of the Court (b) Case No. (c) Orders/directions of the Court, if any and its relevance with the proposed project. 3

(II) Activity 1. Construction, operation or decommissioning of the Project involving actions, which will cause physical changes in the locality (topography, land use, changes in water bodies, etc.) Sr. No. Information/Checklist confirmation 1.1 Permanent or temporary change in land use, land cover or topography including increase in intensity of land use (with respect to local land use plan) Yes /No? Details thereof (with approximate quantities / rates, wherever possible) with source of information data No Proposed Expansion Project is within existing premises of GIDC Phase II, Dahej 1.2 Clearance of existing land, vegetation and buildings? 1.3 Creation of new land uses? No -- 1.4 Pre-construction investigations e.g. bore No -- houses, soil testing? No There will be no clearance of buildings and vegetation required for the project activity. 1.5 Construction works? Yes Approved plan for construction is attached as Annexure: 1. 1.6 Demolition works? No -- 1.7 Temporary sites used for construction No -- workers or housing of construction workers? 1.8 Above ground buildings, structures or Earthworks including linear structures, cut and fill or excavations Yes Approved plan for construction is attached as Annexure: 1. 1.9 Underground works including mining or No -- tunneling? 1.10 Reclamation works? No -- 1.11 Dredging? No -- 1.12 Offshore structures? No -- 1.13 Production and manufacturing Yes List of Products and manufacturing process attached as Annexure: 2. 1.14 Facilities for storage of goods or materials? Yes Dedicated storage area for storage of Raw Materials and finished s, solvents, etc. shall be provided. 1.15 Facilities for treatment or disposal of solid waste or liquid effluents? 1.16 Facilities for long term housing of operational workers? Yes Effluent Treatment Plant will be installed to treat effluent so as to achieve the GPCB norms. Details of water consumption & effluent generation with segregation of effluent streams are attached as Annexure: 3. Details of proposed Effluent Treatment Plant are attached as Annexure: 4. Details of Hazardous waste generation and disposal is attached as Annexure: 5. No -- 4

1.17 New road, rail or sea traffic during No -- construction or operation? 1.18 New road, rail, air waterborne or other No -- airports etc? 1.19 Closure or diversion of existing transport No -- routes or infrastructure leading to changes in traffic movements? 1.20 New or diverted transmission lines or No -- pipelines? 1.21 Impoundment, damming, converting, No -- realignment or other changes to the hydrology of watercourses or aquifers? 1.22 Stream crossings? No -- 1.23 Abstraction or transfers or the water form No No ground water shall be used. The requirement ground or surface waters? of raw water shall be met through GIDC Water Supply. 1.24 Changes in water bodies or the land No -- surface affecting drainage or run-off? 1.25 Transport of personnel or materials for construction, operation or decommissioning? 1.26 Long-term dismantling or decommissioning or restoration works? 1.27 Ongoing activity during decommissioning which could have an impact on the environment? 1.28 Influx of people to an area in either temporarily or permanently? 1.29 Introduction of alien species? No 1.30 Loss of native species of genetic diversity? No 1.31 Any other actions? No No -- No There is no dismantling of any sort. Not applicable. No No Impact on the Environment No This is a well developed Industrial Area and due to project, During construction phase, approximately 800-1000 people will be required on contractual basis and their activities will be limited till the construction of the Unit. The workforce requirement for proposed project will be approximately 2000 persons including contractual workers. 5

2. Use of Natural resources for construction or operation of the Project (such as land, water, materials or energy, especially any resources which are non-renewable or in short supply): Sr. No Information/checklist confirmation Yes/ No? Details there of (with approximate quantities/rates, wherever possible) with source of information data 2.1 Land especially undeveloped or agriculture No land (ha) 2.2 Water (expected source & competing users) unit: KLD Yes Water requirement will meet through the GIDC Water Supply. For detail water balance is refer as Annexure 3. 2.3 Minerals (MT) No Not Applicable 2.4 Construction material -stone, aggregates, sand / soil (expected source MT) Yes Construction material shall be procured from nearby area (mostly within Gujarat state) 2.5 Forests and timber (source- MT) No No wood shall be used as construction material or as a fuel. 2.6 Energy including electricity and fuels Yes source, competing users Unit: fuel (MT), energy (MW) Existing Power Requirement Proposed Additional Power Total Power Requirement after Power Plant: 25 MW DG: 500 KW X 2 Nos. DG: 840 KW X 2 Nos. Requirement Power Plant: 50 MW DG: 4200 KVA X 3 Nos. 12500 KVA Grid Power Expansion Power Plant: 75 MW DG: 500 KW X 2 Nos. DG: 840 KW X 2 Nos. DG: 4200 KVA X 3 Nos 12500 KVA Grid Power Fuel Total Quantity Source Coal 2400 MT/Day ADI Tradlink 2.7 Any other natural resources (use appropriates standard units) No Furnace Oil / 400 KL/Day IOCL LSHS HSD 210 KL/Day IOCL Natural Gas 18,08,185 Sm 3 /Day GAIL/GSPL -- 6

3. Use, storage, transport, handling or ion of substances or materials, which could be harmful to human health or the environment or raise concerns about actual or perceived risks to human health. Sr. No. Information / Checklist confirmation 3.1 Use of substances or materials, which are hazardous (as per MSIHC rules) to human health or the environment (flora, fauna, and water supplies) 3.2 Changes in occurrence of disease or affect disease vectors (e.g. insect or water borne diseases) 3.3 Affect the welfare of people e.g. by changing living conditions? 3.4 Vulnerable groups of people who could be affected by the project e.g. hospital patients, children, the elderly etc., Yes/ No? Details thereof (with approximate quantities / rates wherever possible) with source of information data Yes Please refer Annexure : 7. No No No 3.5 Any other causes No Not applicable as site is located in GIDC Phase II, Dahej. Not applicable as site is located in GIDC Phase II, Dahej Not applicable as site is located in GIDC Phase II, Dahej 4. Production of solid wastes during construction or operation or decommissioning MT/month) Sr. No. Information/Checklist confirmation Yes/ No? 4.1 Spoil, overburden or mine wastes No -- 4.2 Municipal waste (domestic and or commercial wastes) Yes Details thereof (with approximate quantities / rates, wherever possible) with source of information data The domestic and industrial waste water generated is being treated in the Sewage treatment (STP) & Effluent Treatment Plant (ETP) respectively. Municipal waste will be segregated at source. 4.3 Hazardous wastes (as per Hazardous Waste Yes Management Rules) Please refer Annexure: 5 4.4 Other industrial process wastes Yes Please refer Annexure: 5 4.5 Surplus No -- 4.6 Sewage sludge or other sludge from effluent treatment Yes Please refer Annexure: 5 4.7 Construction or demolition wastes Yes There will be no demolition waste. Minor quantities of construction waste will be generated in the form of packaging material and construction waste. Proper care will be taken for handling and reduction of the solid waste generated during construction phase and ultimately the solid waste will be disposed off as per standard practice. 4.8 Redundant machinery or equipment No -- 4.9 Contaminated soils or other materials No -- 4.10 Agricultural wastes No -- 4.11 Other solid wastes No -- 7

5. Release of pollutants or any hazardous, toxic or noxious substances to air (Kg/hr) Sr. No. Information/Checklist confirmation Yes/ No? Details thereof (with approximate quantities/rates, wherever possible) with source of information data 5.1 Emissions from combustion of fossil fuels From stationary or mobile sources Yes Details of flue & process gas emission are attached as Annexure: 6 5.2 Emissions from ion processes Yes Details of emission levels from process are attached as Annexure: 6. Details of Air Pollution Control measures are attached as Annexure: 6 5.3 Emissions from materials handling including storage or transport 5.4 Emissions from construction activities including plant and equipment 5.5 Dust or odours from handling of materials including construction materials, sewage and waste Yes Fugitive emissions from material handling, loading / unloading and transport of material will be minimal due to closed loop system. Loading / Unloading systems will be also connected with the Central Absorption /scrubbing systems No Utmost care will be taken during construction activity and water sprinklers shall be utilized whenever necessary. Yes During operation phase no major source of dust is anticipated. Sewage and waste will be treated in such a manner that no odor problem arise in the area. To further improve the air atmosphere effective odor control system will be provided. 5.6 Emissions from incineration of waste No Not applicable as the Incinerable waste shall be sent to cement industries or common incineration system. 5.7 Emissions from burning of waste in open No No open burning of waste will be carried out. air (e.g. slash materials, construction debris) 5.8 Emissions from any other sources No 8

6. Generation of Noise and Vibration, and Emissions of Light and Heat: Sr. No. Information/Checklist confirmation 6.1 From operation of equipment e.g. engines, ventilation plant, crushers Yes/ No? Details there of (with approximate Quantities /rates, wherever possible) With source of source of information data Yes To the extent possible, noise from Boiler, Turbine, other machineries and equipment shall be minimized. Noise level is lower than 70 db (A) at nearest plant boundary. 6.2 From industrial or similar processes Yes All machinery / equipment shall be well maintained, shall be proper foundation with anti vibrating pads wherever applicable and noise levels within permissible limits. Acoustic enclosures shall be provided for DG set. 6.3 From construction or demolition No 6.4 From blasting or piling No 6.5 From construction or operational traffic No 6.6 From lighting or cooling systems No 6.7 From any other sources No Acoustic enclosures shall be provided for DG set. 7. Risks of contamination of land or water from releases of pollutants into the ground or into sewers, surface waters, groundwater, coastal waters or the sea: Sr. No Information/Checklist confirmation Yes/ No? Details thereof (with approximate quantities / rates, wherever possible) with source of information data 7.1 From handling, storage, use or spillage of hazardous materials Yes All the raw material shall be stored separately in designated storage area and safely. Bund walls shall be provided around raw materials storage tanks for containing any liquid spillage. Other materials shall be stored in bags / drums on pallets with concrete flooring and no spillage is likely to occur. Please refer Annexure : 7. 7.2 From discharge of sewage or other effluents to water or the land (expected mode and place of discharge) No Waste water generated will be treated in ETP and then the treated water is discharged to GIDC drain which goes to the deep sea. Liquid & solid wastes are sent to TSDF for disposal. Hence, no contamination of water body/ land is anticipated 7.3 By deposition of pollutants emitted to air No The factory is located in GIDC Phase II, Dahej. into the land or into water 7.4 From any other sources No Not applicable 7.5 Is there a risk of long term build up of pollution in the environment from these sources? Yes Full- fledged Environmental Management System (EMS) will be installed. i.e. ETP, Air Pollution Control systems, Hazardous Waste Handling and Management as per norms, etc. which will eliminates the possibility of building up of pollution. 9

8. Risks of accident during construction or operation of the Project, which could affect human health or the environment: Sr. No Information/Checklist confirmation Yes/ No? Details thereof (with approximate quantities / rates, wherever possible) with source of information data 8.1 From explosions, spillages, fires etc from storage, handling, use or ion of hazardous substances 8.2 From any other causes No Not applicable 8.3 Could the project be affected by natural disasters causing environmental damage (e.g. floods, earthquakes, landslides, cloudburst etc)? No -- Yes The risk assessment will be carried out and all mitigative measures shall be taken to avoid accidents. 9. Factors which should be considered (such as consequential development) which could lead to environmental effects or the potential for cumulative impacts with other existing or planned activities in the locality Sr. Information/Checklist confirmation No. 9.1 Lead to development of supporting. laities, ancillary development or development stimulated by the project which could have impact on the environment e.g.: * Supporting infrastructure (roads, power supply, waste or waste water treatment, etc.) housing development extractive industries supply industries other 9.2 Lead to after-use of the site, which could have an impact on the environment 9.3 Set a precedent for later developments 9.4 Have cumulative effects due to proximity to Other existing or planned projects with similar effects Yes/ Details thereof (with approximate quantities / rates, No? wherever possible) with source of information data Yes Site is located in GIDC Phase II, Dahej, having the entire required infrastructure. This industrial zone is having existing road infrastructure, power supply will be utilized. Local people will be employed and no housing is required. Please refer Annexure 8. No -- Yes The green belt area will give better aesthetic view of land and building. This should set precedence for subsequent entrepreneurs who will venture such projects. No -- 10

(III) Environmental Sensitivity Sr. No Information/Checklist confirmation Name / Identity 1 Areas protected under international conventions No national or local legislation for their ecological, landscape, cultural or other related value 2 Areas which are important or sensitive for Yes Ecological reasons - Wetlands, watercourses or other water bodies, coastal zone, biospheres, mountains, forests 3 Areas used by protected, important or sensitive No species of flora or fauna for breeding, nesting, foraging, resting, over wintering, migration 4 Inland, coastal, marine or underground waters Yes Arabian Sea: 25 Kms River Narmada: 7 Kms 5 State, National boundaries -- -- 6 Routes or facilities used by the public for to recreation or other tourist, pilgrim areas. 7 Defense installations No NIL Yes Aerial distance (within 25 km). Proposed Project Location Boundary. Site is located in GIDC Phase II, Dahej, Tal. Vagra, Dist. Bharuch, Gujarat. Site is located in GIDC Phase II, Dahej, Dist. Bharuch, Gujarat. Site is located in GIDC Phase II, Dahej, Tal: Vagra, Dist. Bharuch, Gujarat. GIDC is on 4 lane State Highway connecting at Bharuch (40 kms.) with National Highway No. 8. 8 Densely populated or built-up area Yes Nearest village: Suva, approx. 3.0 km in SE direction from the project site. Dahej town, approx. 5.0 km in NW direction from the project site. Bharuch District Headquarters approx. 39.0 km in E direction from the project site. 9 Areas occupied by sensitive man-made land No community facilities) 10 Areas containing important, high quality or scarce No resources (ground water resources, surface resources, forestry, agriculture, fisheries, tourism, tourism, minerals) 11 Areas already subjected to pollution or No environmental damage. (those where existing legal environmental standards are exceeded) 12 Are as susceptible to natural hazard which could cause the project to present environmental problems (earthquake s, subsidence,landslides, flooding erosion, or extreme or adverse climatic conditions) - N.A. 11

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ANNEXURES 1 PLANT LAYOUT 2 LIST OF PRODUCTS WITH PRODUCTION CAPACITY AND RAW MATERIALS 2A BRIEF MANUFACTRING PROCESS, CHEMICAL REACTION AND MASS BALANCE WITH FLOW DIAGRAM 3 WATER CONSUMPTION AND EFFLUENT GENERATION WITH SEGREGATION OF EFFLUENT STREAMS 4 DETAILS OF PROPOSED EFFLUENT TREATMENT PLANT 5 DETAILS OF HAZARDOUS SOLID WASTE MANAGEMENT AND DISPOSAL 6 DETAILS OF AIR POLLUTION CONTROL MEASURES 7 DETAILS HAZARDOUS CHEMICAL STORAGE FACILITY 8 SOCIO - ECONOMIC IMPACTS 9 PROPOSED TERMS OF REFERENCES 13

ANNEXURE: 1 PLANT LAYOUT 14

ANNEXURE: 2 LIST OF PRODUCTS WITH PRODUCTION CAPACITY Sr. No. Name of Product Existing Capacity (MT/Annum) Additional Capacity (MT/Annum) Proposed Capacity (MT/Annum) 1 Trifluoro Acetic Acid 0 2000 2000 2 Parabromofluorobenzene 0 500 500 3 Specialty Product i Tetrafluorobenzyl Alcohol 10000 15100 25100 ii Ethyldifluoroacetate iii Ethyltrifluroacetate iv Ethyltrifluoroacetoacetate v Amino crotonate vi Trifluoroacetic anhydride vii Pentafluorobenzoic Acid viii Pyrazole Acid ix Chlorotrichloro Methyl - Cyclopentene x 2-methyl-4-(1,1,1,2,3,3,3-heptafluoro-2- propyl aniline xi Fluoromethyl ester xii Diphenylphenol xiii Tetrafluoropropene - 1234yf xiv Isobutyl Acetophenone xv 2-Bromo-5-fluorobenzotrifluoride xvi 2,2-Difluroethylamine xvii 2,3-Dichloro-5-trifluoromethyl-pyridine xviii N[1-{6-Chloro-3-pyridinyl)methyl)-2(1H)- pyridinylidene]-2,2,2, trifluoroacetamide xix (1-(3-Chloropyridine-2-yl)-3-((5- (trifluoromethyl)-2h-tetrazol-2-yl)methyl)-1h pyrozol-5-carboxylic acid) xx (N-(4-fluorophenyl)-2-hydroxy-N-isopropylacetamide 4 1,1,2,2-Tetrafluoroethyl Methyl Ether 0 4000 4000 5 Hexafluoropropylene 0 1000 1000 6 Ethyl Difluoroacetoacetate 0 1000 1000 7 Difluoromethanesulphonlychloride 0 1000 1000 8 Triflic Acid 0 1000 1000 9 Trifluoromethanesulfonic Anhydride 0 1000 1000 10 Trimethylsilyltrifluoromethanesulfonate 0 520 520 11 3-Trifluoromethylacetophenone 0 1000 1000 12 2,6-Dichloro-4-(trifluoromethyl) aniline 0 1000 1000 15

Sr. No. Name of Product Existing Capacity (MT/Annum) Additional Capacity (MT/Annum) Proposed Capacity (MT/Annum) 13 Cyanapyrazole 0 2000 2000 14 Trifluoromethylbenzamide 0 2000 2000 15 Trifluoroacetyl chloride 0 1000 1000 16 Sulphur Tetrafluoride 0 500 500 17 2- Trifluoromethylbenzoylchloride 0 1000 1000 18 TrifluoroMethyl-2-EthoxyVinyl Ketone 0 1000 1000 19 2-(2-Methoxy-ethoxymethyl)-6-0 2000 2000 trifluoromethyl-nicotinic acid ethyl ester 20 Mefenamic Acid 0 1000 1000 21 Hexafluoropropylene oxide 0 500 500 22 Pentaflurophenol 0 500 500 23 Monomethylhydrazine 0 4000 4000 24 [3-(4,5-dihydro-1,2-oxazol-3-yl)-4-mesyl-o- 0 500 500 tolyl](5-hydroxy-1-methylpyrazol-4- yl)methanone (Topramezone) 25 Tri Fluoro acetone 0 500 500 26 Methyl tri fluoro acetate 0 500 500 27 Chlorodifluoroacetic Anhydride 0 100 100 28 Bromopentafluorobenzene 0 500 500 29 4-Chlorobenzotrichloride 0 600 600 30 4-Chlorobenzotrifluoride 0 600 600 31 Methyl HydroxyPyrazole 0 100 100 32 6-Fluoro methyl indole 0 100 100 33 Difluoroethoxy ethanol 0 200 200 34 5-Bromo-2-2-difluoro-1-3-benzodioxole 0 1000 1000 35 Difluorobenzodioxole methyl ester 0 20 20 36 2-Fluoro-5-nitrobenzoic acid 0 30 30 37 5-Chloro-3-(difluoromethyl)-1-methyl-1Hpyrazole-4-carboxaldehyde 0 500 500 38 3-Difluoromethyl-5-fluoro-1-methyl-1Hpyrazole-4-carboxaldehyde 0 500 500 39 2,5-Dichloro-4-(1,1,2,3,3,3-0 500 500 hexafluoropropoxy)benzenamine 40 2,4,5-Trifluorophenyl acetic acid 0 50 50 41 3-Aminobenzotrifluoride 0 1000 1000 42 2,4-Dichloro-3,5-dinitrobenzotrifluoride 0 1000 1000 43 3-phenoxy benzaldehyde 0 4000 4000 44 3-phenoxy toluene 0 200 200 45 Methyl-2- Fluoroacrylate 0 700 700 46 Lithium tetrakis (pentafluorophenyl) borate 0 100 100 47 2-fluoro-5-bromobenzonitrile 0 50 50 16

Sr. No. Name of Product Existing Capacity (MT/Annum) Additional Capacity (MT/Annum) Proposed Capacity (MT/Annum) 48 Ethyl-Trifluoropyruvate 0 200 200 49 Isoflurane 0 250 250 50 Desflurane 0 100 100 51 Sevoflurane 0 200 200 52 Trichloroacetyl chloride 0 2000 2000 53 Chlorinated Compound i Trichloroethylene 80000 10000 90000 ii Perchloroethylene iii Methylene dichloride iv Chloroform v Carbon tetrachloride 54 Caustic Chlorine Plant Chlorine 60000 56725 72000 Caustic lye 47.5 % 147485 187200 Hydrochloric Acid (30-33%) 17018 21600 Hydrogen 1588 2016 55 Anhydrous Hydrofluoric acid 15000 25000 40000 56 Chlorotrifluoroethane (HCFC 133a) 0 500 500 57 HFC Refrigerant i 1,1,1,2 Tetrafluroethane (HFC 134a) ii Pentafluoroethane (HFC 125) iii Difluoromethane (HFC- 32 ) iv 1,1 difluoroethane (HFC- 152a) v Refrigerant blend of Difluoromethane (HFC-32) + Pentafluoroethane (HFC-125)(R410a) vi Refrigerant blend of Pentafluoroethane (HFC- 125) + 1,1,1-Trifluoroethane (R143a) + 1,1,1,2 Tetrafluroethane (HFC 134a) (R404a) vii Refrigerant blend of Difluoromethane (HFC-32) + Pentafluoroethane (HFC-125) + 1,1,1,2 Tetrafluroethane (HFC 134a) (R407c) viii Blend of 1,1-Difluoroethane (HFC-152a) + 1,1,1,2 Tetrafluroethane (HFC-134a) 10000 52000 62000 58 Butane (R600a) 0 1000 1000 59 Propane (R290) 0 1000 1000 60 Blend of 1-Chloro-1,1-difluoroethane (R142b) 0 500 500 + Chlorodifluoromethane (R22) 61 Blend of 1,1,1,2 Tetrafluroethane (R134a) + Di 0 500 500 Methyl Ether (DME) 62 R&D Products 0 2000 2000 i Organo Heterocyclic Compounds 17

Sr. No. Name of Product Existing Capacity (MT/Annum) Additional Capacity (MT/Annum) Proposed Capacity (MT/Annum) ii Aryl/Alkyl/Alicyclic Compounds iii Elemental Fluorine/Bromine/Iodine and their Products/Derivatives iv Alkali Metal/Boron/Phosphorous/Sulphur based Product/ Derivatives 63 Hydrofluoric acid (20-70%) 0 34641 34641 64 Anhydrous Hydrochloric Acid 0 1500 1500 Total 175000 412177 587177 Sr. No. Name of Product Existing Capacity Additional Capacity Proposed Capacity 65 Captive Power Plant 25 MW 50 MW 75 MW Note: Product No. 24: [3-(4,5-dihydro-1,2-oxazol-3-yl)-4-mesyl-o-tolyl](5-hydroxy-1-methylpyrazol-4- yl)methanone (Topramezone) is a Pesticide. List of Existing and Proposed By-s Sr. No. Name of By-Product Existing Capacity (MT/Annum) Additional Capacity (MT/Annum) Proposed Capacity (MT/Annum) 1 Succinimide (C4H5NO2) 0 31 31 2 Mix of Ethane + n-butane + Isobutane (R600a) + 0 7327 7327 Propane (R290) 3 Calcium chloride 0 176 176 18

Sr. No. 1 2 LIST OF RAW MATERIALS Quantity Physical form Source Mode of Storage Trifluoro Acetic Acid Trichloroacetyl chloride 1.8860 Liquid Imported /Indigenous Barrels Hydrofluoric acid Anhydride 0.7320 Gas Indigenous Tank Sulphuric acid (98%) 1.6200 Liquid Indigenous Tank Process Water 12.5000 Liquid GIDC Tank Nitrogen 0.1500 Gas Self-Generation Tank Parabromofluorobenzene Fluorobenzene 0.6050 Liquid Imported /Indigenous Barrels Bromine 1.0500 Liquid Indigenous Tank Ferric Chloride 0.0120 Solid Indigenous Barrels Process Water 1.0000 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank 3 I Specialty Product Tetrafluorobenzyl Alcohol PentafluoroBenzonitrile 1.8100 Liquid Imported /Indigenous Barrels Potassium Phosphate 0.1300 Solid Indigenous Barrels Potassium Hydroxide 0.0020 Solid Indigenous Barrels Sodium Bi sulphite 0.0120 Solid Indigenous Barrels Sodium Borohydride 0.2650 Powder Indigenous Barrels Sodium Carbonate 0.0450 Powder Indigenous Barrels Sulphuric Acid 98% 5.4000 Liquid Indigenous Tank Zinc 0.8200 Solid Imported /Indigenous Barrels Acetic Acid 0.0100 Liquid Indigenous Tank Monoglyme 0.3800 Liquid Imported /Indigenous Barrels Activated Carbon 0.0020 Solid Indigenous Barrels Alumina Balls 0.0040 Solid Imported /Indigenous Barrels Molecular Sieve 0.0020 Solid Imported /Indigenous Barrels Methanol 1.5000 Liquid Indigenous Tank Methylene Chloride 1.4500 Liquid Indigenous Tank Process Water 17.5000 Liquid GIDC Tank ii Nitrogen 1.4000 Gas Self-Generation Tank Ethyldifluoroacetate 1,1,2,2-Tetrafluoroethyl Methyl Ether 1.2730 Liquid Imported /Indigenous Tank Ethanol 0.4300 Liquid Indigenous Tank Hydrochloric acid Anhydride 0.0550 Gas Indigenous Cylinder Therminol 55 0.0002 Liquid Imported /Indigenous Barrels Cromia 0.0020 Solid Imported /Indigenous Barrels Ferric Chloride 0.0045 Solid Indigenous Barrels Activated Carbon 0.0020 Solid Indigenous Barrels 19

Sr. No. iii iv v vi vii Quantity Physical form Source Mode of Storage Molecular Sieve 0.0020 Solid Imported /Indigenous Barrels Ceramic Balls 0.0001 Solid Indigenous Barrels Process Water 1.0278 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank Ethyltrifluroacetate Trifluoroacetal fluoride (TFAF) 0.8700 Liquid Indigenous Barrels Ethanol 0.3400 Liquid Indigenous Tank Molecular sieve 0.0070 Solid Imported /Indigenous Barrels Process Water 0.3100 Liquid GIDC Tank Nitrogen 0.3500 Gas Self-Generation Tank Ethyltrifluoroacetoacetate Ethyltrifluoroacetate 0.9100 Liquid Imported /Indigenous Tank Ethyl Acetate 0.4320 Liquid Indigenous Tank Hydrochloric Acid (HCl) 0.2700 Liquid Indigenous Tank Sodium Ethoxide 0.4800 Powder Indigenous Barrels Tri ethyl amine 0.0010 Liquid Indigenous Barrels Molecular Sieve 0.0075 Solid Imported /Indigenous Barrels Hyflow 0.0020 Solid Imported /Indigenous Barrels Process Water 2.1410 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank Amino crotonate Ethyltrifluoroacetoacetate 1.3300 Liquid Indigenous Tank Ammonia (NH3) 0.2600 Gas Indigenous Cylinder Cyclohexane 0.1600 Liquid Indigenous Barrels Process Water 1.0000 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank Trifluoroacetic anhydride Trifluoro acetic acid 1.1300 Liquid Indigenous Barrels Oleum 2.5000 Liquid Indigenous Tank Process Water 1.0000 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank Pentafluorobenzoic Acid Benzonitrile 0.8200 Liquid Indigenous Barrels Chlorine 2.8600 Liquid/gas Indigenous Cylinder Potassium Fluoride 1.9800 Solid Indigenous Barrels Caustic lye 48% 1.7500 Liquid Indigenous Tank Ferric Chloride based (Catalyst) 0.0200 Solid Indigenous Barrels Potassium Hydroxide 0.0050 Solid Indigenous Barrels Sulphuric Acid 98% 2.5000 Liquid Indigenous Tank Molecular Sieve 0.0020 Solid Imported /Indigenous Barrels Activated Carbon 0.0150 Solid Indigenous Barrels 20

Sr. No. viii Quantity Physical form Source Mode of Storage Methanol 0.1200 Liquid Indigenous Tank Toluene 0.4500 Liquid Indigenous Tank Process Water 5.8460 Liquid GIDC Tank Nitrogen 2.0500 Gas Self-Generation Tank Pyrazole Acid - P-17a Ethyldifluoroacetate 1.3185 Liquid Indigenous Tank Acetic Anhydride 1.8000 Liquid Indigenous Tank Anhydrous Ammonia 0.0620 Gas Indigenous Cylinder Anhydrous HCl 0.4652 Gas Imported /Indigenous Cylinder Caustic lye (48%) 1.9410 Liquid Indigenous Tank HCl 30% 1.5290 Liquid Indigenous Tank MMH (35%) 1.0220 Liquid Imported /Indigenous Tank Sodium Ethoxide 0.7400 Powder Indigenous Barrels Sodium Fluoride 0.0130 Solid Indigenous Barrels Trimethylorthoformate 1.2000 Solid Indigenous Barrels Potassium Carbonate 0.1150 Solid Indigenous Barrels Hyflow 0.0270 Liquid Indigenous Barrels Molecular Sieve 0.0020 powder Indigenous Barrels Precipitated Silica 0.0220 Solid Imported /Indigenous Barrels Mix Xylene 0.1200 Solid Imported /Indigenous Barrels Ethyl Acetate 1.1770 Powder Imported /Indigenous Barrels Process Water 14.8100 Liquid GIDC Tank Nitrogen 1.1000 Liquid Self-Generation Tank Pyrazole Acid - P-17b Ethyldifluoroacetate 1.4300 Liquid Indigenous Tank Acetic Anhydride 3.1500 Liquid Indigenous Tank Acetone 2.0500 Liquid Indigenous Tank Anhydrous Ammonia 0.0672 Gas Imported /Indigenous Cylinder Anhydrous HCl 0.5041 Gas Indigenous Cylinder Cautic lye (48%) 0.8800 Liquid Indigenous Tank MMH (35%) 0.8600 Liquid Imported /Indigenous Tank Sodium Ethoxide 0.9106 Powder Indigenous Barrels Sodium Fluoride 0.0141 Solid Indigenous Barrels Sulphuric Acid (98%) 0.5332 Liquid Indigenous Tank Trimethylorthoformate 1.7300 powder Indigenous Barrels Ethyl Acetate 2.1246 Liquid Indigenous Tank Process Water 16.3000 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank Pyrazole Acid - P-17 DMAN 0.9303 Liquid Indigenous Barrels TFEMe 0.8000 Liquid Indigenous Barrels 21

Sr. No. ix x Quantity Physical form Source Mode of Storage NaOH (48%) 1.2630 Liquid Indigenous Tank MMH soln (35%) 0.7897 Liquid Imported /Indigenous Barrels Dry HCl 1.1000 Gas Imported /Indigenous Cylinder HCl (on 100% basis) as 30% solution 0.7000 Liquid Indigenous Tank TEA 0.3800 Liquid Imported /Indigenous Barrels Toluene 1.0000 Liquid Indigenous Tank Methanol 0.1000 Liquid Indigenous Tank Process Water 13.3000 Liquid GIDC Tank Nitrogen 0.3000 Gas Self-Generation Tank Chlorotrichloro Methyl - Cyclopentene Carbon tetrachloride 0.6990 Liquid Indigenous Tank Caustic Flakes 0.0216 Crystals. Indigenous Barrels Cuprous Chloride 0.0770 Crystals. Indigenous Barrels Dicyclopentadiene (DCPD) 0.3808 Liquid Imported /Indigenous Barrels K2CO3 0.0080 powder Indigenous Barrels Monochlorobenzene (MCB) 0.0780 Liquid Imported /Indigenous Tank Tetramethyl ethylene diamine 0.0200 Liquid Imported /Indigenous Barrels Ceramic balls 0.0015 Solid Indigenous Barrels Molecular Sieve 0.0061 Solid Imported /Indigenous Barrels Methyl isobutyl Ketone (MIBK) 0.1290 Liquid Indigenous Barrels Mix Xylene 0.3070 Liquid Indigenous Tank Process Water 4.3960 Liquid GIDC Tank Nitrogen 0.3000 Gas Self-Generation Tank 2-methyl-4-(1,1,1,2,3,3,3-heptafluoro-2-propyl) aniline Hexafluoropropylene (HFP) 1.1860 Gas Indigenous Cylinder Anhydrous HCl 0.2470 Gas Imported /Indigenous Cylinder Bromine 1.2630 Liquid Indigenous Tank Caustic Flakes 0.3600 Crystals. Indigenous Barrels Caustic Lye (48%) 0.3300 Liquid Indigenous Tank Dimethylformamide 0.8923 Liquid Indigenous Tank HCl 30% 0.1910 Liquid Indigenous Tank Ammonium hydroxide solution (25%) 0.9210 Liquid Indigenous Barrels K2CO3 0.0300 powder Indigenous Barrels Potassium Fluoride (KF) 0.8730 Solid Indigenous Barrels Sodium dithionite (Na2S2O4) 0.2680 Powder Indigenous Barrels Tetrabutylammoniumhydrogensulfate 0.2090 Solid Imported /Indigenous Barrels Methyl tert-butyl ether (MTBE) 0.5425 Liquid Indigenous Barrels O-Toluedine 0.6600 Liquid Indigenous Barrels Toluene 1.9854 Liquid Indigenous Tank Process Water 17.6000 Liquid GIDC Tank 22

Sr. No. xi xii xiii xiv xv Quantity Physical form Source Mode of Storage Nitrogen 2.0000 Gas Self-Generation Tank Fluoromethyl ester Chloro Malonic Ester 1.4570 Liquid Imported /Indigenous Barrels CaO 1.2600 Solid Indigenous Barrels Anhydrous Hydrogen fluoride 0.8990 Gas Indigenous Tank NaOH (33%) 2.1782 Liquid Indigenous Tank Triethylamine 0.2540 Liquid Indigenous Barrels Toluene 0.2250 Liquid Indigenous Tank Process Water 57.5224 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank Diphenylphenol Cyclohexanone 4.4170 Liquid Indigenous Tank Heptane 0.5870 Liquid Indigenous Barrels Isopropanol 0.4350 Liquid Indigenous Barrels NaOH Solution (25%) 0.2040 Liquid Indigenous Tank Paladium /alumina 0.0590 Solid Imported /Indigenous Barrels Phosphoric Acid (85%) 0.0490 Liquid Indigenous Barrels Potassium Carbonate 0.0460 powder Indigenous Barrels Xylene 0.0590 Liquid Indigenous Tank Process Water 6.0960 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Tetrafluoropropene - 1234yf Chlorodifluoromethane 1.9200 Liquid Imported /Indigenous Tank Caustic lye 48% 0.2000 Liquid Indigenous Tank Sulphuric Acid 98% 0.0070 Liquid Indigenous Tank Methanol 0.3600 Liquid Indigenous Tank Process Water 1.2910 Liquid GIDC Tank Isobutyl Acetophenone Isobutylbenzene 0.7600 Liquid Imported /Indigenous Tank Acetic anhydride 0.5800 Solid Indigenous Tank Hydrogen Fluoride 0.2600 Liquid Indigenous Tank Process Water 0.6100 Liquid GIDC Tank Nitrogen 0.1000 Liquid/gas Self-Generation Tank 2-Bromo-5-fluorobenzotrifluoride 3-(Trifluoromethyl)aniline (m-abtf) 1.0600 Liquid Imported /Indigenous Tank Acetyl Chloride 0.6200 Liquid Indigenous Tank Sodium Hydroxide (48%) 2.6000 Liquid Indigenous Tank Methylene Chloride 1.1000 Liquid Indigenous Tank Bromine 0.8000 Liquid Indigenous Tank Sodium hydrogen sulfite 1.0000 Solid Indigenous Barrels Hydrochloric Acid 0.3600 Liquid Indigenous Tank 23

