e.i.d. parry (india) limited -...

PRE- FEASIBILITY REPORT

For

Proposed expansion of

Sugar Plant from 4750 TCD to 7500 TCD

Cogeneration power from 15 to 34 MW &

Distillery of 60 KLPD along with 3 MW power plant

E.I.D. – PARRY (INDIA) LIMITED

NAGARAL & NAINIGALI VILLAGE, BAGALKOT TALUK

BAGALKOT DISTRICT, KARNATAKA

E.I.D. - Parry (India) Limited (Bagalkot)

Expansion of Integrated Sugar Complex

Pre-feasibility report

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1.0 EXECUTIVE SUMMARY

E.I.D. - Parry (India) Limited is an existing Sugar & Cogeneration Power plant at Nagaral & Nainigali

Village, Bagalkot Taluk and District.

The following is the capacity of the existing Plant

Sr. No Unit Capacity

1. Sugar 4750 TCD

2. Co-gen Power plant 15 MW

Total area already in possession of the management is 177.2 acres.

Now the company has proposed to enhance the Sugar Plant capacity along with Co-gen Power and

put up a new 60 KLPD Molasses based Distillery. The proposed expansion will be taken up in the

existing plant premises only.

The following will be the capacities after proposed expansion


Existing Expansion Total

1. Sugar 4750 TCD 2750 TCD 7500 TCD

2. Co-gen Power plant 15 MW 19 MW 34 MW

3. Distillery -- 60 KLPD 60 KLPD

4. Power from

incineration boiler

-- 3 MW 3 MW

The following is the summary of the proposed expansion project

S.

No.

Parameters Description

1. Existing Plant capacity Sugar – 4750 TCD

Co-gen power – 15 MW

2. Proposed expansion Sr. No Unit

Capacity


1. Sugar 4750 TCD 2750 TCD 7500

TCD

2. Co-gen

Power plant

15 MW 19 MW 34 MW

3. Distillery -- 60 KLPD 60

KLPD

4. Power from

incineration

boiler

-- 3 MW 3 MW

3. Total area already in

possession

177.2 acres

4. Sy. No. of the land 29, 32/1, 32/2, 33/1/B and 33/1A, 36, 27/2, 27/3,28/1,




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S.

No.


28/2. 29/1, 30/6, 30/3, 30/4b, 30/4a, 30/4c, 30/5a, 30/5b,

33/2a, 35/2, 36/1b, 36/2, 48/1a, 48/1b/1. 39/1, 36/3,

62/1a, 3/3 + 4/1, 30/1+2, 39/2b, 43/1+2/c, 43/1, 135/1

5. Project cost Rs: 351 Crores

6. Water requirement

a. Water requirement for

existing plant

406 KLD

b. Water requirement for the

proposed expansion

1504 KLD

c. Total water requirement 1910 KLD

d. Source of water Krishna river

7. Total effluent generation

a. Effluent generation from the

existing plant

596 KLD

b. Effluent generation from the

proposed expansion

1083 KLD

c. Total effluent generation 1679 KLD

8.

Existing Effluent treatment Sugar Plant

Effluent generated from the Sugar plant is being treated

in specially designed ETP and treated effluent is being

utilized for greenbelt development after ensuring quality

of treated effluent with standards stipulated for onland for

irrigation by CPCB / KSPCB.

Power Plant

Effluent from the power plant is being treated in Sugar

Plant ETP and treated effluent is being utilized for

greenbelt development in the plant premises after

ensuring quality of treated effluent with standards

stipulated for onland for irrigation by CPCB / KSPCB

9. E Effluent treatment (proposed

expansion)

Sugar Plant

Effluent generated from the Sugar plant will be treated in

specially designed ETP and treated effluent will be

utilized for greenbelt development after ensuring quality

of treated effluent with standards stipulated for onland for

irrigation by CPCB / KSPCB.

Power Plant

Effluent from the power plant will be treated in Sugar

Plant ETP and treated effluent will be utilized for

greenbelt development in the plant premises after

ensuring quality of treated effluent with standards

stipulated for onland for irrigation by CPCB / KSPCB




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S.

No.


