Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
PRE-FEASIBILITY REPORT
For
PROPOSED 300 KLPD DISTILLERY PLANT (MOLASSES BASED)/200 KLPD MOLASSES AND 100 KLPD GRAIN ALONG WITH 12.0 MW COGENERATION POWER PLANT
Project Proponent:
DSM SUGAR RAJPURA (A unit of Dhampur Sugar Mills Limited) Rajpura, District-Sambhal
(April, 2019)
Environmental Consultant:
ENVIRO INFRA SOLUTIONS PVT.LTD. Accredited by NABET (Quality Council of India) for EIA studies as ‘A’ Category Consultant (S. No. 48th, as on March, 2019) Address: - 301, 302 & 305, SRBC, Sec.-9, Vasundhara, GZB-201012 Ph.: 0120-4151183 Email: [email protected] Website: www.enviroinfrasolutions.com
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
SUMMARY
1 Dhampur Sugar Mills Ltd. (DHAMPUR) is a company registered under Indian Companies Act, 1956 (Now under the Companies Act, 2013) having its Registered Office at Dhampur Distt. Bijnor. The Company has a sugar Mill at Rajpura Distt. Sambhal.
2 The company is proposing a new distillery plant of 300 KLPD Molasses / Grain based with option of 300 KLPD molasses based or 200 KLPD Molasses based and 100 KLPD Grain based along with 12.0 MW Cogeneration Power at their existing Sugar Mill at Village & Block Rajpura, Tehsil Gunnaur , District Sambhal, Uttar Pradesh. The co- ordinates of site are 28°21'26.63"N and 78°22'50.11"E.
3 Total 45 acres (18.21 ha) land is required for proposed project and out of which 20 acres is existing industrial land in possession of promoters adjacent to existing sugar mill and rest 25 acres of agricultural land will be converted to industrial use after taking due permissions. The benefits of the location are as below;
Required raw material is abundantly available in the nearby adjoining area. Good availability of groundwater Well connected by road/rail network Proximity to spirit and ethanol consuming market Manpower available for industrial purposes Availability of basic Infra Structure with the existing Sugar Mill
4 The molasses based distillery process will have process steps namely - molasses receiving and storage, fermentation, multi-pressure distillation, multi-effect evaporation, spirit storage. Grain based distillery process will have process steps namely - grains receiving and storage, grains handling and milling, slurry preparation/liquefaction, scarification and instantaneous fermentation, fermentation, multi-pressure distillation, decantation, multi-effect evaporation, spirit storage.
5 The industry will generate 12.0 MW power from incineration boiler based cogeneration power plant. Bagasse/coal/rice husk would be used as support fuel @ 30 % along with concentrated spent wash @ 70 % for the boiler furnace.
6. The industry would require utilities for 300 KLPD molasses based or 200 KLPD Molasses and 100 KLPD grain based with the capacity of water treatment plant (DM plant) @ 1125 m3/day and that of cooling towers @ 12000 m3/Hour.
7. The distillery will use molasses as basic raw material. Besides this, processing chemicals would be used for the production of ethanol and other Distillery products. The daily fuel requirements for the 90 TPH boiler furnaces would be around 2110 cum/ day conc. spent wash along with 500 MT/Day (bagasse) or 300 MT/Day (coal).
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
8. The fresh water requirements of the industry would be around 2095 (max) m3/day. The source of fresh water will be ground water.
9. Waste water in the form of spent lees (360 m3/day), MEE condensate (1470 m3/day) would be generated. Besides this, misc. effluent such as floor/fermenter washing effluent @ 50 m3/day, cooling tower blow down @ 75 m3/day, DM plant Reject water @ 75 m3/day and boiler blow down @ 50 m3/day would be generated.
10. The industry will proposed two nos. of Multiple Effect Evaporators of 2200 m3/day capacity (1100 m3/ day X 2), which is sufficient for the treatment of spent wash, thereby maintaining the Distillery as ZERO EFFLUENT DISCHARGE INDUSTRY. The spent lees and MEE condensate would be reused in the process after treatment in CPU combined with Bio Composting of concentrated Spent Wash as per Norms./SOP prescribed by the MoEF&CC vide OM dated 04.09.2018 and dated 25.03.2019.
11. The estimated cost of proposed distillery project and cogeneration of 12 MW of power would be around Rs. 325.87 Cr.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
CHAPTER – 1
INTRODUCTION
Dhampur Sugar Mills Ltd. (DHAMPUR) is an agro based industry having started their operations in the year 1933 with a 300 TCD sugar mill located at Dhampur, Uttar Pradesh in North India. The company has a successful track record of about seven decades of efficient operation. During this period, it has grown into one of the largest sugar manufacturing groups in India, owning at present five sugar mills in the State of Uttar Pradesh with a combined cane crushing capacity of more than 45,500 TCD with Bagasse based power cogeneration Units in all five Sugar Units.
With the passage of time, Dhampur Sugar Mills Ltd. (DHAMPUR) has diversified into molasses based chemicals manufacturing, by setting up a distillery facility for alcohol & alcohol based chemicals, such as Ethyl acetate.
The company is proposing distillery plant of 300 KLPD molasses based/200 KLPD molasses based and 100 grain based along with 12.0 MW Cogeneration Power Plant at Village & Block Rajpura, & District Sambhal, Uttar Pradesh.
The distillery will be based on most modern technologies and the state of art features. Project will result in higher efficiencies, energy conservation and Zero Effluent Discharge. Raw materials i.e. molasses and bagasse will be sourced from the sugar mill located within the plant, other sugar plants of the group and from other sugar mills located nearby.
The estimated cost of proposed project would be around Rs 325.87 Crores. The project would be installed and commissioned within 8 to 12 months from the date of receipt of Environmental Clearance from the Ministry of Environment, Forests & Climate Change, New Delhi.
The industry would operate for 365 days in a year. The distillery plant would require a power input of around 12 MW which would be available from their in-house co-generation power plant.