Sr. No. xvi xvii xviii xix Quantity Physical form Source Mode of Storage Anhydrous Hydrofluoric Acid 0.6000 Liquid Indigenous Tank Sodium nitrite 0.5400 Solid Indigenous Barrels Pyridine 0.0400 Liquid Indigenous Tank Methanol 1.5000 Liquid Indigenous Tank Process Water 7.0000 Liquid GIDC Tank 2,2-Difluroethylamine 1,1,2-Trichloroethane (TCA) 2.3510 Liquid Indigenous Tank Hydrogen Fluoride 1.0570 Liquid Indigenous Tank Ammonia (25%) Solution in Water 2.3170 Liquid Indigenous Tank Process Water 7.2950 Liquid GIDC Tank Nitrogen 0.2000 Liquid/gas Self-Generation Tank 2,3-Dichloro-5-trifluoromethyl-pyridine 2,3-Dichloro-5-trichloromethyl pyridine 2.0500 Liquid Imported /Indigenous Tank Hydrogen Fluoride 0.5100 Liquid Indigenous Tank Dichloromethane 0.2600 Liquid Indigenous Tank Potassium Carbonate 2.3100 Solid Indigenous Barrels Process Water 2.0800 Liquid GIDC Tank Nitrogen 0.1000 Liquid/gas Self-Generation Tank Oxygen 0.2500 Gas Indigenous Cylinder N[1-{6-Chloro-3-pyridinyl)methyl)-2(1H)-pyridinylidene]-2,2,2, trifluoroacetamide 2-Aminopyridine 0.3500 Liquid Imported /Indigenous Tank Trifluoroacetic Acid 0.4400 Liquid Indigenous Tank Thionyl Chloride 0.4800 Liquid Indigenous Tank 2-Chloro-5(chloromethyl) Pyridine 0.5200 Liquid Indigenous Tank (CPMC) Potassium Carbonate 0.3900 Solid Indigenous Barrels Pyridine 0.2600 Liquid Indigenous Tank Ethyl Acetate 0.5900 Liquid Indigenous Tank Dimethyl sulfoxide 0.2000 Liquid Indigenous Tank Methanol 0.3200 Liquid Indigenous Tank Process Water 11.7000 Liquid GIDC Tank (1-(3-Chloropyridine-2-yl)-3-((5-(trifluoromethyl)-2H-tetrazol-2-yl)methyl)-1H pyrozol-5-carboxylic acid) HYPE 0.9400 Liquid Imported /Indigenous Tank Thionyl Chloride 0.5100 Liquid Indigenous Tank Sodium bicarbonate (8%) 3.6700 Solid Indigenous Barrels Potassium Iodide 0.0600 Solid Indigenous Barrels 5-(Trifluoromethyl)-2H-tetrazole sodium 0.5900 Liquid Indigenous Tank salt (TFMT-Na) Sodium Hydroxide (32%) 0.4300 Liquid Indigenous Tank Hydrochloric Acid (20%) 0.6900 Liquid Indigenous Tank Toluene 4.4400 Liquid Indigenous Tank 24

Sr. No. xx 4 5 Quantity Physical form Source Mode of Storage Acetone 0.1700 Liquid Indigenous Tank Methanol 1.9400 Liquid Indigenous Tank Process Water 11.7800 Liquid GIDC Tank (N-(4-fluorophenyl)-2-hydroxy-N-isopropyl-acetamide 4-Fluoro-nitrobenzene 0.9800 Liquid Indigenous Tank Chloroacetyl chloride 0.7700 Liquid Indigenous Tank Sodiumcarbonate 0.6900 Solid Indigenous Barrels N-methyl-pyrollidone (NMP) 0.2900 Solid Imported /Indigenous Barrels Acetone 0.4400 Liquid Indigenous Tank Toluene 0.6900 Liquid Indigenous Tank Process Water 2.8900 Liquid GIDC Tank Hydrogen 0.0700 Gas Indigenous Cylinder Nitrogen 0.1000 Liquid/gas Self-Generation Tank 1,1,2,2-Tetrafluoroethyl Methyl Ether Chlorodifluoromethane (R 22) 1.9250 Liquefied Gas Imported /Indigenous Tank H2SO4 (98%) 0.8500 Liquid Indigenous Tank Caustic Lye (48%) 0.2610 Liquid Indigenous Tank Dimethylformamide 0.0060 Liquid Indigenous Tank Sodium Methoxide (30%) 0.0600 Liquid Indigenous Tank Sodium Sulphite 0.0010 Solid Indigenous Barrels Terpene 0.0150 Liquid Indigenous Barrels Activated Alumina Balls 0.0010 Solid Imported /Indigenous Barrels Molecular Sieve 0.0010 Solid Imported /Indigenous Barrels Silica Gel 0.0010 Crystal Indigenous Barrels Methanol 0.3000 Liquid Indigenous Tank Process Water 4.6350 Liquid GIDC Tank Nitrogen 0.2650 Gas Self-Generation Tank Hexafluoropropylene Chlorodifluoromethane (R 22) 3.2350 Liquefied Gas Imported /Indigenous Tank H2SO4 (98%) 0.9500 Liquid Indigenous Tank Caustic Lye (48%) 0.3450 Liquid Indigenous Tank Dimethylformamide 0.0060 Liquid Indigenous Tank Sodium Sulphite 0.0010 Solid Indigenous Barrels Terpene 0.0150 Liquid Indigenous Barrels Activated Alumina Balls 0.0010 Solid Imported /Indigenous Barrels Molecular Sieve 0.0010 Solid Imported /Indigenous Barrels Silica Gel 0.0010 Crystal Indigenous Barrels Methanol 0.1200 Liquid Indigenous Tank Process Water 6.4740 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank 6 Ethyl Difluoroacetoacetate 25

Sr. No. 7 8 9 Quantity Physical form Source Mode of Storage Ethyldifluoroacetate 1.0420 Liquid Indigenous Tank Anhydrous Ammonia 0.0310 Gas Indigenous Cylinder Anhydrous HCl 0.3850 Gas Imported /Indigenous Cylinder Ethyl Acetate 2.0000 Liquid Indigenous Tank Sodium Ethoxide 0.6180 Powder Indigenous Barrels Sodium Fluoride 0.0200 Solid Indigenous Barrels Hyflow 0.0100 Solid Imported /Indigenous Barrels Molecular Sieve 0.0020 Solid Imported /Indigenous Barrels Process Water 2.3050 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank Difluoromethanesulphonlychloride Chlorodifluoromethane (R22) 1.0300 Liquefied Gas Imported /Indigenous Tank Benzyl Chloride 0.5900 Liquid Indigenous Barrels Chlorine 2.4600 Liquid/gas Indigenous Cylinder Caustic Lye 48% 3.7300 Liquid Indigenous Tank Dilute Hydrochloric Acid 10-30% 1.8800 Liquid Indigenous Tank Methylene Chloride 0.2300 Liquid Indigenous Tank Thiourea 0.8900 Crystalline Imported /Indigenous Barrels Process Water 7.7500 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank Triflic Acid Methanesulfonyl chloride (MSCl) 1.1690 Liquid Imported /Indigenous Tank Potassium Fluoride (KF) 0.6037 Solid Indigenous Barrels Calcium Hydroxide 0.4088 Solid Indigenous Barrels Hydrogen Peroxide (H2O2) 0.0500 Liquid Indigenous Barrels Anhydrous Hydrogen Fluoride (AHF) 0.9079 Gas Indigenous Tank Potassium Hydroxide 2.7298 Flakes Indigenous Barrels Sulphuric Acid 3.2940 Liquid Indigenous Tank Oleum 1.0890 Liquid Indigenous Tank Acetone 0.6198 Liquid Indigenous Tank Dichloromethane (DCM) 0.1289 Liquid Indigenous Barrels Process Water 1.5047 Liquid GIDC Tank Nitrogen 0.2429 Gas Self-Generation Tank Trifluoromethanesulfonic Anhydride Triflic Acid (P-21) 1.3289 Liquid Imported /Indigenous Barrels 48% KOH 0.8333 Flakes Indigenous Barrels P2O5 1.3057 Crystalline Indigenous Barrels Parabromofluoro Benzene (P-4) 0.5343 Liquid Indigenous Barrels Celite 0.0322 Solid Imported /Indigenous Barrels Potassium Fluoride (KF) 0.0200 Solid Indigenous Barrels Process Water 2.1911 Liquid GIDC Tank 26

Sr. No. 10 11 12 13 Quantity Physical form Source Mode of Storage Nitrogen 0.1000 Gas Self-Generation Tank Trimethylsilyltrifluoromethanesulfonate Triflic Acid 0.7115 Liquid Imported /Indigenous Barrels Trimethylsilyl chloride 0.5440 Liquid Imported /Indigenous Barrels Process Water 1.5238 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank 3-Trifluoromethylacetophenone 3-Aminobenzotrifluoride (TFMA) 1.3300 Liquid Imported /Indigenous Barrels Acetaldoxime 50% 1.3000 Liquid Imported /Indigenous Barrels Acetic Acid 0.4900 Liquid Indigenous Tank Caustic Lye 48% 2.2752 Liquid Indigenous Tank CuSO4 Solution 10.7% 0.7700 Liquid Indigenous Barrels Dilute Hydrochloric Acid 10-30% 1.8000 Liquid Indigenous Tank H2SO4 98% 1.5600 Liquid Indigenous Tank KHCO3 Solution 25% 0.1637 Crystalline Indigenous Barrels Sodium Nitrite 0.6100 Solid Indigenous Barrels Mix Xylene 0.4500 Liquid Indigenous Tank Process Water 12.7160 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank 2,6-Dichloro-4-(trifluoromethyl) aniline P-Chloro toluene 1.3890 Liquid Indigenous Tank Chlorine 3.8860 Liquid/gas Indigenous Cylinder Copper 0.0600 Powder Indigenous Barrels Copper Acetate 0.4720 Powder Indigenous Barrels Hydrofluoric Acid (HF) 0.6670 Gas Indigenous Tank NH3 Solution 25% 1.0810 Liquid Indigenous Tank N-methyl-pyrollidone 0.6330 Solid Imported /Indigenous Barrels Caustic Lye 48% 1.9100 Liquid Indigenous Tank Hexane 0.6470 Liquid Indigenous Tank Process Water 10.7040 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Cyanapyrazole P-Chloro toluene 1.1950 Liquid Indigenous Tank Chorine 3.3420 Gas Indigenous Cylinder Caustic Lye 48% 2.3300 Liquid Indigenous Tank Copper Acetate 0.4060 Powder Indigenous Barrels Copper Powder 0.0520 Powder Indigenous Barrels Dilute Hydrochloric Acid 10-30% 1.4400 Liquid Indigenous Tank Hydrofluoric Acid (HF) 0.5740 Gas Indigenous Tank Methylene Chloride 1.0300 Liquid Indigenous Tank NaNO2 0.2820 Liquid Indigenous Barrels 27

Sr. No. 14 15 16 17 Quantity Physical form Source Mode of Storage NH3 Solution 25% 0.9300 Liquid Indigenous Tank N-methyl-pyrollidone 0.5190 Solid Imported /Indigenous Barrels Acetic acid 2.2300 Liquid Indigenous Tank Synthon-2 0.5650 Liquid Imported /Indigenous Barrels Hexane 0.0930 Liquid Indigenous Tank Toluene 0.0590 Liquid Indigenous Tank Process Water 25.2800 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank Trifluoromethylbenzamide O-Xylene 1.1830 Liquid Indigenous Tank Ammonia Sol. -25% 1.4310 Liquid Indigenous Tank Caustic Lye 48% 8.5942 Liquid Indigenous Tank Chlorine 7.9965 Liquid/gas Indigenous Cylinder Hydrofluoric acid Anhydrous 1.1365 Gas Indigenous Tank Methylene Chloride 1.4196 Liquid Indigenous Tank AIBN 0.0572 Fine crystals Imported /Indigenous Barrels Sulphuric Acid 98% 22.4141 Liquid Indigenous Tank Process Water 50.2290 Liquid GIDC Tank Nitrogen 9.8370 Gas Self-Generation Tank Trifluoroacetyl chloride Hydrogen Fluoride 0.7500 Gas Indigenous Tank Chlorine 3.1600 Liquid/gas Indigenous Cylinder Charcoal 0.2100 Solid Indigenous Barrels 48% NaOH Solution 6.0500 Liquid Indigenous Tank Acetic Acid 0.5100 Liquid Indigenous Tank Process Water 4.9100 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank Sulphur Tetrafluoride Fluorine 0.7950 Gas Indigenous Cylinder Sulphur 0.2960 Solid Indigenous Barrels Alumina Balls 0.0010 Solid Imported /Indigenous Barrels Molecular Sieve 0.0010 Solid Imported /Indigenous Barrels Process Water 3.3330 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank 2- Trifluoromethylbenzoylchloride O-Xylene 0.7340 Liquid Indigenous Tank Chlorine 4.9600 Liquid/gas Indigenous Cylinder AIBN 0.0360 Fine crystals Imported /Indigenous Barrels Anhydrous hydrofluoric acid 0.7047 Gas Indigenous Tank NaOH (48%) 5.3310 Liquid Indigenous Tank H2SO4 (98%) 11.2570 Liquid Indigenous Tank 28

Sr. No. 18 19 Quantity Physical form Source Mode of Storage C2 0.7157 Gas Indigenous Cylinder Process Water 25.3720 Liquid GIDC Tank Nitrogen 0.1810 Gas Self-Generation Tank TrifluoroMethyl-2-EthoxyVinyl Ketone Trifluoro Acetyl Fluoride 1.4286 Gas Imported /Indigenous Cylinder Ethyl Vinyl Ether 0.8571 Liquid Imported /Indigenous Barrels Tri Ethyl Amine 0.4286 Liquid Indigenous Barrels Process Water 2.4571 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank 2-(2-Methoxy-ethoxymethyl)-6-trifluoromethyl-nicotinic acid ethyl ester Methoxy AA 0.8403 Liquid Imported /Indigenous Barrels NH3 Solution 25% 0.0790 Liquid Indigenous Tank Toluene 0.1000 Liquid Indigenous Tank Trifluoromethyl-2-ethoxyvinyl Ketone 0.7143 Liquid Imported /Indigenous Barrels Acetic Acid 0.0244 Liquid Indigenous Tank Process Water 2.0000 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank 20 Mefenamic Acid Methoxy AA 0.7000 Liquid Imported /Indigenous Barrels NH3 Solution 25% 0.0660 Liquid Indigenous Tank Toluene 0.1070 Liquid Indigenous Tank Trifluoromethyl-2-ethoxyvinyl Ketone 0.5950 Liquid Imported /Indigenous Barrels Acetic Acid 0.0200 Liquid Indigenous Tank Caustic Lye 30% 0.3830 Liquid Indigenous Tank Dilute Hydrochloric Acid 10-30% 0.3500 Liquid Indigenous Tank Xylene 0.1580 Liquid Indigenous Tank Process Water 0.3913 Liquid GIDC Tank Nitrogen 0.2132 Gas Self-Generation Tank 21 Hexafluoropropylene oxide 12.5% NaOH Solution 6.5975 Liquid Indigenous Tank Chlorine 0.6667 Liquid/gas Indigenous Cylinder HFP 1.5000 Gas Indigenous Tank Toluene 0.5000 Liquid Indigenous Tank Na2CO3 0.2106 Solid Indigenous Barrels PTC 0.0111 Liquid Imported /Indigenous Barrels 35% HCl Solution 0.2870 Liquid Indigenous Tank 30% H2O2 Solution 0.0025 Liquid Indigenous Barrels 20% H2SiF6 Solution 8.8781 Liquid Indigenous Barrels Process Water 3.0280 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank 22 Pentaflurophenol 29

Sr. No. 23 24 Quantity Physical form Source Mode of Storage Bromopentafluorobenzene 1.7143 Liquid Imported /Indigenous Barrels Magnesium 0.1679 Solid Indigenous Barrels Boron trifluorideethereate 0.3429 Liquid Imported /Indigenous Barrels H2O2 0.2393 Liquid Indigenous Barrels NaOH 0.2857 Liquid Indigenous Tank HCl 0.4054 Liquid Indigenous Tank Diethylether 0.3179 Liquid Indigenous Barrels Toluene 0.2714 Liquid Indigenous Tank Process Water 10.1210 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank Monomethylhydrazine Hydrazine Hydrate 100% 0.8170 Liquid Indigenous Tank HCl 0.9583 Liquid Indigenous Tank NaOH 0.6185 Liquid Indigenous Tank Methanol 1.8954 Liquid Indigenous Tank Process Water 1.0000 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank [3-(4,5-dihydro-1,2-oxazol-3-yl)-4-mesyl-o-tolyl](5-hydroxy-1-methylpyrazol-4-yl)methanone (Topramezone) 3-Nitro-o-xylol 1.5031 Liquid Imported /Indigenous Barrels 1,4-Dioxane (C4H8O2) 0.9417 Liquid Imported /Indigenous Tank Acetic Acid 0.4104 Liquid Indigenous Tank Activated Carbon 0.0700 Solid Indigenous Barrels Butyl Acetate 8.0272 Liquid Indigenous Tank Butyl Nitrite 1.8600 Liquid Indigenous Barrels Carbon monoxide 0.3084 Compressed Indigenous Cylinder gas Caustic Lye (48%) 0.4781 Liquid Indigenous Tank Chlorine 0.6212 Liquid/gas Indigenous Cylinder Copper 0.0039 Powder Indigenous Barrels Dimethyl disulfide (C2H6S2) 0.8816 Liquid Indigenous Barrels Ethylene 0.9158 Gas Indigenous Cylinder Hydrochloric acid (15-33%) 6.1618 Liquid Indigenous Tank Hydrochloric acid Anhydride 1.8413 Gas Indigenous Cylinder Hydrogen 0.0382 colorless gas Indigenous Cylinder Hydrogen bromide 1.0417 Liquid Indigenous Tank Hydrogen peroxide 1.3200 Liquid Indigenous Barrels MHP (C4H6N2O) 0.3598 Liquid Imported /Indigenous Barrels Potassium carbonate (K2CO3) 2.4250 powder Indigenous Barrels Potassium methoxide 1.1347 Solid Indigenous Barrels Potassium sulfite 0.0571 Crystalline Indigenous Barrels 30

Sr. No. 25 26 27 28 29 30 Quantity Physical form Source Mode of Storage Pyridine 0.7408 Liquid Indigenous Barrels TPP 0.0385 Liquid Indigenous Barrels Sodium Tungstate Dihydrate 0.0042 Crystals and Imported /Indigenous Barrels (Na2WO4.2H2O) fragments Palladium chloride (PdCl2) 0.0013 Solid Indigenous Barrels Palladium on carbon 0.0021 Powder Indigenous Barrels Methanol 2.8300 Liquid Indigenous Tank Dimethylformamide 4.7776 Liquid Indigenous Tank Process Water 4.2464 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank Tri Fluoro acetone Ethyltrifluoroacetoacetate 1.7857 Liquid Indigenous Barrels H2SO4 0.3600 Liquid Indigenous Tank Process Water 1.5000 Liquid GIDC Tank Nitrogen 0.4480 Gas Self-Generation Tank Methyl tri fluoro acetate TFAF 0.9060 Liquid Indigenous Barrels Methanol 0.2500 Liquid Indigenous Tank Process Water 0.3750 Liquid GIDC Tank Nitrogen 0.0500 Gas Self-Generation Tank Chlorodifluoroacetic Anhydride Chlorodifluoroacetic acid(cdfa) 2.1300 Liquid Indigenous Barrels Oleum 4.4304 Liquid Indigenous Tank Process Water 0.5250 Liquid GIDC Tank Nitrogen 0.0200 Gas Self-Generation Tank Bromopentafluorobenzene Pentafluorobenzene 0.8520 Liquid Indigenous Barrels Bromine 0.9020 Liquid Indigenous Tank Aluminium Chloride 0.0720 Powder Indigenous Barrels Sodium thiosulphate 0.0025 Powder Indigenous Barrels Process Water 1.3310 Liquid GIDC Tank Nitrogen 0.0300 Gas Self-Generation Tank 4-Chlorobenzotrichloride P-Chloro toluene 0.6500 Liquid Indigenous Tank Chlorine 1.5400 Liquid/gas Indigenous Cylinder Caustic Lye 48% 1.4500 Liquid Indigenous Tank Process Water 1.6600 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank 4-Chlorobenzotrifluoride P-Chloro toluene 0.8000 Liquid Indigenous Tank Chlorine 1.7300 Gas Indigenous Cylinder 31

Sr. No. 31 32 33 Quantity Physical form Source Mode of Storage Hydrofluoric Acid (AHF) 0.5600 Gas Indigenous Tank Caustic Lye 48% 1.8400 Liquid Indigenous Tank Process Water 3.8500 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank Methyl HydroxyPyrazole Diethyl ethoxymethylenemalonate (DEMM) 2.7700 Liquid Imported /Indigenous Barrels Diethylamine (DEA) 0.1170 Liquid Indigenous Barrels Monomethyl Hydrazine (MMH)(35%) 1.8900 Liquid Imported /Indigenous Tank Solution HCl (35%) Solution 4.2000 Liquid Indigenous Tank Dioxane 0.9960 Liquid Indigenous Barrels Aqueous Ammonia Solution (15%) 1.3600 Liquid Indigenous Tank Methanol 1.3600 Liquid Indigenous Tank Process Water 8.8400 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank 6-Fluoro methyl indole Difluorobenzene 1.3004 Liquid Indigenous Barrels Acetic Anhydrite 2.3177 Gas Indigenous Cylinder Caustic lye 9.8360 Liquid Indigenous Tank Dimethyl Sulfoxide (C2H6OS) 2.0307 Liquid Indigenous Barrels Ethyl Acetate 4.0000 Liquid Indigenous Tank HCl 30% 2.3373 Liquid Indigenous Tank Iron Powder 2.6462 Granules Indigenous Barrels Methyl Acetoacetate 1.9681 Liquid Indigenous Barrels Methylene chloride 4.0000 Liquid Indigenous Tank NaCl 0.9217 Solid Indigenous Barrels Nitric Acid 0.9193 Liquid Indigenous Barrels Potassium Carbonate 5.1425 powder Indigenous Barrels Sodium Acetate 0.7287 Solid Indigenous Barrels Sodium bicarbonate 2.6333 Crystalline Indigenous Barrels Sulphuric acid (98%) 5.9240 Liquid Indigenous Tank Acetic Acid 8.3892 Liquid Indigenous Tank Heptane 2.7298 Liquid Indigenous Barrels Hexane 4.0000 Liquid Indigenous Tank Toluene 4.0000 Liquid Indigenous Tank Process Water 54.9484 Liquid GIDC Tank Nitrogen 1.0000 Gas Self-Generation Tank Difluoroethoxy ethanol EDFA 0.9900 Diethyl Ether 1.1800 Liquid Indigenous Barrels 32

Sr. No. 34 35 36 Quantity Physical form Source Mode of Storage Lithium Aluminium hydride 0.1000 Solid Indigenous Barrels Ethanol 0.0200 Liquid Indigenous Tank H2SO4 Solution 98% 1.7100 Liquid Indigenous Tank NaHCO3 0.2700 Solid Indigenous Barrels Process Water 7.5300 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank 5-Bromo-2-2-difluoro-1-3-benzodioxole 1-3 Benzodioxole 0.8028 Liquid Imported /Indigenous Barrels Phosphorus pentachloride 2.5090 Powder Imported /Indigenous Barrels Hydrofluoric Acid (AHF) 0.6251 Gas Indigenous Tank HBr 2.0478 Gas Indigenous Cylinder H2O2 50% 0.7651 Liquid Indigenous Barrels Methylene Chloride 0.5100 Liquid Indigenous Tank Process Water 6.2440 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Difluorobenzodioxole methyl ester 1,3 Benzodioxole 1.0078 Liquid Indigenous Barrels 48%NaOH 1.2600 Liquid Indigenous Tank Bromine 1.3200 Liquid Indigenous Tank Hydrochloric acid (15-33%) 0.2400 Liquid Indigenous Tank Hydrofluoric acid Anhydride 0.4100 Gas Indigenous Tank Iron 0.2300 Powder Imported /Indigenous Barrels Methylene chloride 0.4900 Liquid Indigenous Tank n-butyllithium 0.5300 Liquid Indigenous Barrels Phosphorus pentachloride 4.3000 Powder Imported /Indigenous Barrels Sodium Chloride 0.9700 Solid Indigenous Barrels Sulphuric acid (98%) 0.0800 Liquid Indigenous Tank Chloroform 1.4800 Liquid Indigenous Barrels Methanol 0.7900 Liquid Indigenous Tank THF 7.4300 Liquid Indigenous Tank Process Water 6.8800 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank 2-Fluoro-5-nitrobenzoic acid Anthranilic acid 0.9675 Solid Indigenous Barrels Sodium nitrite (NaNO2) 0.5409 Solid Indigenous Barrels AHF 0.3672 Gas Indigenous Cylinder Monoglyme 0.6852 Liquid Imported /Indigenous Barrels Conc. Nitric acid 1.4157 Liquid Indigenous Barrels Conc. Sulfuric acid 1.7856 Liquid Indigenous Tank Methylene dichloride 0.6003 Liquid Indigenous Tank Process Water 13.4747 Liquid GIDC Tank 33

Sr. No. 37 38 39 Quantity Physical form Source Mode of Storage Nitrogen 0.2000 Gas Self-Generation Tank 5-Chloro-3-(difluoromethyl)-1-methyl-1H-pyrazole-4-carboxaldehyde Ethyldifluoroacetoacetate 1.4000 Liquid Imported /Indigenous Tank Difluorobenzene 0.7960 Liquid Indigenous Barrels Formic acid (HCOOH) 0.3960 Liquid Indigenous Barrels Methyl tertiary-butyl ether 0.5080 Liquid Indigenous Tank Monomethylhydrazine 0.6500 Liquid Imported /Indigenous Tank Phosphorus oxychloride (POCl3) 2.1400 Liquid Imported /Indigenous Barrels Sodium bicarbonate (NaHCO3) 0.1760 Crystalline Indigenous Barrels Dimethylformamide 0.5600 Liquid Indigenous Tank Toluene 0.7778 Liquid Indigenous Tank Process Water 17.5220 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank 3-Difluoromethyl-5-fluoro-1-methyl-1Hpyrazole-4-carboxaldehyde Ethyldifluoroacetoacetate 2.3155 Liquid Imported /Indigenous Tank Chlorobenzene 1.3060 Liquid Indigenous Tank Dimethylamine 1.3530 Liquid Indigenous Barrels Caustic lye/ Flakes 0.0040 Liquid Indigenous Tank Formic acid (HCOOH) 0.6491 Liquid Indigenous Barrels Methyl tertiary-butyl ether 0.8432 Liquid Indigenous Tank Mono methylhydrazine 1.6000 Liquid Imported /Indigenous Tank Phosphorus oxychloride (POCl3) 3.5103 Liquid Imported /Indigenous Barrels Potassium fluoride 0.7163 Solid Indigenous Barrels Sodium bicarbonate (NaHCO3) 2.9000 Crystalline Indigenous Barrels Tetrabutyl ammonium 0.1015 Crystalline Indigenous Barrels hydrogensulphate Dimethylformamide 0.9182 Liquid Indigenous Tank Isopropyl alcohol 0.2870 Liquid Indigenous Tank Toluene 3.8230 Liquid Indigenous Tank Process Water 34.1851 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank 2,5-Dichloro-4-(1,1,2,3,3,3- hexafluoropropoxy)benzenamine Dichlorophenol 0.5997 Crystalline Indigenous Barrels Acetonitrile 0.1403 Liquid Indigenous Barrels Caustic Lye 0.0390 Liquid Indigenous Tank Acetone 0.0079 Liquid Indigenous Tank Hexafluoropropylene 0.5518 Gas Indigenous Cylinder Hydrochloric acid (15-33%) 0.0610 Liquid Indigenous Tank 34

Sr. No. 40 41 42 Quantity Physical form Source Mode of Storage Nitric Acid 0.0800 Liquid Indigenous Barrels Potassium hydroxide 0.0878 Flakes Indigenous Barrels Silicate (Ca2SiO4) 0.0036 Crystal Indigenous Barrels Sodium chloride 0.0231 Solid Indigenous Barrels Sulphuric acid (98%) 0.7160 Liquid Indigenous Tank Methanol 0.3341 Liquid Indigenous Tank Toluene 0.0732 Liquid Indigenous Tank Hyflow (Filter aid) 0.0077 Solid Imported /Indigenous Barrels Palladium on carbon 0.2054 Powder Indigenous Barrels Process Water 5.1759 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank Hydrogen 0.0204 colorless gas Indigenous Cylinder 2,4,5-Trifluorophenyl acetic acid Dichloroacetophenone 2.6130 Needles Indigenous Barrels Caustic Lye (48%) 0.8400 Liquid Indigenous Tank Chlorosulfuric acid 6.4400 Liquid Indigenous Barrels Acetonitrile 0.8000 Liquid Indigenous Barrels Hydrochloric acid (15-33%) 2.3000 Liquid Indigenous Tank Morpholine 1.8300 Liquid Imported /Indigenous Barrels Potassium fluoride 3.6140 Solid Indigenous Barrels p-toluenesulfonic acid 0.0400 Liquid Imported /Indigenous Barrels Sulfolane 0.7500 Crystalline Indigenous Barrels Sulfur 0.4500 Solid Indigenous Barrels Process Water 1.0000 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank 3-Aminobenzotrifluoride Benzotrichloride 1.3300 Liquid Indigenous Barrels Hydrofluoric acid Anhydride 0.8000 Gas Indigenous Tank Hydrogen 0.1300 colorless gas Indigenous Cylinder Methanol 0.1300 Liquid Indigenous Tank Nitric acid 0.5600 Liquid Indigenous Barrels Raney nickel 0.0200 Slurry Imported /Indigenous Barrels Sulphuric acid (98%) 1.9600 Liquid Indigenous Tank Process Water 3.3300 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank 2,4-Dichloro-3,5-dinitrobenzotrifluoride Dichlorobenzotrichloride 1.2200 Liquid Imported /Indigenous Barrels Dichlorobenzotrifluoride 0.7700 Liquid Imported /Indigenous Barrels Hydrofluoric acid Anhydride 1.3900 Gas Indigenous Tank Isopropyl alcohol 0.3400 Liquid Indigenous Tank Nitric acid 1.9000 Liquid Indigenous Barrels 35

Sr. No. 43 44 45 Quantity Physical form Source Mode of Storage Oleum 3.5160 Liquid Indigenous Tank Sodium bicarbonate 0.3900 Crystalline Indigenous Barrels Process Water 3.5300 Liquid GIDC Tank Nitrogen 0.3000 Gas Self-Generation Tank 3-phenoxy benzaldehyde Benzaldehyde 0.6613 Liquid Indigenous Barrels Bromine 0.2206 Liquid Indigenous Tank Ammonia solution (25%) 0.0100 Liquid Indigenous Tank Aluminium chloride 1.1458 Powder Indigenous Barrels Caustic Lye (48%) 0.4700 Liquid Indigenous Tank Chlorine 0.2242 Liquid/gas Indigenous Cylinder Copper chloride 0.0120 Powder Indigenous Barrels Formic acid 0.1000 Liquid Indigenous Barrels Hydrochloric acid (15-33%) 1.4700 Liquid Indigenous Tank Hyflow (Filter aid) 0.0009 Solid Imported /Indigenous Barrels Monoethylene glycol 0.0608 Liquid Imported /Indigenous Barrels Phenol 0.5831 Liquid Indigenous Barrels Potassium hydroxide (KOH Solution) 1.3000 Flakes Indigenous Barrels p-toluenesulfonic acid 0.0030 Liquid Imported /Indigenous Barrels Soda ash 0.0500 Granule Indigenous Barrels Sodium chloride 0.0100 Solid Indigenous Barrels Sodium thio sulphate 0.0600 Liquid Indigenous Barrels Sulphuric acid (98%) 0.0300 Liquid Indigenous Tank Toluene 0.0264 Liquid Indigenous Tank Ethyldichloride 0.0968 Liquid Indigenous Tank Process Water 1.0930 Liquid GIDC Tank Nitrogen 0.5000 Gas Self-Generation Tank 3-phenoxy toluene Bromobenzene 1.8050 Liquid Indigenous Barrels m-cresol 0.6208 Liquid Imported /Indigenous Barrels Caustic Lye (48%) 0.1380 Liquid Indigenous Tank Copper Chloride 0.0039 Powder Indigenous Barrels Hydrochloric acid (15-33%) 0.4196 Liquid Indigenous Tank Potassium hydroxide (KOH Solution) 0.1610 Flakes Indigenous Barrels Process Water 0.7796 Liquid GIDC Tank Nitrogen 0.1999 Gas Self-Generation Tank Methyl-2- Fluoroacrylate Hydrofluoric acid 1.2870 Gas Indigenous Tank Tetrafluoroethylene 1.4720 Gas Imported /Indigenous Cylinder Dimethylformamide 2.5096 Liquid Indigenous Tank Caustic Lye (48%) 0.7396 Liquid Indigenous Tank 36

Sr. No. 46 47 48 49 Quantity Physical form Source Mode of Storage Hydroquinone 0.0132 Crystalline Imported /Indigenous Barrels Methanol 0.7308 Liquid Indigenous Tank Paraformaldehyde 0.9246 Crystalline Imported /Indigenous Barrels Sodium iodide 1.1500 Crystalline Indigenous Barrels Trifluoroacetic acid 1.3500 Liquid Indigenous Tank Zinc 0.9810 Solid Indigenous Barrels Process Water 9.5000 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Lithium tetrakis (pentafluorophenyl) borate Pentafluorobenzene 0.3610 Liquid Indigenous Barrels Tert-Butyllithium in pentane solution 0.5700 Liquid Imported /Indigenous Barrels (24%) BF3.etherate solution (50%) 0.0690 Liquid Imported /Indigenous Barrels Diethyl ether 0.4340 Liquid Indigenous Barrels Toluene 0.4230 Liquid Indigenous Tank Process Water 0.0000 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank 2-fluoro-5-bromobenzonitrile Chlorobenzonitrile 1.1313 Crystalline Imported /Indigenous Barrels KF 1.4309 Solid Indigenous Barrels 1,3-Dimethyl-2-imidazolidinone 0.8438 Liquid Imported /Indigenous Barrels Methylene chloride 0.6990 Liquid Indigenous Tank 2-Fluorobenzonitrile 0.7562 Liquid Imported /Indigenous Barrels H2SO4 (98%) 4.5440 Liquid Indigenous Tank N-Bromosuccinimide (C4H4BrNO2) 1.1014 Solid Imported /Indigenous Barrels Ethanol 0.2900 Liquid Indigenous Tank O Toludiene 0.0500 Liquid Indigenous Barrels Process Water 4.8591 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Ethyl-Trifluoropyruvate Hexafluoroacetone 1.7700 Compressed gas Imported /Indigenous Cylinder Ethanol 2.4500 Liquid Indigenous Tank Calcium Hydroxide 0.7900 Solid Indigenous Barrels Silica 0.1600 Crystal Indigenous Barrels Sulphuric acid (98%) 0.9000 Liquid Indigenous Tank Process Water 7.0900 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Isoflurane Trifluoroethanol 0.9000 Liquid Indigenous Barrels 37

Sr. No. 50 51 52 Quantity Physical form Source Mode of Storage KOH (48%) 1.2600 Flakes Indigenous Barrels NaOH (20%) 0.6500 Liquid Indigenous Tank Acetone 0.0500 Liquid Indigenous Tank Process Water 0.5800 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank R-22 0.6700 Liquefied Gas Indigenous Tank Chlorine Gas 0.5800 Liquid/gas Indigenous Cylinder Desflurane Isoflurane 1.5700 Liquid Imported /Indigenous Barrels Flourinating catalyst 0.1000 Solid Imported /Indigenous Barrels Anhydrous Hydrogen fluoride 0.3400 Gas Indigenous Tank Dil HCL (30%) 0.8600 Liquid Indigenous Tank Process Water 0.7200 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Sevoflurane Hexafluoroisopropanol 1.6700 Liquid Imported /Indigenous Barrels Trioxane 0.3600 Crystalline Imported /Indigenous Barrels Anhydrous Hydrogen Fluoride 0.7900 Gas Indigenous Tank Conc. H2SO4 (98%) 2.0000 Liquid Indigenous Tank Aqueous KOH (48%) 3.1300 Flakes Indigenous Barrels Process Water 3.0000 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank Trichloroacetyl chloride Acetic Acid 0.3700 Liquid Indigenous Tank Chlorine 2.6000 Liquid/gas Indigenous Cylinder Charcoal 0.1500 Solid Indigenous Barrels 48% NaOH Solution 4.4000 Liquid Indigenous Tank Process Water 3.2590 Liquid GIDC Tank Nitrogen 0.2000 Gas Self-Generation Tank 53 Chlorinated Compound i Trichloroethylene Ethylene dichloride 0.7540 Liquid Indigenous Tank Chlorine 1.6170 Liquid/gas Indigenous Cylinder Barium Hydroxide/ Sodium Hydroxide 0.0100 Powder Indigenous Barrels Stabilizer (Thymol) 0.0040 Solid Imported /Indigenous Barrels Caustic Lye 48% 0.1028 Crystalline Imported /Indigenous Barrels Alumina Balls 0.0010 Liquid Indigenous Tank Molecular Sieve 0.0010 Solid Imported /Indigenous Barrels Anhydrous Calcium Chloride 0.0010 Solid Imported /Indigenous Barrels Therminol-55 0.0010 Crystalline Indigenous Barrels Charcoal 0.0010 Liquid Imported /Indigenous Barrels 38