Distillery Plant

Spent wash generated from the Process will be

concentrated in Multiple Effective Evaporators up to 55%

solids and will be incinerated in the Boiler mixing with

other fuels like coal or biomass

10. Steam requirement (existing) Steam requirement existing sugar plant is being met from

existing 85 TPH Cogeneration power plant Boiler

11. Steam requirement

(expansion)

Steam required sugar plant will be met from proposed

110 TPH Cogeneration power plant Boiler

Steam required for the Distillery plant and Multiple

Effective Boilers will be met from the 25 TPH Incineration

Boiler

12. Air emissions (existing) Emissions from Project are Particulate matter, SO2 and

NOx

ESP has been provided to Boiler to bring down the

particulate matter to below 100 mg/Nm3.

The exhaust gases from the boiler are being discharged

into the atmosphere through a stack of 70 m height for

effective dispersion of gases into the atmosphere.

13. Air emissions (expansion) Emissions from Project will be Particulate matter, SO2

and NOx

ESP will be provided to 110 TPH Boiler to bring down the

particulate matter to below 50 mg/Nm3.

The exhaust gases from the boiler will be discharged into

the atmosphere through a stack of 67 m height for

effective dispersion of gases into the atmosphere.

14. Noise levels Ambient Noise levels are within the standards prescribed

by MOE&F Notification and its amendments and after

proposed expansion also similar practice will be followed.

15. Solid waste generation

(existing)

Sugar Plant

Press mud generated from the Sugar plant is being given

to farmers as organic manure

Bagasse generated from the Plant is being utilized for

power generation in Co-gen Power plant boiler

Power Plant

Ash generated form the power plant is being given to

farmers as organic manure when bagasse / biomass is

used as fuel and being to disposed off to brick

manufacturers when coal is used as fuel.

16. Solid waste generation

(expansion)

Sugar Plant

Press mud generated from the Sugar plant will be given

to farmers as organic manure

Bagasse generated from the Plant will be utilized as fuel

for power generation in Co-gen Power plant boiler




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S.

No.


Power Plant

Ash generated form the power plant will be given to

farmers as organic manure when bagasse / biomass is

used as fuel and will be disposed off to brick

manufacturers when coal is used as fuel.




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2.0 INTRODUCTION:

2.1 Identification of project and Project Proponent

EID Parry (India) Limited is a distinguished and rapidly expanding sugar producer in India. Our

sugar manufacturing facility is certified ISO 9001:2008, FSSC:22000:2005 and the distillery is

certified "zero-effluent.”

We are deeply committed to a larger vision of our social responsibility, of looking after the needs

and quality of life of the farmers and local communities. Through our effective farmer partnership

model we provide assistance in farming practices and undertake various economic initiatives for the

benefit of the local communities.

The Promoters

The following is the list of promoters of the group

S.No Name Designation

1. Mr. A.Vellayan Chairman

2. Mr. V.Ravichandran Vice Chairman

3. Mr. Anand Narayan Bhatia Director

4. Mr. V.Manickam Director

5. Mr. M.B.N.Rao Director

6. Mr. Rca Godbole Director

7. Mr. V.Ramesh Managing Director

8. Mr. S.Suresh Dy. Managing Director

2.2 Brief Description of nature of Product:

2.2.1 Sugar

Sugar known as sucrose or saccharose is an anhydrous crystalline organic product of comparatively

99.96% purity. The physical properties of sucrose are defined as follows

CRYSTALLINE NATURE:

Sucrose crystals are hard and belong to the mono-clinic system, characterized by three axes of

unequal length. Density of sucrose is equal to 1.606 gm/cu.cm. The presence of impurities in sugar

has a remarkable influence on the formation of the crystals.




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SOLUBILITY:

Sucrose is very soluble in water and in dilute ordinary alcohol. The solubility in water increases with

the rise in temperature, such that for a 10% sucrose solution, the boiling point is 100.04 Deg.C and

for a 90% sucrose solution the boiling point is 130 Deg.C. It is insoluble in chloroform, in cold

absolute alcohol, either and glycerine.

SPECIFIC GRAVITY:

The specific gravity of sucrose varies from 1.033 to 1.106 according to the concentration of the

solution. The density of the sugar solution is determined in practice by brix and beaume spindles or

balling saccharimeter.