Table1: Salient Features of the Project
S. No. Particulars Details 1. Nature & Size of the Project Proposed New 300 KLPD molasses based/200 KLPD molasses based and 100 grain based along with 12.0 MW Cogeneration Power Plant at Village & Block Rajpura, & District Sambhal, Uttar Pradesh. 2. Category of the Project Sr. No. 5(g); Category ‘A’ 3. Location Details Village Rajpura Block Rajpura Tehsil Gunnaur District Sambhal
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
State Uttar Pradesh Latitude 28°21'26.63"N Longitude 78°22'50.11"E Toposheet No. H44S7 4. Total Plant Area Total 45 acres (18.21 ha) land is required for proposed project and out of which 20 acres is existing industrial land and rest 25 acres of agricultural land will converted to industrial use. 5. Greenbelt / Plantation Area 14.85 Acres, i.e. ~33% of the project area will be covered under greenbelt/ plantation 6. Environmental Setting Details Nearest Village Rajpura Nearest Town & City Anupshahar (10.5 km in west direction) Nearest National Highway / NH 93 (10 km) State Highway Nearest Railway station Babrala Railway Station (10.3 km, aerial) Indira Gandhi International Airport, New Delhi Nearest Airport (Approx. 126.0 Km, aerial) National Parks, Wildlife No National Parks, Wildlife Sanctuaries, Sanctuaries, Conservation Conservation Reserves, Tiger / Elephant Reserves, Tiger/Elephant Reserves fall within 10 km radius from the plant Reserves site River / Water Body (within 10 km Ganga River – 10 km radius) 7. Products to be manufactured Ethanol/RS/ENA – 300 KLPD Cogeneration of power – 12 MW 8. By Products Conc. spent wash – 600 m3/day KLD, DDGS – 60 MT/day 9. Raw Material Consumption Molasses – upto 1350 MT/day Chemicals - enzymes (@28 kg/day), Sulphuric Acid (@8050 kg/day), Urea (@395 kg/day), anti- foam agent (@1400 kg/day), yeast (@700 kg/day and DPA @ 130 kg/day) 10. Fuel Consumption Conc. Spent Wash 34.5 MT/hour and Bagasse- 20.8 MT/hour or Coal – 12.5 MT/hour 11. Water Requirement & Source Fresh water requirement is 2095 KLD will be met through bore well after taking necessary permission from CGWA. 12. Quantity of Effluent generation Spent Wash @ 2070 m3/day 13. Disposal of treated effluent Concentrated Spent Wash will be used as fuel in Boiler & condensates to be reused for dilution of molasses and cooling tower make-up after treating in CPU.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
14. Details of process emissions Process emissions from boiler furnace of 90 TPH capacities 15. Proposed air pollution control Bag Filter, Stack height – 80 meters device along with stack height 16. Cost of the Project: Rs (in 325.87 Crores) 17. Working Days 365 days / annum
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
CHAPTER – 2
PROJECT LOCATION
Dhampur Sugar Mills Ltd. are 300 KLPD molasses based/200 KLPD molasses based and 100 grain based along with 12.0 MW Cogeneration Power Plant at Village & Block Rajpura, & District Sambhal, Uttar Pradesh. The company is already having 20 acres land at the existing location and rest 25 acres land will be converted from agriculture to industrial use for the proposed project.
2.1 SELECTION OF SITE
The basic criteria for the selection of site for the molasses/grain based distillery plant and cogeneration power plant are as below;
a) Raw material and biomass availability b) Raw material cost c) Transportation cost d) Accessibility to markets within and nearby states e) Availability of water f) Availability of land in abundance g) Connectivity of road/rail network. h) Market for final Product Advantages of the location at Village & Block Rajpura, Tehsil Gunnaur & District Sambhal, Uttar Pradesh for proposed project. The promoters of the project are already having around 20 acres of land Village & Block Rajpura, Tehsil Gunnaur & District Sambhal, Uttar Pradesh. Besides this, the other benefits of the location are as below; a. Required raw material is available at site and nearby adjoining area. b. Good availability of ground water c. Well connected by road/rail network d. Govt. of India support for Ethanol for mixing in fuel gasoline e. Manpower available for industrial purposes
2.2 DETAILS OF ALTERNATIVE SITES
The proposed project will be done within the existing plant premises/acquiring adjacent agriculture land. Therefore, no alternative site has been considered by the company. The following points justify implementation of the project: Proposed project is located adjacent to the company owned existing sugar mill. Easy availability of raw material i.e. molasses from the existing and nearby sugar mill(s). Nearness to NH-93 (within 10.0 km) and State Highway SH-39 (within 12.0 km) makes it easier to transport raw materials & final product to market. There is no National Park, Wildlife Sanctuary, Conservation Reserves and Tiger Reserves within 10 km radius of the project site.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
2.3 SITE DETAILS
The plant site is located around 1.5 Km away from Rajpura Town. The connectivity of the site to airport, railway and road is as follows: a. Airport connectivity- The nearest airport is Indira Gandhi International Airport, New Delhi which is about 126 Kilometers (aerial). b. Rail connectivity- The nearest railway station is Babrala Railway Station, which is about 10.3 kilometers from the site. c. Road connectivity- Nearness to NH-93 (within 10.0 km) and State Highway SH- 39 (within 12.0 km). d. Police Station – Rajpura Kotwali at the distance 1.5 km. e. Hospital- Government PHC & CHC within 1.5 to 3.0 km in Rajpur Town. f. Schools, Colleges, Bank, ATM, Dispensaries, Hospitals, Markets, Police Station & Places of Worship in nearby area of the project site.
Topography & Climate: The Topography of the area is mainly a plain. The project area has a pleasing climate with cool and foggy winter and generally hot and humid summer. The wet session starts from July to October during which the area receives rainfall. The temperature of the project area is varying from 480C in summer and 30C in winter.