Sr. No. ii iii 54 55 Quantity Physical form Source Mode of Storage Catalyst - Nitrile based 0.0002 Solid Indigenous Barrels Process Water 2.8157 Liquid GIDC Tank Nitrogen 0.0050 Gas Self-Generation Tank Perchloroethylene Ethylene dichloride 0.7540 Liquid Indigenous Tank Chlorine 1.6170 Liquid/gas Indigenous Cylinder Barium Hydroxide/ Sodium Hydroxide 0.0098 Powder Indigenous Barrels Catalyst - Nitrile based 0.0002 Solid Imported /Indigenous Barrels Stabilizer (Thymol) 0.0040 Crystalline Imported /Indigenous Barrels Caustic Lye 48% 0.1243 Liquid Indigenous Tank Alumina Balls 0.0010 Solid Imported /Indigenous Barrels Molecular Sieve 0.0010 Solid Imported /Indigenous Barrels Anhydrous Calcium Chloride 0.0010 Crystalline Indigenous Barrels Therminol-55 0.0005 Liquid Imported /Indigenous Barrels R-22 0.0001 Liquefied Gas Imported /Indigenous Tank Charcoal 0.0010 Solid Indigenous Barrels Process Water 2.8157 Liquid GIDC Tank Nitrogen 0.0051 Gas Self-Generation Tank Chloromethanes Methanol 0.3650 Liquid Indigenous Tank Chlorine 1.2200 Liquid/gas Indigenous Cylinder Aluminium Oxide 0.0005 Powder Indigenous Barrels 48% Caustic Solution 0.0900 Liquid Indigenous Tank 98% Sulfuric Acid 0.5000 Liquid Indigenous Tank Amylene 0.0010 Liquid Indigenous Tank Desiccant (Silica Gel & Calcium Chloride) 0.0005 Solid Imported /Indigenous Barrels Process Water 1.5320 Liquid GIDC Tank Nitrogen 0.0014 Gas Self-Generation Tank Caustic & Chlorine Plant Sodium Chloride 1.7200 Solid Indigenous Covered Shed Sulfuric Acid 0.0360 Liquid Indigenous Tank Process Water 3.9240 Liquid GIDC Tank Nitrogen 0.0100 Gas Self-Generation Tank Anhydrous Hydrofluoric acid Fluorspar 2.6000 Solid Imported /Indigenous Covered Shed Aluminium 0.0080 Solid Indigenous Barrels Calcium Chloride 0.0002 Solid Indigenous Covered Shed Calcium oxide 0.0350 Solid Indigenous Covered 39

Sr. No. 56 Quantity Physical form Source Mode of Storage Shed Oleum 1.0720 Liquid Indigenous Tank Sulphuric Acid 98% 1.4550 Liquid Indigenous Tank Sodium Hydroxide (30%) 0.2800 Liquid Indigenous Barrels R22 Refrigerant 0.0001 Liquefied Gas Imported /Indigenous Tank Process Water 2.6200 Liquid GIDC Tank Nitrogen 0.0100 Gas Self-Generation Tank Chlorotrifluoroethane (HCFC 133a) Trichloroethylene 1.2160 Liquid Indigenous Tank Hydrofluoric Acid (HF) 0.8800 Gas Indigenous Tank Caustic Lye 48% 0.0070 Liquid Indigenous Tank Crome- Alumina 0.0050 Granules Imported /Indigenous Barrels Activated carbon 0.0050 Solid Indigenous Barrels Molecular sieve 0.0050 Solid Imported /Indigenous Barrels Sulphuric Acid 98% 0.2410 Liquid Indigenous Tank Process Water 1.5000 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank 57 HFC Refrigerant i 1,1,1,2 Tetrafluroethane (HFC 134a) Trichloroethylene 1.4000 Liquid Indigenous Tank Hydrofluoric Acid (HF) 0.9600 Gas Indigenous Tank Caustic Lye 48% 0.0070 Liquid Indigenous Tank Crome- Alumina 0.0020 Granules Imported /Indigenous Barrels Activated carbon 0.0200 Solid Indigenous Barrels Molecular sieve 0.0200 Solid Imported /Indigenous Barrels Sulphuric Acid 98% 0.2310 Liquid Indigenous Tank Ferric Chloride 0.0100 Solid Indigenous Barrels Process Water 2.6900 Liquid GIDC Tank ii iii Nitrogen 0.0130 Gas Self-Generation Tank Pentafluoroethane (HFC 125) Perchloroethylene 1.4680 Liquid Imported /Indigenous Tank Hydrofluoric Acid (HF) 1.0150 Gas Indigenous Tank Caustic Lye 48% 0.0070 Liquid Indigenous Tank Crome - Alumina 0.0050 Solid Imported /Indigenous Barrels Activated carbon 0.0050 Solid Indigenous Barrels Molecular sieve 0.0050 Solid Imported /Indigenous Barrels Sulphuric Acid 98% 0.2120 Liquid Indigenous Tank Process Water 2.9480 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank Difluoromethane (HFC- 32 ) Methylene chloride 1.6610 Liquid Indigenous Tank 40

Sr. No. iv v vi vii viii 58 59 60 Quantity Physical form Source Mode of Storage Hydrofluoric Acid (HF) 0.9930 Gas Indigenous Tank Caustic Lye 48% 0.2100 Liquid Indigenous Tank Crome- Alumina 0.0050 Granules Imported /Indigenous Barrels Activated carbon 0.0050 Solid Indigenous Barrels Molecular sieve 0.0050 Solid Imported /Indigenous Barrels Sulphuric Acid 98% 0.2441 Liquid Indigenous Tank Process Water 3.3750 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Cylinder 1,1 difluoroethane (HFC- 152a) 1,1 difluoroethane (HFC- 152a) 1.0000 Liquid Indigenous Tank Refrigerant blend of Difluoromethane (HFC-32) + Pentafluoroethane (HFC-125)(R410a) R-32 0.5000 Liquefied Gas Imported /Indigenous Tank R-125 0.5000 Liquefied Gas Imported /Indigenous Tank Refrigerant blend of Pentafluoroethane (HFC-125) + 1,1,1-Trifluoroethane (R143a) + 1,1,1,2 Tetrafluroethane (HFC 134a) (R404a) R-125 0.4400 Liquefied Gas Imported /Indigenous Tank R-143a 0.5200 Liquefied Gas Imported /Indigenous Tank R-134a 0.0400 Liquefied Gas Imported /Indigenous Tank Refrigerant blend of Difluoromethane (HFC-32) + Pentafluoroethane (HFC-125) + 1,1,1,2 Tetrafluroethane (HFC 134a) (R407c) R-32 0.2300 Liquefied Gas Imported /Indigenous Tank R-125 0.2500 Liquefied Gas Imported /Indigenous Tank R-134a 0.5200 Liquefied Gas Imported /Indigenous Tank Blend of 1,1-Difluoroethane (R152a) + 1,1,1,2 Tetrafluroethane (R134a) R 134a (1112- Tetrafluoroethane) 0.5000 Liquefied Gas Indigenous Tank R 152 a (Difluoroethane) 0.5000 Liquefied Gas Imported /Indigenous Tank Activated carbon 0.0010 Solid Indigenous Barrels Nitrogen 0.0010 Gas Self-Generation Tank Butane (R600a) Liquefied Petroleum Gas 3.8023 Liquefied Gas Indigenous Tank Activated carbon 0.0050 Solid Indigenous Barrels Process Water 2.0000 Liquid GIDC Tank Nitrogen 0.1000 Gas Self-Generation Tank Propane (R290) Liquefied Petroleum Gas 5.5249 Liquefied Gas Indigenous Tank Activated carbon 0.0050 Solid Indigenous Barrels Process Water 2.0000 Liquid GIDC Tank Nitrogen 0.1000 Gas Indigenous Tank Blend of 1-Chloro-1,1-difluoroethane (R142b) + Chlorodifluoromethane (R22) R 142 b (Chlorodifluoroethane) 0.5000 Liquefied Gas Imported /Indigenous Tank R 22 (Chlorodifluoromethane) 0.5000 Liquefied Gas Indigenous Tank 41

Sr. No. 61 Quantity Physical form Source Mode of Storage Activated carbon 0.0010 Solid Indigenous Barrels Nitrogen 0.0010 Gas Self-Generation Tank Blend of 1,1,1,2 Tetrafluroethane (R134a) + Di Methyl Ether (DME) Dimethylether 0.5000 Liquid Indigenous Barrels R 134a (1112- Tetrafluoroethane) 0.5000 Liquefied Gas Indigenous Tank Activated carbon 0.0010 Solid Indigenous Barrels Nitrogen 0.0010 Gas Self-Generation Tank 62 R&D Products Organo Heterocyclic Compounds Pyridines - Liquid Imported /Indigenous Tank Picolines - Liquid Imported /Indigenous Tank i Unsaturated Ketones - Liquid Imported /Indigenous Tank Carbohydrates - Liquid / Solid Imported /Indigenous Tank / Bags Ethers - Liquid Indigenous Tank Aryl/Alkyl/Alicyclic Compounds Acid Chlorides - Liquid Imported /Indigenous Tank Benzonitriles - Liquid Imported /Indigenous Tank Alkens - Gas/Liquid/So lid Imported /Indigenous Tank / Barrels Alkanes - Gas/Liquid/So lid Imported /Indigenous Tank / Barrels Amines - Liquid Imported /Indigenous Tank Benzoic Acid - Colourless Indigenous Barrels ii crystalline solid Phenols - Liquid Imported /Indigenous Tank Anilines - Colourless to Imported /Indigenous Tank yellow liquid Pt/Pd/Ru/Rh based catalyst - Liquid/Solid Imported /Indigenous Tank / Barrels Dimethylformamide (DMF) - Colourless Indigenous Tank liquid Alcohols - Liquid Indigenous Tank Toluene - Liquid Indigenous Tank iii Elemental Fluorine/Bromine/Iodine and their Products/Derivatives Anhydrous Hydrofluoric acid (AHF) - Liquid Indigenous Tank Potassium Fluoride (KF) - Powder Indigenous Barrels Iodine (I2) - Solid Indigenous Barrels Bromine - Liquid Indigenous Tank Hydrogen Bromide - Liquid Indigenous Tank 42

Sr. No. iv 63 Quantity Physical form Source Mode of Storage Potassium Iodide - Solid Indigenous Barrels Sulfonic Acids - Crystalline solids Imported /Indigenous Barrels Alkali Metal/Boron/Phosphorous/Sulphur based Product/ Derivatives Boron trifluoride (BF3) - Colorless gas / Imported /Indigenous Tank / Colorless liquid Cylinder Phosphorus Trichloride (POCl3) - Liquid Indigenous Tank Phosphorus pentachloride (PCl5) - Powder Indigenous Barrels Boric Acid - Powder Indigenous Barrels Thionyl Chloride - Liquid Indigenous Tank Thilols - Liquid Imported /Indigenous Tank Hydrofluoric Acid (20 to 70%) Hydrogen Fluoride 0.3000 Gas Indigenous Tank Process Water 0.7000 Liquid GIDC Tank 43

ANNEXURE: 2A BRIEF MANUFACTRING PROCESS, CHEMICAL REACTION AND MASS BALANCE WITH FLOW DIAGRAM 1. Trifluoro Acetic Acid (TFA) Process Description: Trichloroacetyle chloride will react with Anhydrous Hydrofluoric acid in presence of catalyst and form Trifluoro acetyl fluoride, Chlorodifluoro acetyl fluoride and hydrochloric acid, Chlorodifluoro acetyl fluoride again recycled from crude distillation section to 2nd reactor (CDFAF) and converted in TFAF.TFAF from TFAF tower going to derivative stream and remain go for hydrolysis,30 % HCl produced from HCl scrubbing section. After hydrolysis this material goes to sulfuric acid addition section and final distillation section for final. 30 % HCl stream from hydrolysis section and 75 % Sulfuric acid from final distillation section for sale as a Product. Chemical Reaction: CCl3COCl + 4AHF CF3COOH + 4HCl 182 80 114 146 Material Balance: Input Output Key RM Product Trichloroacetyl chloride MT 1.886 Trifluoro acetic acid MT 1.000 Hydrofluoric acid (20-70%) MT 0.220 Reagent Hydrofluoric acid Anhydride MT 0.732 Inorganic Acid Sulphuric acid (98%) MT 1.620 Sulphuric acid (75%) MT 2.790 Hydrochloric acid (30%) MT 4.555 Water Process Water MT 12.500 Wastewater Effluent MT 8.173 Gas Nitrogen MT 0.150 Process Gaseous Emission Nitrogen, HCl and HF Stack Emission MT 0.150 Total Input MT 16.888 Total Output MT 16.888 44

2. Parabromofluorobenzene Process Description: Fluoro benzene will brominate in the Glass Reactor to form crude PBFB, It will be distillate to produce pure PBFB (Parabromofluorobenzene). Chemical Reaction: C6H5F + Br2 C6H4BrF + HBr Fluoro benzene Bromine Para bromo fluoro benzene Hydrogen Bromide 96.0 160.0 175.0 81.0 Material Balance: Input Output Key RM Product Fluorobenzene MT 0.605 Parabromofluorobenzene MT 1.000 Reagent Inorganic Acid Bromine MT 1.050 Hydrogen Bromide (48-50%) MT 1.080 Ferric Chloride MT 0.012 Sodium Salt Water Sodium sulphate MT 0.030 Process Water MT 1.000 Wastewater Gas Effluent MT 0.496 Nitrogen MT 1.000 Process Residue and Waste Heavies MT 0.061 Process Gaseous Emission Nitrogen & Bromine Stack Emission MT 1.000 Total Input MT 3.667 Total Output MT 3.667 45

3. Specialty Product i. Tetrafluorobenzyl Alcohol (TFBAlc) Process Description: Pentafluorobenzonitrile (PFBN) in aqueous phase in presence of catalyst will reacted. The Reaction Mass will filter and taken for distillation. The intermediate (IP 1) after purification taken for hydrolysis in presence of sulfuric acid catalyst. The Reaction Mass will be filtered and wet cake will take for esterification. Esterification reaction carried out in Alcohol solvent in presence of Sulfuric acid. RM is extracted and boils off to get pure Intermediate (IP 3). In Step IV, reaction will carried out in presence of Catalyst and solvent. After reaction, RM will acidify and organic layer will extract from Aqueous Layer. Organic layer will boil off and taken for fine distillation. Chemical Reaction: 2 C6F5CN + 2 Zn + H2SO4 + NaBH4 + 7 H2O 2 C6F4HCH2OH + ZnF2 + Zn(OH)2 + (NH4)2 SO4 + H3BO3 386.13 130.82 98.02 37.84 126.11 360.2 103.41 99.42 132.06 61.83 46

Material Balance: Input Output Key RM Product Penta fluoro Benzonitrile MT 1.810 Tetrafluorobenzyl Alcohol (TFBAlc) MT 1.000 Reagent Inorganic Acid Potassium Phosphate MT 0.130 Sulphuric acid (70%- 95%) MT 7.700 Potassium Hydroxide MT 0.002 Sodium Bi sulphite MT 0.012 Zinc Salt Sodium Borohydride MT 0.265 Zinc Fluoride & Zinc Oxide Cake MT 1.750 Sodium Carbonate MT 0.045 Sulphuric Acid 98% MT 5.400 Spent Catalyst Zinc MT 0.820 Alumina Balls MT 0.004 Acetic Acid MT 0.010 Molecular Sieve MT 0.002 Monoglyme MT 0.380 Spent Carbon Solid RM Activated Carbon MT 0.002 Activated Carbon MT 0.002 Alumina Balls MT 0.004 Spent Organic Solvent Molecular Sieve MT 0.002 Organic containing halogenated Solvents MT 1.374 Solvent Wastewater Methanol MT 1.500 Effluent MT 17.500 Methylene Chloride MT 1.450 Process Gaseous Emission Water Nitrogen Emission MT 1.400 Process Water MT 17.500 Gas Nitrogen MT 1.400 Total Input MT 30.732 Total Output MT 30.732 47

ii. Ethyldifluoroacetate (EDFA) Process Description: TFEMe is received with Ethanol present into it. It will water washed to remove water & then dried to remove Moisture. Dry TFEMe is pyrolyzed in presence of Iron based Catalyst to produce Acetyl fluoride. The vent of the reactor, containing Acetyl fluoride, will take to the esterification section, where the vent gas reacts with ethanol to form crude EDFA. Crude EDFA will distill to produce pure EDFA. HF will send to HF Scrubber to produce HF (approx.40 %). Catalyst activation will done use of HCl gas. Excess HCl will go to HCl scrubber. Water & Methanol mixture will either distilled for Methanol recovery or it will be go to Organic stripper, before sending it to ETP. Chemical Reaction: CHF2CF2OCH3 CHF2COF + CH3F 132.06 98.02 34.03 TFEMe Acetylfluoride CHF2COF + C2H5OH CHF2COOC2H5 + HF 98 46.07 124.08 20.01 Acetylfluoride Ethanol EDFA 48

Material Balance: Input Output Key RM Product 1,1,2,2-Tetrafluoroethyl MT 1.273 Ethyldifluoroacetate (EDFA) MT 1.000 Methyl Ether Ethanol MT 0.430 Hydrofluoric acid (40%) MT 1.270 Reagent Inorganic Acid Hydrochloric acid MT 0.055 Hydrochloric acid (10-30%) MT 0.183 Anhydride Therminol 55 MT 0.0002 Spent Catalyst Solid RM Cromia MT 0.002 Cromia MT 0.002 Molecular Sieve MT 0.002 Ferric Chloride MT 0.005 Ferric Chloride MT 0.005 Activated Carbon MT 0.002 Molecular Sieve MT 0.002 Spent Carbon Ceramic Balls MT 0.000 Spent Carbon MT 0.002 Water Spent Organic Solvent Process Water MT 1.028 Methyldifluoroacetate & MT 0.005 Propyldifluoroacetate Methanol MT 0.064 Gas Ethyldifluoroacetate & MT 0.001 Polyldifluoroacetate Nitrogen MT 1.000 Wastewater Effluent MT 0.263 Process Gaseous Emission Nitrogen, HCl & HF Stack Emission MT 1.000 Total Input MT 3.797 Total Output MT 3.797 49

iii. Ethyltrifluoroacetate Process Description: Reaction of Trifluoroacetyl fluoride (TFAF) with Ethanol to form Ethyl Trifluoro acetate (ETFA) and Hydrogen fluoride. HF is separated from distillation and pure ETFA is recovered. Chemical Reaction: CF3COF + C2H5OH CF3COOC2H5 + HF 116.015 46.069 142.078 20.006 TFAF ETFA Material Balance: Input Output Key RM Product Trifluoro acetal fluoride MT 0.870 Ethyltrifluoroacetate MT 1.000 (TFAF) (P7/ETFA) Hydrofluoric Acid 30-40 % MT 0.510 Reagent Ethanol MT 0.340 Wastewater Effluent MT 0.010 Solid RM Molecular sieve MT 0.007 Spent Catalyst Spent molecular sieve MT 0.007 Water Process Water MT 0.310 Process Gaseous Emission Nitrogen & HF stack emission Gas Nitrogen MT 0.350 MT 0.350 Total Input MT 1.877 Total Output MT 1.877 50

iv. Ethyltrifluoroacetoacetate Process Description: ETFA (Ethyltrifluroacetate) is reacted with catalyst in presence of excess Ethyl Acetate to form ETFAA. The catalyst is neutralized with HCl and the NaCl formed is filtered out. ETFAA is recovered by distillation. Chemical Reaction: CH3COOC2H5 + NaOC2H5 + CF3COOC2H5 CF3COCH2COOC2 + C2H5OH + NaOC2H5 H5 88.11 68.06 142.08 184.11 46.07 68.06 Ethyl Acetate Sodium Ethoxide ETFA ETFAA Ethanol Sodium Ethoxide NaOC2H5 + HCl NaCl + C2H5OH 68.06 36.46 58.45 46.07 Sodium Ethoxide Hydrochloric Acid Sodium Chloride Ethanol 51

Material Balance: Input Output Key RM Product Ethyl tri fluoro acetate MT 0.910 Ethyltrifluoroacetoacetate MT 1.000 Reagent Inorganic Acid Ethyl acetate MT 0.432 Hydrochloric acid (5% to 10%) MT 0.030 Hydrochloric acid MT 0.270 Sodium Ethoxide MT 0.480 Wastewater Tri ethyl amine MT 0.001 Effluent MT 2.226 Solid RM Spent Organic Solvent Molecular sieve MT 0.007 Ethanol MT 0.450 Hyflow MT 0.002 Organic containing Chlorinated MT 0.120 Solvents/ Fluorinated compounds Water Spent Catalyst Process Water MT 2.141 Spent molecular sieve MT 0.008 Gas Sodium Salt Nitrogen MT 0.500 Sodium chloride salt MT 0.410 Process Gaseous Emission Nitrogen and HCl stack emission MT 0.500 Total Input MT 4.744 Total Output MT 4.744 52

v. Amino Crotonate Process Description: In the process of TFAA, trifluoroacetic acid reacts with Oleum and from trifluoroacetic anhydride. Reaction times maintain will 04 hrs. Distillation done after four hours and final collect in vessel and Sulfuric acid recycle in P-2 plant for reprocessing. Chemical Reaction: TFA + SO3 TFASO3H 114 80 194 Trifluoro acetic ac Oleum TFASO3H + TFA TFAA + H2SO4 194 114 210 98 Trifluoro acetic acid Trifluoroacetic anhydride Sulphuric Acid Material Balance: Input Output Key RM Product Ethyltrifluoroacetoacetate MT 1.330 Amino crotonate MT 1.000 Reagent Process Residue and Waste Ammonia (NH3) MT 0.260 Residue (Heavies) MT 0.230 Cyclohexane MT 0.160 Heavies produced after evaporation of P9 aqueous MT 0.020 Water Wastewater Process Water MT 1.000 Effluent MT 1.300 Gas Process Gaseous Emission Nitrogen MT 1.000 Nitrogen MT 1.000 Plant stack containing NH3 & water traces MT 0.200 Total Input MT 3.750 Total Output MT 3.750 53

vi. Trifluoroacetic Anhydride (TFAA) Process Description: In the process of TFAA, trifluoroacetic acid reacts with Oleum and from trifluoroacetic anhydride. Reaction times maintain will 04 hrs. Distillation done after four hours and final collect in vessel and Sulfuric acid recycle in P-2 plant for reprocessing. Chemical Reaction: TFA + SO3 TFASO3H 114 80 194 Trifluoro acetic ac Oleum TFASO3H + TFA TFAA + H2SO4 194 114 210 98 Trifluoro acetic acid Trifluoroacetic anhydride Sulphuric Acid Material Balance: Input Output Key RM Product Trifluoro acetic acid MT 1.130 Trifluoroacetic anhydride MT 1.000 Reagent Inorganic Acid Oleum MT 2.500 Sulphuric Acid MT 2.630 Water Wastewater Process Water MT 1.000 Effluent MT 1.000 Gas Process Gaseous Emission Nitrogen MT 0.100 Nitrogen Stack Emission MT 0.100 Total Input MT 4.730 Total Output MT 4.730 54

vii. Pentafluorobenzoic Acid (PFBA) Process Description: Benzonitrile (BN) will chlorinate in the Reactor. Chlorinated BN then fluorinated to form Fluorinated BN, PFBN (Pentafluorobenzonitrile). It will be hydrolysed by using Sulphuric Acid & H2O to produce PFBA. Chemical Reaction: C6H5CN + 5 Cl2 C6Cl5CN + 5 HCl 103.11 354.53 275.34 182.3 Benzonitrile Chlorine Chlorinated BN Hydrochloric acid C6Cl5CN + 5 KF C6F5CN + 5 KCl 275.34 290.48 193.07 372.75 Chlorinated BN Potassium Potassium PFBN Fluoride Chloride 2C6F5CN + 4 H2O + H2SO4 2C6F5COOH + (NH4)2SO4 386.13 72.06 98.01 424.15 132.06 Sulphuric Ammonium PFBN Water PFBA Acid Sulphate 55

Material Balance: Input Output Key RM Product Benzonitrile MT 0.820 Pentafluorobenzoic Acid (PFBA) MT 1.000 Reagent Inorganic Acid Caustic lye 48% MT 1.750 Sulphuric acid (70%- 95%) MT 3.100 Chlorine MT 2.860 Hydrochloric acid (15-33%) MT 3.380 Ferric Chloride based MT 0.020 Sodium Hypo chlorite MT 6.000 (Catalyst) Molecular Sieve MT 0.002 Activated Carbon MT 0.015 Wastewater Potassium Fluoride MT 1.980 Effluent MT 0.278 Potassium Hydroxide MT 0.005 Sulphuric Acid 98% MT 2.500 Spent Catalyst Molecular Sieve MT 0.002 Solvent Methanol MT 0.120 Process Gaseous Emission Toluene MT 0.450 Nitrogen, HCl and Cl2 Stack Emission MT 2.050 Water Spent Organic Solvent Process Water MT 5.846 Organic By- Product containing Chlorinated Solvents/ Fluorinated compounds MT 0.060 Gas Potassium Salt Nitrogen MT 2.050 KF & KCl Mix cake MT 2.549 Total Input MT 18.418 Total Output MT 18.418 56

viii. Pyrazole Acid Process Description: EDFA is reacted in presence of Sodium Ethoxide catalyst to form salt of EDFAA in presence of Ethyl acetate Salt is acidified with Dry HCL to form EDFAA and Sodium Salt at RT. It is taken to filtration to remove sodium chloride salts EDFAA with solvents then taken to distillation column to recover EDFAA crude EDFAA is reacted in presence of Acetic Anhydride with Orthoformate to give Enolether. The Enolether from step -2 is reacted with MMH in presence of Xylene to form Pyrazole ester & ethanol. Pyrazole ester on reacting with caustic lye to form Pyrazole sodium & on further acidification with HCL to form Pyrazole acid salt. Pyrazole acid salt will be filtered & dried to get dry Pyrazole acid. Chemical Reaction: Step 1 Claisen Condensation Protonation CH3COOC2H5 + NaOC2H5 + CHF2COOC2H = CF2COCH + 2 88.106 68.061 124.087 188.117 92.138 Ethyl Acetate Sodium EDFA EDFAA-Na Ethanol CF2COCH2COOC2H5Na + HCl = CHF2COC + NaCl 188.117 36.461 166.125 58.453 EDFAA-Na EDFAA Step 2 Enolether Formation Parallel Reaction CHF2COCH2COOC2H5 + HC(OC2H5)3 = CF2C2OO + 2 166.125 148.202 222.188 92.138 EDFAA Triethyl Enolether 2 C2H5OH + 2 (CH3CO)2 O = 2 + 2 92.138 204.181 120.106 176.213 Ethanol Acetic Acetic Ethyl Step 3 Pyrazole Ester Formation CF2C2OOCH2COO(C2H5)2 + CH3(NH)NH2 = CF2COOC + C2H5OH + H20 222.188 46.058 204.162 46.069 18 Enolether MMH Pyrazole Ethanol - Pyrazole Sodium Formation CF2COOCHC(C2H5)CHCH + NaOH = CF2COOC + C2H5OH 204.162 40.008 198.101 46.069 Pyrazole Ester Carboxyla Ethanol Pyrazole acid formation CF2COOCHCCHCH3N2Na + HCL = CF2COO(C + NaCl 198.101 36.50 176.109 58.453 Carboxylate Pyrazole 57

Material Balance: Option: 1 Input Output Key RM Product Ethyldifluoroacetate MT 1.319 Pyrazole Acid MT 1.000 Reagent Ammonium Salt Acetic Anhydride MT 1.800 Ammonium chloride cake MT 0.110 Anhydrous Ammonia MT 0.062 Anhydrous HCl MT 0.465 Spent Organic Solvent Cautic lye (48%) MT 1.941 Mix Xylene, MT 3.260 Triethylorthoformate, Ethyl acetate & Acetic anhydride HCl 30% MT 1.529 Ethyl Acetate & Ethanol MT 1.185 MMH (35%) MT 1.022 Sodium Ethoxide MT 0.740 Sodium Salt Sodium Fluoride MT 0.013 Sodium Fluoride MT 0.013 Trimethylorthoformate MT 1.200 NaCl Cake MT 0.305 Potassium Carbonate MT 0.115 Spent Catalyst Solid RM Hyflow MT 0.027 Hyflow MT 0.027 Molecular Sieve MT 0.002 Molecular Sieve MT 0.002 Precipitated Silica MT 0.022 Process Residue and Waste Organic Residue MT 0.226 Solvent Mix Xylene MT 0.120 Wastewater Ethyl Acetate MT 1.177 Effluent MT 20.236 Water Process Gaseous Emission Process Water MT 14.810 Nitrogen MT 1.100 Gas Nitrogen MT 1.100 Total Input MT 27.464 Total Output MT 27.464 58

Option: 2 Input Output Key RM Product Ethyldifluoroacetate MT 1.430 Pyrazole Acid MT 1.000 Reagent Ammonium Salt Acetic Anhydride MT 3.150 Ammonium chloride cake MT 0.119 Anhydrous Ammonia MT 0.067 Anhydrous HCl MT 0.504 Spent Organic Solvent Cautic lye (48%) MT 0.880 Acetone, MT 9.782 Trimethylorthoformate, Ethyl acetate & Acetic anhydride MMH (35%) MT 0.860 Ethyl Acetate & Ethanol MT 1.393 Sodium Ethoxide MT 0.911 Sodium Fluoride MT 0.014 Sodium Salt Sulphuric Acid (98%) MT 0.533 NaCl Cake MT 0.331 Trimethylorthoformate MT 1.730 Sodium Fluoride MT 0.014 Solid RM Process Organic Residue Hyflow MT 0.027 Organic Residue MT 0.245 Molecular Sieve MT 0.002 Spent Catalyst Solvent Hyflow MT 0.027 Acetone MT 2.050 Molecular Sieve MT 0.002 Ethyl Acetate MT 2.125 Wastewater Water Effluent MT 17.670 Process Water MT 16.300 Process Gaseous Emission Gas Nitrogen MT 1.000 Nitrogen MT 1.000 Total Input MT 31.583 Total Output MT 31.583 59

Option: 3 Input Output Key RM Product Ethyldifluoroacetate MT 0.930 Pyrazole Acid MT 1.000 Reagent Sodium Salt TFEMe MT 0.800 NaCl MT 1.263 NaOH (48%) MT 1.263 MMH solution (35%) MT 0.790 Wastewater Dry HCl MT 1.100 Effluent MT 17.000 HCl (on 100% basis) as 30% MT 0.700 solution Process Gaseous Emission Solvent Nitrogen MT 0.300 TEA MT 0.380 Toluene MT 1.000 Spent Organic Solvent Methanol MT 0.100 Methanol MT 0.100 Toluene MT 1.000 Water Process Water MT 13.300 Gas Nitrogen MT 0.300 Total Input MT 20.663 Total Output MT 20.663 60

ix. Chloro Trichloro Methyl Cyclopentene Process Flow Diagram: Dicyclopentadiene (DCPD) will crack to Cyclopentadiene (CPD) at temperature of 150 C. CPD will react with CCl4 in presence of catalyst solution comprising of CuCl, TMEDA (Tetramethylethylenediamine) & MIBK (Methyl isobutyl Ketone) and mixture of CCl4 & MIBK. This leads to the formation of CTCM-CP. Reaction mass will go for filtration. CuCl cake will send for drying & sold. CCl4 & MIBK will stripped off from the Reactor mass, go for water wash. Aqueous layer will send for caustic treatment & then post organic stripping, send to ETP. Organic layer will send to Distillation after addition of xylene & desired Product will obtain. Product distillation overhead will go to a distillation column for Xylene & MIBK recovery & recycling. Chemical Reaction: C10H12 2 C5H6 132 132 Dicyclopentadiene Cyclopentadiene C5H6 + CCl4 C6H6Cl4 66 154 220 Cyclopentadiene Carbontetrachloride Chloro trichloro Methyl - Cyclopentene 61

Material Balance: Input Output Key RM Product Carbon tetrachloride MT 0.699 Chloro Trichloro Methyl - Cyclopentene MT 1.000 Reagent Spent Organic Solvent Caustic Lye (48%) MT 0.022 Dicyclopentadyene & Chlorobenzene MT 0.218 Cuprous Chloride MT 0.077 Methyl isobutyl Ketone & Mix MT 0.389 Xylene Dicyclopentadiene (DCPD) MT 0.381 K2CO3 MT 0.008 Spent Catalyst Monochlorobenzene (MCB) MT 0.078 Ceramic balls MT 0.001 Tetramethyl ethylene diamine MT 0.020 Molecular Sieve MT 0.006 Solid RM Copper Salt Ceramic balls MT 0.001 CuCl Cake MT 0.098 Molecular Sieve MT 0.006 Wastewater Solvent Effluent MT 4.396 Methyl isobutyl Ketone MT 0.129 (MIBK) Mix Xylene MT 0.307 Process Gaseous Emission Nitrogen MT 0.300 Water Process Water MT 4.396 Potassium Salt K2CO3 Cake MT 0.015 Gas Nitrogen MT 0.300 Total Input MT 6.424 Total Output MT 6.424 62

x. 2-methyl-4-(1,1,1,2,3,3,3-heptafluoro-2-propyl) aniline Process Description: Bromination of Hexafluoro propene (HFP) to form Dibromo hexafluoropropane (DBHFP). Heptafluoroisopropyl bromide (HFIPBr) formation by reaction of Potassium fluoride and DBHFP with Dimethyl Formamide (DMF) as Solvent and HFIPBr Separation by distillation. DMF recovery by filtration: HFPOT formation by reaction of Ortho-Toluedine (O-T) and HFIPBr in Water with sodium dithionite and Catalyst. HFPOT crude mass treatment to separate O-T and TBA. Solvent swapping MTBE by Toluene HFPOT & Isomer salt formation to separate HFPOT Isomer. Hydrolysis of HFPOT salt with NH3 Aq. Solution. HFPOT Toluene separation. Chemical Reaction: Br2 + C3F6 C3F6Br2 160 150 310 Bromine HFP Dibromohexafluoropropane C3F6Br2 + KF C3F7Br + KBr 310 58 249 119 DBHFP Potassium fluoride Heptafluoroisopropyl (HFIPBR) bromide Potassium bromide C3F7Br + C6H5NH2CH3 Na2S2O4/TBAHS/Water C6H5NH2CH2C3F7 248.9 107 275 81 HFIPBR O-Toluidine HFPOT & HFPOT Isomer Hydrogen bromide + HBr 63