OPTICAL ROTATION:

Sucrose and glucose rotate the plane polarised light in a `clockwise‟ direction or to the right and are

called dextro-rotatory. Fructose, rotate in a `counter clock wise‟ direction or to the left and is known

as levorotatory. The specific rotation of sucrose is 66.5 Deg.

CHEMICAL PROPERTIES:

Dry sugar (sucrose) melts at 160 Deg.C into a thick transparent liquid which on cooling again

becomes crystalline. If heated for a long time at 160 Deg.C sucrose splits up into glucose and

levulosane. At higher temperatures between 190 to 220 Deg.C the decomposition is more complete

and caramel is produced. On further, heating, carbondioxide, carbon monoxide, acetic acid and

acetone are produced.

In the presence of moisture, sucrose decomposes at 100 Deg.C and becomes dark in colour

liberating water. On prolonged heating of sucrose at the boiling point and at ordinary pressures, the

dissolved sucrose combines with water and breaks up into glucose and fructose in equal parts and

the phenomenon is called Hydrolysis of Inversion.

APPLICATIONS:

The principal use of sugar as explained is as the sweetening agent in foods. The consumption of

sugar is distributed in the various sectors such as for daily human consumption in household sector

for food processing industries, beverages, baking industry, confectioneries and miscellaneous

users. Sucrose serves as raw materials for manufacture of glucose, fructose, invert sugar syrups

etc.




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Non food uses of sugar constitute a small amount of total sugar consumption. They include use of

sugar as a scurose octacetate, a denaturant in ethyl alcohol, as sucrose diacetate, Hexa-

isobutyrate, octa benzoate, as mono and difatty acid esters for surfactants, as allyl sucrose, in

plasticisers and as raw materials for manufacture of various chemicals like glycerol, mannitol etc.

Dextran is a polysaccharide produced from sucrose by the biological process and is a very effective

plasma volume expander. Sucrose when administered by intravenous infusion relieves shock and

prevents loss of body fluids after excessive burns, wounds or infectious diseases. Other industries

wherein sucrose is finding application include drying oil esters for surface coating industries and

sugar derived detergents.

PRODUCT SPECIFICATIONS:

The specifications required for white sugar complying with Indian sugar standards are defined as

follows:

Characteristics Requirements

Moisture (%) weight 0.05% Max.

Pol 99.5% Min.

Reducing sugars (%) by weight 0.10% max.

Conductivity x [106] 100 max.

Sulphur dioxide (ppm) 70 max.

Calcium oxide (CaO) (mg/100gm) 30 max.

Turbidity, (%) by weight 15 ax.

2.2.2 Power

Power is generated by converting the mechanical energy i.e steam generated from Boiler into

electrical energy through Turbine.

The power generated will be utilized for meeting the power requirements for sugar, Distillery and

other auxiliaries. Remaining power after meeting the power requirement for the project, will be

exported to nearby grid

2.2.3 DISTILLERY PRODUCTS

Extra Neutral Alcohol

ENA IS 6613 – 1972 is an Extra Neutral Alcohol, Basic raw material for IMFL.

Produced from Molasses, Sweet Swargam, Cane Juice and Grain etc.

Rectified Spirit IS 323 – 1959 Quality is inferior to ENA.

ENA is nothing but refined Rectified Spirit.

ENA Process is a physical process in which Aldehydes, Esters and Fusel Oils impurities are

separated by virtue of their difference in Boiling Points by steam Distillation.




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ENA RS ETHANOL

01 Ethanol content percent by Volume at 15 . 6O C,Min

94.68 94.68 99.50

02 Acidity gms/100 ml1 Max 0.002 0.002 0.006

03 Residue on Evaporation gms/100 ml1 Max

0.002 0.005 0.005

04 Ester content gms/100 ml Max 0.01 0.02 0.02

05 Aldehydes gms/100 ml1 Max 0.004 0.006 0.006

06 PP Times, Minutes 30 Nil Nil

2.3 Demand – Supply Gap:

The sugar industry today is facing fierce competitive situation due to fluctuations in sugar prices in

the national & international markets, higher cane prices to be paid to the cane growers, rising input

costs, etc. The survival and growth of this industry depends on energy efficiency, cost optimization

and revenue generation from bi-products and down steam products including power, ethanol,

chemicals, etc.

The implementation of cogen power plant concurrently with the sugar modernization cum expansion

project along with other by-products, right from the beginning goes a long way to integrate the

operations and improve sustainability.