2.4 UTILIZATION OF LAND
The distillery plant can be divided into four sections w.r.t land utilization i.e. (1) boiler area (2) process and distillation area (3) utilities and (4) green area. The industry has planned the new ethanol plant in their existing 20 acres of land and additional 25 acres adjacent land. The detailed breakup of the land for various uses would be as follows;
S.No. Particulars Land Area (Acres) 1. Area for plantation/green area 14.85 2. Area for roads/open spaces 2.3 3. Area for fuel/ash storage 9.5 4. Boiler & Cogeneration Plant 1.0 5. Area for other plant and machinery 17.35 Total land area 45
2.5 NEED FOR THE PROJECT The Government of India, through Oil Marketing Companies (OMCs), is implementing the Ethanol Blended Petrol (EBP) Programme under which, OMCs sell ethanol blended petrol with percentage of ethanol upto 10%. The Government has fixed the price of ethanol for the ethanol supply year 2016-17 at Rs.39/ per litre. Additionally, Excise Duty, VAT/GST and transportation charges (as decided by OMCs) are to be paid by OMCs. OMCs have procured 103 crore litres of ethanol during the ethanol supply year 2015-16 (till 7.11.2016). In 2015, the Government has asked OMCs to target 10 % blending of ethanol in as many States as possible. A Steering Committee and a Working Group on biofuels have been constituted in Ministry of Petroleum and Natural Gas. They are holding regular consultations with concerned stakeholders.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
Environmentally, the use of ethanol blends has assisted in reducing carbon monoxide emissions. In the United States, one out of every eight gallons of gasoline sold contains ethanol. Most of this ethanol is purchased as blends of 10% ethanol and 90% gasoline, known as E10, and is used as an octane enhancer to improve air quality. Domestic ethanol production in CY 2017 will decline by eight percent to 1.9 billion liters due to the decline in sugarcane area planted for a second consecutive year (marketing year (MY) 2016/17). Fuel ethanol will achieve a two-percent national average blending rate, as ethanol will replace 700 million liters of gasoline. The current average for ethanol blending is estimated at 1.9 percent.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
CHAPTER – 3
PROCESS DESCRIPTION
3.0 Dhampur Sugar Mills Ltd. are proposing 300 KLPD molasses based/200 KLPD molasses based and 100 grain based along with 12.0 MW Cogeneration Power Plant at Village & Block Rajpura, & District Sambhal, Uttar Pradesh. The company is already having 20 acres land at the existing location and rest 25 acres land will be converted from agriculture to industrial use for the proposed project. 3.1 MOLASSES BASED DISTILLERY PLANT OPERATION The process will have following steps/operations; a) Molasses storage and handling b) Fermentation c) Multi-pressure distillation d) Multi-effect evaporation e) Spirit storage 3.1.1 Molasses storage and handling Molasses is a by-product of the sugar factory and is generally stored in steel tanks. It is either pumped directly into the steel storage tanks or first unloaded in a pit and then transferred into the storage tanks. Sometimes, external cooling is done in these tanks to control the temperatures in molasses tanks. In the distillery plant, as per the requirement, molasses is pumped using positive displacement pumps and transferred to the fermentation section. It is first weighed and then pumped into individual fermenters through magnetic type flow meters. The weighing is done generally with load cell based system having a counter for measurement of quantity of molasses being processed in a given period of time. After weighing of molasses, it is then pumped to the molasses dilutor/broth mixer located alongside each fermenter.
3.1.2 Fermentation The fermentation process is engineered to operate in Batch Mode depending upon the quality of molasses. The purpose of fermentation is to convert the fermentable sugars into alcohol. During fermentation, sugars are broken down into Alcohol. Significant heat release takes place during fermentation. The fermenter temperature is maintained by forced recirculation flow through plate heat exchangers. Some quantity of spent wash would be recycled in the fermentation depending on solids concentration in fermented wash and molasses composition.
Fermentation Process & Sections
Molasses Handling and Distribution - Screened molasses from day storage is transferred to molasses receiving tank and molasses is weighed. Weighed molasses is distributed to cell mass propagation, fermentation and yeast activation section.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
Yeast Propagation -Culture yeast is grown in laboratory during plant start up. Yeast propagation section comprises of molasses diluter and hygienically engineered yeast vessels equipped with heating, cooling and air sparging facility.
Pre-fermentation-In pre-fermenter vessel, molasses, process water, nutrients and additive are added for activation/growth of cell mass. Filtered air is sparged as required for repairing of cell membranes and other cell components. Activated cell mass is transferred to fermenter- 1 to maintain desired cell mass concentration in Fermenter.
Dilute molasses media is prepared in yeast vessel by recirculating media through molasses diluter. Laboratory propagated cell mass is scaled up in series of yeast vessels. Sterile air is sparged in pasteurized and cooled dilute molasses medium for optimum growth of yeast. Temperature is maintained by recirculation cooling water through jacket of yeast vessels. Cell mass from yeast vessel is transferred to yeast activation vessel to build up cell mass required for fermentation by cell mass transfer pump.
Yeast culturing and propagation Some quantity of molasses would be received into the yeast culturing vessel and sterilized by steam. Yeast seed material would be prepared and added to the yeast culture vessels (VI1-CV4) by inoculation molasses with yeast. The contents of the yeast culturing vessel would then be transferred to the yeast activation vessel (pre-fermentor) which would be continuously aerated to allow oxygen for the yeast cell growth/multiplication.
3.1.3 Multi-pressure distillation This process utilizes columns namely the analyzer column, degassifier column, Rectifier cum-Exhaust column, recovery column Dehydration molecular seives in ideal heat integration in order to reduce the energy consumption.
Pre-heated fermented wash will be fed to Degasifying Column. Fermented wash will strip off alcohol by ascending vapors in analyzer Column. Rectifier vapours provide energy to analyzer Column through a Thermosyphonre boiler. Vapours of Degasifying Column are condensed and taken to Recovery Feed Tank. First calandria of Integrated evaporator are run by Analyservapours. These vapour are condensed and taken into Rectifier Feed Tank. Analyzer Condensate is concentrated in Rectifier Column, which operates under pressure. Condensing steam provides energy to Rectifier Column through a vertical Thermosyphonre boiler. Fuel Oil build up is avoided by taking fusel oil draws from appropriate trays. Final industrial alcohol product draw is taken from the top of the rectifier column and collected into the feed tank of recovery column. Now this alcohol fed into the recovery column. The vapours drawn from the recovery column is superheated and sent to molecular sieve bed 1, where the vapour is dehydrated, condensed and cooled and pumped to storage. A portion of dry vapour is purged to molecular sieve bed 2, under vacuum, to regenerate the bed in preparation for cycle changeover when bed 2 goes on line. The regeneration process releases the absorbed water and ethanol low strength vapours. These are condensed and recycled with the feed to the Recovery Column. A stillage stream is obtained from the bottom of the recovery column.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
Heat Integration and Energy Input Points
• Condensing steam through a vertical Thermosyphon Reboiler provides energy to Rectifier cum Exhaust Column. • Rectifier cum Exhaust Column meets the energy requirement of analyzer cum Degasifying Column • Condensing steam through a vertical Thermosyphon Reboiler provides energy to Recovery Column. • Condensing analyzer vapours through Istcalanderia of integrated evaporator provides the energy to integrated evaporator.