Material Balance: Input Output Key RM Product Hexafluoropropylene (HFP) MT 1.186 2-methyl-4- (1,1,1,2,3,3,3- heptafluoro-2-propyl aniline (HFPOT)- P19 MT 1.000 Reagent Spent Organic Solvent Anhydrous HCl MT 0.247 Dimethylformamide MT 0.780 Bromine MT 1.263 Caustic Flakes MT 0.360 Sodium Salt Caustic Lye (48%) MT 0.330 Sodium bromide MT 0.030 Dimethylformamide MT 0.892 HCl 30% MT 0.191 Wastewater Ammonium hydroxide solution MT 0.921 Effluent MT 22.148 (25%) K2CO3 MT 0.030 Potassium Fluoride (KF) MT 0.873 Process Gaseous Emission Sodium dithionite (Na2S2O4) MT 0.268 Nitrogen MT 2.000 Tetrabutylammonium MT 0.209 hydrogensulfate Potassium Salt Solvent Potassium fluoride & Potassium bromide MT 2.039 Methyl tert-butyl ether (MTBE) MT 0.543 O-Toluedine MT 0.660 Process Residue and Waste Toluene MT 1.985 2-methyl-4- (1,1,1,2,3,3,3- heptafluoro-2-propyl aniline (HFPOT)& Toluene MT 1.250 Water Process Water MT 17.600 Gas Nitrogen MT 2.000 Organic Waste MT 0.311 Total Input MT 29.558 Total Output MT 29.558 64

xi. Fluoromethylester Process Description: Chloro Malonic Ester and HF will react in presence of Triethylamine to produce FME and HCl. The reaction mass will wash with water and separated into organic layer and aqueous layer. The aqueous layer will extract with Toluene and send to neutralization and filtration. The toluene extract and organic layer will distill to obtain to FME. Organic residue from distillation will send to sales / incineration. In neutralization and filtration step, the aqueous layer will treat with 33% NaOH solution and CaO and the resultant slurry will filter to separate CaF2 solids, which will be sold as by-s. The aqueous effluent will goes to ETP for further treatment and disposal. Chemical Reaction: Triethylamine C7H11O4Cl + HF C7H11O4F + HCl 194.5 20 178 36.5 Material Balance: Input Output Key RM Product Chloro Malonic Ester MT 1.457 Fluoromethyl ester (FME) MT 1.000 Reagent Calcium Salt CaO MT 1.260 CaF2 Solids MT 1.330 Anhydrous Hydrogen fluoride MT 0.899 NaOH (33%) MT 2.178 Wastewater Triethylamine MT 0.254 Effluent MT 61.116 Organic Heavies MT 0.350 Solvent Toluene MT 0.225 Process Gaseous Emission Nitrogen MT 1.000 Water Process Water MT 57.522 Gas Nitrogen MT 1.000 Total Input MT 64.796 Total Output MT 64.796 65

xii. Diphenylphenol Process Description: Three molecules of Cyclohexanone combines to form Trimmer-->Step-1 Mass will Distilled to obtain Trimmer from mixture of solvent, dimmer and Trimmer will dehydrogenate to form SC-03--> Step-2 Organic mass from step-2 undergo series of workup step to Crystallize the Finally crude will be filtered and dried to obtain of desired quality Solvent recovery will be done to recycle part of the solvent back in the process. Organic Residue left after distillation is sent for incineration. Chemical Reaction: 3 Cyclohexanone M.W- 98.15 NaOH Trimer + Isomers + 2 H 2 O M.W- 258.41 M.W- 18 2 Cyclohexanone M.W- 98.15 NaOH Dimer + 2 H 2 O M.W- 178.28 M.W- 18 Trimer + Isomers M.W- 258.41 Dehydrogenation 2,6-Diphenylphenol + 6H 2 M.W- 246.31 M.W- 2 Material Balance: Input Output Key RM Product Cyclohexanone MT 4.417 Diphenylphenol (SC-03) MT 1.000 Reagent Calcium Salt Heptane MT 0.587 CaF2 Solids MT 0.199 Isopropanol MT 0.435 NaOH Solution (25%) MT 0.204 Wastewater Paladium /alumina MT 0.059 Effluent MT 7.353 Phosphoric Acid (85%) MT 0.049 Organic Heavies MT 3.400 Potassium Carbonate MT 0.046 Process Gaseous Emission Solvent Nitrogen MT 0.200 Xylene MT 0.059 Water Process Water MT 6.096 Gas Nitrogen MT 0.200 Total Input MT 12.152 Total Output MT 12.152 66

xiii. Tetrafluoropropene - 1234yf Process Description: Chlorodifluoromethane reacts with methanol to give Tetrafluoropropene - 1234yf. Chemical Reaction: 2CHClF2 + CH3OH CF3-CF=CH2 + 2HCl + H2O R22 HFO Material Balance: Input Unit Quantity Output Unit Quantity Key RM Product Chlorodifluoromethane MT 1.920 Tetrafluoropropene - 1234yf MT 1.000 Reagent Inorganic Acid Caustic lye 48% MT 0.200 Hydrochloric Acid 15-30% MT 2.200 Sulphuric Acid 98% MT 0.007 Sulphuric Acid, 70-98% MT 0.250 Solvent Wastewater Methanol MT 0.360 Effluent MT 0.160 Spent Caustic, 0.5% MT 0.128 Water Heavies MT 0.040 Process Water MT 0.241 Plant Wash 1.050 Total Input MT 3.778 Total Output MT 3.778 67

xiv. Isobutyl Acetophenone Process Description: Isobutyl benzene reacts with acetic anhydride in presence of Hydrogen Fluoride and forms Isobutyl Acetophenone and Acetic acid. Chemical Reaction: C10H14 + (CH3CO)2O C12H16O + CH3COOH AHF 134.22 102.09 20.01 176.25 60.05 Isobutyl benzene Acetic Anhydride Hydrogen Fluoride IBAP Acetic Acid Material Balance: Input Output Key RM Product Isobutylbenzene MT 0.760 Isobutyl Acetophenone MT 1.000 Reagent Spent Organic Solvent Acetic anhydride MT 0.580 Acetic Acid MT 0.340 Hydrogen Fluoride MT 0.260 Process Gaseous Emission Water Nitrogen, Oxygen and MT 0.100 Organic Stock Emission Process Water MT 0.610 Wastewater Gas Effluent, Acidic MT 0.870 Nitrogen MT 0.100 Total Input MT 2.310 Total Output MT 2.310 68

xv. 2-Bromo-5-fluorobenzotrifluoride Process Description: Reaction of 3-(Trifluoromethyl)aniline with Acetyl Chloride to give 3-(Trifluorophenyl) acetamide 3- trifluorophenyl Acetamide is Brominated with Br2 to give 4-Bromo-3-(trifluoromethylphenyl) acetamide 4-Bromo-3-(trifluoromethylphenyl) Acetamide is reacted with HCl to give 2-Bromo-5- aminobenzotrifluoride 2-Bromo-5-aminobenzotrifluoride is fluorinated with HF to give 2-Bromo-5- fluorobenzotrifluoride Chemical Reaction: Step-1 C6H4 -CF3-NH2 + CH3COCl C6H4 -CF3-NHCOCH3 + HCl DCM M.Wt 161 78.5 203 36.5 3-(Trifluoromethyl)aniline Acetyl Chloride 3-(Trifluorophenyl) acetamide Hydrochloric acid Step-2 C6H4 -CF3-NHCOCH3 + Br2 C6H3 -CF3-Br-NHCOCH3 + HBr Step-3 203 159.81 282 80.81 3-(Trifluorophenyl) acetamide Bromine 4-Bromo-3- Hydrobromic acid (trifluoromethylphenyl) C6H3 -CF3-Br-NHCOCH3 + HCl + CH3OH + NaOH C6H3 -CF3-Br-NH2 + NaCl + H2O + CH3COOCH3 M.Wt 282 36.5 32 40 240 58.5 18 74 4-Bromo-3- Hydrochloric acid MethanolSodium Hydroxide 2-Bromo-5-aminobenzotrifluoride Sodium Chloride Water Methyl Acetate (trifluoromethylphenyl) Step-4 C6H3 -CF3-Br-NH2 + NaNO2 + 2HF C6H3 -CF3-Br-F + NaF + 2H2O + N2 M.Wt 240 68.9 20 243 42 18 28 2-Bromo-5- Sodium NitriteHydrogen Fluoride 2-Bromo-5-fluorobenzotrifluoride Sodium Fluoride Water Nitrogen aminobenzotrifluoride 69

Material Balance: Input Key RM 3-(Trifluoromethyl)aniline (m-abtf) Output Product MT 1.060 2-Bromo-5- MT 1.000 fluorobenzotrifluoride (BFBTF) Hydrofluoric acid (20-60%) MT 3.200 Reagent Acetyl Chloride MT 0.620 Spent Organic Solvent Sodium Hydroxide (48%) MT 2.600 Traces of Methanol, Methylene Chloride & Pyridine MT 1.044 Methylene Chloride MT 1.100 Bromine MT 0.800 Solid Waste Sodium hydrogen sulfite MT 1.000 Solid Waste MT 0.377 Hydrochloric Acid MT 0.360 Anhydrous Hydrofluoric MT 0.600 Wastewater Acid Sodium nitrite MT 0.540 Aqueous Effluent MT 11.019 Pyridine MT 0.040 Organic residue MT 0.580 Solvent Methanol MT 1.500 Water Process Water MT 7.000 Total Input MT 17.220 Total Output MT 17.220 70

xvi. 2,2-Difluroethylamine Process Description: 1,1,2-Trichloroethane (TCA) reacts with Hydrogen Fluoride in presence of catalyst and form 1-Chloro- 2,2-Difluroethane, 1-Chloro-2,2-difluoroethane reacts with Ammonia to form 1-Chloro-2,2- diflouroethane. Chemical Reaction: C2H3Cl3 Catalyst + 2 HF C2H3ClF2 + 2 HCL 133.40 20.01 100.50 36.46 1,1,2-Trichloroethane Hydrogen Fluoride 1-Chloro-2,2-difluoroethane Hydrochloric acid C2H3ClF2 + NH3 C2H5F2N + NH4Cl Water 100.50 17.031 81.06 53.49 1-Chloro-2,2-difluoroethane Ammonia 1-Chloro-2,2-difluoroethane Hydrochloric Acid Material Balance: Input Key RM 1,1,2-Trichloroethane (TCA) Output Product MT 2.351 2,2-Difluroethylamine (DFEA) MT 1.000 Hydrochloric acid (15-33%) MT 4.280 Reagent Hydrofluoric acid (20-60%) MT 1.170 Hydrogen Fluoride MT 1.057 Ammonia (25%) Solution in Water MT 2.317 Wastewater Aqueous Effluent MT 6.570 Water Process Water MT 7.295 Process Gaseous Emission Nitrogen, Oxygen and Organic Stock Emission Gas Nitrogen MT 0.200 MT 0.200 Total Input MT 13.220 Total Output MT 13.220 71

xvii. 2,3-Dichloro-5-trifluoromethyl-pyridine Process Description: 2,3-Dichloro-5-trichloromethyl pyridine reacts with hydrofluoric acid in presence of catalyst and oxygen and forms 2,3-Dichloro-5-trifluoromethyl-pyridine (DCTFMP). Chemical Reaction: Catalyst C6H2Cl5N + 3 HF C12H16O + 3 HCL Oxygen 265.35 20.01 216.00 36.46 DTCMP Hydrogen Fluoride DCTFMP Hydrogen Chloride Material Balance: Input Key RM 2,3-Dichloro-5- trichloromethyl pyridine Output Product MT 2.050 2,3-Dichloro-5- trifluoromethyl-pyridine (DCTFMP) MT 1.000 Hydrofluoric acid (20-60%) MT 0.154 Reagent Hydrogen Fluoride MT 0.510 Inorganic Acid Dichloromethane MT 0.260 Hydrochloric acid (15-33%) MT 2.813 Potassium Carbonate MT 2.310 Wastewater Water Aqueous Effluent MT 2.983 Process Water MT 2.080 Process Gaseous Emission Gas Nitrogen MT 0.100 Oxygen MT 0.250 Nitrogen, Oxygen and Organic Stock Emission MT 0.600 Total Input MT 7.560 Total Output MT 7.560 72

xviii. N[1-{6-Chloro-3-pyridinyl)methyl)-2(1H)-pyridinylidene]-2,2,2, trifluoroacetamide Process Description: Reaction of 2-Aminopyridine with Trifluoro acetic Acid to form 2-(2,2,2-Trifluoroacetylamino)pyridine Reaction of 2-(2,2,2-Trifluoroacetylamino)pyridine with 2 Chloro 5-(chloromethyl)pyridine to give N[1-{6- Chloro-3-pyridinyl)methyl)-2(1H)-pyridinylidene]-2,2,2, trifluoroacetamide. Chemical Reaction: Ethyl Acetate C5H6N2 + CF3COOH + SOCl2 + 2 C5H5N C7H5N2OF3 + C5H5N. HCl + SO2 2-Amino Pyridine Trifluoroacetic AciThionyl Chloride Pyridine 2(2,2,2 Trifluoroamino)Pyridine Pyridine Hydrochloride Sulfur Dioxide M.W. - 94.11 M.W. - 114 M.W. - 119 M.W. - 79 M.W. - 79 M.W. - 79 M.W. - 79 DMSO, Water 2 C7H5N2OF3 + 2 C6H5Cl2N + K2CO3 2 C13H9N3ClOF3 + 2KCl + CO2 + H2O 2(2,2,2 Trifluoroamino)Pyridine hloro-5(chloromethyl) Pyrid Potassium Carbonate M1011 Potassium ChloridCarbon Dioxide Water M.W. - 79 M.W. - 79 M.W. - 79 M.W. - 315.68 M.W. - 74 M.W. - 44 M.W. - 29 Material Balance: Input Output Key RM Product 2-Aminopyridine MT 0.350 N[1-{6-Chloro-3- pyridinyl)methyl)-2(1h)- pyridinylidene]-2,2,2, trifluoroacetamide (M1011) MT 1.000 Reagent Solid Waste Trifluoroacetic Acid MT 0.440 Solid Waste MT 0.193 Thionyl Chloride MT 0.480 2-Chloro- 5(chloromethyl) Pyridine (CPMC) MT 0.520 Wastewater Potassium Carbonate MT 0.390 Aqueous Effluent MT 13.583 Mixed Organic MT 0.474 Solvent Pyridine MT 0.260 Ethyl Acetate MT 0.590 Dimethyl sulfoxide MT 0.200 Methanol MT 0.320 Water Process Water MT 11.700 Total Input MT 15.250 Total Output MT 15.250 73

xix. (1-(3-Chloropyridine-2-yl)-3-((5-(trifluoromethyl)-2H-tetrazol-2-yl)methyl)-1H pyrozol-5-carboxylic acid) Process Description: Reaction of HYPE with Thionyl Chloride to form CLOPE, Reaction of CLOPE with 5-(Trifluoromethyl)-2Htetrazole sodium salt (TFMT-Na) to form TEPE, Hydrolysis of TEPE with Aquesous NaOH followed by HCl to form (1-(3-Chloropyridine-2-yl)-3-((5-(trifluoromethyl)-2H-tetrazol-2-yl)methyl)-1H pyrozol-5- carboxylic acid). Chemical Reaction: C11H10N3ClO3 + SOCl2 Toluene C11H9N3Cl2O2 + SO2 + HCl HYPE Thionyl Chloride Aq. NaHCO3 CLOPE Sulfur Dioxide Hydrochloric Acid M.W. 267.7 M.W. - 119 M.W. 286 M.W. 64 M.W. 36.5 Acetone, Water C11H9N3Cl2O2 + C2F3N4 - Na C13H9N7ClO2F3 NaCl + CLOPE TFMT-Na TEPE Sodium Chloride M.W. 286 M.W. 160 M.W. 387.5 M.W. 58.5 Methanol, Water C13H9N7ClO2F3 + NaOH + HCl C12H7N7ClO2F3 + NaCl + CH3OH TEPE Sodium Hydroxide Hydrochlorid Acid TESA Sodium Chloride Methanol M.W. 387.5 M.W. 40 M.W. 35.5 M.W. 373.7 M.W. 58.5 M.W. 32l 74

Material Balance: Input Output Key RM Product HYPE MT 0.940 (1-(3-Chloropyridine-2-yl)- 3-((5-(trifluoromethyl)-2Htetrazol-2-yl)methyl)-1H pyrozol-5-carboxylic acid) MT 1.000 Reagent Wastewater Thionyl Chloride MT 0.510 Aqueous Effluent MT 19.400 Sodium bicarbonate (8%) MT 3.670 Mixed Organic MT 4.820 Potassium Iodide MT 0.060 5-(Trifluoromethyl)-2Htetrazole MT 0.590 sodium salt (TFMT- Na) Sodium Hydroxide (32%) MT 0.430 Hydrochloric Acid (20%) MT 0.690 Solvent Toluene MT 4.440 Acetone MT 0.170 Methanol MT 1.940 Water Process Water MT 11.780 Total Input MT 25.220 Total Output MT 25.220 75

xx. (N-(4-fluorophenyl)-2-hydroxy-N-isopropyl-acetamide Process Description: Reaction of FNB with hydrogen and acetone in presence of catalyst and toluene solvent to form FIPA, Reaction of FIPA with Chloroacetyl Chloride in presence of toluene solvent to form CFPIPA, Reaction of CFPIPA with Sodium carbonate and Water in presence of N-methyl-pyrollidone (NMP) solvent to form (N-(4-fluorophenyl)-2-hydroxy-N-isopropyl-acetamide (FOE-OH). Chemical Reaction: C6H4FNO2 + 4 H2 + C3H6O Toluene C9H12FN + 3 H2O FNB Hydrogen Acetone Catalyst FIPA Water 141.1 2.02 58.08 153.2 18.01 Toluene C9H12FN + C2H2Cl2O C11H13ClFNO HCl + FIPA Chloroacetylchloride CFPIPA Hydrogen Chloride 153.2 112.94 229.678 36.46 NMP 2 C11H13ClFNO + Na2CO3 + H2O 2 C11H14FNO2 + 2 Nacl + CO2 CFPIPA Sodium carbonate Water FOE-OH Sodium chloride Carbon dioxide 229.678 105.988 18.01 211.23 58.44 44.01 76

Material Balance: Input Output Key RM Product 4-Fluoro-nitrobenzene MT 0.980 (N-(4-fluorophenyl)-2- hydroxy-n-isopropylacetamide (FOE-OH) MT 1.000 Reagent Inorganic Acid Chloroacetyl chloride MT 0.770 Hydrochloric acid (15- MT 0.756 33%) Sodiumcarbonate MT 0.690 N-methyl-pyrollidone (NMP) MT 0.290 Wastewater Aqueous Effluent MT 3.780 Solvent Acetone MT 0.440 Process Residue and Waste Toluene MT 0.690 Residue MT 0.160 Water Process Gaseous Emission Process Water MT 2.890 Nitrogen, Hydrogen + Organic Vent to Stack MT 1.224 Gas Hydrogen MT 0.070 Nitrogen MT 0.100 Total Input MT 6.920 Total Output MT 6.920 77

4. 1,1,2,2-Tetrafluoroethyl Methyl Ether (TFEMe) Process Description: Chlorodifluoromethane (R22) wills pyrolyse at High Temp. In electrically heated furnace. On Pyrolysis, R22 breaks in to No. of s with HCl gas as. Product Gas Mix containing HCl will pass through HCl absorbers where Fresh water will circulate in absorber to absorb HCl gas & make Gas HCl free. In this stage 30 % HCl solution will generate as of the process. Gas will be washed with Alkali solution & dried before sending to Compressor section. Product gas will be compressed at High pressure to achieve condensation of the Gas mix. In Liquid form which will be fed to Distillation section for separation of s. Distillation Section: In this section Tetrafluoroethylene (TFE) & Hexafluoropropylene (HFP) will separate out from gas mix. Unreacted R22 will separate & recycle back to Reaction section. Residue from the Distillation section will treat with solvent & send for Incineration. Tetrafluoroethyl methyl ether Reaction Section: TFE will react with Methanol in presence of Catalyst in pressure Reactor to form TFEMe. TFEMe Distillation Section: TFEMe + unreacted Methanol mix will feed to Distillation column for Separation of TFEMe & unreacted Methanol. Unreacted Methanol will recycle back to Reactor. Chemical Reaction: CHClF2 CF2 + HCl 86.5 50 36.5 Chlorodifluoromethane Difluorocarbene Hydrochloric Acid CF2 + CF2 C2F4 50 50 100 Difluorocarbene Difluorocarbene TFE C2F4 + CF2 C3F6 100 50 150 TFE Difluorocarbene HFP C2F4 + CH3OH CHF2CF2OCH3 100 32 132 TFE Methanol TFEMe 78

Material Balance: Input Key RM Chlorodifluoromethane (R 22) Output Product MT 1.925 1,1,2,2-Tetrafluoroethyl Methyl Ether (96%) MT 1.000 Reagent Inorganic Acid H2SO4 (98%) MT 0.850 Sulphuric Acid (95%) MT 0.877 Caustic Lye (48%) MT 0.261 Hydrochloric Acid 30% MT 2.825 Dimethylformamide MT 0.006 Sodium Methoxide (30%) MT 0.060 By- Sodium Sulphite MT 0.001 Sodium Methoxide (6%) MT 0.030 Terpene MT 0.015 Spent Organic Solvent Solid RM Terpene MT 0.015 Activated Alumina Balls MT 0.001 Dimethylformamide MT 0.006 Molecular Sieve MT 0.001 Silica Gel MT 0.001 Process Residue and Waste Spent Organic residue MT 0.100 Solvent Methanol MT 0.300 Spent Catalyst Activated Alumina Balls MT 0.001 Water Molecular Sieve MT 0.001 Process Water MT 4.635 Silica Gel MT 0.001 Gas Wastewater Nitrogen MT 0.265 Effluent MT 3.200 Process Gaseous Emission Nitrogen & HCl traces emission MT 0.265 Total Input MT 8.321 Total Output MT 8.321 79

5. Hexafluoropropylene Process Description: Reaction Section: Chlorodifluoromethane (R22) will pyrolyse at High Temp. In electrically heated furnace. On Pyrolysis, R22 breaks in to No. of s with HCl gas as. Refining Section: Product Gas Mix containing HCl will pass through HCl absorbers where Fresh water will circulate in absorber to absorb HCl gas & make Gas HCl free. In this stage 30 % HCl solution will generate as of the process. Gas will be washed with Alkali solution & dried before send to Compressor section. Product gas will compress at High pressure to achieve condensation of the Gas mix in Liquid form which will be feed to Distillation section for separation of s. Distillation Section: In this section Tetrafluoroethylene (TFE) & Hexafluoropropylene (HFP) will separate out from gas mix. Unreacted R22 will separate & recycle back to Reaction section. Residue from the Distillation section will treat with solvent & send for Incineration. Tetrafluoroethyl methyl ether Reaction Section: TFE will react with Methanol in presence of Catalyst in pressure Reactor to form TFEMe. TFEMe Distillation Section: TFEMe + unreacted Methanol mix will feed to Distillation column for Separation of TFEMe & unreacted Methanol. Unreacted Methanol will recycle back to Reactor. Chemical Reaction: CHClF2 CF2 + HCl 86.5 50 36.5 R 22 Difluorocarbene Hydrochloric Acid CF2 + CF2 C2F4 50 50 100 Difluorocarbene Difluorocarbene TFE C2F4 + CF2 C3F6 100 50 150 TFE Difluorocarbene HFP 80

Material Balance: Input Output Key RM Product Chlorodifluoromethane (R 22) MT 3.235 Hexafluoropropylene MT 1.000 Reagent Inorganic Acid H2SO4 (98%) MT 0.950 Sulphuric Acid (95%) MT 0.980 Caustic Lye (48%) MT 0.345 Hydrochloric Acid 30% MT 4.450 Dimethylformamide MT 0.006 Sodium Sulphite MT 0.001 Spent Catalyst Terpene MT 0.015 Activated Alumina Balls MT 0.001 Molecular Sieve MT 0.001 Solid RM Silica Gel MT 0.001 Activated Alumina Balls MT 0.001 Molecular Sieve MT 0.001 Wastewater Silica Gel MT 0.001 Effluent MT 2.944 Solvent Spent Organic Solvent Methanol MT 0.120 Terpene MT 0.015 Dimethylformamide MT 0.006 Water Process Water MT 6.474 Process Gaseous Emission Nitrogen & HCl traces emission MT 1.000 Gas MT 1.000 Nitrogen Process Residue and Waste Spent Organic residue MT 1.751 Total Input MT 12.149 Total Output MT 12.149 81

6. Ethyl Difluoroacetoacetate (EDFAA) Process Description: EDFA will react in presence of Sodium Salt catalyst to form salt of EDFAA in presence of suitable solvent. Salt will acidify with Dry HCL to form EDFAA and Sodium Salt at RT. Solvent will recover from reaction mass and taken for filtration. Crude Product will further distillate and purify to get desired quality. Stripped solvent will treat with ammonia gas to neutralize wherein ammonium chloride will formed neutralized solvent mix will separate through distillation & recycle in process. Chemical Reaction: CHF2COOC2H5 + CH3COOC2H5 + NaOC2H5 CHF2COCH2COOC2H5 + C2H5OH + NaOC2H5 124.087 88.106 68.061 166.125 46.069 68.061 EDFA Ethyl Acetate Sod. Ethoxide EDFAA NaOC2H5 + HCl NaCl + C2H5OH 68.061 36.461 58.453 46.069 Material Balance: Input Output Key RM Product Ethyldifluoroacetate MT 1.042 Ethyl Difluoroacetoacetate (EDFAA) MT 1.000 Reagent Spent Organic Solvent Anhydrous Ammonia MT 0.031 Ethyl Acetate & Ethanol Mixture MT 1.562 Anhydrous HCl MT 0.385 Ethyl Acetate MT 2.000 Sodium Salt Sodium Ethoxide MT 0.618 NaCl Cake MT 0.592 Sodium Fluoride MT 0.020 Solid RM Hyflow MT 0.010 Process Residue and Waste Molecular Sieve MT 0.002 Spent Organic residue MT 0.226 Water Spent Catalyst Process Water MT 2.305 Hyflow MT 0.010 Molecular Sieve MT 0.002 Gas Nitrogen MT 1.000 Wastewater Effluent MT 2.981 Process Gaseous Emission Nitrogen MT 1.000 Total Input MT 7.393 Total Output MT 7.393 82

7. Difluromethane Sulfonyl Chloride Process Description: Benzyl chloride, thio-urea & caustic lye will react to form benzyl Mercaptan thiouron HCl. This on reaction with HCl gives Benzyl Mercaptan. This will be sent to filtration to separate DCDA cake. Layer separation was done to separate Benzyl Mercaptan from aqueous layer. Aqueous layer was extracted with MDC (Methylene Chloride) to recover Benzyl Mercaptan on reaction with R22 (Chlorodifluoromethane) & caustic to form BDFMS (Benzyl Difluoromethyl Sulphide). Layer separation was done to separate the aqueous layer. BDFMS formed will go for reaction with chlorine & water in the presence of MDC as a solvent to give DFMSC Layer separation was done to remove aqueous layer. Organic layer was taken to distillation to recover pure DFMSC. Chemical Reaction: C6H5CH2Cl + CS(NH2)2 C6H5CH2SCNHNH2.HCl 126.5 76 202.5 Benzyl chloride Thiourea Benzylthiouron.HCl C6H5CH2SCNHNH2.HCl + 2 NaOH C6H5CH2SNa + NaCl + 0.6 H2NCNHNHCN + 2H2O 202.5 80 146 58.5 42 36 BM Sodium salt Sodium Chloride DCDA Water C6H5CH2SNa + HCl C6H5CH2SH + NaCl 146 36.5 124 58.5 BM Sodium salt Benzyl Mercaptan C6H5CH2SH + CHF2Cl + NaOH C6H5CH2SCHF2 + NaCl + H2O 124 86.5 40 174 58.5 18 Benzyl Mercaptan R22 Sodium Hydroxide BDFMS Sodium Chloride Water C6H5CH2SCHF2 + 3Cl2 + 2H2O CLSO2CHF2 + C6H5CH2Cl + 4HCl 174 213 36 150.5 126.5 146 BDFMS Chlorine Water DFMSC Benzyl chloride Hydrochloric Acid 83

Material Balance: Input Output Key RM Product Chlorodifluoromethane (R22) MT 1.030 Difluoromethanesulphonlyc hloride MT 1.000 Reagent Inorganic Acid Benzyl Chloride MT 0.590 Sodium Hypochlorite MT 7.500 Chlorine MT 2.460 Hydrochloric Acid 10-30% MT 1.000 Caustic Lye 48% MT 3.730 Dilute Hydrochloric Acid 10-30% MT 1.880 Inorganic Salt Methylene Chloride MT 0.230 Solid waste MT 0.270 Thiourea MT 0.890 Wastewater Water Effluent MT 8.790 Process Water MT 7.750 Process Gaseous Emission Gas Nitrogen Cl2 & HCl traces MT 0.100 emission Nitrogen MT 0.100 Total Input MT 18.660 Total Output MT 18.660 84

8. Triflic Acid Process Description: Methane sulfonyl chloride (MSCl) reacted with Potassium Fluoride (KF) solution to get Methanesulfonylfluroide (MSF). MSF will be reacted with HF and per fluorinated to form per fluorinated MSF as intermediate Perfluorianted MSF reacts with KOH and converted to Potassium Triflate (KT) which is an intermediate This KT then treated with conc. H2SO4 to get Trifluoromethanesulfonic acid (P-21). Chemical Reaction: CH3SO2Cl + KF CH3SO2F + KCl 114.6 58.1 98.1 74.6 MSCl potassium fluoride MSF Potassium Chloride CH3SO2F + 3 HF CF3SO2F + 3 H2 98.1 20 152.1 2 MSF Hydrogen Fluoride Pefluorinated MSF Hydrogen CF3SO2F + 2 KOH CF3SO3K + KF + H2O 152.1 56.1 188.2 58.1 18 Pefluorinated MSF potassium hydroxide Potassium Triflate potassium fluoride Water CF3SO3K + H2SO4 CF3SO3H + KHSO4 188.2 98.1 150.1 136.2 Potassium Triflate Sulfuric acid Triflic acid Potassium hydrogen Sulfate 85

Material Balance: Input Output Key RM Product Anhydrous Hydrogen Fluoride MT 1.169 Trifluoromethanesulfonic MT 1.000 (AHF) acid (P-21) Potassium Fluoride (KF) MT 0.604 30% Hydrofluoric Acid MT 0.749 Reagent Inorganic Acid Calcium Hydroxide MT 0.409 Sulphuric acid (70-95%) MT 5.302 Hydrogen Peroxide (H2O2) MT 0.050 Anhydrous Hydrogen Fluoride MT 0.908 By- (AHF) Potassium Hydroxide MT 2.730 CaF2 Solids MT 0.782 Sulphuric Acid MT 3.294 Oleum MT 1.089 Process Residue and Waste Organic Residue MT 0.560 Solvent Acetone MT 0.620 Wastewater Dichloromethane (DCM) MT 0.129 Effluent MT 3.138 Water Process Gaseous Emission Process Water MT 1.505 Nitrogen & HF traces emission MT 0.243 Gas Potassium Salt Nitrogen MT 0.243 Potassium Salt MT 0.975 Total Input MT 12.749 Total Output MT 12.749 86

9. Trifluoromethanesulfonic Anhydride Process Description: Trifluoromethanesulfonic Anhydride (P-22) prepared by the reaction of Triflic Acid (P-21) & Phosphorous Pentoxide (P2O5). After reaction, P22 separated by distillation. Then water added to residue to separate H3PO4 (Phosphoric Acid) solution. Vent Gases generated during Reaction and distillation will be scrubbed in 20% KOH solution. Chemical Reaction: Celite 6 CF3SO3H + P2O5 3 CF3SO2SO3CF3 + 2 H3PO4 PBFB 150.08 141.94 282.14 98 Triflic Acid Phosphorous Pentoxide Trifluoromethanesulfonic Anhydride Phosphoric Acid Material Balance: Input Output Key RM Product Triflic Acid (P-21) MT 1.329 Trifluoromethanesulfonic Anhydride MT 1.000 Reagent By- 48% KOH MT 0.833 Phosphoric Acid Solution MT 2.421 (75%) P2O5 MT 1.306 Parabromofluoro Benzene (P-4) MT 0.534 Inorganic Salt Potassium Fluoride (KF) MT 0.020 Solid Waste MT 0.032 Solid RM Wastewater Celite MT 0.032 Effluent MT 2.239 Water Process Gaseous Emission Process Water MT 2.191 Nitrogen MT 0.100 Gas Process Residue and Waste Nitrogen MT 0.100 Organic Residue MT 0.554 Total Input MT 6.346 Total Output MT 6.346 87

10. Trimethylsilyl trifluoromethanesulfonate Process Description: Trimethylsilyl trifluoromethanesulfonate (P23) prepared by the reaction of Triflic Acid (P21) & Trimethylsilyl Chloride (TMSC). After reaction, P23 will be separated by distillation. Vent Gases generated during Reaction scrubbed with process water to make.30% HCl. Chemical Reaction: CF3SO3H + (CH3)3SiCl (CH3)3Si-SO3CF3 + HCl 150.08 108.64 222.25 36.47 Triflic Acid Trimethylsilylchloride Trimethylsilyl trifluoromethanesul fonate Hydrogen Chloride Material Balance: Input Output Key RM Product Triflic Acid (P-21) MT 0.712 Trimethylsilyl trifluoromethanesulfonate MT 1.000 Reagent Inorganic Acid Trimethylsilyl chloride MT 0.544 Hydrochloric Acid 30 % MT 0.748 Water Wastewater Process Water MT 1.524 Effluent MT 1.000 Gas Process Gaseous Emission Nitrogen MT 0.100 Nitrogen & HCl traces emission MT 0.100 Process Residue and Waste Organic Residue MT 0.031 Total Input MT 2.879 Total Output MT 2.879 88

11. 3-Trifluoromethylacetophenone Process Description: TFMA reacts with dilute sulfuric acid and NaNO2 to form salt-->step-1 Salt formed in the above step is coupled with Acetaldoxime in presence of catalyst to form intermediate complex--> Step-2 Organic mass from step-2 is hydrolysed in presence of Diluted HCl to form TFMAP-->Step-3 Organic mass from step-3 undergo series of workup step to neutralize the mass and reduce the impurity contents. Solvent recovery will be done to recycle part of the solvent back in the process. Finally crude will be distilled to obtain of desired quality and residue from distillation will be sent for incineration. Chemical Reaction: C6H4-NH2-CF3 + H2SO4 C6H4--CF3-NH3HSO4 161 98 259 TFMA Sulfuric Acid Hydrozen Sulfate salt of TFMA C6H4--CF3-NH3HSO4 + NaNO2 + 0.5H2SO4 C6H4--CF3-N2 HSO4 + 0.5Na2SO4 + 2H2O 259 69 98 270.2 142 18 Hydrozen Sulfate salt of TFMA Sodium Nitrite Sulfuric Acid Diazonium Salt Sodium Sulfate Water C6H4--CF3-N2 HSO4 + 3CCHNOH C6H4-CF3-C2H3-NOH + N2 + H2SO4 Acetic Acid/CuSO4/NaOH 270.2 59.1 203 28 98 Diazonium Salt Acetaldoxime TFMAPOL Nitrogen Sulfuric Acid C6H4-CF3-C2H3-NOH + H2O + NH2OH C6H4-CF3-C2H3O HCl / Water Glass 203 18 188.2 33 TFMAPOL Water TFMAP Hydroxlyamine 89

Material Balance: Input Output Key RM Product Acetaldoxime 50% MT 1.300 3- Trifluoromethylacetopheno ne (TFMAP: SC-04) MT 1.000 Reagent Wastewater Acetic Acid MT 0.490 Effluent MT 21.185 Caustic Lye 48% MT 2.275 CuSO4 Solution 10.7% MT 0.770 Process Gaseous Emission Dilute Hydrochloric Acid 10 - MT 1.800 Nitrogen MT 0.100 30% H2SO4 98% MT 1.560 KHCO3 Solution 25% MT 0.164 Process Residue and Waste Sodium Nitrite MT 0.610 Organic Residue MT 1.280 TFMA MT 1.330 Solvent Mix Xylene MT 0.450 Water Process Water MT 12.716 Gas Nitrogen MT 0.100 Total Input MT 23.565 Total Output MT 23.565 90

12. 2,6-Dichloro-4-(trifluoromethyl)aniline Process Description: P-Chloro toluene will be photo chlorinated to form 4-ClBTC. 4-ClBTC was reacted with AHF to form 4- ClBTF. 4-ClBTF will treat with ammonia to form 4-ABTF. 4 -ABTF will treat with chlorine to form 2, 6- Dichloro-4-(trifluoromethyl) aniline. Chemical Reaction: C6H4 -Cl-CH3 126.5 P-chloro toluene + 3Cl2 C6H4-Cl-CCl3 + 3 HCl 213 230 109.5 Chlorine 1-chloro-4-(trichloromethyl) Hydrochloric acid benzene ( 4-ClBTC) C6H4-Cl-CCl3 230 4-ClBTC + 3 HF C6H4-Cl-CF3 + 3 HCl 60 180.5 109.5 Hydrogen floride 1-chloro-4-(trifluoromethyl) Hydrochloric acid benzene (4-ClBTF) C6H4-Cl-CF3 180.5 4-ClBTF + 2 NH3 C6H4-NH2-CF3 + NH4Cl 34 Cu, Cu(OAc)2 161.12 53.5 Ammonia 4 - Amino benzo trifluoride( Ammonium chloride 4-ABTF) C6H4-NH2-CF3 161.12 4-ABTF + 2 Cl2 + 2NH3 C6H4-NH2-F3-Cl2 + 2 NH4Cl 142 34 230 107 Chlorine Ammonia 2, 6-Dichloro-4-(trifluoromethyl) aniline Ammonium chloride 91