Sugar Industry Overview, India & Karnataka

The origin of Indian sugar industry dates back to 1930, when the first sugar factory was set up in the

pre-independence era. Over the last 76 years, the sugar industry has steadily grown and has

become the backbone of the agricultural and rural economy in India. Today, sugar is the second

largest agro processing industry, next to the textile industry. India is one of the largest producers of

sugar in the world, with a production of over 15 million tones. Sugar factories are located mostly in

the rural India. They act as centers of development, provide largest direct employment in the rural

areas and contribute substantially to the Central and State exchequers. The prospects of earning

foreign exchange from export of sugar are also quite high.

Sugar factories in India have capacities ranging from 1250 TCD to 10000 TCD. The Indian sugar

industry has developed indigenous capabilities for design, manufacture, supply, operation and

maintenance, R&D and cane development. The major stakeholders of this industry in India are

Ministry of Agriculture, Govt. of India, Ministry of Consumer Affairs, Food and Public Distribution,

federations of co-operative and private sector sugar factories at the national and the State levels,

sugarcane growing farmers, equipment and technology suppliers, research institutions, consultants

and service providers, financial institutions and Central / State Governments.

A total of 619 sugar factories are in operation today, with additional few new sugar factories under

implementation in different parts of the nation. The area under sugar cane cultivation, sugar cane




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production, sugar cane crushing in sugar factories, average season days, sugar recovery and sugar

production has increased steadily over the years. The crop yield per hectare and recovery has

improved, particularly in the last decade.

Sugar factories in India are spread over the entire country, however 92.73% of them are located in 9

States viz., Uttar Pradesh, Bihar, Punjab and Haryana in the north, Maharashtra and Gujarat in the

west and Karnataka, Andhra Pradesh & Tamil Nadu in the south. More than 80% sugar factories

are below 3500 TCD capacity and balance have higher capacities. About 61.23% of the Indian

sugar factories are in the co-operative and Government / joint sectors / Public and balance 38.77%

in the private sector.

Following Table no 1.3 shows the distribution of sugar factories all over India.

Status of Sugar Factories in India

State Private Public Co-op Total

Assam 1 2 3

Orissa 4 4 8

Bihar 13 15 28

Uttar Pradesh 116 14 28 158

Uttarakhand 4 2 4 10

Punjab 8 16 24

Haryana 3 13 16

Andhra Pradesh 20 1 12 33

Telangana 10 1 11

Tamilnadu 27 3 16 46

Maharashtra 80 169 249

Gujarat 5 22 27

Madhya Pradesh 16 2 5 23

Kerala 1 1 2

Rajasthan 1 1 1 3

Karnataka 48 3 25 76

Pondicherry 1 1 2

Goa

1 1

Chattisgarh

1 1

Dadra Nagar & Haveli

1 1

West Bengal 2 1 3

All India Total 360 42 325 727

Source: Sugar India Year book, 2016




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The Ministry of Consumer Affairs, Food & Public Distribution, and Government of India revised the

standard specifications for sugar plant & equipment, in the year 1987. The special committee

finalized specifications for economical capacity of 2500 TCD, expandable to 3500 TCD, employing

higher-pressure boiler and turbine configuration and efficient equipment, with a potential to export

incidental surplus power to the grid.

The Indian sugar industry was de licensed in the year 1998 vide press note No. 12 issued by the

Government of India, Ministry of Industry, Department of Industrial Policy and Promotion, on August

31, 1998. The salient features of de licensing are as follows:

The sugar industry stands deleted from the list of industries requiring compulsory licensing

under the provisions of Industries Development and Regulation Act, 1951. However, in order

to avoid unhealthy competition among sugar factories to procure sugarcane, a minimum

distance of 15 km would continue to be observed between and existing sugar factory and a

new factory, by exercise of powers under the Sugar Control Order, 1966.

The entrepreneurs, who wish to de-license their sugar factory, would require filing an

Industrial Entrepreneur Memoranda (IEM) with the secretariat of industrial assistance in the

Ministry of Industry, as laid down for all de-licensed industries, in terms of the press note

dated August 2, 1991, as amended from time to time.