3.1.4 Multi Effect Evaporation The spent wash generated from the distillation process would be fed to two stage evaporation system. The MEE would be having two stages and would be integrated with the main ethanol plant. In stage I, the MEE columns would concentrate the solids from 18.0 % w/w to 25.0 % w/w. In stage II, MEE system would increase the concentration of solids from 25 % to 60 % w/w by using steam. The vapours evolved would be condensed in the condensers and collected in a collection tank. Some part of the condensate would be used in slurry preparation and balance after treatment in the condensate polishing units would be reused in the cooling tower for makeup water. 3.1.5 Spirit storage Spirit storage would be divided into two sections. One would be daily spirit receiver section and the other would be bulk storage section. The spirit coming out of distillation would be transferred to daily spirit receivers. Subsequently, after gauging, the spirit would be transferred to respective bulk storage tanks. The bulk storage tanks would be fabricated in MS.
3.2 GRAIN BASED DISTILLERY PROCESS/OPERATIONS The grain based distillery process will have following steps/operations; a) Grains receiving and storage b) Grains handling and milling c) Slurry preparation/liquefaction d) Saccharification and instantaneous fermentation e) Fermentation f) Multi-pressure distillation g) Decantation h) Multi-effect evaporation i) Spirit storage
3.2.1 Grain receiving and storage Grains such as broken rice, rotten wheat, maize, bajra and other edible grains are procured from various sources, and are stored in silos.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
3.2.2 Grain handling and milling The grain would be lifted in bucket elevators, screened followed by removal of stones and iron matter. Cleaned grains would then be milled using dry milling process in hammer mills. The flour would be fed through the bucket elevators and conveyed to the batch tipping machine through a screw conveyor. The flour addition would be metered through the batch tipping machine with load cell arrangement, before transferring the flour to the slurry tank through another screw conveyor (pre-masher) for slurry preparation process.
3.2.3 Slurry preparation/liquefaction In liquefaction process, starch is hydrolyzed to dextrin. The Liquefaction is carried out in Single stage Liquefaction Tank. Feedstock Flour is transferred to Pre-masher and mixed with Recycle Streams and liquefying enzyme. Slurry from Pre-masher is taken to Liquefaction tank where temperature is maintained by means of steam. Necessary retention time is maintained in the Liquefaction Tank. Slurry pH is maintained by supplying dilute caustic solution. Contents in Slurry Tank are kept in suspension by Agitation. The Liquefied Slurry is then cooled in Slurry Cooler using cooling water supply and transferred to Pre-fermentation and Fermentation section.
3.2.4 Saccharification and instantaneous fermentation Yeast seed material is prepared in Pre-fermenter by inoculating sterilized mash with yeast. Optimum temperature is maintained by circulating cooling water. The contents of the Pre-fermenter are then transferred to Fermenter. The purpose of Fermentation is to convert the fermentable substrate into alcohol. To prepare the mash for Fermentation, it is diluted with water. Yeast is added in sufficient quantity to complete Fermentation to produce alcohol.
At the start of the cycle, the fermenter is charged with mash and contents of the Pre- fermenter. Significant heat release takes place during fermentation. This is removed by passing the mash through heat exchangers to maintain an optimum temperature. The
recirculating pumps also serve to empty the fermenters into Beer Well. CO2 can then be
taken to CO2 vent line where it is vented out. After emptying of fermenter, it is cleaned with CIP using cleaning nozzles. After CIP, fermenter is ready for next batch to be filled.
3.2.5 Fermentation
The fermentation process is engineered to operate in batch mode depending upon the quality of raw material. The purpose of fermentation is to convert the fermentable sugars into alcohol. During fermentation, sugars are broken down into alcohol and carbon- dioxide. Significant heat release takes place during fermentation. 3.2.6 Multi-Pressure Distillation
Multi-Pressure Distillation system has Seven Distillation columns operating at various pressure conditions. Heat energy from columns operating under high pressure is utilized for columns operating under low pressure to optimize the operation for energy consumption.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
Wash to ENA Mode: Following Columns will be under operation:
1. Analyzer Column 2. Degasser Column 3. Pre-Rectifier Column 4. ED Column 5. Rectifier cum Exhaust Column 6. Recovery Column 7. Simmering Column
Pre-heated fermented wash will be fed to Degasser column. Fermented wash is stripped off alcohol by ascending vapors in analyzer column. Rectifier vapors provide energy to analyzer column through a Thermosyphonreboiler. Vapors of Degasser column are condensed and taken to Recovery Feed Tank. The condensed analyzer vapors are taken to Pre-Rectifier Column. Analyzer Condensate is concentrated in Pre-Rectifier column, which operates under pressure. Condensing steam provides energy to pre- rectifier column through a vertical Thermosyphonreboiler. A Technical Alcohol cut of about 1-2% of total spirit is taken from the Pre-Rectifier column.
Concentrated alcohol draw from Pre-Rectifier column is fed to ED column for purification. Dilution water in the ratio of 1:10 is added in this column for concentrating higher alcohol at the top. Top of this column is condensed in its condensers and fed to recovery feed tank while bottoms are fed to Rectifier cum Exhaust Column for concentration. Rectifier Column operates under pressure and condensing steam provides energy to this column through a vertical Thermosyphonre boiler. Technical Alcohol cut is taken out from the top of this column while ENA draw is taken out from appropriate upper trays and fed to Simmering Column after cooling. Fusel Oil build up is avoided by taking fusel oil draws from appropriate trays.
These fusel oils along with the condensate of Degasifying & Extractive Distillation columns are fed to recovery column for concentration. A technical alcohol cut is taken out from the top of this column. Simmering Column is operated under high reflux for better separation of methanol and di-acetyls. Final ENA product draw is taken from the bottom of this column.
3.2.7 Decantation & Thin Slops Recycle Section
Decantation section comprises of a Centrifuge Decanter for separation of suspended solids from Spent Wash coming out of Grain Distillation Plant. Wet cake has upto 30% w/w solids as removed from bottom of Decanter which can be sold directly in wet form as cattle feed (DWG).