Material Balance: Input Output Key RM Product P-Chloro toluene MT 1.389 2,6-Dichloro-4- (trifluoromethyl)aniline (Synthon-1) MT 1.000 Reagent Inorganic Acid Chlorine MT 3.886 Hydrochloric Acid 10-30% MT 7.200 Copper MT 0.060 Hypo chlorite Solution (12%) MT 5.970 Copper Acetate MT 0.472 Hydrofluoric Acid (HF) MT 0.667 Ammonia Solution NH3 Solution 25% MT 1.081 NH3 Solution 25% MT 2.531 NMP MT 0.633 Caustic Lye 48% MT 1.910 Wastewater Effluent MT 0.720 Solvent Hexane MT 0.647 Process Gaseous Emission Nitrogen, HCl, Cl2 and Ammonia MT 0.200 traces Water Process Water MT 10.704 Process Residue and Waste Organic Residue MT 1.976 Gas Nitrogen MT 0.200 Ammonium Salt Ammonium chloride + Cu Salt MT 2.052 Total Input MT 21.649 Total Output MT 21.649 92

13. Cyanapyrazole Process Description: P-Chloro toluene will be photo chlorinated to form 4-ClBTC. 4-ClBTC will react with AHF to form 4-ClBTF. 4-ClBTF was treated with ammonia to form 4-ABTF. 4 -ABTF was treated with chlorine to form synthon 1 Synthon 1 will be diazotized and coupled with synthon 2 to form cyanopyrazole. Chemical Reaction: C6H4 -Cl-CH3 126.5 P-chloro toluene + 3Cl2 C6H4-Cl-CCl3 + 3 HCl 213 230 109.5 Chlorine 1-chloro-4-(trichloromethyl) Hydrochloric acid benzene ( 4-ClBTC) C6H4-Cl-CCl3 230 4-ClBTC + 3 HF C6H4-Cl-CF3 + 3 HCl 60 180.5 109.5 Hydrogen floride 1-chloro-4-(trifluoromethyl) Hydrochloric acid benzene (4-ClBTF) C6H4-Cl-CF3 180.5 4-ClBTF + 2 NH3 C6H4-NH2-CF3 + NH4Cl 34 Cu, Cu(OAc)2 161.12 53.5 Ammonia 4 - Amino benzo trifluoride( Ammonium chloride 4-ABTF) C6H4-NH2-CF3 161.12 4-ABTF + 2 Cl2 + 2NH3 C6H4-NH2-F3-Cl2 + 2 NH4Cl 142 34 230 107 Chlorine Ammonia 2, 6-Dichloro-4-(trifluoromethyl) aniline Ammonium chloride HCl+ NaNO2 C6H4-NH2-CF3-Cl2 + CH (CN) COOC2H5 acetic acid 230 152 Syn-1 Syn-2 Ethyl 2,3 dicyanopropionate CF3 C6H2Cl2 C3HN2 CN2H2 321 Cyanopyrazole 93

Material Balance: Input Output Key RM Product P-Chloro toluene MT 1.195 Cyanapyrazole MT 1.000 Reagent Inorganic Acid Caustic Lye 48% MT 2.330 Hydrochloric Acid 10-30% MT 6.191 Chlorine MT 3.342 Hypo chlorite solution MT 4.820 Copper Acetate MT 0.406 Copper Powder MT 0.052 Wastewater Dilute Hydrochloric Acid MT 1.440 Effluent MT 22.358 10-30% Hydrofluoric Acid (HF) MT 0.574 Methylene Chloride MT 1.030 Process Gaseous Emission NaNO2 MT 0.282 Nitrogen, HCl, Cl2 and Ammonia MT 0.500 traces NH3 Solution 25% MT 0.930 NMP MT 0.519 Ammonium Salt Acetic acid MT 2.230 Ammonium chloride + Cu salt MT 1.765 Synthon-2 MT 0.565 Ammonia Solution Solvent NH3 Solution 25% MT 2.170 Hexane MT 0.093 Toluene MT 0.059 Process Residue and Waste Organic Residue MT 2.023 Water Process Water MT 25.280 Gas Nitrogen MT 0.500 Total Input MT 40.827 Total Output MT 40.827 94

14. Trifluoromethylbenzamide (TFMBA) Process Description: Step 1: Ortho Xylene, AIBN and Chlorine will charge to the reactor to produce step -1. The vent gases was scrubbed Step 2: Step-1 Product and HF will charge to the reactor to produce step -2 s. The vent gases scrubbed. Step 3: Step-2 Product, Methylene dichloride and H2SO4 will charge to the reactor for hydrolysis to form Step-3 Product and vent gas was scrubbed. Further processing of will be done and taken to the next step. Step 4: Step-3, AIBN and Chlorine will charge in the reactor.the vent gases was scrubbed. And taken to the next step. Step 5: Step-4, ammonia solution and water was added the reactor. Further processing of will be done. Pure Product will be obtained at the end of this step and it will be sent to storage. Chemical Reaction: Step 1 Penta chloro xylene (PCX) Formation C8H10 + 5Cl2 C8H5Cl5 + 5HCl 106 355 278.5 182.5 O-Xylene Chlorine o-pentachloroxylene Hydrogen Chloride Step 2 TriFluoroDiChloroXylene (TFDCX) Formation C8H5Cl5 + 3HF C8H5Cl2F3 + 3HCl 278.5 60 229.0 109.5 o-pentachloroxylene Chlorine o-trifluorodichloroxylene Hydrogen Chloride Step 3 TriFluoromethylbenzaldehyde (TFMB) Formation C8H5Cl2F3 + 2H2O C8H5F3O + 2HCl + H2O 229.0 36 174.0 73.0 18 o-trifluorodichloroxylene Water TriFluoromethylbenzaldehyde Hydrogen Chloride Water Step 4 TriFluoromethylbenzoylChloride (TFMBC) Formation C8H5F3O + Cl2 C8H4F3OCl + HCl 174.0 71 208.5 36.5 TriFluoromethylbenzaldehyde Water Trifluoromethylbenzoylchloride Hydrogen Chloride Step 5 TriFluoromethylbenzoylChloride (TFMBC) Formation C8H4F3OCl + 2NH3 C8H6F3ON + NH4Cl 208.5 34 189.0 53.5 Trifluoromethylbenzoylchloride Ammonia Trifluoromethylbenzoylchloride Ammonium Chloride 95

Material Balance: Input Output Key RM Product O-Xylene MT 1.183 Trifluoromethylbenzamide (TFMBA) MT 1.000 Reagent Inorganic Acid Ammonia Sol. -25% MT 1.431 Sulphuric Acid 75% MT 23.104 Caustic Lye 48% MT 8.594 Hydrochloric Acid 30% MT 24.748 Chlorine MT 7.996 Hypo chlorite Solution MT 24.661 Hydrofluoric acid Anhydrous MT 1.136 Methylene Chloride MT 1.420 Wastewater AIBN MT 0.057 Effluent MT 19.055 Sulphuric Acid 98% MT 22.414 Process Residue and Waste Water Organic Heavies MT 0.718 Process Water MT 50.229 P28 Traces MT 1.176 Gas Process Gaseous Emission Nitrogen MT 9.837 Nitrogen, HCl and Cl2 traces MT 9.837 Total Input MT 104.298 Total Output MT 104.298 96

15. Trifluoroacetyl chloride Process Description: In the process of TFAC, Hydrogen Fluoride, Chlorine and 48% NaOH Solution will react with Acetic Acid from Trifluoroacetyl chloride. Reaction maintaining few hrs. After maintaining distillation done and final collect in vessel and 30% HCl solution, 30% HF Solution sold as & Hypo solution sold as by-. Chemical Reaction: HF + 4Cl -2 + CH3COOH 2 HCl + HF + NaOCl + 20.1 35.4 60.05 73 20.1 74.44 132.47 Hydrogen Floride Chlorine Acetic Acid Hydrochloric Acid Hydrogen Floride Sodium Hypochlorite Trifluoroacetyl chloride Material Balance: Input Output Key RM Product Hydrogen Fluoride MT 0.750 Trifluoroacetyl chloride MT 1.000 Reagent Inorganic Acid Chlorine MT 3.160 Hydrochloric Acid 30 % MT 4.580 Charcoal MT 0.210 Hydrofluoric Acid 30 % MT 0.600 48% NaOH Solution MT 6.050 Sodium Hypochlorite MT 7.850 Acetic Acid MT 0.510 Wastewater Water Effluent MT 1.000 Process Water MT 4.910 Process Gaseous Emission Gas Nitrogen, HCl, Cl2 and HF traces MT 0.500 Nitrogen MT 0.500 Inorganic Salt Solid waste MT 0.340 Process Residue and Waste Organic Heavies MT 0.220 Total Input MT 16.090 Total Output MT 16.090 97

16. Sulphur Tetrafluoride Process Description: Fluorine gas will purge into the Sulfur Monochloride for the formation of Sulfur Tetrafluoride and Sulfur Dichloride. Sulfur Dichloride will convert back to Sulfur Monochloride by reaction with Sulfur. The Sulfur Tetrafluoride gas coming out of the reactor will condense collected and filled into the cylinders. Chemical Reaction: S + 4 F SF4 32 72 104 Sulfur Fluorine Sulphur Tetrafluoride Material Balance: Input Output Key RM Product Fluorine MT 0.795 Sulphur Tetrafluoride (SF4) MT 1.000 Reagent Spent Catalyst Sulphur MT 0.296 Spent Alumina MT 0.0004 Spent Molecular Sieve MT 0.0004 Solid RM Alumina Balls MT 0.001 Wastewater Molecular Sieve MT 0.001 Effluent MT 3.334 Water Process Gaseous Emission Process Water MT 3.333 Nitrogen + HF traces MT 0.291 Gas Nitrogen MT 0.200 Total Input MT 4.626 Total Output MT 4.626 98

17. 2- Trifluoromethyl benzoylchloride Process Description: Step 1: Ortho Xylene, AIBN and Chlorine will charge to the reactor to produce step -1. The vent gas was scrubbed. Step 2: Step-1 Product and HF will charge to the reactor to produce step -2 s. The vent gas was scrubbed. Step 3: Step-2 Product, Methylene dichloride and H2SO4 will charge to the reactor for hydrolysis to form Step-3 Product and vent gas was scrubbed. Further processing of will be done and taken to the next step. Step 4: Step-3, AIBN and Chlorine will charge in the reactor.the vent gases will be scrubbed. Purification from the reaction mass was carried out and will be obtained. Chemical Reaction: Step 1 Penta chloro xylene (PCX) Formation C8H10 + 5Cl2 C8H5Cl5 + 5HCl 106 355 278.5 182.5 O-Xylene Chlorine o-pentachloroxylene Hydrogen Chloride Step 2 TriFluoroDiChloroXylene (TFDCX) Formation C8H5Cl5 + 3HF C8H5Cl2F3 + 3HCl 278.5 60 229.0 109.5 o-pentachloroxylene Chlorine o-trifluorodichloroxylene Hydrogen Chloride Step 3 TriFluoromethylbenzaldehyde (TFMB) Formation C8H5Cl2F3 + 2H2O C8H5F3O + 2HCl + H2O 229.0 36 174.0 73.0 18 o-trifluorodichloroxylene Water TriFluoromethylbenzaldehyde Hydrogen Chloride Water Step 4 TriFluoromethylbenzoylChloride (TFMBC) Formation C8H5F3O + Cl2 C8H4F3OCl + HCl 174.0 71 208.5 36.5 TriFluoromethylbenzaldehyde Water 2- Trifluoromethyl benzoylchloride Hydrogen Chloride 99

Material Balance: Input Output Key RM Product O-Xylene MT 0.734 2- Trifluoromethyl Benzoyl Chloride MT 1.000 Reagent Inorganic Acid Chlorine MT 4.960 Sulphuric Acid (75%) MT 14.708 AIBN MT 0.036 Hydrochloric Acid 30% MT 15.583 Anhydrous hydrofluoric MT 0.705 Sodium Hypo Chlorite MT 15.656 acid NaOH (48%) MT 5.331 H2SO4 (98%) MT 11.257 Wastewater Ethylene (C2) MT 0.716 Effluent MT 1.934 Water Process Gaseous Emission Process Water MT 25.372 Nitrogen, HCl and Cl2 stack emission MT 0.181 Gas Process Residue and Waste Nitrogen MT 0.181 Organic Heavies MT 0.229 Total Input MT 49.291 Total Output MT 49.291 100

18. TrifluoroMethyl-2-EthoxyVinyl Ketone Process Description: TFAF, EVE and TEA are charged into the reactor. Reaction mass will be washed with water and taken for next step after washing can be boiled off. Chemical Reaction: 3CF3COF + 3CH2CHOCH2CH3 + (C2H5)3N 3CF3COCHCHOCH2CH3 + (C2H5)3N.3HF 116 72.1 101.2 168.1 161.2 Material Balance: Input Output Key RM Product Trifluoro Acetyl Fluoride MT 1.429 TrifluoroMethyl-2- EthoxyVinyl Ketone (TEK) MT 1.000 Reagent Wastewater Ethyl Vinyl Ether MT 0.857 Effluent MT 3.142 Tri Ethyl Amine MT 0.429 Process Gaseous Emission Water Nitrogen MT 0.200 Process Water MT 2.457 Process Residue and Waste Gas Organic Heavies MT 1.029 Nitrogen MT 0.200 Total Input MT 5.371 Total Output MT 5.371 101

19. 2-(2-Methoxy-ethoxymethyl)-6-trifluoromethyl-nicotinic acid ethyl ester Process Description: Charge Methoxy AA and Toluene into the reactor and purge Ammonia. Water removed from the reaction mixture and crude taken for next step. Step 1 and Step 2 material will charge into the reactor in presence of acetic acid. A low boiler was removed and crude will be further purified at reduced pressures. Chemical Reaction: CH3OC2H4OCH2COCH2COOC2H5 204.2 + NH3 CH3OC2H4OCH2CNH2CHCOOC2H5 + H2O 17 203.2 18 CH3OC2H4OCH2CNH2CHCOOC2H5 203.2 + CF3COCHCHOCH2CH3 MEFNA Ester + CH3CH2OH + H2O 168.1 307 46 18 Material Balance: Input Output Key RM Product Methoxy AA MT 0.840 2-(2-Methoxy-ethoxymethyl)- 6-trifluoromethyl-nicotinic acid ethyl ester MT 1.000 Reagent Wastewater NH3 Solution 25% MT 0.079 Effluent MT 2.087 Toluene MT 0.100 Trifluoromethyl-2- MT 0.714 Process Gaseous Emission ethoxyvinyl Ketone Acetic Acid MT 0.024 Nitrogen MT 0.100 Water Process Residue and Waste Process Water MT 2.000 Organic Heavies MT 0.671 Gas Nitrogen MT 0.100 Total Input MT 3.858 Total Output MT 3.858 102

20. Mefenamic Acid Process Description: Charge Methoxy AA and Toluene into the reactor and purge Ammonia. Water removed from the reaction mixture and crude taken for next step. Step 1 and Step 2 material will charge into the reactor in presence of acetic acid. A low boiler was removed and crude will be further purified at reduced pressures. MEFNA Ester will react with NaOH and HCl followed by layer separation in presence of solvent. Organic layer was 60% MEFNA solution which will be. Chemical Reaction: CH3OC2H4OCH2COCH2COOC2H5 + NH3 CH3OC2H4OCH2CNH2CHCOOC2H5 + H2O 204.2 17 203.2 18 CH3OC2H4OCH2CNH2CHCOOC2H5 + 3COCHCHOCH2C MEFNA Ester + CH3CH2OH + H2O 203.2 168.1 307 46 18 MEFNA Ester + NaOH + HCl MEFNA + EtOH + NaCl 307.3 40 36.5 279.2 46 58.6 Material Balance: Input Output Key RM Product Methoxy AA MT 0.700 Mefenamic Acid MT 1.000 Reagent Wastewater NH3 Solution 25% MT 0.066 Effluent MT 1.180 Toluene MT 0.107 Trifluoromethyl-2-ethoxyvinyl MT 0.595 Process Gaseous Emission Ketone Acetic Acid MT 0.020 Nitrogen MT 0.213 Caustic Lye 30% MT 0.383 Dilute Hydrochloric Acid 10 - MT 0.350 Process Residue and Waste 30% Xylene MT 0.158 Organic Heavies MT 0.590 Water Process Water MT 0.391 Gas Nitrogen MT 0.213 Total Input MT 2.983 Total Output MT 2.983 103

21. Hexafluoropropylene oxide Process Description: Sodium Hypochlorite solution will prepare by reacting Chlorine with NaOH. Sodium Hypochlorite will react with Hexafluoro Propylene for the formation of Hexafluoro Propylene oxide. Mixture of HFP/HFPO was taken for Extractive Distillation to get pure HFPO. Organic layer was taken for Toluene recovery and aqueous layer will be Effluent treatment. Chemical Reaction: 2NaOH + Cl2 NaOCl + NaCl + H2O 40 70.8 74.4 58.4 18 C3F6 + NaOCl C3F6O + NaCl 150 74.4 166 58.4 Material Balance: Input Output Key RM Product 12.5% NaOH Solution MT 6.598 Hexafluoropropylene oxide MT 1.000 Reagent Wastewater Chlorine MT 0.667 Effluent MT 18.362 HFP MT 1.500 Toluene MT 0.500 Process Gaseous Emission Na2CO3 MT 0.211 Nitrogen MT 0.100 PTC MT 0.011 35% HCl Solution MT 0.287 Process Residue and Waste 30% H2O2 Solution MT 0.003 Organic Heavies MT 0.101 20% H2SiF6 Solution MT 8.878 Inorganic Salt Water Solid Cake MT 2.218 Process Water MT 3.028 Gas Nitrogen MT 0.100 Total Input MT 21.781 Total Output MT 21.781 104

22. Pentaflurophenol Process Description: Magnesium will charge with BPFB and diethyl ether. To the reaction mixture BF3.Et2O, Hydrogen Peroxide and water will be added. Reaction was then taken for purification to obtain pure Pentaflurophenol. Chemical Reaction: BPFB + Mg Pentafluorophenyl Magnesium Bromide 246.1 24 270.2 3 Pentafluorophenyl Magnesium B + BF3.Et2O + 3*H2O2 3*Pentafluorophenol + 3MgBrF + H3BO3 + Et2O 270.2 142 34.1 184 123 61 74 Material Balance: Input Output Key RM Product Bromopentafluorobenzene MT 1.714 Pentaflurophenol MT 1.000 Reagent Wastewater Magnesium MT 0.168 Effluent MT 12.205 Boron trifluoride ethereate MT 0.343 H2O2 MT 0.239 Process Gaseous Emission NaOH MT 0.286 Nitrogen MT 0.100 HCl MT 0.405 Process Residue and Waste Solvent Organic Heavies MT 0.037 Diethylether MT 0.318 Toluene MT 0.271 Spent Organic Solvent Diethylether & Toluene MT 0.589 Water Bromopentafluorobenzene MT 0.034 traces Process Water MT 10.121 Gas Nitrogen MT 0.100 Total Input MT 13.966 Total Output MT 13.966 105

23. Monomethylhydrazine Process Description: Hydrazine Hydrate charged into the mix of Methanol and HCl. Reaction mixture will filtrate to recover Hydrazine Dihydrochloride. NaOH added to the filtrate for the formation of MMH and NaCl. Material will be filtered and filtrate was taken for final distillation to get 35-40% MMH solution in water. Chemical Reaction: NH2.NH2.H2O + HCl + CH3OH CH3.NH2.NH.HCl + 2H2O 50 36.5 32 82.5 18 CH3.NH2.NH.HCl + NaOH H2O + CH3.NH.NH2 + NaCl 82.5 40 18 46 58.5 Material Balance: Input Key RM Hydrazine Hydrate 100% Output Product MT 0.817 Monomethylhydrazine (MMH) MT 1.000 Reagent By- HCl MT 0.958 Hydrazine Hydrate.2HCl MT 0.677 NaOH MT 0.618 Sodium Salt Solvent NaCl Salt MT 0.723 Methanol MT 1.895 Spent Organic Solvent Water Methanol MT 1.643 Process Water MT 1.000 Wastewater Gas Effluent MT 1.000 Nitrogen MT 0.200 Process Gaseous Emission Nitrogen MT 0.200 Process Residue and Waste Organic Heavies MT 0.246 Total Input MT 5.489 Total Output MT 5.489 106

24. [3-(4,5-dihydro-1,2-oxazol-3-yl)-4-mesyl-o-tolyl](5-hydroxy-1-methylpyrazol-4-yl)methanone (Topramezone) Process Description: Step 1: 3-Nitro-o-xylol reacts with potassium methoxide and butyl nitrite in presence of DMF and catalytic quantity of butanol to form salt of OXIM. This salt will be hydrolysed with concentrated HCl to form EXP-Oxim and potassium chloride. Precipitated was filtered and washed. EXP-Oxim thus obtain will take to Step-2 without drying. Step 2: Step-1 Product (EXP-Oxim) was dried using azeotropic distillation and chlorinated with vapor chlorine in presence of Butyl Acetate as solvent. The chlorinated EXP-HSCl in butyl acetate was cyclized using ethylene in a pressurized reactor. Cyclization takes place in presence of K2CO3, water, butyl acetate and ethylene in a pressurized reactor. After the reaction was acidified using HCl (15-33%) and crystallized by removing butyl acetate and cooling. Step 3: Step-2 was hydrogenated by reacting with Hydrogen in presence of Pd/C catalyst under pressure at a temperature of 30 ⁰C. Activated Carbon will add to the reaction mixture as filtration media. Methanol was used as solvent for the reaction. Step 4: Step-3 was brominated using HBr(48%) and H2O2 (50%). Potassium sulfite will be used to kill any residual peroxide and the mixture was washed with caustic solution to remove any impurities. Pyridine was used as solvent for the reaction. Step 5: Step-4 will take for thiomethylation where it will react with DMDS and n-butyl Nitrite in presence of Cu (catalyst). Subsequently the reaction mass was washed with HCl and NaOH to remove Cu from the reaction mixture. DMDS was also used as solvent in this reaction. Step 6: The resulting from step-5 was oxidized using H2O2 (50%) in the presence of Sodium Tungstate as catalyst and Acetic acid as solvent. It will be crystallized by cooling and filtered. Step 7: Step-6 reacts with MHP, K2CO3 and Carbon monoxide in presence of TPP & PdCl2 as catalyst and 1, 4-dioxane as solvent and activated carbon as filtration media for catalyst removal. After azeotropioc removal of 1, 4-dioxane with water, the salt was hydrolyzed using HCl and purified using methanol. The will be subsequently filtered and dried before packaging. 107

Chemical Reaction: Step 1 OXIMATION C8H9NO2 + C4H9NO2 + KOCH3 + HCl DMF C8H8N2O3 + C4H9OH + CH3OH + KCl 151 103 70 37 180 74 32 75 Potassium Potassium 3-Nitro-o-xylol n-butyl Nitrite Hydrogen chlroide Oxim Butanol Methanol Methoxide Chloride Step 2 CHLORINATION / CYCLISATION C8H8N2O3 + Cl2 + C2H4 + K2CO3 BuOAc C10H10N2O3 + H2O + CO2 + 2KCl 180 71 28 138 206 18 44 149 Potassium Potassium Oxim Chlorine Ethylene Isoxazolin Water Carbondioxide Carbonate Chloride Step 3 HYDROGENATION C10H10N2O3 + 3H2 Methanol Pd/C C10H12N2O + 2H2O 206 6 176 36 Isoxazolin Hydrogen Anilin Water Step 4 BROMINATION Pyridine C10H12N2O + HBr + H2O2 C10H11BrN2O + 2H2O 176 81 34 255 36 Anilin Hydrogen Bromide Peroxide Bromanilin Water Step 5 THIOMETHYLATION C10H11BrN2O 255 Bromanilin + C2H6S2 + C4H9NO2 C11H12BrNOS + C5H12SO + N2 + H2O 94 103 286 120 28 18 DMDS n-butyl Nitrite Bromid ByProduct Step 6 OXIDATION C11H12BrNOS + 2H2O2 Acetic Acid Na2WO4.2H2O C11H12BrNO3S + 2H2O 286 68 318 36 Bromid Hydrogen Peroxide Sulfon Water Step 7 CARBONYLATION C11H12BrNO3S + C4H6N2O + CO + K2CO3 PdCl2 TPP, Act. C C16H17N3O5S + KHCO3 + KBr 318 98 28 138 363 100 119 Sulfon MHP Carbon Monoxide Potassium Potassium Potassium SC-05 Carbonate bicarbonate Bromide 108

Material Balance: Input Output Key RM Product 3-Nitro-o-xylol MT 1.503 [3-(4,5-dihydro-1,2-oxazol-3-yl)- 4-mesyl-o-tolyl](5-hydroxy-1- methylpyrazol-4-yl)methanone (SC-05) MT 1.000 Reagent Spent Catalyst 1,4-Dioxane (C4H8O2) MT 0.942 Spent Catalyst-1 MT 0.028 Acetic Acid MT 0.410 Spent Catalyst-2 MT 0.038 Activated Carbon MT 0.070 Butyl Acetate MT 8.027 Wastewater Butyl Nitrite MT 1.860 Effluent MT 39.010 Carbon monoxide MT 0.308 Caustic Lye (48%) MT 0.478 Process Gaseous Emission Chlorine MT 0.621 Nitrogen MT 1.000 Copper MT 0.004 HCl traces Stack Emission MT 1.466 Dimethyl disulfide (C2H6S2) MT 0.882 Ethylene MT 0.916 Process Residue and Waste Hydrochloric acid (15-33%) MT 6.162 Organic Heavies MT 1.500 Hydrochloric acid Anhydride MT 1.841 Hydrogen MT 0.038 Hydrogen bromide MT 1.042 Hydrogen peroxide MT 1.320 MHP (C4H6N2O) MT 0.360 Potassium carbonate (K2CO3) MT 2.425 Potassium methoxide MT 1.135 Potassium sulfite MT 0.057 Pyridine MT 0.741 TPP MT 0.039 Catalyst Sodium Tungstate Dihydrate MT 0.004 (Na2WO4.2H2O) Palladium chloride (PdCl2) MT 0.001 Palladium on carbon MT 0.002 Solvent Methanol MT 2.830 Dimethylformamide MT 4.778 109

Input Output Water Process Water MT 4.246 Gas Nitrogen MT 1.000 Total Input MT 44.042 Total Output MT 44.042 110

25. Tri Fluoro acetone Process Description: Ethyltrifluoroacetoacetate, in presence of Sulfuric acid reacts with water at a temperature of 90 ⁰C to form TFAc, Ethanol and carbon dioxide. This was subsequently separated. Chemical Reaction: C6H7F3O3 + H2O H2SO4 C3H3F3O + C2H6O + CO2 184 18 112 46 44 P8 Water TFAc Ethanol Carbondioxide Material Balance: Input Output Key RM Product Ethyltrifluoroacetoacetate MT 1.786 Tri Fluoro acetone (TFAc) MT 1.000 Reagent Inorganic Acid H2SO4 MT 0.360 Sulphuric Acid (75%) MT 0.371 Water Spent Organic Solvent Process Water MT 1.500 Ethanol MT 0.469 Gas Wastewater Nitrogen MT 0.448 Effluent MT 1.806 Process Gaseous Emission Nitrogen MT 0.448 Total Input MT 4.094 Total Output MT 4.094 111

26. Methyl tri fluoro acetate Process Description: In the process of Methyl trifluoroacetate, TFAF react with Methanol and to get Methyl trifluoroacetate. Reaction maintains few hrs after distillation done and final collect in vessel and Hydrofluoric Acid 30-40 % solution sold as. Chemical Reaction: C2F4O + CH3OH HF + 116.01 32.04 20.01 128.05 Material Balance: Input Output Key RM Product TFAF MT 0.906 Methyl tri fluoro acetate MT 1.000 (MTFA) Hydrofluoric Acid 30-40 % MT 0.521 Reagent Methanol MT 0.250 Wastewater Effluent MT 0.010 Water Process Water MT 0.375 Process Gaseous Emission Nitrogen & HF traces MT 0.050 Gas Nitrogen MT 0.050 Total Input MT 1.581 Total Output MT 1.581 112

27. Chlorodifluoroacetic anhydride Process Description: In the process of CDFAA, CDFAF reacts with water which converts to HF & CDFA, CDFA was purified through distillation. Pure CDFA reacts with Oleum at specified temperature over a period of time which produces crude CDFAA & pure CDFAA will recover through distillation. Sulphuric was generated, which will saleable. Chemical Reaction: CF2ClCOF + H2O ClCF2COOH + HF 132.5 18.0 130.5 20.0 CDFAF Water CDFA ClCF2COOH + H2SO4.SO3 (ClCF2CO)2O + H2SO4 130.5 178.0 242.5 98.0 CDFA Oleum(Fuming) CDFAA Sulphuric acid Material Balance: Input Output Key RM Product Chlorodifluoroacetic acid(cdfa) MT 2.130 Chlorodifluoroacetic acid MT 1.000 anhydride (CDFAA) Hydrofluoric Acid 30-40 % MT 0.511 Reagent Oleum MT 4.430 Inorganic Acid Sulphuric Acid (90-95%) MT 5.564 Water Process Water MT 0.525 Wastewater Effluent MT 0.011 Gas Nitrogen MT 0.020 Process Gaseous Emission Nitrogen & HF traces MT 0.020 Total Input MT 7.105 Total Output MT 7.105 113

28. Bromopentafluorobenzene Process Description: Pentafluorobenzene was brominated in the Glass Reactor to form crude BPFB; it will be distillate to produced pure BPFB (Bromopentafluorobenzene). Chemical Reaction: C6F5H + Br2 C6F5Br + HBr 168.0 160.0 247.0 81.0 PFB Material Balance: Input Output Key RM Product Pentafluorobenzene MT 0.852 Bromopentafluorobenzene (BPFB) MT 1.000 Reagent Inorganic Acid Bromine MT 0.902 HBr (48-50%) MT 1.100 Aluminium Chloride MT 0.072 Sodium thiosulphate MT 0.003 Process Residue and Waste Heavies MT 0.080 Water Process Water MT 1.331 Wastewater Effluent MT 0.979 Gas Nitrogen MT 0.030 Process Gaseous Emission Nitrogen & Bromine traces MT 0.030 Total Input MT 3.190 Total Output MT 3.189 114

29. 4-Chlorobenzotrichloride Process Description: P-Chloro toluene was photo chlorinated to form 4-ClBTC. Chemical Reaction: C6H4 -Cl-CH3 126.5 P-chloro toluene + 3 Cl2 213 Chlorine C6H4-Cl-CCl3 230 1-chloro-4-(trichloromethyl) + 3 HCl 109.5 Hydrochloric acid benzene ( 4-ClBTC) Material Balance: Input Output Key RM Product P-Chloro toluene MT 0.650 4-Chlorobenzotrichloride (PCBTC) MT 1.000 Reagent Inorganic Acid Chlorine MT 1.540 Hydrochloric Acid 10-30% MT 1.580 Caustic Lye 48% MT 1.450 Sodium Hypochlorite MT 2.120 Water Process Residue and Waste Process Water MT 1.660 Heavies MT 0.100 Gas Wastewater Nitrogen MT 0.200 Effluent MT 0.500 Process Gaseous Emission Nitrogen, HCl & Cl2 traces MT 0.200 Total Input MT 5.500 Total Output MT 5.500 115

30. 4-Chlorobenzotrifluoride Process Description: P-Chloro toluene was photo chlorinated to form 4-ClBTC. 4-ClBTC will react with AHF to form 4-ClBTF. Chemical Reaction: C6H4 -Cl-CH3 + 3 Cl2 C6H4-Cl-CCl3 + 3 HCl 126.5 213 230 109.5 P-chloro toluene Chlorine 1-chloro-4-(trichloromethyl) Hydrochloric acid benzene ( 4-ClBTC) C6H4-Cl-CCl3 + 3 HF C6H4-Cl-CF3 + 3 HCl 230 60 180.5 109.5 4-ClBTC Hydrogen floride 1-chloro-4-(trifluoromethyl) Hydrochloric acid benzene (4-ClBTF) Material Balance: Input Output Key RM Product P-Chloro toluene MT 0.800 4-Chlorobenzotrifluoride MT 1.000 (PCBTF) Hydrofluoric Acid 15-60% MT 0.500 Reagent Chlorine MT 1.730 Inorganic Acid Hydrofluoric Acid (HF) MT 0.560 Hydrochloric Acid 10-30% MT 4.050 Caustic Lye 48% MT 1.840 Sodium Hypochlorite MT 2.630 Water Process Residue and Waste Process Water MT 3.850 Heavies MT 0.100 Gas Wastewater Nitrogen MT 0.100 Effluent MT 0.500 Process Gaseous Emission Nitrogen, Cl2, HCl and HF traces MT 0.100 Total Input MT 8.880 Total Output MT 8.880 116

31. Methyl Hydroxy Pyrazole Process Description: Diethyl ethoxymethylenemalonate (DEMM) reacts with diethyl amine to form monoamide. This reacts with monomethyl hydrazine and extracted with water/ethanol to form intermediate. This intermediate again reacts with HCL and washed with water to form MHP. Chemical Reaction: 117

Material Balance: Input Key RM Diethyl ethoxymethylenemalonate (DEMM) Output Product MT 2.770 Methyl Hydroxy Pyrazole (MHP) MT 1.000 Reagent Inorganic Salt Diethyl amine (DEA) MT 0.117 Solid Waste MT 1.000 Monomethyl Hydrazine (MMH) MT 1.890 (35%) Solution HCl (35%) Solution MT 4.200 Process Residue and Waste Dioxane MT 0.996 Heavies MT 0.750 Aqueous Ammonia Solution MT 1.360 (15%) Wastewater Solvent Effluent MT 18.183 Methanol MT 1.360 Process Gaseous Emission Water Nitrogen MT 0.500 Process Water MT 8.840 HCl traces MT 0.600 Gas Nitrogen MT 0.500 Total Input MT 22.033 Total Output MT 22.033 118

32. 6-Fluoro methyl indole Process Description: Difluorobenzene reacts with nitric acid to 2,5-difluoronitrobenzene-->Step-1 2,5-difluoronitrobenzene reacts with methyl acetoacetate, potassium carbonate to give 2-(4-fluoro-2-nitro-phenyl)-3-hydroxy-2- butenoic acid methyl ester-->step-2 The crude Step-2 reacts with acetic acid and 50% Sulphuric acid to get 4-fluoro-2-nitrophenyl-acetone-->Step-3 FNPA was reduced with iron and acetic acid in presence of sodium acetate and acetic acid to give FMI-->Step-4. Chemical Reaction: C6H4F2 + HNO3 + H2SO4 C6H3FNO2 + H2O + H2SO4 DFB Nitric Acid Sulphuric Acid DFNB Water Sulphuric Acid 114.09 63.01 98.07 159.09 18.01 98.07 2 C6H3FNO2 + 2 C5H8O3 + K2CO3 2 C11H10FNO5 + 2 KF + CO2 H2SO4 DFNB Methyl Acetoacetate Potassium Carbonate FNPH-BAME Potassium Fluoride Carbon Dioxide Sulphuric Acid 159.09 116.11 137.9 255.05 58.09 44.01 98.07 C11H10FNO5 + H2O C9H8FNO3 + CH4O + CO2 FNPH-BAME Water FNPA Methanol Carbon Dioxide 255.05 18.01 197.01 32.04 44.01 C9H8FNO3 + 3 Fe C9H8FN + 3 FeO FNPA Iron FMI Iron Oxide 197.01 55.85 149.09 5.74 119

Material Balance: Input Output Key RM Product Difluorobenzene MT 1.300 6-Fluoro methyl indole (FMI) MT 1.000 Reagent Spent Organic Solvent Acetic Anhydrite MT 2.318 Ethyl acetate, Methylene MT 15.200 Chloride, Hexane & Toluene Caustic lye MT 9.836 Dimethyl Sulfoxide (C2H6OS) MT 2.031 Inorganic Salt Ethyl Acetate MT 4.000 Solid Waste MT 10.874 HCl 30% MT 2.337 Iron Powder MT 2.646 Process Residue and Waste Methyl Acetoacetate MT 1.968 Organic Residue MT 2.000 Methylene chloride MT 4.000 NaCl MT 0.922 Wastewater Nitric Acid MT 0.919 Effluent MT 90.369 Potassium Carbonate MT 5.143 Sodium Acetate MT 0.729 Process Gaseous Emission Sodium bicarbonate MT 2.633 Nitrogen MT 1.000 Sulphuric acid (98%) MT 5.924 HCl traces MT 1.330 Solvent Acetic Acid MT 8.389 Heptane MT 2.730 Hexane MT 4.000 Toluene MT 4.000 Water Process Water MT 54.948 Gas Nitrogen MT 1.000 Total Input MT 121.773 Total Output MT 121.773 120