Entrepreneurs who have been issued Letter of Intent (LoI) for manufacture of sugar need not

file an initial IEM. In such cases, the LoI holder shall only file Part B of the IEM at the time of

commencement of commercial production against the LoI issued to them. It is however

open to entrepreneurs to file an initial IEM (in lieu of LoI / industrial license held by them) if

they so desire, whenever any variation from the conditions and parameters stipulated in the

LoI / industrial license is contemplated.

The statistics on economic and commercial performance for the industry is quite fluctuating. The

changes in the agro climatic conditions and sugarcane crop production, as well as the sugar

markets have been mainly responsible for these fluctuations. Efficiency, quality, and integration

have become order of the day for this industry. The industry has grown till today over the last seven

decades. The strength and capacity built so far will surely help meet these challenges. The

following are major options to meet these challenges:

a. Effecting substantial improvement in cane development and management, including

cultivation practices, varietals and water management, so as to improve yield and

recovery, without affecting the average fibre content.

b. Effecting visible improvement in the operational efficiencies and reduction of sugar losses.

c. Effecting and sustaining improvement in energy efficiency, both in steam and power, for

saving of additional bagasse, for both sugar and by-products manufacture.




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d. Expansion of capacities and diversification into absolute alcohol/ethanol and cogeneration

power projects.

e. Effecting adequate capacity building within and without.

f. Maximizing sugar exports for value addition.

g. Effective marketing in the national and international markets.

h. Product quality and diversification.

i. Commercializing the excess power capacity by exporting to utilities or to other bulk power

consumers.

Ministry of Consumer Affairs, Food & Public Distribution Department of Food & Public Distribution

Government of India has issued a revised order dated November 10, 2006, amending Sugarcane

(Control) Order, 1966. The key provisions of this order are outlined below:

a. No new sugar factory shall be set up within a radius of 15 km of any existing sugar factory or

another new sugar factory in a State or two or more States.

b. Before filing the Industrial Entrepreneur Memorandum (IEM) with a Central Govt., a

certificate from the Cane Commissioner or Director Sugar or specified authority of the

concerned State Govt. shall be obtained regarding the distance criteria re-defined as above.

c. Submission of performance guarantee of Rs. 1 crore to Chief Director, Sugar, Dept. of Food

& Public Distribution, within 30 days of filing the IEM, as a surety for implementation of the

IEM within the stipulated or extended time.

d. The stipulated time for taking effective steps shall be 2 years and commercial production

shall commence within 4 years from the date of filing of the IEM, failing which the IEM shall

stand de-recognized and performance guarantee shall be forfeited.

e. If an IEM remains un-implemented within the stipulated or extended time limits, the

performance guarantee shall be forfeited after giving a reasonable opportunity of being

heard.

f. The above clauses will be applicable for IEM already acknowledged as on the date of this

notification, but who have not taken effective steps for its implementation, duly defined, shall

furnish a performance guarantee of Rs. 1 crore to the Chief Director, Sugar.

Power Sector Review

The maximum demand met by the state has increased from 7,815 MW in FY 2011 to 9,549 MW

in FY 2015 showing a growth of 22% during the 4 year period, while energy requirement has

increased by 29% during the same period. The maximum demand deficit has however reduced

due to many DSM activities undertaken by DISCOMs and sourcing of power on short term

basis to meet the need.




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The average daily consumption of registered rural domestic consumers has increased to 1.19

kWh in FY 2015 at CAGR of 4% during the last 6 years. On the other hand, the average

daily consumption of registered domestic urban consumers has increased to 3.00 kWh in FY

2015 at CAGR of 3% during the same period.

As per projections made in 18th EPS of CEA, the projected energy demand and maximum demand

for the state of Karnataka was 89,285 MU and 14,945 MW in FY 2019 as against the now

calculated energy requirement of 87,626 MU and maximum demand of 14,710 MW in FY

2019.

Ethanol Sector Overview, India and Karnataka

The use of alcohol as a drink is an age-old story. It appears that in India the technique for

fermentation and distillation was available even in the Vedic times. Alcohol is an integral part of the

Ayurvedic system of medicine also.

Carew & Co. Ltd. set up the first distillery in the country at Cownpore (Kanpur) in 1805 for

manufacture of Rum for the British army. The technique of fermentation, distillation and blending of

alcoholic beverages was developed in India on the lines of practices adopted overseas, particularly

in Europe.