Thin slops coming out of Decanter are collected in a tank and partly recycled into the process & further for Evaporation for concentration upto 30% w/w solids. The concentrated thin slops called as Syrup is mixed with Wet cake and sold in wet form as cattle feed (DWGS) or the entire mixture can be dried in a DDGS Dryer and then sold in dry form as Cattle feed (DDGS).
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3.2.8 Evaporation System - Integrated Evaporation Scheme
The suggested treatment scheme Effect working on the principle of falling film & Force Circulation
Analyzer vapors is fed to the first effect evaporator shell side and steam is fed to shell side finisher at the given pressure and temperature as the heating medium. Vapors from last effect are condensed in Surface Condenser. A Shell & tube type Multi-pass Surface condenser is employed for condensing the shell side vapors. The product at the desired concentration of upto 35% is obtained at the outlet of Finisher. Each effect is provided with recirculation cum transfer pump. The condensate from surface condensers is collected in a common condensate pot. The condensate is transferred for further treatment / Recycle by using centrifugal pump. The Pure steam condensate are collected in receiving vessels and can be pumped to desired battery limit Highly efficient operating pumps have been provided for pumping the required fluid. The plant is having high level of automation to get consistent output at required concentration. The system operates under vacuum. Water-ring vacuum pumps are used to maintain a desired vacuum. Cooling water from cooling tower is used in the surface condensers for condensing vapors.
3.2.9 DWGS Dryer with Cooling and Conveying System
System Description for Dryer
. Wet distiller’s grains shall be fed into the dryer housing at controlled rate through a suitable feeding system. The Fluidized Bed Dryer is enclosed in an insulated dryer housing and its outer flights are fixed. Dry saturated steam is to be supplied to the dryer through rotary joint at one end & the condensate is discharged through joint mounted on another end. . During the course of fluidization, these flights pick up the material and shower them on to the tube bundles. The heat transfer is primarily by conduction. The water vapors are exhausted through an Exhaust Blower & passed through a cyclone separator for separating fines. . Dry product partially recycled back to Feed conditioner for feed conditioning through Product Screw & Recycle Conveyor. . Entire operation of the Dryer is controlled through Control panel.
3.2.9 Spirit storage Spirit storage would be divided into two sections. One would be daily spirit receiver section and the other would be bulk storage section. The spirit coming out of distillation would be transferred to daily spirit receivers (separated for Ethanol/RS/ENA).
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
Subsequently, after gauging, the spirit would be transferred to respective bulk storage tanks.
3.3 POWER COGENERATION The power plant will be using the combustion technology. The basic steps involve fuel handling, boiler, turbo generator and power evacuation system. Proposed co- generation plant would consist of a high-pressure water tube steam boiler and a steam turbine. Fuel in the steam boiler will be burnt with the help of air in the boiler furnace. Water will be circulated in the boiler drum and tubes thus getting heated by the flame burning in the boiler furnace. Water would come out of the boiler drum located at the top of the boiler as steam. Flue gases from the boiler furnace would come in contact with the steam coming out of boiler drum. Steam after coming in contact with the flue gases would get heated up further thus getting superheated. Super-heated steam leaves the boiler in a pipe. Flue gases after super heating the steam pass through economizer where they pre-heat the boiler feed water before it enters the boiler drum. High pressure superheated steam from boiler would be passed through steam turbine. While passing through the turbine, the high pressure and temperature steam rotates the turbine rotor and an electric alternator. This electric power generated is consumed in house, i.e., for running the ethanol plant and utilities like power plant auxiliaries, etc., and surplus power will be exported to the state grid. A part of the MP/LP steam is extracted for use in ethanol plant operations. The condensed steam returns to the steam boiler as condensate and is again boiled as steam. To the possible extent, feed water requirements of the boiler would be met essentially by the condensate. The steam condensate will be available at 45-50oC and will be directly used in the feed water circuit, although with certain monitoring for certain circuits. The make up for the plant operation would be condensate water and a DM water treatment plant of adequate capacity would be provided. The power generation cycle would be provided with a de-aerator serving the dual purpose of de-aerating the feed water as well as heating the feed water with the extraction steam.
3.4 SUNDRY UTILITIES
3.4.1 Steam Generator The industry would install an incinerator boiler of 90 T/hour of steam generation capacity with concentrated spent wash and bagasse/coal as fuel in the ratio of 70:30 respectively. The design of the boiler will be of single drum, vertical, natural circulation, radiant furnace with water cooled membrane walls, three-stage super heater with inter stage de- super heater, balanced draft, water tube type and continuous ash discharge. Major accessories of the boilers would consist of the following: a) FD, ID & SA fans b) HP and LP chemical dosing system c) Blow down tank d) Spray-cum-tray type de-aerator e) 2 x 100% capacity boiler feed pumps f) Fuel feeding system
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
g) Controls and instruments
Boiler Feed Water The boiler shall be capable of operating with the following feed water quality* requirements; a) pH (at 25ºC) : 8.8-9.2 b) Oxygen : ≤0.005 ppm c) Hardness : NIL d) Total Iron : ≤0.01 ppm e) Total Copper : ≤0.01 ppm f) Total Silica : ≤0.02 ppm g) Residual hydrazine : 0.01-0.02 ppm
h) Total CO2 : NIL i) Specific electrical conductivity : 0.5 micro ohms/cm
+ * At 25°C measured after cation exchanger in the H form and after CO2 removal (max.)
Steam Purity The boiler shall be capable of supplying uninterrupted steam at the MCR rating with following steam purity levels. a) Total dissolved solids : 0.1 ppm (max) b) Silica (max) : 0.02 ppm
3.4.2 Condensate system The condensate recovered from the surface condenser and that from the process plant will be used to meet the dilution water requirements. De-mineralized (DM) water would be used for the make-up water requirements of the boilers.
3.4.3 Water Treatment (DM) plant It is proposed that the water to be used will be received from the ground water. The water quality will require pre-treatment to satisfy the quality required for boiler feed water and some other process operations. Treatment will involve sand filtration, activated carbon filtration, softener and reverse osmoses treatment suitable for ultimate quality of water required (RO).
3.4.4 Electrical system The industrial plant power requirement (including that for power plant auxiliaries) will be about 12 MW. The industry would get the required power from their in-house incineration boiler based power cogeneration plant. Industry plans to propose power cogeneration plant of 12 MW.