33. Difluoroethoxy ethanol Process Description: EDFA reactions with LiAlH4 in Diethylether to form intermediate complex--> Step-1 Ethanol reacts with excess LiAlH4 to form lithium & Aluminium salts of ethanol Intermediate complex formed in Step-1 will react with H2SO4 to form EDFE --> Step-2 NaHCO3 reacts with H2SO4 to neutralize the reaction mass and organic layer was separated. Product was boiled off from organic layer. Chemical Reaction: Step-1 Diethylether 4 C4H6F2O2 + 4 C2H5OH + 2 LiAlH4 [C4H7F2O2]L + C4H7F2O2]3A + [C2H5O]Li + [C2H5O]3Al + 4H2 124.1 46.06 37.95 131.99 402.13 51.99 162.13 2.01 EDFA Ethanol Lithium Aluminium Hydride Lithium Salt of EDFE Aluminium Salt of EDFE Lithium Salt of EDFE Aluminium Salt of EDFE Hydrogen Step-2 [C4H7F2O2]Li + [C4H7F2O2]3Al + 2 H2SO4 4 C4H8F2O2+ 0.5 Li2SO4 + 5 Al2(SO4)3 131.99 402.13 98 126.1 109.88 341.96 Lithium Salt of EDFE Aluminium Salt of EDFE Sulfuric Acid EDFE Lithium Sulfate Aluminium Sulfate H2SO4 + 2 NaHCO3 Na2SO4 + 2 CO2 + + 2 H2O 98 Sulphuric Acid 84 142.04 44 18 Sodium Bicarbonate Sodium Sulphate Carbon Dioxide Water 121

Material Balance: Input Output Key RM Product EDFA MT 0.990 Difluoroethoxy ethanol (EDFE) MT 1.000 Reagent Process Residue and Waste Diethyl Ether MT 1.180 Organic Residue MT 0.050 Lithium Aluminium hydride MT 0.100 Ethanol MT 0.020 Wastewater H2SO4 Solution 98% MT 1.710 Effluent MT 10.464 NaHCO3 MT 0.270 Process Gaseous Emission Water Nitrogen& H2 MT 0.506 Process Water MT 7.530 CO2 Stream MT 0.280 Gas Nitrogen MT 0.500 Total Input MT 12.300 Total Output MT 12.300 122

34. 5-Bromo-2-2-difluoro-1-3-benzodioxole Process Description: Reaction of 1, 3-benzodioxole with Phosphorus pentachloride to give 2, 2-Dichloro-1, 3-benzodioxole 2, 2-Dichloro-1,3benzodioxole was fluorinated with HF to give 2, 2-Difluoro-1, 3-benzodioxole. 2, 2- Difluoro-1, 3-benzodioxole was Brominated with HBr to give 5-Bromo-2, 2-Difluoro-1, 3-benzodioxole. Chemical Reaction: Step-1 C6H4 -O2-CH2 + 2 PCl5 C6H4-O2-CCl2 + 2 PCl3 + 2 HCl 122 208.24 191 137.33 36.5 1,3-benzodioxole Phosphorus pentachloride 2,2-Dichloro-1,3-benzodioxole Phosphorus trichloride Hydrochloric acid Step-2 C6H4-O2-CCl2 + 2HF C6H4-O2-CF2 + 2 HCl DCM 191 20 158 36.5 2,2-Dichloro-1,3-benzodioxole Hydrogen Fluoride 2,2-Difluoro-1,3-benzodioxole Hydrochloric acid C6H4-O2-CF2 + 2 HBr + H2O2 C6H3-Br-O2-CF2 + HBr + 2H2O Step-3 158 2,2-Difluoro-1,3-benzodioxole 80.91 34 237 80.91 18 Hydrogen Bromide Hydrogen peroxide 5-Bromo-2,2-Difluoro-1,3-benzodioxole Hydrogen Bromide Water (DFBD) 123

Material Balance: Input Output Key RM Product 1-3 Benzodioxole MT 0.803 5-Bromo-2-2-difluoro-1-3- MT 1.000 benzodioxole (Br-DFBD) Hydrofluoric Acid 15-60% MT 0.950 Reagent Phosphorus pentachloride MT 2.509 Inorganic Acid Hydrofluoric Acid (HF) MT 0.625 HBr Solution 30% MT 4.557 Hydrochloric Acid 10-30% MT 3.122 HBr MT 2.048 H2O2 50% MT 0.765 By- Methylene Chloride MT 0.510 Phosphorus trichloride MT 1.807 Water Process Residue and Waste Process Water MT 6.244 Organic Residue MT 0.828 Gas Wastewater Nitrogen MT 0.200 Effluent MT 1.240 Process Gaseous Emission Nitrogen, Bromine, HCl and HF traces MT 0.200 Total Input MT 13.704 Total Output MT 13.704 124

35. Difluorobenzodioxole methyl ester Process Description: 1, 3 benzodioxole reacts with phosphorus pentachloride to form DCBD- Me and phosphorus trichloride.in next step DCBD Me reacts with hydrogen fluoride to form 2, 2 difluoro 1, 2 benzodioxole and HCL. 2, 2 Difluoro benzodioxole reacts with bromine to form 5-Bromo-2, 2-Difluoro-1, 3- Benzodioxole and HBr. This intermediate of step 3 reacts with n-buli to form 2, 2-Difluoro-1, 3- Benzodioxole carboxylic acid, lithium bromide and butane this reacts with methanol and after layer separation and final distillation DFBD-Me is recovered. Chemical Reaction: Step-1 C7H6O2 + PCl5 C7H4O2Cl2 + PCl3 122 208.24 191 137.33 1,3 Benzodioxole Phosphorous Pentachloride 2,2-Dichloro-1,2-benzodioxole Phosphorous Trichloride Step-2 C7H4O2Cl2 + 2 HF C7H4O2F2 + 2HCl 191 20 158 36.5 2,2-Dichloro-1,2-benzodioxole Anhydrous HF 2,2-Difluro-1,2-benzodioxole Hydrogen Chloride Step-3 C7H4O2F2 + Br2 C7H4O2F2Br + HBr Fe 158 160 237 81 2,2-Difluro-1,2-benzodioxole Bromine 5-Bromo-2,2-Difluoro-1,3-Benzodioxole Hydrogen Bromide Step-4 C7H4O2F2Br CO2 + n-buli C8H4O4F2 + C4H10 + LiBr 237 64 202 58 87 5-Bromo-2,2-Difluoro-1,3-Benzodioxole Bromine 2,2-Difluoro-1,3-Benzodioxole carboxylic acibutane Lithuim Bromide Step-5 C8H4O4F2 H2SO4 + CH3OH C9H6O4F2 + H20 202 32 216 18 2,2-Difluoro-1,3-Benzodioxole carboxylic acid 2,2-Difluoro-1,3-Benzodioxole carboxylic acid Methanol methyl ester Water 125

Material Balance: Input Output Key RM Product 1,3 Benzodioxole MT 1.008 Difluorobenzodioxole methyl ester (DFBD-Me) MT 1.000 Reagent Inorganic Acid 48%NaOH MT 1.260 Hydrochloric acid (15-33%) MT 4.980 Bromine MT 1.320 HBr Sol. MT 2.200 Hydrochloric acid (15- MT 0.240 33%) Hydrofluoric acid MT 0.410 By- Anhydride Iron MT 0.230 PCl3 recovered MT 1.500 Methylene chloride MT 0.490 n-butyllithium MT 0.530 Wastewater Phosphorus pentachloride MT 4.300 Effluent MT 10.448 Sodium Chloride MT 0.970 Spent Caustic MT 1.790 Sulphuric acid (98%) MT 0.080 Process Residue and Waste Solvent Mixed Organic MT 5.500 Chloroform MT 1.480 Methanol MT 0.790 Process Gaseous Emission THF MT 7.430 Nitrogen, Bromine and HCl traces MT 0.500 Water Process Water MT 6.880 Gas Nitrogen MT 0.500 Total Input MT 27.918 Total Output MT 27.918 126

36. 2-Fluoro-5-nitrobenzoic acid Process Description: In step-1 Anthranilic acid reacted with sodium nitrate and hydrogen fluoride to make 2-fluorobenzoic acid. Now the formed 2-fluorobenzoic acid reacted with concentrated HNO3 along with conc. Sulfuric acid to make 2-fluoro-5-nitrobenzoic acid. After that this will be separated and purified through various work up. Chemical Reaction: Step-1 + NaNO2 + 2 HF + NaF + 2 H2O + N2 Anthranilic acid Sodium nitrate hydrogen fluoride 2-Fluorobenzoic acid Sodium Fluoride Water Nitrogen 137 69 20 140 42 18 28 Step-2 + Conc. HNO3 + H2O Conc. H2SO4 2-Fluorobenzoic acid Conc. Nitric acid conc. Sulfuric acid 2-Fluoro-5-nitrobenzoic acid water 140 63 98 185 18 127

Material Balance: Input Output Key RM Product Anthranilic acid MT 0.968 2-Fluoro-5-nitrobenzoic acid (FNBA) MT 1.000 Reagent Inorganic salts Sodium nitrite (NaNO2) MT 0.541 Inorganic salts MT 0.255 AHF MT 0.367 Monoglyme MT 0.685 Wastewater Methylene dichloride MT 0.600 Effluent MT 18.582 Conc. Nitric acid MT 1.416 Conc. Sulfuric acid MT 1.786 Process Gaseous Emission Nitrogen MT 0.200 Water Process Water MT 13.475 Gas Nitrogen MT 0.200 Total Input MT 20.037 Total Output MT 20.037 128

37. 5-Chloro-3-(difluoromethyl)-1-methyl-1H-pyrazole-4-carboxaldehyde Process Description: Synthesis of step-1 will be done by the reaction of EDFAA with MMH solution and formic acid in presence of MTBE as a solvent at temperature 0-5 C. Synthesis of step-2 will be done by the reaction of step-1 with POCL3 and dimethylformamide in presence of chlorobenzene as a solvent at temperature 100-103 C. Chemical Reaction: Step-1 166 148 C6H8F2O3 + CH2O2 + CH3NHNH2 C5H6N2F2 + C2H5OH + H20 + CH2O2 166 46 46 148 46 18 46 EDFAA Formic Acid MMH BCS-9801 Ethanol water Formic acid Step-2 BCS-9801 + POCL3 + (CH3)2 N-CHO + 2H2O C6H5F2N2OC + 2HCl + H3PO4 + (CH3)2NH 148 153.3 73 36 194 73 98 45 BCS-9801 Phosphorus DMF water BCS-9802 Hydrochloric Phosphoric Acid Di-Methylamine Oxychloride Acid 129

Material Balance: Input Output Key RM Product Ethyldifluoroacetoacetate MT 1.400 5-Chloro-3- (difluoromethyl)-1-methyl- 1H-pyrazole-4- carboxaldehyde (BCS-9802) MT 1.000 Reagent Process Residue and Waste Difluorobenzene MT 0.796 Organic Waste MT 0.990 Formic acid (HCOOH) MT 0.396 Methyl tertiary-butyl ether MT 0.508 Wastewater Monomethylhydrazine MT 0.650 Effluent MT 22.936 Phosphorus oxychloride MT 2.140 (POCl3) Sodium bicarbonate (NaHCO3) MT 0.176 Process Gaseous Emission Nitrogen MT 0.200 Solvent Dimethylformamide MT 0.560 Toluene MT 0.778 Water Process Water MT 17.522 Gas Nitrogen MT 0.200 Total Input MT 25.126 Total Output MT 25.126 130

38. 3-Difluoromethyl-5-fluoro-1-methyl-1H-pyrazole-4-carboxaldehyde Process Description: Synthesis of step-1 will be done by the reaction of EDFAA with MMH solution and formic acid in presence of MTBE as a solvent at temperature 0-5 C. Synthesis of step-2 will be done by the reaction of step-1 with POCL3 and dimethylformamide in presence of chlorobenzene as a solvent at temperature 100-103 C. Synthesis of step-3 will be done by the reaction of step-2 with potassium fluoride in presence TBAHS as a phase transfer catalyst at temperature 150-155 C. Chemical Reaction: Step-1 C6H8F2O3 + CH2O2 + CH3NHNH2 C5H6N2F2 + C2H5OH + H20 + CH2O2 166 46 46 148 46 18 46 EDFAA Formic Acid MMH BCS-9801 Ethanol water Formic acid Step-2 BCS-9801 + POCL3 + (CH3)2 N-CHO + 2H2O C6H5F2N2OC + 2HCl + H3PO4 + (CH3)2NH 148 153.3 73 36 194 73 98 45 BCS-9801 Phosphorus Oxychloride DMF water BCS-9802 Hydrochloric Acid Phosphoric Acid Di-Methylamine Step-3 BCS-9802 TBAHS (catalyst) + KF C6H5F37N2O + KCl 339.5 194 58 178 74.5 9803 Step-2 Potassium fluoride BCS-9803 131

Material Balance: Input Output Key RM Product Ethyldifluoroacetoacetate MT 2.315 3-Difluoromethyl-5-fluoro-1- methyl-1h-pyrazole-4- carboxaldehyde MT 1.000 Reagent Potassium Salt Chlorobenzene MT 1.306 Potassium fluoride & MT 0.773 Potassium chloride Dimethylamine MT 1.353 Caustic lye/ Flakes MT 0.004 Process Residue and Waste Formic acid (HCOOH) MT 0.649 Organic Waste MT 1.514 Methyl tertiary-butyl ether MT 0.843 Monomethylhydrazine MT 1.600 Wastewater Phosphorus oxychloride MT 3.510 Effluent MT 51.225 (POCl3) Potassium fluoride MT 0.716 Sodium bicarbonate MT 2.900 Process Gaseous Emission (NaHCO3) Tetrabutyl ammonium hydrogensulphate MT 0.102 Nitrogen MT 0.500 Solvent Dimethylformamide MT 0.918 Isopropyl alcohol MT 0.287 Toluene MT 3.823 Water Process Water MT 34.185 Gas Nitrogen MT 0.500 Total Input MT 55.012 Total Output MT 55.012 132

39. 2,5-Dichloro-4-(1,1,2,3,3,3-hexafluoropropoxy)benzenamine Process Description: 2, 5 Dichloro phenol will react with HFP gas in presence of Acetonitrile to form DHB---- Step 1 reaction. Crude mass from step-1 undergo distillation to recover solvent and pure DHB was taken for step 2 reaction. In step-2 DHB undergo nitration using nitric acid, in presence of sulfuric acid, to form DHNB---- Step 2 reaction. DHNB crude undergoes workup followed by distillation to obtain pure DHNB, recovered solvents will be recycled and aqueous effluent will be sent for treatment. DHNB was hydrogenated using Hydrogen gas in presence of catalyst to form DHA. DHA crude will be distilled to obtained pure and recovered solvents will be recycled for subsequent batches. Chemical Reaction: Step-1 KOH/HCl/CH3CN C6H4Cl2O + C3F6 ------------------------> C9H4Cl2F6O 2,5, Dichloro Phenol HFP gas DHB 163 150 313 Step-2 H2SO4 C9H4Cl2F6O + HNO3 ------------------------> C9H3NO3Cl2F6 + H2O DHB 313 Nitric acid DHNB Water 63 358 18 Step-3 CH3OH C9H3NO3Cl2F6 + 3H2 ------------------------> C9H5NOCl2F6 + 2H2O DHNB 358 Hydrogen DHNB Water 6 328 18 133

Material Balance: Input Output Key RM Product Dichlorophenol MT 0.600 2,5-Dichloro-4-(1,1,2,3,3,3- hexafluoropropoxy)benzena mine (DHA) MT 1.000 Reagent Process Residue and Waste Acetonitrile MT 0.140 Organic Waste MT 0.770 Caustic Lye MT 0.039 Acetone MT 0.008 Wastewater Hexafluoropropylene MT 0.552 Effluent MT 6.357 Hydrochloric acid (15-33%) MT 0.061 Nitric Acid MT 0.080 Process Gaseous Emission Potassium hydroxide MT 0.088 Nitrogen MT 0.500 Silicate (Ca2SiO4) MT 0.004 Sodium chloride MT 0.023 Sulphuric acid (98%) MT 0.716 Solvent Methanol MT 0.334 Toluene MT 0.073 Solid RM Hyflow (Filter aid) MT 0.008 Palladium on carbon MT 0.205 Water Process Water MT 5.176 Gas Nitrogen MT 0.500 Hydrogen MT 0.020 Total Input MT 8.627 Total Output MT 8.627 134

40. 2,4,5-Trifluorophenyl acetic acid Process Description: Dichloroacetophenone will react with Chlorosulfonic acid to form 5-Acetyl-2, 4-dichlorobenzene-1- sulfonyl chloride-- Step-1 reaction. 5-Acetyl-2, 4-dichlorobenzene-1-sulfonyl chloride was fluorinated using KF in presence of Aceto nitrile solvent-- Step-2 reaction. 5-Acetyl-2, 4-dichlorobenzene-1-sulfonyl fluoride was fluorinated using KF to form 1-(2, 4, 5-trifluorophenyl) ethanone---step-3 reaction. Reaction mass from step-3 will be reacted with morpholine and sulfur to form 2, 4, 5 Tri fluorophenyl acetic acid-- Step-4 reaction. Chemical Reaction: Step-1 C8Cl2OH6 + ClSO3H ------------------------> C8Cl3O3SH5 + H2O 189 116.5 287.5 18 Step-2 Áceto Nitrile C8Cl3O3SH5 + KF ------------------------> C8Cl2FO3SH5 + KCl 287.5 58 271 74.5 Step-3 Sulfolane C8Cl2FO3SH5 + 3KF ------------------------> C8F3OH5 + KSO2F + 2 KCl 271 58 174 122 74.5 Step-4 C8F3OH5 + C4H9NO + S NaOH/HCl ------------------------> C8F3O2H5 + C4H9NS 174 87 32 190 103 135

Material Balance: Input Output Key RM Product Dichloroacetophenone MT 2.613 2,4,5-Trifluorophenyl acetic acid (TPAA) MT 1.000 Reagent Process Residue and Waste Caustic Lye (48%) MT 0.840 Organic Waste MT 6.340 Chlorosulfuric acid MT 6.440 Acetonitrile MT 0.800 Inorganic Salt Hydrochloric acid (15- MT 2.300 Salt MT 2.820 33%) Morpholine MT 1.830 Potassium fluoride MT 3.614 Wastewater p-toluenesulfonic acid MT 0.040 Effluent MT 10.517 Sulfolane MT 0.750 Sulfur MT 0.450 Process Gaseous Emission Nitrogen MT 0.100 Water Process Water MT 1.000 Gas Nitrogen MT 0.100 Total Input MT 20.777 Total Output MT 20.777 136

41. 3-Aminobenzotrifluoride Process Description: Benzotrichloride reacts with AHF to form benzotrifluoride which again reacts with sulphuric acid and nitric acid to form 3 nitro benzotrifluoride. 3 nitrobenzotrifluoride reacts with hydrogen in presence of Raney nickel and MeOH to form 3 amino benzo trifluoride. Chemical Reaction: Step-1 C7H5Cl3 + 3HF C7H5F3 3HCl Step-2 195.5 20 148 36.5 Benzotrichloride A.Hydrogen Fluoride Benzotrifluoride Hydrogen Chloride C7H5F3 + HNO3 + H2SO4 C7H5F3NO2 + H20 + H2SO4 148 63 98 191 18 98 Benzotrifluoride Conc. Nitric Acid Conc. Sulphuric Acid 3-Nitro Benzo Trifluoride Water Sulphuric Acid Step-3 C7H5F3NO2 + 3 H2 C7H5F3NH2 + 2 H20 Raney Ni/MeOH 191 2 203 18 3-Nitro Benzo trifluoride Hydrgen 3-Amino Benzo Trifluoride Water 137

Material Balance: Input Output Key RM Product Benzotrichloride MT 1.330 3-Aminobenzotrifluoride MT 1.000 (ABTF) Hydrofluoric acid (20-70%) MT 1.000 Reagent Hydrofluoric acid Anhydride MT 0.800 Inorganic Acid Hydrogen MT 0.130 Hydrochloric acid (15-33%) MT 3.510 Methanol MT 0.130 Nitric acid MT 0.560 Process Residue and Waste Raney nickel MT 0.020 Organic Waste MT 0.700 Sulphuric acid (98%) MT 1.960 Inorganic Salt Water Salt MT 0.100 Process Water MT 3.330 Wastewater Gas Effluent MT 1.950 Nitrogen MT 0.100 Process Gaseous Emission Nitrogen, HCl and HF traces MT 0.100 Total Input MT 8.360 Total Output MT 8.360 138

42. 2,4-Dichloro-3,5-dinitrobenzotrifluoride Process Description: Dichlorobenzotrichloride reacts with AHF to form 2, 4 Dichlorobenzotrifluoride. Distillation of step-2 mass for AHF cuts and 2, 4 Dichlorobenzotrifluoride cuts, AHF cuts will be recycled back in process. 2, 4 Dichlorobenzo trifluoride nitration with nitric acid and oleum for i.e 2, 4 Dichloro 3, 5 dinitrobenzotrifluoride. Filtration of mass with sodium bicarbonate wash & followed by drying of wet cake for moisture removal. Purification & filtration of mass with IPA wash to give pure (2, 4 Dichloro 3, 5 dinitrobenzotrifluoride) as cake. IPA recovery will be done to recycle part of the solvent back in the process. Chemical Reaction: Step-2 C7H3-Cl5 + 3 HF C7H3Cl2F3 + 3 HCl 264.5 20 20-40 kg/cm2 215 36.5 2,4 Dichlorobenzotrichloride 2,4 Dichlorobenzotrifluoride Step-3 80-90 C C7H3Cl2F3 + H2SO4 + 2 HNO3 C7HF3Cl2 (NO2)2 + 2 H2O + H2SO4 215 98 63 305 18 98 2,4 Dichlorobenzotrifluoride 2,4 Dichloro 3,5 dinitrobenzotrifluoride Material Balance: Input Output Key RM Product Dichlorobenzotrichloride MT 1.220 2,4-Dichloro-3,5- dinitrobenzotrifluoride (DCDNBTF) MT 1.000 Reagent Inorganic Acid Dichlorobenzotrifluoride MT 0.770 Sulphuric acid (70%- 95%) MT 8.800 Hydrofluoric acid MT 1.390 Anhydride Isopropyl alcohol MT 0.340 Process Residue and Waste Nitric acid MT 1.900 Organic Waste MT 2.730 Oleum MT 3.516 Sodium bicarbonate MT 0.390 Wastewater Effluent MT 0.526 Water Process Water MT 3.530 Process Gaseous Emission Nitrogen MT 0.300 Gas Nitrogen MT 0.300 Total Input MT 13.356 Total Output MT 13.356 139

43. 3-phenoxy benzaldehyde Process Description: Benzaldehyde reacts with chlorine and bromine to form Meta bromobenzaldehyde which reacts with mono ethylene glycol in second step to form metabromobenzaldehydeacetal. Metabromobenzaldehydeacetal reacts with phenol and potassium hydroxide to form metaphenoxy benzaldehyde which will be distilled out to find the pure. Chemical Reaction: Step-1 2> C6H5CHO + Cl2 + Br2 2 C6H4CHOBr + 2 HBr + 2 HCL 106 71 160 185 81 36.5 ` Benzaldehyde Bromine meta-bromobenzaldehyde Hydrogen Bromide Step-2 C6H4CHOBr + C2H6O2 C9H9BrO2 + H2O 185 62 229 18 meta-bromobenzaldehyde Mono ethylene glycol meta-bromobenzaldehydeacetal Water Step-3 C9H9BrO2 + C6H5OH + KOH C13H10O2 + C2H6O2 + KBr 229 94 56 198 62 119 meta-bromobenzaldehydeacetal Phenol Potassium Hydroxide meta-phenoxy-benzaldehyde MEG Potassium Bromide 140

Material Balance: Input Output Key RM Product Benzaldehyde MT 0.661 3-phenoxy benzaldehyde (MPBD) MT 1.000 Reagent Inorganic Acid Ammonia solution (25%) MT 0.010 Hydrochloric acid (15-33%) MT 0.690 Aluminium chloride MT 1.146 Bromine MT 0.221 Process Residue and Waste Caustic Lye (48%) MT 0.470 Organic Waste MT 0.328 Chlorine MT 0.224 Copper chloride MT 0.012 Wastewater Formic acid MT 0.100 Effluent MT 5.610 Hydrochloric acid (15- MT 1.470 33%) Hyflow (Filter aid) MT 0.001 Process Gaseous Emission Monoethylene glycol MT 0.061 Nitrogen & HCl traces MT 0.500 Phenol MT 0.583 Potassium hydroxide MT 1.300 (KOH Solution) p-toluenesulfonic acid MT 0.003 Soda ash MT 0.050 Sodium chloride MT 0.010 Sodium thio sulphate MT 0.060 Sulphuric acid (98%) MT 0.030 Solvent Toluene MT 0.026 Ethyledichloride MT 0.097 Water Process Water MT 1.093 Gas Nitrogen MT 0.500 Total Input MT 8.128 Total Output MT 8.128 141

44. 3-phenoxy toluene Process Description: 3- phenoxy toluene prepared by reacting m-cresol and bromobenzene in presence of Bis(triphenylphosphine)cuprous catalyst. After reaction 3-Phenoxytoluene will be separated by distillation. Then inorganic salts (KBr & NaBr) separated out by filtration. Remaining mixture treated with hydrochloric acid and sent for further treatment and disposal. Chemical Reaction: Material Balance: Input Output Key RM Product m-cresol MT 0.621 3-phenoxy toluene MT 1.000 Bromobenzene MT 1.805 Inorganic salts Reagent Inorganic salts MT 0.600 Caustic Lye (48%) MT 0.138 Copper Chloride MT 0.004 Process Residue and Waste Hydrochloric acid (15-33%) MT 0.420 Organic Waste MT 0.990 Potassium hydroxide (KOH Solution) MT 0.161 Wastewater Water Effluent MT 1.339 Process Water MT 0.780 Process Gaseous Emission Gas Nitrogen MT 0.200 Nitrogen MT 0.200 Total Input MT 4.129 Total Output MT 4.129 142

45. Methyl-2- Fluoroacrylate Process Description: Tetra fluoro ethylene reacts with formaldehyde, AHF and NaOH solution to form tetrafluorooxetane after distillation of the first step s it will be reacts with methanol in presence of sodium iodide and zinc to form methyl 2 fluoro acrylatea and HF as a-. Chemical Reaction: 143

Material Balance: Input Output Key RM Product Hydrofluoric acid Anhydride MT 1.287 Methyl-2- Fluoroacrylate MT 1.000 1,1,2,2-Tetrafluoroethylene MT 1.472 Hydrofluoric acid (20-70%) MT 5.865 Reagent Zinc Salt Dimethylformamide MT 2.510 Zinc Fluoride MT 1.530 Caustic Lye (48%) MT 0.740 Hydroquinone MT 0.013 Process Residue and Waste Methanol MT 0.731 Organic Waste MT 3.030 Paraformaldehyde MT 0.925 Sodium iodide MT 1.150 Inorganic Salt Trifluoroacetic acid MT 1.350 Solid Waste MT 1.600 Zinc MT 0.981 Wastewater Water Effluent MT 7.632 Process Water MT 9.500 Process Gaseous Emission Gas Nitrogen & HF traces MT 0.200 Nitrogen MT 0.200 Total Input MT 20.858 Total Output MT 20.858 46. 144

47. Lithium tetrakis (pentafluorophenyl) borate Process Description: Four molecules of Pentafluorobenzene combines with t-butyl lithium in presence of Boron trifluoride etherate to form LTKPFPB-->Step-1. Mass will filtered and dried to obtain the from mixture of solvent and Product. The filtrate will sent for solvent recovery to recycle part of the solvent back in the process. Chemical Reaction: Step-1 Reaction - 40 o C M.W- 168 M.W- 64 M.W- 68 M.W-686 Material Balance: Input Output Key RM Product Pentafluorobenzene MT 0.361 Lithium tetrakis (pentafluorophenyl) borate (LTKPFPB) MT 1.000 Reagent Process Residue and Waste tert-butyllithium in pentane MT 0.570 Organic Waste MT 0.380 solution (24%) BF3.etherate solution (50%) MT 0.069 Diethyl ether MT 0.434 Wastewater Toluene MT 0.423 Effluent MT 0.477 Gas Process Gaseous Emission Nitrogen MT 0.200 Nitrogen MT 0.200 Total Input MT 2.057 Total Output MT 2.057 145

48. 2-fluoro-5-bromobenzonitrile Process Description: Chlorobenzonitrile reacts with potassium fluoride to form 2 fluorobenzonitrile and potassium chloride. 2-FBN again reacts with N bromosuccinimide to form 2-fluoro-5-bromobenzonitrile. Chemical Reaction: Step-1 C6H4CNCl + KF C6H4CNF + KCl 137.5 58 121 74.5 ` 2-Chlorobenzonitrile Potessium Fluoride 2-Fluorobenzonitrile Potessium Chloride Step-2 C6H4CNF + C4H4O2NBr C6H3CNFBr + C4H4O2NH 121 178 200 99 2-Fluorobenzonitrile N-Bromosuccinimide 2-Fluoro-5-bromobenzonitrile Succinimide 146

Material Balance: Input Output Key RM Product Chlorobenzonitrile MT 1.131 2-fluoro-5-bromobenzonitrile (FBBN) MT 1.000 Reagent Inorganic Acid Potassium Fluoride MT 1.431 Sulphuric Acid 65% MT 10.310 1,3-Dimethyl-2-imidazolidinone MT 0.844 Methylene chloride MT 0.699 Potassium Salt 2-Fluorobenzonitrile MT 0.756 KCl-KF mixture MT 0.870 H2SO4 (98%) MT 4.544 N-Bromosuccinimide MT 1.101 By- (C4H4BrNO2) Ethanol MT 0.290 Succinimide (C4H5NO2) MT 0.620 O Toluedine MT 0.050 Process Residue and Waste Water Organic Waste MT 0.813 Process Water MT 4.860 Wastewater Gas Effluent MT 2.093 Nitrogen MT 0.200 Process Gaseous Emission Nitrogen MT 0.200 Total Input MT 15.906 Total Output MT 15.906 147

49. Ethyl-Trifluoropyruvate Process Description: Hexafluoroacetone reacts with ethanol to form ETFFP. ETFFP formed in the above step was washed with Distilled water to get pure ETFFP. The Aqueous layer containing HF and EtOH will be neutralized with Calcium Hydroxide to precipitated Calcium Fluoride and get fluoride removed from aqueous effluent. The pure ETFFP reacts with 98% H2SO4 and Silica to form rude ETFP, Ethanol, SO3 and SiF4 and water. The exit gas from reaction containing SO3 and SiF4 was scrubbed in water. The crude ETFP was distilled to get pure. Chemical Reaction: Step-1 C3F6O + 2 C2H5OH C7F4O3H10 + 2 HF 166 46 218 20 Hexafluoroacetone Ethanol ETFFP Hydrogen Fluoride Step-2 C7F4O3H10 + 0.25 SiO2 + H2SO4 C5F3O3H5 + C2H5OH + 0.25 SiF4 + SO3 + 0.5 H20 218 60 98 170 46 104 80 18 ETFFP Silica Sulfuric Acid ETFP Ethanol Silicon Tetrafluoride Sulfur Trioxide Water Material Balance: Input Output Key RM Product Hexafluoroacetone MT 1.770 Ethyl-Trifluoropyruvate (ETFP) MT 1.000 Reagent By- Ethanol MT 2.450 CaF2 solid MT 0.830 Calcium Hydroxide MT 0.790 Silica MT 0.160 Process Residue and Waste Sulphuric acid (98%) MT 0.900 Organic Waste MT 1.108 Water Wastewater Process Water MT 7.090 Effluent MT 10.222 Gas Process Gaseous Emission Nitrogen MT 0.200 Nitrogen MT 0.200 Total Input MT 13.360 Total Output MT 13.360 148

50. Isoflurane Process Description: Trifluoroethanol reacts with potassium oxide and R-22 to form Ester, water and potassium chloride this ester intermediate reacts with chlorine to form isoflurane and HCL. Chemical Reaction: Step-1 + KOH + R-22 Ester + H20 + KCl Trifluoro Ethanol Potassium Oxide Chlorodifluoromethane Intermediate + Water Potassium Chloride MW : 100 MW: 56.1 MW : 86.5 MW: 150 MW : 18 MW : 74.6 Step-2 Ester + Cl2 Isoflurane + HCl Intermediate Chlorine Gas Isoflurane Hydrochloric Acid MW: 150 MW: 71 MW: 184.5 MW: 36.5 Material Balance: Input Output Key RM Product Trifluoroethanol MT 0.900 Isoflurane MT 1.000 Reagent By- KOH (48%) MT 1.260 CaF2 solid MT 0.800 NaOH (20%) MT 0.650 Acetone MT 0.050 Process Residue and Waste Organic Waste MT 0.250 Water Process Water MT 0.580 Wastewater Effluent MT 2.640 Gas Nitrogen MT 0.200 Process Gaseous Emission R-22 MT 0.670 Nitrogen MT 0.200 Chlorine Gas MT 0.580 Total Input MT 4.890 Total Output MT 4.890 149

51. Desflurane Process Description: Isoflurane reacts with anhydrous hydrogen fluoride in presence of fluorinated catalyst to form desflurane. 15-33% HCL also produces as a. After layer separation it will be distilled to get pure. Chemical Reaction: Step-1 C3H2ClF5O + HF + Fluorinating Catalyst C3H2F6O + HCl Isoflurane Anhydrous HF Catalyst Desflurane Hydrochloric acid MW: 184.5 MW: 20 - MW: 168 MW : 36.5 Material Balance: Input Output Key RM Product Isoflurane MT 1.570 Desflurane MT 1.000 Hydrofluoric acid (20-60%) MT 1.000 Reagent Flourinating catalyst MT 0.100 Inorganic Acid Anhydrous Hydrogen fluoride MT 0.340 Hydrochloric acid (15-33%) MT 0.230 Dil HCL(30%) MT 0.860 Spent Catalyst Water Spent Catalyst MT 0.100 Process Water MT 0.720 Process Residue and Waste Gas Organic Waste MT 0.150 Nitrogen MT 0.200 Wastewater Effluent MT 1.110 Process Gaseous Emission Nitrogen, HCl and HF traces MT 0.200 Total Input MT 3.790 Total Output MT 3.790 150

52. Sevoflurane Process Description: Hexafluoroisopropanol reacts with Anhydrous HF to form sevoflurane after washing with water and aqueous KOH the mixture will be distilled out to get pure. Chemical Reaction: Material Balance: Input Output Key RM Product Hexafluoroisopropanol MT 1.670 Sevoflurane MT 1.000 Hydrofluoric Acid (33%) MT 1.280 Reagent Trioxane MT 0.360 Potassium Salt Anhydrous Hydrogen Fluoride MT 0.790 K2SO4 solid MT 1.560 Conc. H2SO4 (98%) MT 2.000 Aqueous KOH (48%) MT 3.130 Process Residue and Waste Organic Waste MT 2.280 Water Process Water MT 3.000 Wastewater Effluent MT 4.830 Gas Nitrogen MT 0.200 Process Gaseous Emission Nitrogen & HF traces MT 0.200 Total Input MT 11.150 Total Output MT 11.150 151

53. Trichloroacetyl chloride Process Description: Acetic acid reacts with chlorine to chlorine to form Trichloroacetyl chloride and hydrogen chloride. It will be further filtered and distilled to GET TCAC. Chemical Reaction: C2H4O2 + 3Cl2 C2Cl4O + H20 + 2HCl 60 213 182 18 73 Acetic acid Chlorine Trichloroacetylchloride Water Hydrogen Chloride Material Balance: Input Output Key RM Product Acetic Acid MT 0.370 Trichloroacetyl chloride (TCAC) MT 1.000 Reagent Inorganic Acid Chlorine MT 2.600 Hydrochloric Acid 30% MT 1.330 Charcoal MT 0.150 Sodium Hypochlorite MT 7.039 48% NaOH Solution MT 4.400 Inorganic Salt Water Solids MT 0.250 Process Water MT 3.259 Process Residue and Waste Gas Organic Waste MT 0.160 Nitrogen MT 0.200 Wastewater Effluent MT 1.000 Process Gaseous Emission Nitrogen, HCl and Cl2 traces MT 0.200 Total Input MT 10.979 Total Output MT 10.979 152