The original use of alcoholic fermentation was of course for preserving fruit juices. Now the

fermentation is adapted for the preparation of fermented grain beverages and then distilled

beverages. The utilization of Ethanol, for industrial use is a recent phenomenon. It became

important towards the end of the Second World War.

When large-scale production of alcoholic beverages was taken up, various Governments found that

alcohol was a good source for increasing government revenue through collection of tax. When

synthetic organic chemistry advanced rapidly, about a century ago, alcohol became an

indispensable chemical for this industry. However extensive manufacturing of alcohol for industrial

use was hampered due to excessive taxes. The problem was to device a means for conserving

government‟s interest in tax collection on potable alcohol and at the same time making alcohol for

industrial use relatively free of tax. Thus different governments introduced the process of

denaturation of alcohol for industrial use.

During the Second World War, the demand for the industrial alcohol increased 4-5 times, above the

prewar period, due to the production of smokeless powder for weapons. The imports of molasses

were hampered due to war conditions. This leads to evolving the process of grain fermentation for

meeting the requirement of Ethanol.




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In India, after the protection granted to the sugar Industry in 1932, a large number of sugar factories

were established in the country, particularly in Maharashtra and Uttar Pradesh where irrigation

facilities existed for cultivation of sugarcane. Increase in sugar production resulted in accumulation

of molasses, which resultantly, caused unmanageable environmental problems. At that time the

demand for molasses was almost insignificant and the sugar mills had to incur considerable

expenditure for disposal of molasses. For resolving these problems a joint committee of U.P. and

Bihar was constituted in 1938 to explore the possibilities of using molasses for developing alcohol-

based industries. The Committee recommended establishment of distilleries for production of

alcohol, utilizing molasses as a substrate.

The committee also recommended that alcohol produced by the distilleries should be admixed with

petrol, to supplement motor fuel. This helped in solving the problems of disposal of molasses. It also

filled up the gap in the demand and supply of motor spirit.

As a result, after meeting alcohol requirement for manufacture of gasohol, substantial quantity of

alcohol was diverted for production of alcohol based chemicals.

Present Status

Fossil fuels are declining. Transportation sector consumes more than 50% of the fuels.

Environmental degradation from these fuels is a major problem all over the world. World oil

production is expected to last till 2125 A.D., if consumption at the present level is maintained. On

this background the use of Ethanol for fuel blending should be given a top priority.

India requires ethanol for the following three major purposes:-

For potable liquor

For industrial use

For fuel blending

Today, the distillery industry of India uses only molasses for manufacturing alcohol. There are

handful of grain distillery units (e.g. Seagram Manufacturing Ltd.) and the alcohol produced by them

is used for captive use to make value added liquors.

All other liquor (IMFL) manufacturers use alcohol produced from molasses. In advanced countries,

liquor for human consumption is made only from grain alcohol. It is known that alcohol produced

from molasses can have residues such as sulphates, sulphites, higher aldehydes, higher alcohols,

higher acids and ketones etc., which are not present in alcohol from, grains.




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However, no such above-mentioned distinction is made in India. Thus alcohol produced only from

one source i.e. molasses is used for all 3 purposes (liquor, industrial use, fuel blending). There is an

urgent need to bring in above quality consciousness in the IMFL industry and appropriate policy

measures by the Govt.

Today, Indian distillery industry broadly consists of two parts:

One is alcohol production from molasses for industrial alcohol and two alcohol production from

molasses for liquor purposes.

Ethanol demand for fuel blending is a recent phenomenon. For this purpose, alcohol from molasses

is used.

The potable distillery producing Indian Made Foreign Liquor (IMFL) has a steady but limited

demand. The alcohol produced is now being utilized in the ratio of approximately 52 per cent for

potable purpose and the balance 48 percent for industrial purpose.

Ethanol blending

Ethanol blending is the practice of blending petrol with ethanol. Many countries, including India,

have adopted ethanol blending in petrol in order to reduce vehicle exhaust emissions and also to

reduce the import burden on account of crude petroleum from which petrol is produced. It is

estimated that a 5% blending (105 crore litres) can result in replacement of around 1.8 million

Barrels of crude oil . The renewable ethanol content, which is a byproduct of the sugar industry, is

expected to result in a net reduction in the emission of carbon dioxide, carbon monoxide (CO) and

hydrocarbons (HC). Ethanol itself burns cleaner and burns more completely than petrol it is blended

into. In India, ethanol is mainly derived by sugarcane molasses, which is a by-product in the

conversion of sugar cane juice to sugar.