3.4.5 Cooling Water The maximum cooling water requirement will be 1800 m3/day. The cooling tower will be counter/cross flow induced draft cooling tower. The cooling tower shall be designed for a cooling range of 10°C, and an approach of 3°C while operating under the atmospheric wet bulb temperature of about 28°C. The cooling tower shall be carefully sited such that there is no re-entertainment of the vapors in to the cooling tower. Evaporation loss will depend on season and an average figure will be less than 1.25 % in the region. The
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cooling tower blow-downs will be 75 m3/day. The quantity of water lost in the cooling tower would be met through recirculation water addition, multiple effect evaporation condensate and fresh water addition. 3.4.6 Fuel requirements and Fuel handling
The boiler will be designed to accept concentrated spent wash and biomass/coal as fuel. The maximum fuel requirement will be about 37.5 MT/hr spent wash and 20.8 MT/hour bagasse or 12.5 MT/hr coal. In case of use of coal, the same would be sourced from the local traders of the area. The fuel from the storage will be mixed in a yard and conveyed to the boiler by a combination of belt conveyors. The system shall have provision for returning the excess fuel to the storage yard from the boiler. The fuel handling system shall be designed for a capacity of 90 TPH.
Molasses (900MT/620 KL)
Yeast Culturing and CO2 Treated Lees/Condensates Fermentation (1820) (200 KL)
Fresh Water (1000) Steam Condensate (700)
Steam (700) Multi-pressure Distillation Spent Wash (1380) (1820)
Spent Lees (240)
Alcohol (200)
Steam Condensate (580)
Steam (580) Multi Effect Evap. (1380)
Conc. Spent Wash (450)
MEE Condensate (930)
Figure 2.2 : Idealised Water Balance (200 KLPD Molasses Based Distillery Operation)
All values are for 24 hours (per day) operations Values are in Volume basis expect specified, Density of Molasses @ 1500 kgs./m3
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
Molasses (1350 MT/930 KL)
Yeast Culturing and CO2 Lees/Condensates Fermentation (2730 KL) (300 KL)
Fresh Water (1500 KL) Steam Condensate (1050)
Steam (1050) Multi-pressure Distillation Spent Wash (2070) (2730)
Spent Lees (360)
Alcohol (300)
Steam Condensate (870) Steam (870) Multi Effect Evap. (2070)
Conc. Spent Wash (600)
MEE Condensate (1470)
Figure 2.2 :Idealized Water Balance (300 KLPD Molasses Based Distillery Operation)
All values are for 24 hours (per day) operations Values are in Volume basis expect specified, Density of Molasses @ 1500 kgs./m3
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
Grain (250 MT) Milling Section Fiber/Dust/Husk (15 MT)
Fresh Water (310 KL)
MEE/Lees Cond. (250 KL) Liquefaction (700 KL)
Steam (75 MT)
Thin Slops (65)
Fermentation (700 KL) CO2
Steam Condensate (320 MT)
D M water (100 KL)
Multi-pressure Distillation Spent Wash (600 KL) (700 KL) Steam (320 MT) Spent Lees (100 KL)
Alcohol (100 KL)
Wet Cake (85 MT)
Decantation (600 KL) Thin Slops (515 KL)
Thick Slop (60 MT)
Steam (50 MT) MEE (450 KL) MEE condensate (390KL)
Steam condensate (100 MT)
Steam (100 MT) Dryer (145 MT) DDGS (60 MT)
Figure 2 : Idealised Water Balance (for proposed 100 KLPD grain based distillery plant) Condensates (85 MT) All values are in V/V except grains which are in MT/day
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Recycled Condensate (970) Evaporation Losses (1150)
Cooling Tower (1200)
Fresh Water (230) CT Blow Down (50)
Water Balance for Cooling Towers (200 KLPD Molasses Based Distillery Operation)
Recycled Condensate (1530) Evaporation Losses (1725)
Cooling Tower (1800)
Fresh Water (270) CT Blow Down (75)
Water Balance for Cooling Towers (300 KLPD Molasses/Grain Based Distillery Operation)
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
CHAPTER – 4 RAW MATERIALS
4.0 Dhampur Sugar Mills Ltd. are proposing 300 KLPD molasses based distillery plant along with Co-Generation Power Plant of 12.0 MW capacity at their existing location at Village & Block Rajpura, Tehsil Gunnaur & District Sambhal, Uttar Pradesh. The company is already having 20 acres land at the existing location and rest 25 acres land will be converted from agriculture to industrial use for the proposed project. 4.1 RAW MATERIALS REQUIREMENTS FOR MOLASSES/GRAIN BASED DISTILLERY
The distillery will use molasses as basic raw material. Besides this, processing chemicals would be used for the production of Ethanol. Phase wise daily consumption of raw materials for the distillery plant is given below;
S. No. Item Unit Proposed Requirement 1. Molasses MT 1350 2. Grains MT 250 3. Enzymes Kgs. 28 4. Sulphuric Acid Kgs. 8050 5. Urea Kgs. 395 6. Anti-foam agent Kgs. 1400 7. Yeast Kgs. 700 8. DAP Kgs. 130
4.2 RAW MATERIAL AVAILABILITY
Dhampur Sugar Mills Ltd. are having their own sugar mills adjoining to the proposed project having a daily cane crushing capacity of 8500 TCD. The sugar mills operate for more than 180 days in a year. Annual molasses generation from the sugar mills is 2,43,000 MT. Besides this, the promoters of the industry are having 4 more sugar mills in Uttar Pradesh nearby the site. Molasses would be made available from those sugar mills. Further, molasses is available from open market also.
4.3 TRANSPORTATION
Dhampur Sugar Mills Ltd. is located at Village & Block Rajpura, Tehsil Gunnaur & District Sambhal, Uttar Pradesh. The road connectivity to the site is through an existing metaled road. The required raw materials would be transported through the metaled road connected to the site only.