54. Chlorinated Compound i. Trichloroethylene Process Description: Chlorination Section: In Chlorination section, a reaction between Ethylene dichloride and Chlorine is carried-out in presence of catalyst. The HCl + Organicvapours from reactor are sent to HCl distillation column to recover the organics. The organic from reactor is distilled to obtain a mixture of Tetra / Penta / Hexa Chloroethanes, which will be sent to cracker section. The distillation top organic liquid is sent as recycle to chlorination reactor. The distillation top HCl + Organics are dried in CaCl2 and sent to HCl distillation for the recovery of organics. Cracker Section: The mixture of Tetra / penta / hexa chloroethanes are vaporized and cracked in a process furnace. The high temperature vapours from furnace are routed through a packed bed reactor and the vapors are condensed and collected. The liquid is routed to distillation section and HCl vapors are sent to HCl distillation for the recovery of organics. Distillation Section: In this section, the cracker is distilled in a series of 4 columns. The s P11 and P12 are routed to MTF for further storage and sale. Stabilizer is added in the Product. The separated light and heavy organics, consisting of Chlorinated butadiene. The mixture is washed with Aqueous Ba (OH) 2 solution before separating the P11 and P12 s. The aqueous BaCl2 solution will be sent to ETP for further treatment. HCl Distillation Section: In this section, two separate columns are provided to recover the organics from HCl + Organics vapor mixture coming from the process. The recovered organics are recycled back to the process. The HCl vapors are absorbed in process water to prepare 30% HCl solution, which will be sold as. Control System: Plant is controlled by DCS/PLC from the main control room. Each parameter is continuously monitored, recorded and controlled automatically. Various trips / interlocks are given to handle any kind of emergency. Multiple alarm system has been used to take care of any deviation in terms of operation & safety. The critical pumps are on emergency power supply (UPS). Most of the emergency control actions are remote controlled from control room, rather than manual action in field. Chemical Reaction: C2H4Cl2 + 2 Cl2 C2HCl3 + 3 HCl 99.0 142.0 131.5 109.5 Ethyledichloride Trichloroethylene 153

Material Balance: Input Output Key RM Product Ethylene dichloride MT 0.754 Trichloroethylene MT 1.000 Chlorine MT 1.617 Anhydrous HCl MT 0.010 Inorganic Acid Hydrochloric Acid 30% MT 3.189 Reagent Sodium Hypochlorite MT 0.170 Barium Hydroxide/ MT 0.010 Sodium Hydroxide Stabilizer (Thymol) MT 0.004 By- Caustic Lye 48% MT 0.103 Dilute Trichloroethylene MT 0.023 Alumina Balls MT 0.001 Calcium Chloride MT 0.001 Molecular Sieve MT 0.001 Mix Trichloroethylene & MT 0.341 Perchloroethylene Anhydrous Calcium MT 0.001 Chloride Therminol-55 MT 0.001 Charcoal MT 0.001 Spent Catalyst Catalyst - Nitrile based MT 0.0002 Spent Alumina Balls MT 0.001 Spent Molecular Sieve MT 0.001 Water Catalyst - Nitrile based MT 0.0002 Process Water MT 2.816 Spent Carbon Gas Spent Charcoal MT 0.001 Nitrogen MT 0.005 Wastewater Aqueous effluent - acidity MT 0.049 Aqueous effluent - Alkaline MT 0.522 Process Gaseous Emission Nitrogen, HCl and Cl2 Traces MT 0.005 Total Input MT 5.313 Total Output MT 5.313 154

ii. Perchloroethylene Process Description: Chlorination Section: In Chlorination section, a reaction between Ethylene dichloride and Chlorine is carried-out in presence of catalyst. The HCl + Organic vapors from reactor are sent to HCl distillation column to recover the organics. The organic from reactor is distilled to obtain a mixture of Tetra / Penta / Hexa Chloroethanes, which will be sent to cracker section. The distillation top organic liquid is sent as recycle to chlorination reactor. The distillation top HCl + Organics are dried in CaCl2 and sent to HCl distillation for the recovery of organics. Cracker Section: The mixture of Tetra / penta / hexa chloroethanes are vaporized and cracked in a process furnace. The high temperature vapours from furnace are routed through a packed bed reactor and the vapors are condensed and collected. The liquid is routed to distillation section and HCl vapors are sent to HCl distillation for the recovery of organics. Distillation Section: In this section, the cracker is distilled in a series of 4 columns. The s P11 and P12 are routed to MTF for further storage and sale. Stabilizer is added in the Product. The separated light and heavy organics, consisting of Chlorinated butadiene. The mixture is washed with AqueousBa(OH)2 solution before separating the P11 and P12 s. The aqueous BaCl2 solution will be sent to ETP for further treatment. HCl Distillation Section: In this section, two separate columns are provided to recover the organics from HCl + Organics vapor mixture coming from the process. The recovered organics are recycled back to the process. The HCl vapors are absorbed in process water to prepare 30% HCl solution, which will be sold as. Control System: Plant is controlled by DCS/PLC from the main control room. Each parameter is continuously monitored, recorded and controlled automatically. Various trips / interlocks are given to handle any kind of emergency. Multiple alarm system has been used to take care of any deviation in terms of operation & safety. The critical pumps are on emergency power supply (UPS). Most of the emergency control actions are remote controlled from control room, rather than manual action in field. Chemical Reaction: C2H4Cl2 + 3 Cl2 C2Cl4 + 4 HCl 99.0 213.0 166.0 146.0 Ethyledichloride Perchloroethylene 155

Material Balance: Input Output Key RM Product Ethylene dichloride MT 0.754 Perchloroethylene MT 1.000 Chlorine MT 1.617 Anhydrous HCl MT 0.010 Inorganic Acid Hydrochloric Acid 30% MT 3.188 Reagent Sodium Hypochlorite MT 0.170 Barium Hydroxide/ Sodium MT 0.010 Hydroxide Catalyst - Nitrile based MT 0.0002 By- Stabilizer (Thymol) MT 0.004 Dilute Trichloroethylene MT 0.023 Caustic Lye 48% MT 0.124 Calcium Chloride (Solid/ MT 0.001 Liquid) Alumina Balls MT 0.001 Mix of Trichloroethylene & MT 0.363 Perchloroethylene Molecular Sieve MT 0.001 Anhydrous Calcium Chloride MT 0.001 Spent Catalyst Therminol-55 MT 0.001 Spent Alumina Balls MT 0.001 R-22 MT 0.000 Spent Molecular Sieve MT 0.001 Charcoal MT 0.001 Catalyst - Nitrile based MT 0.0002 Water Spent Carbon Process Water MT 2.816 Spent Charcoal MT 0.001 Gas Wastewater Nitrogen MT 0.005 Aqueous effluent - acidity MT 0.049 Aqueous effluent - Alkaline MT 0.522 Process Gaseous Emission Nitrogen, HCl and Cl2 Traces MT 0.005 Total Input MT 5.335 Total Output MT 5.335 156

iii. Chloromethanes Process Description: In Chlorination section, main raw materials are: Chlorine and. Reaction takes place in presence of UV rays or thermally or catalytically. At the outlet of reactor, a mixture of C2, C3 and C4 is obtained along with HCL and un-reacted C1. The necessary quantity of 100% HCL is sent to C1 reactor and balance goes for absorption to 33% from the HCL distillation (removal column). This is followed by C1 removal columns. After C1 and HCL removal, the mixture ofc2, C3 and C4 is sent to crude storage. The ion of C2/C3/C4 depends on the ratio ofc1 & Cl2 feed in the reactor. C1 Reactor & C1 Wash Section: In C1 section, main raw materials are: Methanol and 100% HCL (From chlorination section). The reaction takes place in the presence of catalyst. C1 (Methyl Chloride) is formed which after purification (removal of acidity, free chlorine & moisture, etc.) and compression is sent to storage. Wash & Distillation Section: In this section, crude CMS is treated for removal of residual acidity and moisture (drying). The dried CMS is fed to distillation train for C2, C3 and C4 ion. CMS plant is controlled by DCS/PLC from the main control room. Each parameter is continuously monitored, recorded and controlled automatically. Various trips / interlocks are given to handle any kind of emergency. Multiple alarm system has been used to take care of any deviation in terms of operation & safety. The critical pumps are on emergency power supply (UPS). Most of the emergency control actions are remote controlled from control room, rather than manual action in field. Chemical Reaction: CH3OH + HCl CH3Cl + H2O 3236.5 50.5 18 50.5 71 85 36.5 85 71 119.5 36.5 119.5 71 142 36.5 CH3Cl + Cl2 CH2Cl2 + HCl CH2Cl2 + Cl2 CHCl3 + HCl CHCl3 + Cl2 CCl4 + HCl 157

Material Balance: Input Output Key RM Product Methanol MT 0.365 1 Methylene Chloride MT 0.650 2 Chloroform MT 0.340 Reagent 3 Carbon Tetrachloride MT 0.010 Chlorine MT 1.220 Aluminium Oxide MT 0.001 Inorganic Acid 48% Caustic Solution MT 0.090 95% Sulfuric Acid MT 0.247 98% Sulfuric Acid MT 0.500 15-30% Hydrochloric Acid MT 1.689 Amylene MT 0.001 Hypo Chlorite MT 0.200 Desiccant (Silica Gel & Calcium Chloride) MT 0.001 Water Spent Catalyst Process Water MT 1.532 Aluminium Oxide MT 0.001 Desiccant (Silica Gel & Calcium Chloride) MT 0.001 Gas Nitrogen MT 0.001 Wastewater Effluent MT 0.568 Diluted CMS MT 0.004 Process Gaseous Emission Nitrogen and HCl stack emissions MT 0.001 Total Input MT 3.710 Total Output MT 3.710 158

55. Caustic and Chlorine Plant Process Description: The process is based on Membrane Cell technology. The main steps in the process to manufacture caustic soda are Purification of brine. Electrolysis. Concentration and flaking of caustic soda solution. Brine Purification Brine for ion exchange membrane Chlor-Alkali process is prepared by dissolving salt in the return brine from the electrolysis plant, and purified in two stages. Primary purification removes impurities like calcium, magnesium, sulphate, iron, silica etc. Secondary purification is required to make brine suitable for the ion exchange membrane Primary Brine Purification: Primary Brine Purification section consists of Salt Handling system, Brine Saturator, Reactor Clarifier, Clarified Brine Tank and associated facilities. This process includes Brine saturation, chemicals dosage, reaction and sedimentation. The purpose of this process is to re-saturate the return brine with raw salt and to remove impurities from the saturated raw brine. The return brine is fed from the top of the Brine Saturator and saturated with salt. The salt is continuously supplied to the top of the saturator by a Belt Conveyor System. Suspended solids in the brine are removed by settling in the Clarifier provided with water seal & insulated from the sides. The brine, thus clarified, flows into clarified Brine tank over the weir of Clarifier & is pumped out and recirculated to the brine system before reactor for better clarification. Slurry is periodically measured for better control. A part of slurry is sent to Sludge Filter System. The clarified brine is sent to Secondary Brine purification section by clarified brine pump. Secondary Brine Purification: Secondary Brine Purification Section consists of Brine Filter and Ion Exchange Resin Column. This specially developed Ion exchange resin can remove multivalent cations harmful to the Ion exchange membrane. The brine thus purified is fed to Electrolyser and electrolysis is conducted. 159

Electrolysis Electrolyser Electrolyser consists of the metal anode and the activated cathode, the Ion exchange membrane, press unit for mounting cell frames, Cell frames holding the Ion Exchange membrane in between are fixed by the oil cylinder installed at the end of the press unit. This structure ensures no leakage of electrolytes because uniform pressure can be applied to gasket surface and cell frame of metal structure ensures no electrolyte leakage caused by deformation even after a long period of operation. Anolyte Circulation Anolyte circulation system is composed of Anolyte Circulation Tank and anolyte circulation pump. Anolyte is fed into each of anode compartment of cell frames through sub headers and hoses, and recirculated to Anolyte circulation Tank. Purified brine is fed to maintain anolyte concentration within a designed level. A part of the anolyte, is taken out from Anolyte Circulation Tank to Depleted Brine Tank by overflow. Anolyte Circulation system is designed to ensure steady and uniform distribution of anolyte to each cell and to cope-up with any change in electrolysis conditions such as ion rate change. The diluted brine collected in Depleted Brine Tank is sent to De-chlorination Tower for removal of Chlorine gas. Chlorine gas generated in electrolyser is separated in Anolyte Circulation Tank and sent to Chlorine gas cooling, drying and compression section. Catholyte Circulation Catholyte Circulation System is composed of Catholyte Circulation Tank, Catholyte Circulation Pump and Catholyte Cooler. Catholyte is circulated through cathode compartment of cell frames to Catholyte Circulation Tank by Catholyte Circulation Pump, and a part of it is taken out from Catholyte Circulation Tank to Caustic Soda Tank and sent out to caustic evaporation section. To keep the concentration of caustic soda at designed level, demineralised water is fed to catholyte inlet sub-header. Hydrogen gas generated in Electrolyser is separated from the catholyte in catholyte Circulation Tank and sent to Hydrogen Gas Cooling and Compression Section. Heat generated in electrolyser is removed by cooling water in Catholyte Cooler. De Chlorination of Return Brine De-chlorination section is composed of De-Chlorination Tower, De-Chlorination Tower Cooler, Ejector, Ejector Cooler and associated facilities. Return brine, (depleted brine) from Electrolysis Section is saturated with chlorine. In the tower, chlorine is stripped together with water vapor, and passed through De-chlorination Tower cooler. The vapour is condensed there and the chlorine gas is sucked by the steam ejector to Ejector Cooler. Steam is condensed there and the chlorine gas is then introduced to chlorine gas main line. The depleted brine dechlorinated through De-chlorination tower, still contains small amount of free chlorine which can cause damage to the filter elements in Brine Filters and damage ion exchange resin in Ion Exchange Resin Columns. Sodium sulphite is added to kill free chlorine. Return brine is then fed to Return Brine Tank & pumped to salt saturator. Caustic Concentration The caustic soda concentration system consists of triple effect falling film evaporators operating on backward feed flow scheme. 30% caustic solution 80 0C is fed to third effect evaporator. Vapours are separated from solution and concentrated solution of third effect evaporator is pumped to second effect evaporator after passing through two heat exchangers in series. In the second effect evaporator, flash 160

evaporation of liquor takes place and liquor is further heated by steam and vapors are separated in second effect evaporator to concentrate liquor. The concentrate from the second effect evaporator is pumped through first effect evaporator after passing through two heat exchangers in series. Steam at 11 Kg/cm2a pressure is used to attain required concentration of caustic. Chlorine Liquefaction & Bottling Chlorine Gas Washing and Cooling Chlorine Gas coming out of Anolyte circulation tank contains water vapour saturated at about 900 C and has little amount of Sodium Chloride as entrainment. Gas is first washed by process water in a direct contact scrubbing packed tower. Condensate is sent to dechlorination tower. The process water is in turn cooled by cooling tower. Cooled gas is then passed through a packed tower having chilled process water circulation at 160 C so as to cool the gas to reduce water vapors load. Chlorine gas temperature is generally around 15-20 deg C as cooling below 9-10 0C will result into formation of Chlorine hydrate. Cooled gas is then dried with direct spray of sulfuric acid in packed towers. Chlorine Gas Drying The cooled chlorine gas is led to chlorine Gas Drying Tower. The moisture of chlorine gas is absorbed into sulfuric Acid of 98% concentration fed into the two stage chlorine gas drying tower, and gets diluted to 70% by absorption of moisture from chlorine gas. Chlorine Gas Drying Tower has a cooler to cool circulating sulfuric Acid. The Dry Chlorine gas is sent for compression. Chlorine Gas Compression Dry chlorine gas from chlorine Gas Drying Section is compressed to 4 MT/cm2 by using Acid Ring type Compressor. Chlorine Gas Liquefaction and Filling Chlorine gas from compressor is sent to chlorine Gas Liquefaction Unit to be condensed by the Freon 22 refrigerant. The unliquefied gases along with inert gas from Liquefier are sent to HCI Synthesis unit for burning with Hydrogen to produce HCl. Liquefied chlorine enters Chlorine Storage Tank from where it is transferred by means of compressed dry air to chlorine bottling section. Part of liquid Chlorine is vaporised and sent to nearby customers through pipeline. Waste Chlorine Neutralization / Sodium Hypochlorite Section Waste chlorine gas, only in case of plant emergency is led to the Sodium Hypochlorite Unit. Chlorine Gas during start up and plant tripping is fed to the absorption tower. This unit consists of packed tower in which caustic solution is circulated to absorb waste chlorine. Temperature of the liquid is controlled by heat transfer through plate type heat exchanger with chilled water. After a desired strength of sodium hypochlorite is reached, the solution is sent to a Hypo Reactor. Here it is reacted with fresh chlorine to produce marketable quality Sodium Hypochlorite. HCL Synthesis The HCI Synthesis unit consists of combustion furnace fitted with absorbers. The chlorine gas reacts with Hydrogen to form HCI gas which is cooled and absorbed in DM water. The flow rate of DM water is adjusted to obtain 30-33% HCI Solution. The flow rates of Chlorine and Hydrogen are controlled by flow 161

controllers. Safety Interlocking provisions are made which get actuated by flame protection device. The Hydrochloric Acid Solution is collected in a tank from where is pumped to HCI Storage Tanks. Hydrogen Bottling and Storage Hydrogen gas is compressed and filled in hydrogen cylinders banks of the customers and also stored in cylinder banks. Caustic Soda and Flaking Plant Flaker plant is a double effect evaporator. 32% Caustic is feed to produce 98% Caustic Flakes. Salt mixture (KNO3, NaNO2 & NaNO3) which is heated by burning Hydrogen is a heating media to increase Caustic lye temperature in final concentrator. 98 % Caustic flakes is then cooled and packed using a polythene liner to avoid moisture pick-up as it is a hygroscopic. Solid Waste Generation The membrane cells require brine of extremely good quality for electrolysis. Presence of even traces of Ca, Mg etc. are harmful to the membranes. Hence extensive treatment is required. This is done in two stages viz. primary treatment and secondary treatment. In the primary stage Ca, Mg impurities are chemically precipitated out of brine while sulphate impurities are removed by using latest nano-filtration sulphate removal system to minimize the solid waste generation. The solid waste will be sent to secured landfill site. After settling and filtration, brine is further treated in ion exchange columns, called as secondary treatment to remove traces of Ca, Mg to yield pure brine of quality suitable for membrane cells. The precipitated impurities containing Ca, Mg along with insoluble etc. are settled in a clarifier and are drawn out as thick sludge (4-10% w/w). This sludge is pumped to sludge filtration unit by clarifier sludge pump to minimize the quantity for disposal as well as to recover brine. The cake from the decanter is disposed to secured land fill site and clear filtrate brine is recycling back to clarifier. Chemical Reaction: 2 NaCl + 2H2O Cl2 + H2 + 2NaOH 117 36 71 2 80 162

Material Balance: Input Output Key RM Product Sodium Chloride MT 1.720 Chlorine MT 1.000 Caustic Lye 47.5% MT 3.251 Reagent Hydrogen MT 0.028 Sulfuric Acid MT 0.036 Hydrochloric Acid 15-33% MT 0.300 Water Inorganic Acid Process Water MT 3.924 Sulphuric Acid, 70-90% MT 0.040 Sodium Hypo chlorite MT 0.086 Gas Nitrogen MT 0.010 Wastewater Aqueous Effluent MT 0.975 Process Gaseous Emission Chlorine traces & Nitrogen MT 0.010 Total Input MT 5.690 Total Output MT 5.690 163

56. Anhydrous Hydrofluoric acid Process Description: HF is produced in an indirectly heated rotary reactor (kiln) under small vacuum by the reaction of Sulfuric acid & dried Fluorspar. Oleum is used to convert the moisture into H2SO4. Crude HF thus produced, is distilled in Distillation Columns to produce pure HF. Chemical Reaction: CaF2 + H2SO4 2 HF + CaSO4 78.08 98.06 40.00 136.14 H2O + H2S2O7 2 H2SO4 18.00 178.12 196.12 Material Balance: Input Output Key RM Product Fluorspar MT 2.600 Anhydrous Hydrofluoric acid MT 1.000 Hydrofluoric Acid (30-40%) MT 0.105 Reagent Aluminium MT 0.008 Inorganic Acid Calcium Chloride MT 0.0002 Hydrofluorosilicic Acid (15%-40%) MT 0.600 Calcium oxide MT 0.035 Oleum MT 1.072 By- Sulphuric Acid 98% MT 1.451 Gypsum (CaSO4) MT 4.060 Sodium Hydroxide MT 0.280 Aluminium Trifluoride (AlF3) MT 0.025 (30%) R22 Refrigerant MT 0.0001 Calcium chloride MT 0.001 Calcium fluoride MT 0.145 Water Process Water MT 2.620 Wastewater Gas Aqueous Effluent MT 2.040 Nitrogen MT 0.010 Spent Calcium Chloride Brine MT 0.0002 Process Gaseous Emission Nitrogen MT 0.100 HF traces MT 0.00005 Total Input MT 8.076 Total Output MT 8.076 164

57. Chlorotrifluoroethane (HCFC 133a) Process Description: Trichloroethylene (TCE) is reacted with Hydrofluoric Acid in presence of Catalyst to produce R 133a. Chemical Reaction: C2HCl3 + 3HF = CF3CH2Cl + 2HCl 131.388 60.019 118.485 72.922 Material Balance: Input Unit Quantity Output Unit Quantity Key RM Product Hydrofluoric Acid (HF) MT 0.880 Chlorotrifluoroethane (HCFC MT 1.000 133a) Reagent Hydrofluoric Acid 20-70 % MT 0.200 Caustic Lye 48% MT 0.007 Crome- Alumina MT 0.005 Inorganic Acid Activated carbon MT 0.005 Sulphuric Acid, 70-90% MT 0.250 Molecular sieve MT 0.005 Hydrochloric Acid 15-33% MT 2.098 Sulphuric Acid 98% MT 0.241 Trichloroethylene MT 1.216 Spent Carbon Activated carbon MT 0.005 Water Process Water MT 1.500 Spent Catalyst Crome- Alumin MT 0.005 Gas Molecular sieve MT 0.005 Nitrogen MT 0.100 Wastewater Aqueous Effluent, alkaline MT 0.296 Process Gaseous Emission Nitrogen, HCl and HF traces MT 0.100 Total Input MT 3.959 Total Output MT 3.959 165

58. HFC Refrigerant i. 1,1,1,2 Tetrafluroethane (HFC 134a) Process Description: Trichloroethylene (TCE) is reacted with Hydrofluoric Acid in presence of Catalyst to produce R 133a. R 133a is then reacted with HF in another Reactor in presence of Catalyst to produce R 134a. HCl produced is separated from R 134a. R134a thus produced is sent to the wash section & distilled to get the pure. Chemical Reaction: C2HCl3 + 3HF = CF3CH2Cl + 2HCl 131.388 60.019 118.485 72.922 CF3CH2Cl + HF = CH2FCF3 + HCl 118.485 20.006 102.031 36.461 Material Balance: Input Output Key RM Product Hydrofluoric Acid (HF) MT 0.960 1,1,1,2 Tetrafluroethane (HFC MT 1.000 134a) Trichloroethylene MT 1.400 Hydrofluoric Acid 20-70 % MT 0.210 Reagent Inorganic Acid Caustic Lye 48% MT 0.007 Sulphuric Acid, 70-90% MT 0.250 Crome- Alumina MT 0.002 Hydrochloric Acid 15-33% MT 3.600 Activated carbon MT 0.020 Molecular sieve MT 0.020 Spent Carbon Sulphuric Acid 98% MT 0.231 Activated carbon MT 0.020 Ferric Chloride MT 0.010 Spent Catalyst Water Crome- Alumin MT 0.002 Process Water MT 2.690 Molecular sieve MT 0.020 Gas Process Residue and Waste Nitrogen MT 0.013 Chlorinated Organic Compounds MT 0.010 Wastewater Aqueous Effluent, alkaline MT 0.128 Aqueous Effluent, acidic MT 0.100 Process Gaseous Emission Nitrogen, HCl and HF traces MT 0.013 Total Input MT 5.353 Total Output MT 5.353 166

ii. Pentafluoroethane (HFC 125) Process Description: Perchloroethylene (PCE) is reacted with Hydrofluoric Acid in presence of Catalyst to produce R 123. R 123 is then reacted with HF in another Reactor in presence of Catalyst to produce R 125. HCl produced is separated from R 125. R125 thus produced is sent to the wash section & distilled to get the pure. Chemical Reaction: 2C2Cl4 + 10HF = 2C2HF5 + 8HCl 331.667 200.063 240.043 291.688 Material Balance: Input Unit Quantity Output Unit Quantity Key RM Product Perchloroethylene MT 1.468 Pentafluoroethane (HFC 125) MT 1.000 Hydrofluoric Acid (HF) MT 1.015 Hydrofluoric Acid 20-70 % MT 0.155 Hydrochloric acid Anhydrous MT 0.010 Reagent Caustic Lye 48% MT 0.007 Inorganic Acid Crome- Alumina MT 0.005 Sulphuric Acid, 70-90% MT 0.221 Activated carbon MT 0.005 Hydrochloric Acid 15-33% MT 4.074 Molecular sieve MT 0.005 Sulphuric Acid 98% MT 0.212 Spent Carbon Activated carbon MT 0.005 Water Spent Catalyst Process Water MT 2.948 Crome- Alumina MT 0.005 Molecular sieve MT 0.005 Gas Nitrogen MT 0.100 Wastewater Aqueous Effluent, alkaline MT 0.190 Process Gaseous Emission Nitrogen, HCl and HF traces MT 0.100 Total Input MT 5.765 Total Output MT 5.765 167

iii. Difluoromethane (HFC - 32 ) Process Description: Methylene chloride will react with Hydrofluoric Acid in presence of Catalyst to produce Difluoromethane (HFC - 32). Chemical Reaction: CH2Cl2 + 2HF = CH2F2 + 2HCl 84.933 40.013 52.023 72.922 Material Balance: Input Output Key RM Product Methylene chloride MT 1.661 Difluoromethane (HFC- 32 ) MT 1.000 Hydrofluoric Acid (HF) MT 0.993 Hydrofluoric Acid 20-70 % MT 0.227 Hydrochloric acid Anhydrous MT 0.010 Reagent Caustic Lye 48% MT 0.210 Inorganic Acid Crome- Alumina MT 0.005 Sulphuric Acid, 70-90% MT 0.158 Activated carbon MT 0.005 Hydrochloric Acid 15-33% MT 4.897 Molecular sieve MT 0.005 Sulphuric Acid 98% MT 0.244 Spent Carbon Activated carbon MT 0.005 Water Process Water MT 3.375 Spent Catalyst Crome- Alumina MT 0.005 Gas Molecular sieve MT 0.005 Nitrogen MT 0.100 Wastewater Aqueous Effluent, alkaline MT 0.190 Process Gaseous Emission Nitrogen, HCl and HF traces MT 0.100 Total Input MT 6.598 Total Output MT 6.598 168

iv. 1,1 difluoroethane (HFC - 152a) Process Description: 1, 1 difluoroethan (HFC 152a) will be filled and sold as finished goods. Material Balance: Input Output Key RM Product 1,1 difluoroethan (HFC 152a) MT 1.000 1,1 difluoroethan (HFC 152a) MT 1.000 Total Input MT 1.000 Total Output MT 1.000 v. Refrigerant blend of Difluoromethane (HFC-32) + Pentafluoroethane (HFC-125) (R410a) Process Description: In the process of R-410a, mixture of Difluoromethane (CH2F2, called R-32) and Pentafluoroethane (CHF2CF3, called R-125) and to get R-410a. Chemical Reaction: ½ CH2F2 + ½ CHF2CF3 -----------------> R-410a (CH2F2 + 50% CHF2CF3) MW: 52.02 MW: 120.02 MW: 72.6 Material Balance: Input Output Key RM Product R-32 MT 0.500 R410a MT 1.000 R-125 MT 0.500 Total Input MT 1.000 Total Output MT 1.000 169

vi. Refrigerant blend of Pentafluoroethane (HFC-125) + 1,1,1-Trifluoroethane (R143a) + 1,1,1,2 Tetrafluroethane (HFC 134a) (R404a) Process Description: In the process of R-404a, mixture 52 % 1,1,1-Trifluoroethane (C2H3F3, called R-143a), 44 % Pentafluoroethane (CHF2CF3, called R-125) and 4 % 1,1,1,2-Tetrafluoroethane (CH2FCF3, called R-134a) to get R-404a. Chemical Reaction: R-143a + R-125 + R-134a -------->R404a (52% R-143a, 44 % R-125 and 4 % R-134a) 84.04 120.02 102.03 97.6 Material Balance: Input Unit Quantity Output Unit Quantity Key RM Product R-125 MT 0.440 R-404a MT 1.000 R-143a MT 0.520 R-134a MT 0.040 Total Input MT 1.000 Total Output MT 1.000 vii. Refrigerant blend of Difluoromethane (HFC-32) + Pentafluoroethane (HFC-125) + 1,1,1,2 Tetrafluroethane (HFC 134a) (R407c) Process Description: In the process of R-407c, It will blend of Difluoromethane (R-32), Pentafluoroethane (R-125), and 1, 1, 1, 2-tetrafluoroethane (R-134a) to get R-407c. Chemical Reaction: R-32 + R-125 + R-134a ---------------------> R407c MW: 52.02 MW: 120.02 MW: 102.03 MW: 97.6 Material Balance: Input Output Product Key RM R-32 MT 0.230 R-407c MT 1.000 R-125 MT 0.250 R-134a MT 0.520 Total Input MT 1.000 Total Output MT 1.000 170

viii. Blend of 1,1-Difluoroethane (R152a) + 1,1,1,2 Tetrafluroethane (R134a) Process Description: R 134a (1112 - Tetrafluoroethane) blend with R 152 a (Difluoroethane) to get final. Material Balance: Input Output Key RM Product R-32 MT 0.500 Blend of R152a + R134a MT 1.000 R-125 MT 0.500 Spent Carbon Reagent Spent Carbon MT 0.001 Activated Carbon MT 0.001 Process Gaseous Emission Gas Nitrogen MT 0.001 Nitrogen MT 0.001 Total Input MT 1.002 Total Output MT 1.002 171

59. Butane (R600a) Process Description: Propane &butane can be separated from LPG as a raw material sourced from refineries. Due to the presence of ethane and n-butane along with the desired s, they should either be removed or converted to useful s. Ethane being the most volatile of all, removed in the first column, working at a pressure of approximately 26 MT/cm2G, as off gas. Alternatively, in case ethane is not present in the sourced LPG this column is not required. Now Propane (R290) is removed in the second column, working at a pressure of around 15 MT/cm2G and sent to storage, leaving primarily n-butane &butane in the remaining gas mixture. Since our of prime focus is butane (R600a), a conversion (isomerization) of n-butane to butane is required. "Hydrogen Once through Butamer Process" technology provided by UOP (Honeywell) is one of the processes which take care of the conversion from n-butane to butane. This conversion reactor containing high activity chloride-alumina catalyst works integrated with a stabilizer column which purge out the remaining gases to scrubber or used as fuel. This technology requires Hydrogen make-up for isomerization reaction. Therefore after recovery of butane in the third column working at a pressure of around 6 MT/cm2G the n-butane gas is sent to the isomerization unit and converted into butane. Alternatively potential market for n-butane can be explored in order to avoid the isomerization process. Also an additional flare system to be considered for hydrocarbon venting in case of plant trip, start-upshutdown etc. Storage vessels for propane, butane and n-butane will be Spherical type high pressure storage vessels (Kindly refer the vapour pressure of the components. Capacity & purity considered for the purpose of ASPEN simulation. 172

Material Balance: Input Output Key RM Product Liquefied Petroleum Gas MT 3.802 Butane (R600a) MT 1.000 Reagent By- Activated carbon MT 0.005 Propane (R290) MT 0.688 Ethane MT 0.084 Water n-butane MT 2.030 Process Water MT 2.000 Spent Carbon Gas Activated carbon MT 0.005 Nitrogen MT 0.100 Wastewater Aqueous Effluent, alkaline MT 2.000 Process Gaseous Emission Nitrogen MT 0.100 Total Input MT 5.907 Total Output MT 5.907 173

60. Propane (R290) Process Description: Propane &butane can be separated from LPG as a raw material sourced from refineries. Due to the presence of ethane and n-butane along with the desired s, they should either be removed or converted to useful s. Ethane being the most volatile of all, removed in the first column, working at a pressure of approximately 26 MT/cm2G, as off gas. Alternatively, in case ethane is not present in the sourced LPG this column is not required. Now Propane (R290) is removed in the second column, working at a pressure of around 15 MT/cm2G and sent to storage, leaving primarily n-butane &butane in the remaining gas mixture. Since our of prime focus is butane (R600a), a conversion (isomerization) of n-butane to butane is required. "Hydrogen Once through Butamer Process" technology provided by UOP (Honeywell) is one of the processes which take care of the conversion from n-butane to butane. This conversion reactor containing high activity chloride-alumina catalyst works integrated with a stabilizer column which purge out the remaining gases to scrubber or used as fuel. This technology requires Hydrogen make-up for isomerization reaction. Therefore after recovery of butane in the third column working at a pressure of around 6 MT/cm2G the n-butane gas is sent to the isomerization unit and converted into butane. Alternatively potential market for n-butane can be explored in order to avoid the isomerization process. Also an additional flare system to be considered for hydrocarbon venting in case of plant trip, start-upshutdown etc. Storage vessels for propane, butane and n-butane will be Spherical type high pressure storage vessels (Kindly refer the vapour pressure of the components. Capacity & purity considered for the purpose of ASPEN simulation. 174

Material Balance: Input Output Key RM Product Liquefied Petroleum Gas MT 5.525 Propane (R290) MT 1.000 Reagent By- Activated carbon MT 0.005 butane (R600a) traces MT 1.453 Ethane traces MT 0.122 Water n-butane traces MT 2.950 Process Water MT 2.000 Spent Carbon Gas Activated carbon MT 0.005 Nitrogen MT 0.100 Wastewater Aqueous Effluent, alkaline MT 2.000 Process Gaseous Emission Nitrogen MT 0.100 Total Input MT 7.630 Total Output MT 7.630 175

61. Blend of 1-Chloro-1,1-difluoroethane (R142b) + Chlorodifluoromethane (R22) Process Description: R 142 b (Chlorodifluoroethane) blends with R 22 (Chlorodifluoromethane) to get final. Material Balance: Input Key RM R 142 b (Chlorodifluoroethane) R 22 (Chlorodifluoromethane) Unit Quantity Output Unit Quantity Product MT 0.500 Blend of R142b + R22 MT 1.000 MT 0.500 Spent Carbon Reagent Spent Carbon MT 0.001 Activated Carbon MT 0.001 Process Gaseous Emission Gas Nitrogen MT 0.001 Nitrogen MT 0.001 Total Input MT 1.002 Total Output MT 1.002 176

62. Blend of 1,1,1,2 Tetrafluroethane (R134a) + Di Methyl Ether (DME) Process Description: R 134a (1112 - Tetrafluoroethane) blends with Dimethylether to get final. Material Balance: Input Unit Quantity Output Unit Quantity Key RM Product Dimethylether MT 0.500 Blend of R134a + DME MT 1.000 R 134a (1112- Tetrafluoroethane) MT 0.500 Spent Carbon Reagent Spent Carbon MT 0.001 Activated Carbon MT 0.001 Process Gaseous Emission Gas Nitrogen MT 0.001 Nitrogen MT 0.001 Total Input MT 1.002 Total Output MT 1.002 63. R&D Product Fluorospecialty R & D batches of various fluorine based agro intermediate will also be taken. These will be trial for their effectiveness and adverse reaction etc. and alternative routes will be trial again and again to get the proper specialty as per accepted norms. 177

64. Hydrofluoric Acid 20-70% Process Description: HF gas will generate as gas which will be absorbed in water to generate 20-70% HF solution. It shall be sold as. Chemical Reaction: HF + H 2 O HF Material Balance: Input Key RM Unit Quantity Hydrogen Fluoride MT 0.300 Water Process Water MT 0.700 Output Product Hydrofluoric Acid (20% to 70 %) Unit Quantity MT 1.000 Total Input MT 1.000 Total Output MT 1.000 65. Anhydrous Hydrochloric Acid Process Description: Anhydrous Hydrochloric Acid generated as primary route from Trichloroethylene (Product No. 53-i), Perchloroethylene (Product No. 53-ii), Pentafluoroethane (HFC 125) (Product No. 57-ii) and Difluoromethane (HFC - 32) (Product No. 57-iii), it shall be sold as. 178