The practice of blending ethanol started in India in 2001. Government of India mandated blending of

5% ethanol with petrol in 9 States and 4 Union Territories in the year 2003 and subsequently

mandated 5% blending of ethanol with petrol on an all-India basis in November 2006 (in 20 States

and 8 Union Territories except a few North East states and Jammu & Kashmir). This was also an

attempt to reduce the Under-recovery of Public Sector Oil Marketing Companies (OMCs). Ministry

of Petroleum and Natural Gas, on 1 September, 2015, inter-alia has asked OMCs to target ten

percent blending of ethanol in Petrol in as many States as possible. In countries like US, blending is

allowed upto 10%. Subsequent to Brazil's bio-fuel programme, which began in 1976, close to 94%

of cars sold in Brazil are flexible fuel cars that can handle ethanol blends from 18 per cent upward .

Ethanol blending first found mention in the Auto fuel policy of 2003. It suggested developing

technologies for producing ethanol/ bio fuels from renewable energy sources and introducing

http://www.arthapedia.in/index.php?title=Under-recovery




15

vehicles to utilise these bio fuels. Later, as per National Policy on Bio-fuels, announced in

December 2009, oil companies were required to sell petrol blended with at least 5% of ethanol. It

proposed that the blending level be increased to 20% by 2017.

Ethanol, being a by product of the sugar industry, was expected to be freely available. However, Oil

marketing companies (OMCs) were not even able to get bids for more than 50% of the amount

offered for purchase . Further, the Government decided on 22.11.2012 that procurement price of

ethanol will henceforth be decided between Oil Marketing Companies (OMCs) and suppliers of

ethanol. In addition, on 03.07.2013, it was decided that ethanol would be procured only from

domestic sources. This led to a rise in ethanol prices, which to a great extent reportedly eroded the

economy of the blend. At present, government has permitted OMCs to implement the ethanol

blending programme in notified 20 States and 4 Union Territories as per the availability of ethanol.

There are reportedly significant transaction barriers which impede smooth supplies of ethanol for

blending. In several States, State not only imposes levy on molasses but also regulates the

movement of non-levy molasses. Inter-state movement of ethanol requires No-Objection-

Certificates (NOCs) from the State Excise Authorities along with permits from dispatching and

receiving States. Most States impose “Export/Import” duties on ethanol leaving and entering their

boundaries. There are some instances where Octroi is levied on ethanol for entry into municipal

limits. Hence States were requested by the Central Government to liberalise restrictions on the

supply of ethanol so that its blending with petrol can be encouraged while improving the financial

health of sugar sector and also liquidation of cane dues of farmers.

As per the estimates given in Auto Fuel Vision and Policy 2025 issued in May 2014, blended petrol

is available only in 13 states and the average blend is 2%. During the sugar year 2014-15, OMCs

have achieved a blending percentage of 2.3% as per the press release dated 25 April 2016.

Hence, in order to improve the availability of ethanol, the Government, on December 10, 2014, fixed

the price of Ethanol in the Range of Rs. 48.50 to Rs. 49.50, depending upon the distance of

distillery from the depot/installation of the OMCs. (The rates are inclusive of all central and statutory

levies, transportation cost etc, which would be borne by the Ethanol suppliers). Fixation of ethanol

price based on distance, has encouraged movement of ethanol to longer distances, including States

having lack of distilleries. Further, ethanol produced from other non-food feedstocks besides

molasses, like cellulosic and ligno cellulosic materials including petrochemical route, has also been

allowed to be procured subject to meeting the relevant Bureau of Indian Standards (BIS)

specifications.




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2.4 Employment generation (Direct & Indirect):

The man power required for the industry is 500 Nos. which is inclusive of 275 nos. on permanent

basis and rest all will on Temporary or contract basis.