The molasses for the ethanol plant would be available from within the complex only as the promoters of the project have sugar mill of 8500 TCD capacity. The external molasses required would be transported through the molasses tankers and the molasses would be stored in the molasses storage tanks at site. Similarly, around 70 %
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of the fuel requirements would be met in-house from the concentrated spent wash. The remaining fuel requirements would be met through biomass/coal which would be transported at site through covered trucks. The alcohol would be transported to various destinations through alcohol tankers only. The company would make adequate arrangements for the parking of trucks at site, separately. In all, the parking arrangements for 50 commercial vehicles would be made at site. 4.4 STORAGE OF RAW MATERIALS
The molasses would be stored in molasses tanks for 30 days capacity. Adequate number of molasses tanks would be constructed near the process area. Chemicals would be stored in HDPE bags/cans and would be kept in storage shed having a surface area of more than 1000 sq. meters. The chemicals storage shed would be completely impervious in construction. Fuel for boiler furnace i.e. biomass/coal would be stored in open area and partially in covered area with a storage capacity of 15 days.
4.5 FUEL REQUIREMENTS FOR BOILER
Dhampur Sugar Mills Ltd. would be installing 12 MW cogeneration power plant. The industry would generate power through incinerator boiler of 90 T/hour of steam generation capacity with concentrated spent wash and bagasse or coal as fuel in the ratio of 70 % : 30 % respectively. The daily fuel requirements for the 90 TPH boiler furnaces would is given below;
S. No. Item Unit Fuel Requirements for the 90 TPH Boiler 1. Concentrated Spent Wash MT/day 600 2. Bagasse MT/day 500 3. Coal MT/day 300
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CHAPTER – 5
PRODUCTION
5.0 Dhampur Sugar Mills Ltd. are proposing 300 KLPD molasses based/200 KLPD molasses based and 100 grain based along with 12.0 MW Cogeneration Power Plant at Village & Block Rajpura, & District Sambhal, Uttar Pradesh. The company is already having 20 acres land at the existing location and rest 25 acres land will be converted from agriculture to industrial use for the proposed project. 5.1 Production from Molasses/grain based Distillery Phase wise daily production of products and by-products from the distillery plant is given below; S.No. Item Unit Proposed 1. Industrial Alcohol/Ethanol/ENA KL 300
5.3 Production from Cogeneration Power Plant Phase wise daily production of power and steam from the cogeneration power plant is given below; S.No. Item Unit Proposed 1. Electrical Power MW/DAY 288 2. Steam MT/Day 1050
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CHAPTER – 6
ENVIRONMENTAL MANAGEMENT AND POLLUTION CONTROL
6.0 Dhampur Sugar Mills Ltd. are proposing 300 KLPD molasses based/200 KLPD molasses based and 100 grain based along with 12.0 MW Cogeneration Power Plant at Village & Block Rajpura, & District Sambhal, Uttar Pradesh. The company is already having 20 acres land at the existing location and rest 25 acres land will be converted from agriculture to industrial use for the proposed project. During the operation of the distillery unit and the cogeneration power plant, environmental pollution would be generated from different sources. The industry would adopt the latest technologies for the abetment of pollution generated by the production process.
6.1 WATER REQUIREMENTS
The impending water uses and consequent water pollution may be because of the following;
a) Process and dilution water b) Boiler feed water make-up c) Cooling water make-up d) Washing e) Water treatment plant maintenance
Process and dilution water
Average fresh water requirement on this account will be around 2095 KLD and 1500 KLD will be used for process and dilution. This figure is after adjusting for all recycle and reuse potential of various streams. No effluent will result out of these.
Boiler feed water make-up and boiler blow-down
The industry’s overall boiler feed water requirement will be about 200 m3/day. Boiler water requirement will be met through fresh treated water. The maximum DM water required would be 75 m3/day. The blowdown, contributing to wastewater generation will be about 50 m3/day.
Cooling water make-up and blowdown
Around 1.25 % water is lost in evaporation, drift, and blow-down losses. Cooling tower make-up requirements would be partially met with MEE condensate and Spent lees, after its treatment in CPU. Thus, fresh make-up water requirement for cooling towers would be 270 m3/day.
Washing
The wash water requirement (for washing of fermenters and floor) will be about 50 m3/day.
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Overall water requirement and wastewater generation The industry will use ground water for meeting the fresh water requirements. Total average water consumption by the project is summarized below;
S. No. Purpose Option – 1 Option – 2 Molasses Grain based Molasses based Grain based based (300 (200 KL ) (100 KL) (0 KL) KL) (KL/day) (KL/day) (KL/day) (KL/day) A. Fresh Water Requirements 1 Process & 1500 0 1000 310 dilution water 2 Cooling water 270 0 230 200 3 Washing 50 0 30 20 Requirements 4 Boiler makeup 200 0 100 100 water 5 DM Plant 75 0 50 25 Maintenance 6 Total 2095 0 1410 655 B. Waste Water Discharge 1. Spent Lees 360 0 240 100 2. MEE Condensate 1470 0 930 475 3. Washing effluent 50 0 30 20 4. Cooling tower 75 0 50 30 blow down 5. DM Plant Reject 75 0 50 25 Water 6. Boiler Blow Down 50 0 35 15 7. Total 2080 0 1335 665 C. Waste Water 1830 0 1170 575 Recycled
6.2 EFFLUENT GENERATION
The proposed molasses/grain based distillery process will result in generation of following types of effluents from the process operations;
Spent Wash from Distillation Process: The project would result in generation of spent wash from the distillation process. Spent wash @ 2070 m3/day would be generated after
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the proposed distillery plant @ 300 KL/day. Whole of the spent wash would go to multi- effect evaporation system for further concentration. During this process Conc. Spent wash having solids concentration of around 60 % would be generated @ 600 KL/day. The concentrated spent wash would be used as fuel in the boiler furnace along with coal as fuel in the ratio of 70 : 30 respectively.
Condensates from Process and MEE: The project would result in generation of process condensates (spent lees) from the distillation process and multiple effect evaporation condensates. Spent lees @ 360 m3/day would be generated and MEE condensate @ 1470 m3/day would be generated. A part of the condensates would be used in the process for molasses dilution and the remaining after treatment would be used for makeup water of cooling towers. a) Effluent from other processes : Besides the above mentioned streams, effluent would be generated from misc. other streams such as – floor/fermenter washing effluent @ 50 m3/day, cooling towers blow down @ 75 m3/day, D.M. plant reject @ 75 m3/day and boiler blowdown @ 50 m3/day. This effluent would be moderately polluted and after treatment would be used in cooling tower makeup & dilution.