Sr. No. 1 2 3 ANNEXURE: 3 WATER CONSUMPTION AND EFFLUENT GENERATION WATER CONSUMPTION Category Existing Water Consumpti on (KL/Day) Addition al Water Consump tion (KL/Day) Domestic 429 389 818 Gardening (drip irrigation)** Industrial a) UF RO water reused for process 0 215 215 2142 3163 5305 b) Cooling Tower 3838 2198 6036 c) Washings 71 69 140 CPP a) Boiler i) Boiler for 1985 706 2691 process ii) CPP* 1788 8572 10360 iii) DM & RO 883 4710 5593 Reject b) Cooling Tower 1662 3573 5235 Sub Total of CPP 6318 17561 23879 Total Proposed Water Consumption (KL/Day) Treated water to be reused. (KL/Day) Assuming 85 % efficiency of UF & RO Treatment for the Utilities Effluent stream, it gives 18460 KLD of treated water which will be reused and 3258 KLD reject. 4 Total 12798 23595 36393 18460 17933 * 1263 KLD UF/RO Treated reused in Boiler ** 650 KLD Treated Sewage utilization for Gardening 35 KL one time Requirement HBr- 168 Losses 650 STP 650 815 requirement gardening 35 KL Cond. Total Fresh Water Consumption (KL/Day) (1) 18460 KLD of water will be recovered after UF & RO treatment and taken back to the raw water collection tank. (2) Hence, 17933 KLD of fresh water will be consumed for the proposed expansion project. 179

Wastewater Generation Sr. No. Category Existing Waste Water Generation (KL/Day) Additional Waste Water Generation (KL/Day) Total Proposed Waste Water Generation (KL/Day) Treated water to be reused. (KL/Day) 1 Domestic** 340 310 650 650 KLD After its treatment in STP, it will be used for greenbelt development with drip irrigation system. 2 Industrial Total waste water Generation for Discharge (KL/Day) 100 % Domestic effluent will be reused in greenbelt development with drip irrigation system 3 i) Process 688 2003 2691 ii) Cooling Tower 691 955 1646 iii) Washing 71 69 140 Sub Total 2048 2429 4477 CPP a) Process Boiler 1985 706 2691 CPP Boiler 950 9410 10360 Assuming 85 % efficiency of UF RO Treatment for the Utilities Effluent stream, it gives 18460 KLD of treated water which will be reused and 3258 KLD reject. From 3258 KLD reject, 100 KLD reject utilization for Ash quenching & dust suppression. Hence, 4509 KLPD of waste water will be finally discharged to Sea through GIDC Sewer. (It includes the 1895 KLPD UF & RO reject & 2614 KLPD from Biological Treatment) b) Cooling Tower 400 1028 1428 c) DM & RO 923 4670 5593 Reject Sub Total 4258 15814 20072 We shall explore the possibility to recover water from 3158 KLPD reject of RO. It will give 1263 KLPD (40 %) recovered water for reuse and rest quantity 1895 KLPD along with treated waste water of 2614 KLPD, total 4509 KLPD will be discharge to GIDC drain. 4 Total (1+2+3) 6646 18553 25199 19110 4509 * 1263 KLD UF/RO Treated reused in Boiler ** 650 KLD Treated Sewage utilization for Gardening 180

WATER BALANCE DIAGRAM Fresh Water 17933 kl/d 18460 36393 kl/d recycled from HBr recovery 215 818 140 Gardening Domestic 33.76 kld Washing 18460 18644 11271 5305 Cooling Process Boiler Tower 2614 Water 33.76 HBr/Br Recovery 8197 Process & one time water need Evaporation Drying 215 650 17281 3074 Losses Losses 2691 140 Gardening 23186 Effluent Treatment Plants Evaportaion & losses in sludge 217 kl/d 22969 Waste Water Recycling Facility Recovered Water recycled in Utility SEA DISCHARGE 18460 kl/d 4509 kl/d 181

ANNEXURE: 4 ETP DETAILS Existing & Proposed effluent treatment plant scheme The existing& proposed domestic and industrial effluent treatment plant shall be treated with four different streams as following: 1. Low TDS with Low Organic effluent stream 2. High TDS with High Organic effluent stream 3. Utility Effluent stream generated by cooling tower and boiler blow down 4. Domestic effluent stream Detailed explanation, including technical details of each wastewater stream to be treated in Effluent Treatment Plant has been explained in further sections of this chapter. 1. Treatment Scheme for Low TDS with Low Organic effluent stream : Stage wise effluent characteristics details Parameter Unit Inlet effluent quality Physiochemical Treatment Secondary treated quality followed by Bio Tower Secondary treated quality followed by Activated Sludge Process Tertiary treated quality Final treated quality Flow (Existing) Cu. M 500 500 500 500 500 500 Flow (Additional Cu. M 2115 2115 2115 2115 2115 2115 Proposed) ph - 04 to 11 9 to 10 7.5 to 8.5 7 to 7.5 7 to 7.5 7 to 7.5 TSS mg/l 1000 < 100 < 100 < 100 < 100 < 100 TDS mg/l 3000 3000 3000 3000 3000 3000 NH4-N mg/l 500 400 40 20 20 20 BOD mg/l 4000 4000 1800 90 90 90 COD mg/l 5000 4000 2000 200 200 200 Fluoride mg/l < 50 < 10 < 10 < 10 < 10 < 10 182

Low TDS with low organic effluent treatment plant shall be establish for treatment of COD less than 5000 mg/l, TDS less than 3000 mg/l, Fluoride < 50 mg/l and also for heavy metals like antimony, zinc, nickel, copper, barium, lead and iron with combine physio-chemical, anaerobic and aerobic biological process and tertiary treatment system. The collected influent is equalized in collection by continuous air diffusion system. Equalization Influent coming from different plant pits is collected in equalization tank. Through equalization ph is stabilized and chemical requirements are minimized for neutralization. Physio-chemical treatment Hydroxide and sulphide treatment shall be provided for removal of heavy metals and fluoride. For this process hydrated lime and ferrous sulphate dosed for removal of suspended solid, fluoride and heavy metals. In this system calcium shall react with fluorides, hydroxide (OH - ) &sulphate shall react with heavy metals. Flash Mixer The colloidal particles present in effluent require coagulation for flocs to agglomerate. In flash mixer, the coagulants viz., non-ferric alum or PAC, shall be added under rapid mixing. Flocculator The coagulated effluent shall be then fed to Flocculator where polyelectrolyte shall be added under slow mixing for formation of flocs readily settleable. Sedimentation Process In Tube Settler; suspended solids, calcium fluoride (CaF) and heavy metals are removal by sedimentation through Primary Tube Settler. Settled solid (Suspended Solid, Calcium Fluoride and metal hydroxide or sulphide) shall be sent to Filter Press for dewatering. The SS free supernatant shall be collected and sent to the equalization tank. 183

Bio Tower A bio tower operates by having the wastewater fall through a packed bed tower filled with permeable packing. The packing has both aerobic and anaerobic microorganisms growing on it. The bio tower shall be operated with recycling. Bio towers use stationary filter media for the treatment of wastewater. The following are several steps that are often considered to improve nitrification: The fixed film reactor and activated sludge process shall be run in series. This will allow most of the BOD removal to occur in the first stage and improved nitrification to occur in the second stage. The amount of ventilation and hydraulic recirculation is increased and shall be operated by 10 times recycling of feed rate. This will allow nitrifying bacteria to operate at increased growth rates. Hydraulic dosing shall be increased by high recirculation rates. Shearing off of excessive bio-growth shall allow enhanced ventilation and promote new growth for added nutrient removal. Activated Sludge Process In activated sludge process wastewater containing organic matter is aerated in an aeration basin in which micro-organisms metabolize the suspended and soluble organic matter. Part of organic matter is synthesized into new cells and part is oxidized to CO2 and water to derive energy. In activated sludge systems the new cells formed in the reaction are removed from the liquid stream in the form of a flocculent sludge in secondary settling tanks. A part of this settled biomass, described as activated sludge is returned to the aeration tank and the remaining forms waste or excess sludge. Physio-chemical treatment The supernatant from ASP shall be then fed to Flocculator where PAC / sodium hypochlorite shall be added under slow mixing for formation of flocs and destruction of micro-organisms. Sedimentation The treated effluent shall be then fed to tube settler for tertiary SS removal. Sludge Decanting and Dewatering The primary sludge from primary tube settler and biological sludge from Activated Sludge Process shall be collected in the sludge holding tank, and then fed in to the Filter Press or decanter for dewatering. Leachate 184

shall be transferred to the equalization tank and the dewatered sludge shall be stored in impervious designated area. The dewatered calcium fluoride and metal content sludge shall be sent to secured landfill site or shall be sold to actual users by confirming of the heavy metal content. Stage-wise Low TDS with Low COD effluent treatment plant details Equalization Tank Primary Treatment Bio Tower Activated Sludge Process Tertiary Treatment Treated Effluent Quantity : 2615 KLD Quantity : 2615 KLD Quantity : 2615 KLD Quantity : 2615 KLD Quantity : 2615 KLD Quantity : 2615 KLD ph 4 to 11 ph 9 to 10 ph 7.5 to 8.5 ph 7 to 8 ph 7 to 8 ph 7 to 8 COD < 5000 mg/l COD < 4000 mg/l COD < 2000 mg/l COD < 200 mg/l COD < 200 mg/l COD < 200 mg/l BOD < 4000 mg/l BOD < 4000 mg/l BOD < 1800 mg/l BOD < 90 mg/l BOD < 90 mg/l BOD < 90 mg/l TSS < 1000 mg/l TSS < 100 mg/l TSS < 100 mg/l TSS < 100 mg/l TSS < 100 mg/l TSS < 100 mg/l Fluoride < 50 mg/l Fluoride < 15 mg/l Fluoride < 15 mg/l Fluoride < 15 mg/l Fluoride < 15 mg/l Fluoride < 15 mg/l NH4-N < 500 mg/l NH4-N < 400 mg/l NH4-N < 40 mg/l NH4-N < 20 mg/l NH4-N < 20 mg/l NH4-N < 20 mg/l Chemical Sludge Quantity : 65 MT Biological Sludge Quantity : 60 MT To GIDC Drain for Sea Disposal Press Filter Decanter Dewatered Sludge Quantity : 6.5 MT Disposed to Secured Landfill Site Dewatered Sludge Quantity : 6 MT Disposed to Secured Landfill Site Schematic Diagram of Low TDS with Low organic Effluent Treatment Plant 185

Details of Unit Size of Existing Low TDS with Low organic effluent stream S. No. Treatment Unit Unit No. Size Total Retention Time L B H KL In Day 1 Equalization Tank 1 12 12 3.8 547 1.09 2 Neutralization Tank 2 9.1 9.1 3.3 273 0.55 3 Flash Mixer 1 1.9 1.9 2.3 8 0.02 4 Flocculator 1 2.3 2.3 2.3 12 0.02 5 Tube Settler 1 4 4 2.5 40 0.08 6 Trickling Filter Feed Sump 1 9 9 2.75 223 0.45 7 Trickling Filter 2 14 7.6 1169 2.34 8 Aeration Tank 2 21 21 5.2 1800 3.60 9 Secondary Clarifier 2 5 3.4 67 0.13 10 Holding Tank 1 6.5 6.5 3.3 109 0.22 11 Tertiary Flocculator 1 2.1 2.1 2.8 10 0.02 12 Tertiary Tube Settler 1 4.5 4.5 3.6 57 0.11 13 Final Collection Tank 2 6.15 10 3.8 113 0.23 14 Sludge Collection Sump 1 10.2 4.2 3 245 0.49 15 Guard Tank 1 21 21 5 1731 3.46 16 Leachate Collection Tank 1 3.2 3.2 1.5 12 0.02 Details of Unit Size of Proposed Low TDS with Low organic effluent stream S. No. Treatment Unit Unit No. Total Retention Time KL 1 Equalization Tank 2 1157 1.09 2 Neutralization Tank 2 578 0.55 3 Flash Mixer 1 35 0.03 4 Flocculator 1 51 0.05 5 Tube Settler 2 85 0.08 6 Trickling Filter Feed Sump 1 942 0.89 7 Trickling Filter 2 2473 2.34 8 Aeration Tank 2 3807 3.60 9 Secondary Clarifier 2 141 0.13 10 Holding Tank 1 463 0.44 11 Tertiary Flocculator 1 41 0.04 12 Tertiary Tube Settler 2 121 0.11 13 Final Collection Tank 1 477 0.45 14 Sludge Collection Sump 2 518 0.49 15 Guard Tank 2 3661 3.46 16 Leachate Collection Tank 1 51 0.05 186

2. Treatment Scheme for High TDS with High Organic effluent stream : Stage wise effluent characteristics details Parameter Unit Inlet effluent quality Quantity (Existing) Quantity (Additional Proposed) Primary treated quality Stripper Column MEE Condensate ATFD Condensate ATFD Salt Cu. M 100 100 1 69 15 15 MT Cu. M 1346 1346 13 929 202 202 MT ph - 04 to 11 7 to 8 7 to 8 7 to 8 7 to 8 7 to 8 TSS mg/l 1000 < 100 < 100 < 100 < 100 - TDS mg/l 150000 150000 105000 3000 2500 - NH4-N mg/l 300 200 20 20 20 - COD mg/l 50000 45000 250000 5000 2500 - Organic % - - - - - < 20 % High TDS with high organic effluent treatment plant is establishing with physio-chemical, Stripper Column and Multi effect Evaporated with Agitated Thin Film Dryer process. The collected influent is equalized in collection by continuous air diffusion system. Equalization Influent coming from different plant pits with having COD less than 50000 mg/l and TDS less than 150000 mg/l are collected in equalization tank. Through equalization ph is stabilized and chemical requirements are minimized for neutralization. Physio-chemical treatment The equalized flow shall be fed to neutralization tanks for neutralization process. When ph is below 8, it is required to dose caustic soda 50 % or lime solution. When ph is above 9, it is required to dose recovered HCl. Flash Mixer The colloidal particles present in effluent require coagulation for flocs to agglomerate. In flash mixer, the coagulants viz., non-ferric alum or PAC, shall be added under rapid mixing. 187

Flocculator The coagulated effluent shall be then fed to Flocculator where polyelectrolyte shall be added under slow mixing for formation of flocs readily settleable. Sedimentation The effluent shall be then fed to tube settler for solids separation. Settled Solids removed from Primary Tube Settler to sludge holding tank. Feed Tank The primary treated clear overflow effluent collected in to Feed Tank. Quadruple Effect Evaporators with Agitated Thin Film Dryer The clarified effluent shall be pumped to Stripper Column through Pre-heaters for removal of low boilers. Condensate of stripper shall be collected in stripper condensate tank. It shall be disposed to CHWIF for incineration. The concentrated stream shall be fed in to Multi Effect Evaporated (MEE) column for evaporation. MEE condensate shall be collected in MEE condensate tank. It shall be transferred to Low TDS with low COD stream for further treatment. The MEE concentrated stream shall be fed in to Agitated Thin Film Dryer (ATFD). ATFD condensate shall be collected in to ATFD condensate tank. It shall be transferred to Low TDS with low COD stream for further treatment and the ATFD salt shall be disposed to secured landfill site. Sludge Decanting and Dewatering The primary sludge from primary tube settler shall be collected in the sludge holding tank, and then fed in to the Filter Press for dewatering. Leachate shall be transferred to the equalization tank and the dewatered sludge shall be stored in impervious designated area. Sludge should be disposed to secured landfill site. 188

Stage-wise High TDS with high COD effluent treatment plant details Equalization Tank Primary Treatment Stripper Column Quadruple Effect Evaporator Agitated Thin Film Dryer Quantity : 1446 KLD Quantity : 1446 KLD Quantity : 1446 KLD Quantity : 1432 KLD Quantity : 434 KLD ph 4 to 11 ph 7 to 8 ph 7 to 8 ph 7 to 8 ph 7 to 8 COD < 50000 mg/l COD 45000 mg/l COD < 45000 mg/l COD : < 40000 mg/l COD : < 125000 mg/l TDS < 100000 mg/l TDS < 100000 mg/l TDS < 100000 mg/l TDS < 105000 mg/l TDS < 400000 mg/l TSS < 1000 mg/l TSS < 100 mg/l TSS < 100 mg/l TSS < 100 mg/l TSS : < 100 mg/l NH4-N < 300 mg/l NH4-N 200 mg/l NH4-N < 20 mg/l NH4-N < 20 mg/l NH4-N : < 20 mg/l ATFD Salt Quantity : 217 MT Organic Content : < 20 % ph : 7 to 8 Chemical Sludge Quantity : 31 MT Condensate Quantity : 14 MT Organic Content : 25 % Condensate Quantity : 998 MT Organic Content : 0.7 % Condensate Quantity : 217 MT Organic Content : 0.25 % Disposed to Secured Landfill Site Press Filter Disposed to CHWIF for Incineartion Sent to Low TDS with low COD Stream Sent to Low TDS with low COD Stream Dewatered Sludge Quantity : 3.1 MT Disposed to Secured Landfill Site Schematic Diagram of High TDS with High organic Effluent Treatment Plant Details of Unit Size of Existing High TDS with High organic effluent stream S. Treatment Unit Unit Size Total Retention No. No. L B H KL Time in Day 1 Equalization Tank 1 7.9 7.9 4.1 256 2.56 2 Neutralization Tank 2 6.05 6.05 3.3 121 1.21 3 Flash Mixer 1 1.35-2.3 3 0.03 4 Flocculator 1 1.65-2.3 5 0.05 5 Tube Settler 1 3.5 3.5 2.5 31 0.31 6 Feed Tank 1 7.9 7.9 3.9 243 2.43 7 Condensate Tank 1 3.5 4.25 3.5 52 0.52 8 Sludge Collection Sump 1 4.6 2.3 2.3 24 0.24 9 Leachate Collection Tank 1 1.5 1.5 1.5 3 0.03 10 Quadruple Effect Evaporator with 1 - - - 100 1.00 ATFD 189

BASIS OF DESIGN 100 KLD Multi Effect Evaporator with Agitated Thin Film Dryer We have considered 5500 kg/hr feed with the inlet of 1 % w/w Low boilers (Solvent). We have considered for the design basis as Solvent 1 % w/w. Stripper Section Type of System : Packed Bed type stripper system CAPACITY : Organics : (55 kg/hr Solvent + 55 kg/hr Water) Feed Rate : 5500 Kg/hr (15% w/w TDS) FEED PROPERTIES : Organics : 1 % w/w basis. (Solvent) Low Boilers Solvent : Water Specific Gravity : 1.15 Temperature : 30 C Viscosity : 4-6 cp TOP PRODUCT FROM STRIPPER : Organics : (55 kg/hr Solvent + 55 kg/hr Water) Temperature : 50-55 C BOTTOM PRODUCT FROM STRIPPER (TO : EVAPORATOR) OPERATING CONDITIONS : Mode of Heating : Steam Steam : 150 kg/hr @ Dry Saturated at 3 bar (g) Power (Installed/ Absorbed) : 16 KW / 13 KW Cooling Water : 12 m3/hr MATERIAL OF CONSTRUCTION : All contact parts : Duplex steel Vapour / Condensate : SS 316L Evaporated Section Type of System : Four effect Forced circulation evaporator CAPACITY (Evaporation Plant) Evaporation Rate : 3850 kg/hr Feed Rate : 5500 Kg/hr Product Rate : 1650 Kg/hr (50%w/w solids) FEED PROPERTIES Solid Content Range (w/w) : 15 % w/w ( TSS less than 500 ppm)(cod : 80000 to 100000 mg/lit) Form : Clear Solution with totally dissolved solids 190

Solvent : Water Specific Gravity & PH : 1.15 & Min. 6.5 and Max. 7.5 Viscosity 4-6 cp (assumed) Temperature : 30 C OPERATING CONDITIONS Mode of Heating : Dry Saturated Steam at 3 kg/cm2 (g) MATERIAL OF CONST. : Feed/ Product : Duplex steel Vapour Liquid Separators : SS 316L Non-contact parts : SS 316L UTILITY SPECIFICATIONS Power (Evaporator) : Voltage : 415 / 4 wire Frequency: 50 HZ Connected Load : 68 kw Consumed Load : 54.5 kw Steam (Evaporator) : Dry Saturated at 3.0 kgs/cm2 (g) Before Control valve Cooling water Space Requirement Normal at 2 kgs./sq.cm(g) Inlet temp 32 C /Outlet temp. 37 C Make up & Seal water : 15 ml x 12 mw x 15 mh : 1170 kg/hr : 120 m3/hr. 1.2 m3/hr : Agitated Thin Film Dryer Section CAPACITY : 915 kg/h WATER EVAPORATION FEED RATE : 2000 kg/h INITIAL SOLIDS : 50 % FINAL MOISTURE IN DRY PRODUCT : 5-10 % WATER EVAPORATION : 915 kg/h DRY SOLID OUTPUT : 1085 kg/h DRY SATURATED STEAM REQUIREMENT At 7 kg/cm2-g PRESSURE : 1100 kg/h ELECTRICAL LOAD : 47 kw (Each) NORMAL CONSUMPTION : 38 kw (Each) COOLING WATER CIRCULATION RATE AT 32 C - 37 C : 100 m3/h COOLING WATER INLET TEMP : 32 C COOLING WATER OUTLET TEMP : 37 C 191

Technical Specifications (Mechanical) Jacket temperature 250 C (Design) Jacket pressure 15 kg/cm2-g (Design) Surface area 20 square meters (Approximately) 2 nos. Rotor Design High Performance hinged blades (dryer type) Rotor speed approximately 270-300 rpm Distributor Distribution ring Power 38 KW, 415V 50Hz Top bearing Taper Roller type Bottom bearing Roller type OR Bush bearing Agitated Thin Film Dryer (Section A) Agitated Thin Film Dryer 20 m2 2 nos. Inner Shell: SS 316L Outer Shell: SS 316L (Quoted Separately) Accessories (Section B) Balance Tank for Feed 1 no. SS 316L Vapour Exhaust Duct (1 Lot) 1 no. SS 316L Blower 1 no. SS 316L SS Pipes & Fittings (Sch 10 1 lot) 1 no. SS 316L (Sch. 10) Surface Condenser 1 no. Shell: SS 316L, Tubes: Duplex Steel Tube Sheet: Duplex Steel Details of Unit Size of Proposed High TDS with High organic effluent stream S. No. Treatment Unit Unit No. Total KL Retention Time in Day 1 Equalization Tank 2 1800 2.57 2 Neutralization Tank 2 850 1.21 3 Flash Mixer 1 25 0.04 4 Flocculator 1 40 0.06 5 Tube Settler 1 225 0.32 6 Feed Tank 2 850 1.21 7 Condensate Tank 1 370 0.53 8 Sludge Collection Sump 1 170 0.24 9 Leachate Collection Tank 1 25 0.04 10 Quadruple Effect Evaporator with ATFD 2 500 1 11 Quadruple Effect Evaporator with ATFD 4 100 1 192

BASIS OF DESIGN 500 KLD Multi Effect Evaporator with Agitated Thin Film Dryer We have considered 27778 kg/hr feed with the inlet of 1 % w/w Low boilers (Solvent). We have considered for the design basis as Solvent 1 % w/w. Stripper Section Type of System : Packed Bed type stripper system CAPACITY : Feed Rate (15% w/w TDS) : 27778 kg/hr OPERATING CONDITIONS : Mode of Heating : Steam Steam @ Dry Saturated at 3 bar (g) : 760 kg/hr Evaporation Section Type of System : Four effect Forced circulation evaporator CAPACITY (Evaporation Plant) Evaporation Rate : 19444 kg/hr Feed Rate : 27778 kg/hr Product Rate (50%w/w solids) : 8333 kg/hr FEED PROPERTIES Solid Content Range (w/w) : 15 % w/w ( TSS less than 500 ppm)(cod : 80000 to 100000 mg/lit) Specific Gravity & PH : 1.15 & Min. 6.5 and Max. 7.5 OPERATING CONDITIONS Mode of Heating : Dry Saturated Steam at 3 kg/cm2 (g) Steam (Evaporator) : Dry Saturated at 3.0 kgs/cm2 (g) Before Control valve : 5850 kg/hr ATFD Section AGITATED THIN FILM DRYER : CAPACITY (Water Evaporation) : 4600 kg/hr FEED RATE : 10000 kg/hr INITIAL SOLIDS : 50% FINAL MOISTURE IN DRY PRODUCT : 5-10 % WATER EVAPORATION : 10000 DRY SOLID OUTPUT : 5400 kg/hr DRY SATURATED STEAM REQUIREMENT At 7 kg/cm2-g PRESSURE : 5500 kg/hr 193

3. Treatment Scheme for Utility Effluent generated from DM/Softener, cooling tower and boiler blow down: Stage wise effluent characteristics details Parameter Unit Inlet effluent Primary treated Permeate Concentrated quality quality treated quality treated quality Flow (Existing) Cu. M 2850 2850 2422 428 Flow (Additional Cu. M 18868 Proposed) 18868 16038 2830 ph - 7 to 8 7 to 8 6 to 7 7 to 8 TSS mg/l 100 < 50 Nil Nil TDS mg/l 2500 2500 < 225 < 16500 COD mg/l 50 25 < 5 < 100 Utility Effluent (from DM / Softener reject, cooling Tower and Boiler Blow Down) treatment plant is established with physio-chemical, Ultrafiltration and Reverse Osmosis process. The collected influent is equalized in collection by continuous air diffusion system. Equalization Utility waste water, DM plant waste water and blow downs from boiler and cooling tower shall be collected in collection tank. Physio-chemical treatment Acid, Alkali & coagulant pump shall be provided to pump Acid, Alkali & coagulant dosing in ph control tank. ph tank stirrer shall be provided to mix effluent & chemicals in the tank. ph indicator shall be provided in tube stirrer ph shall be interlocked with Acid & Alkali dosing pumps. Sedimentation Mix effluent from ph control tank shall overflow in tube settler. We are providing tube settler with cool deck media for better setting of suspended solids in tube settler. Settler sludge at bottom of tube settler shall be pumped in filter press feed sump. Filter Feed Sump: Tube settler shall over flow to filter feed sump collected effluent shall be pumped to dual media filter. For removing of suspended solids, turbidity & smell. We are providing dual media filter with one working & one 194

stand by condition. This dual media is periodically required to be cleared of accumulated solids by back washing the filter using fresh water in reverse flow sequence. Ultrafiltration System: Ultrafiltration (UF) is a form of filtration that uses a membrane to separate different fluids or ions. Ultrafiltration is not as fine a filtration process as Nano filtration, but it also does not require the same energy to perform the separation. Ultrafiltration also uses a membrane that is partially permeable to perform the separation, but the membrane's pores are typically much larger than the membranes pores that are used in Nano filtration. Ultrafiltration is most commonly used to separate a solution that has a mixture of some desirable components and some that are not desirable. One of the uses that demonstrate the usefulness of Ultrafiltration is separation of oil in an emulsion from water. In this case, oil emulsions, for example, machining coolant emulsions can have the oil separated and concentrated, with the water phase being discharged to sanitary sewer, and the concentrated oil phase being disposed of at a lower cost. Ultrafiltration is capable of concentrating bacteria, some proteins, some dyes, oils and colloidal or emulsified components. Ultrafiltration is only somewhat dependent upon the charge of the particle and is much more concerned with the size of the particle. Ultrafiltration is typically not effective at separating dissolved organic streams. Reverse Osmosis System: Reverse osmosis is a membrane separation process for removing solvent from a solution. When a semi permeable membrane separates a dilute solution from a concentrated solution, solvent crosses from the dilute to the concentrated side of the membrane in an attempt to equalize concentrations. The flow of solvent can be prevented by applying an opposing hydrostatic pressure to the concentrated solution. The magnitude of the pressure required to completely impede the flow of solvent is defined as the "osmotic pressure". If the applied hydrostatic pressure exceeds the osmotic pressure (see figure below), flow of solvent will be reversed, that is, solvent will flow from the concentrated to the dilute solution. This phenomenon is referred to as Reverse Osmosis. The figure illustrates the concepts of osmosis, osmotic pressure and reverse osmosis schematically. 195

Sludge Decanting and Dewatering The primary sludge from primary tube settler shall be collected in the sludge holding tank, and then fed in to the Filter Press for dewatering. Leachate shall be transferred to the equalization tank and the dewatered sludge shall be stored in impervious designated area. Sludge should be disposed to secured landfill site. Stage-wise Utility effluent treatment plant details Equalization Tank Primary Treatment Ultrafiltration Reverse Osmosis Reject Water Quantity : 21718 KLD Quantity : 21718 KLD Quantity : 21718 KLD Quantity : 21718 KLD Quantity : 3258 KLD ph 7 to 8 ph 7 to 8 ph 7 to 8 ph 7 to 8 ph 7 to 8 COD < 50 mg/l COD < 25 mg/l COD < 25 mg/l COD < 25 mg/l COD < 100 mg/l TDS < 2500 mg/l TDS < 2500 mg/l TDS < 2500 mg/l TDS < 2500 mg/l TDS < 16500 mg/l TSS < 100 mg/l TSS < 50 mg/l TSS Nil TSS Nil TSS Nil Chemical Sludge Permeate Water To GIDC Drain for Sea Quantity : 54 MT Quantity : 18460 MT Disposal ph 6 to 7 COD < 5 mg/l Press Filter TDS < 225 mg/l TSS Nil Dewatered Sludge Quantity : 5.4 MT Disposed to Secured Landfill Site Reuse in Cooling Tower Make up / Process 196

Details of Unit Size of Existing Utility effluent treatment plant S. No. Treatment Unit Unit No. Total, KL Retention Time 1 Effluent Collection Tank 1 1500 0.53 2 ph Control Tank 1 5 0.00 3 Tube Settler 1 40 0.01 4 Filter Feed Sump 1 100 0.04 5 Permeate Tank 1 800 0.28 6 Reject Tank 1 1000 0.35 7 Ultra-Filtration 4 1000 m2 Hollow-Fibre PES - Membranes in PVC Housing 8 Reverse Osmosis Module 3 4 : 2 Array with 36 nos. 8 dia. x 40 L - Low Fouling Brackish Water membranes Details of Unit Size of Proposed Utility effluent treatment plant S. No. Treatment Unit Unit No. Total, KL Retention Time 1 Effluent Collection Tank 2 5000 0.53 2 ph Control Tank 1 40 0.004 3 Tube Settler 1 270 0.03 4 Filter Feed Sump 1 670 0.07 5 Permeate Tank 1 5500 0.58 6 Reject Tank 2 3500 0.37 7 Ultra-Filtration 3 7000 m2 Hollow-Fibre PES - Membranes in PVC Housing 8 RO Module 3 - - 197

4. Treatment Scheme for Domestic effluent stream : Stage wise effluent characteristics details Parameter Unit Inlet Secondary Activated Ultrafiltration Final effluent treated quality Carbon treated quality followed by Tower treated quality Fluidized treated quality Membrane Bioreactor quality Flow (Existing) Cu. M 150 150 150 150 150 Flow (Additional Cu. M 500 Proposed) 500 500 500 500 ph - 8 to 9 7 to 8.5 7 to 8.5 7 to 8.5 7 to 8.5 TSS mg/l 300-400 < 10 < 10 < 1 < 1 BOD mg/l 300-500 < 30 < 20 < 20 < 20 Collection Tank: Raw sewage from the plant through the pipeline comes to the collection tank. The sewage with the help of cutter pump (1 Working + 1 Stand by) transfer to bar Screen chamber Bar Screen: Raw sewage from the source is usually received into the bar screen chamber by gravity. Screen provided will remove all floating and big size matter such as plastic bottles, polythene bags, glasses, stones, etc., which may otherwise choke the pipeline and pumps. Oil & Grease Trap: If the sewage generated includes maximum quantity from kitchen and canteen, there is a possibility of higher concentrations of oil and grease in the raw sewage. It needs to be removed before biological treatment as it otherwise may cause problems for biological treatment. A small tank with a baffle wall is need for oil & grease trap. Equalization: Sewage with having BOD between 300 500 mg/l and TSS between 300 400 mg/l is collected in equalization tank. Through equalization ph is stabilized and chemical requirements are minimized for neutralization. 198

Fluidized Membrane Bio Reactor (FMBR): In this system raw sewage enters at the top of the tank. Air is introduced at the bottom of the tank through floating type diffused aeration system. Media will be in suspension because of the turbulence created by the air. The bacteria required for the oxidation of the organic matter is attached to the media and some part is suspended in the tank. After oxidation, the bacteria grow in number and need to be separated from the aeration tank liquor. The lamella section inside the biological reactor helps in clarification and separation of the bacteria (sludge) and clear overflow flows into chlorine contact tank. Lamella plates helps in increasing the settling area and removing the particles effectively in a smaller plan area. Alum dosing of around 5-6ppm in the clarifier for improving the settling of suspended solids. In chlorine contact tank, Sodium hypo Chlorite (NaOCl) is added for disinfecting the clarified sewage. 10% concentration of NaOCl with 10-15ppm dosage is in Chlorine Contact tank. Tertiary Treatment: Multi Grade Sand Filter Function: Filtration of suspended particle. Water with the help of filter feed pump is transferred to MGF. Activated Carbon Filter Function: Deodorization, Decolourization & Dechlorination After ACF, the water pass through UF, this acts as filter assisting in further reduction of BOD, COD, & TSS. Treated Water Collection Tank: The treated sewage water shall be collected in treated water collection tank for reuse in Gardening or in monsoon season it shall be treated with Utility effluent stream for further reuse. Sludge Decanting and Dewatering: The sludge from the Clarifier to be removed from the bottom of the Clarifier and transferred to sludge drying bed. Sludge fed in to the centrifuge for drying of the sludge & the dried sludge may be used as manure for development of greenbelt & the substrate may be recycled back to the equalization tank. 199

Stage-wise Domestic effluent treatment plant details Inlet Influent Quality Secondary Treatment Activated Carbon Tower Ultrafiltration Treated Effluent Quantity : 650 KLD Quantity : 650 KLD Quantity : 650 KLD Quantity : 650 KLD Quantity : 650 KLD ph 8 to 9 ph 7 to 8.5 ph 7 to 8.5 ph 7 to 8.5 ph 7 to 8.5 BOD 300 to 500 BOD < 30 BOD < 20 BOD < 20 BOD < 20 TSS 300 to 400 TSS < 10 TSS < 10 TSS < 1 TSS < 1 Biological Sludge Quantity : 13 MT Centrifuge to reuse in Gardening or in monsoon season it shall be treated with Utility Effluent Dewatered Sludge Quantity : 1.3 MT Use as Manure Schematic Diagram of Sewage Treatment Plant 200

Details of Unit Size of Existing Sewage effluent treatment plant S. No. Treatment Unit Unit No. Size Total Retention Time L B H KL 1 Collection Tank 1 2 7.7 2.6 40 0.27 2 Manual Screen Bar 1 0.9 0.6 0.5 0.3 0.002 3 Oil & Grease Trap 1 1.7 3.6 3.5 21 0.14 4 Equalization Tank 1 10 5 3 150 1.00 5 Aeration Tank 1 2.2 6 2.5 33 0.22 6 Tube Settler 1 2.2 2.2 2.5 12 0.08 7 Chlorine Contact Tank 1-5 0.03 8 Activated Carbon Tower 1-2 - 9 Multi Grade Filter 1-2 - 10 Ultrafiltration Unit 1 - - - 11 Treated water collection tank 1 10 5 3 150 1.00 Details of Unit Size of Proposed Sewage effluent treatment plant S. No. Treatment Unit Unit No. Size Retention Time KL 1 Collection Tank 1 500 1.00 2 Manual Screen Bar 1 1.0 0.00 3 Oil & Grease Trap 1 71 0.14 4 Equalization Tank 1 500 1.00 5 Aeration Tank 1 150 0.30 6 Tube Settler 1 40 0.08 7 Chlorine Contact Tank 1 7 0.01 8 Activated Carbon Tower 1 7 0.01 9 Multi Grade Filter 1 - - 10 Ultrafiltration Unit 1 - - 11 Treated water collection tank 1 500 1.00 Mode of disposal Mode of disposals as available for which provision of Effluent Treatment System is envisaged is as follows: 4509 KLD effluents after treatment sent to GIDC sewer line Dahej Vilayat pipe line / Common Disposal System up to the sea. All solid wastes as well as ETP/MEE sludge will be sent to TSDF facility. 201

Online flow meter Online flow meter has been provided at final outlet of ETP. Rainwater Harvesting Rainwater harvesting is a mechanism involved in collecting, storing and using rainwater when it is most needed. A rainwater harvesting system comprises of various stages transporting rainwater through pipes or drains, filtration, and storage in tanks for reuse. It is proposed to have Roof-top rain water harvesting at site. We have considered only the Roof tops of the clean terraces for rain water harvesting considering the chemical industry. The roof-top rain water will transfer through a network of pipes linked through storm water drain. The storm water connected to storm water collection sump. Rain water will be transferred from collection tank to Utility collection tank for reuse. We collect the first rain water in collection tank through storm water drain and reuse it after appropriate treatment. 202