The details of effluent generation from each unit are as given below;
S. No. Purpose Proposed (300 m3/day) 1. Molasses based distillery process 1.1 Spent Wash 2070 1.2 Spent Lees 360 1.3 MEE Condensate 1470 1.4 Washing effluent 50 1.5 Cooling tower blow down 75 1.6 Boiler blow down 50
6.3 Air Pollution Generation
The air pollution will be due to combustion emissions released by the boiler furnace attached to the 90 TPH incineration boiler. The boiler furnace, AFBC type, will use chiefly concentrated spent wash and biomass/coal as fuel in the ratio of 70 % : 30 %. with a maximum consumption of about 40.0 MT/hour. The critical SPM concentration in the flue gas will be less than 30.0 g/Nm3. Majority of the particulates (about 60-70%) will have sizes in the range of 2-10 m. The emissions are expected to have temperature in the range of 140-150C. As per the statutory norms (as applicable to the industry), the flue gas emission shall not have SPM levels (in the stack) exceeding 50 mg/Nm3. Additionally, the stack height requirements for discharge of emissions will need to be complied with.
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6.4 SOLID WASTE GENERATION
Solid waste generated would be yeast sludge and ash from the boiler. Yeast sludge will generate @ 7.3 MT/Day. The boiler furnace will result in maximum ash generation @ 90 MT/Day. The following are the management.
Yeast sludge & ash will be used in bio-composting plant. Surplus ash from the boiler would be supplied / utilized as per CPCB/MoEF&CC guidelines.
6.5 HAZARDOUS WASTE GENERATION
The plant facility will result in generation of about 3.5 KL/year of spent oils (lubricants and transformer oil), which will be stored on site and sold to authorized recyclers.
6.6 THE POLLUTION CONTROL SYSTEM
6.6.1 Wastewater Treatment System
The industry would install multiple effect evaporators for the treatment of spent wash generated from the proposed unit. Whole of the spent wash after decantation would be sent to the MEE for concentration of solids. The details of the MEE for spent wash are as given below;
Multiple Effect Evaporation
The multiple effect evaporation system would be designed to handle the total spent wash @ 2070 m3/day. The multiple effect evaporation system will have two stages. The spent wash generated from the distillation process would be fed to two stage evaporation system. The MEE would be having two stages and would be integrated with the main ethanol plant. In stage I, the MEE system would concentrate the solids from 18.0 % w/w to 25.0 % w/w. In stage II, the evaporation system would increase the concentration of solids from 25 % to 60 % w/w. The vapours evolved would be condensed in the condensers and collected in a collection tank. Some part of the condensate would be used in slurry preparation and balance after treatment in the condensate polishing units would be reused in the cooling tower for makeup water.
Treatment of Condensates Out of the total quantity (360 m3/day) of spent lees and condensates generated, 2070 m3/day would be used in the molasses dilution preparation process of the ethanol plant. The remaining condensates & other effluent i.e.1170 m3/day after treatment would be used in the makeup of cooling towers. The condensates would be treated in a condensate polishing unit consisting of anaerobic digestion, aeration, clarification, sand filtration and activated charcoal filtration before its final reuse in cooling water makeup. Industry would install a CPU unit of 2344 m3/day for the treatment of condensates & other effluents.
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Spent Wash Storage Lagoon The industrial unit will provide spent wash storage lagoon of 15 days capacity. In all the capacity of spent wash storage lagoon would be a maximum of 30000 m3. The spent wash storage lagoon would be made impervious with HDPE lining below the concrete surface of the lagoon for prevention of ground water pollution from any possible leachate. The spent wash storage lagoon would be used in case of repair of the MEE or any other unforeseen emergencies.
6.6.2 Air Pollution Control System
The air pollution will be due to combustion emissions released by the boiler furnace attached to the proposed 90 TPH boiler. The boiler furnace will use chiefly spent wash and coal/bagasse as fuel, with a maximum consumption of about 55 MT/hour.
Bag filters will be provided to spent wash incineration boiler for pollution control to control particulate matter concentration within the CPCB prescribed limits. Stack height will be provided as per CPCB norms. Bag filters are used as dust collector as the ash particle sizes are 20 microns (80% of the qty.) The air to cloth ratio is limited to less than 0.5 m3/m2/min - 0.7 m3/m2/min. The bag filter shall be designed to provide an outlet dust concentration level of 50 mg/Nm3 with the boiler operating with concentrated spent wash and bagasse as fuel.
Ambient air quality and stack emission is regularly monitored to keep check on emissions. Same will be continued in future. Green belt has already developed and the industry is continuing developing green belt which will help in attenuating the pollutants emitted by the plant.
Maximum dust content in flue gases at bag filter outlet will be 50.0 g/Nm3. The emissions are expected to have temperature in the range of 150-1900C.
As per the statutory norms (as applicable to the industry), the flue gas emission shall not have SPM levels (in the stack) exceeding 150 mg/Nm3. Additionally, the stack height requirements for discharge of emissions will need to be complied with the applicable norms of CPCB.
DG Sets: The industrial have one DG set of 750 kVA as backup to power supply. The DG set is housed in an acoustic chamber. The combustion emission outlet, of the DG set, is provided with a muffler along with a minimum stack height as per the applicable norms of CPCB.
6.6.3 Ash management
The air pollution control system, for the new boiler furnace, will comprise of;
a) Ash vessels b) Conveying pipes c) Ash silo d) Ash storage
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e) Ash disposal
This ash handling will be totally enclosed system. The ash handling system shall be designed to take care of 100% fuel burning. Ash collected from the bottom of furnace (bottom ash) and the ash collected in the air heater hoppers and Bag filters (air pollution control system) hoppers will be taken to an ash silo through a pneumatic conveying system. Ash silo will have the capacity of storage for 1 day of ash. The ash from the silo will be unloaded through the ash conditioner and stored on land. This ash will be finally used in bio composting plant.
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Pre-Feasibility Report Dhampur Sugar Mills Ltd. Rajpura
CHAPTER – 7
PROJECT ESTIMATES
ESTIMATED OVERALL PROJECT INVESTMENT
The estimated cost of project for the proposed 300 KLPD molasses based/200 KLPD molasses based and 100 grain based along with 12.0 MW Cogeneration Power Plant at Village & Block Rajpura, & District Sambhal, Uttar Pradesh would about Rs. 325.87 Cr. Out of which 6.25 Cr. is for land.
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