S.No. Particulars No. Employees

1. Technical & Administrative Staff 150

2. Skilled & Semi Skilled 275

3. Unskilled & Helpers 75

Total 500




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3.0 PROJECT DESCRIPTION:

3.1 Type of the Project:

The proposed Project mainly involves

Production of Sugar from Sugarcane

Power generation using Bagasse / Coal as fuel

Production of Rectified Spirit / ENA / Ethanol using Molasses as raw material

3.2 Location

E.I.D. - Parry (India) Limited is an existing Sugar & Cogeneration Power plant at Nagaral & Nainigali

Village, Bagalkot Taluk and District.

Now the company has proposed to enhance the Sugar Plant capacity along with Co-gen Power and

put up a new 60 KLPD Molasses based Distillery. The proposed expansion will be taken up in the

existing plant premises only.

3.3 Details of the Alternate sites:

No Alternate sites have been examined as existing premises has been given permission to set up

Sugar Plant.

3.4 Size or Magnitude of Operation:

The following will be the capacities after proposed expansion



1. Sugar 4750 TCD 2750 TCD 7500 TCD

2. Co-gen Power plant 15 MW 19 MW 34 MW

3. Distillery -- 60 KLPD 60 KLPD

4. Power from

incineration boiler

-- 3 MW 3 MW

3.5 Process details:

3.5.1 Sugar Process Description

Milling:

Sugarcane from the fields are weighed and fed in cane carrier by means of cane unloaders. The

cane is passed through kicker, leveler and Fibrizer. The Fibrizer improves the extraction of the mills

by breaking the rigid ness of the cane and so facilitating its disintegration and extraction of its juice.

The fibres are then crushed in mill house, consisting of the 4 mills. During crushing, juices present in




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the cane cells are extracted by the mills. The juice obtained from milling is sent for process, fibre

that comes out from 4th mill is termed as bagasse and it is used as fuel in boilers.

Boilers:

In boilers condensate water is converted into steam by burning bagasse as fuel. Steam produced in

boilers is used in the steam turbine to generate power and the exhaust steam coming out from the

turbine is used in the process for sugar manufacturing.

Power House:

Power House consists of steam turbine and alternator. The alternator is driven by steam turbine and

power is generated. The generated power is used to meet the in-house power requirement of the

factory and the surplus power is exported to grid. The in-house LP steam from the steam turbine is

used for sugar processing at the boiling house.

Clarification:

The extracted juice from mills is called as raw juice and it is heated to 70 – 75 Deg. C. in juice

heaters and treated simultaneously with the milk of lime and sulphur dioxide gas in order to

separate the impurities. The sulphited juice is again heated to 102 Deg. C through juice heaters and

allowed to settle in the clarifier. The purified juice, which comes out from clarifier, is called as clear

juice and is sent to evaporator for concentration. The settled impurities are called mud. The mud

contains small amount of juice, which is separated in vacuum filters.

Evaporation:

The clear juice after clarification is concentrated in evaporators by evaporating the 75% of the water

present in it. Evaporators are huge vessels consist of calendria where the juice is made to flow

through the tubes and around w3hich steam is passed. The clear juice of 12 – 15 Brix is

concentrated to 60 Brix. Concentrated juice is then called syrup. The syrup is again treated with

sulphur dioxide (Bleaching agent).

Crystallization:

The sulphited syrup is concentrated further in the vessels called pans. During the above process,

sugar crystals are developed by means of exhaustion. The formed crystals are then cooled in

crystallisers. The crystals are surrounded by thin film liquid called as mother liquor. The crystal

along with the mother liquor (Molasses) is called as massecuite.




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Curing:

The above massecuites are centrifuged in centrifugals, where crystals are separated from the

mother liquor. Separated mother liquor of A & B massecuites are again used for boiling and

maximum exhausted mother liquor is called as Final Molasses, which is stored in the steel tanks

and sent to distillery for manufacture of Ethyl alcohol. The separated sugar crystals are dried in

hopper, sieved in graders and bagged.




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Bagging:

Sugar is bagged in `A‟ Twill Gunny bags and each bag contain 100 kg / 50 kg sugar nett. The bags

are stacked in sugar godowns and are dispatched as per the directions given by the Directorate of

Sugar, New Delhi.

3.5.2 Co-generation Power Plant

Sugar plant will be installed with 2750 TCD in addition to existing 4750 KLD capacity. The

cogeneration capacity is so designed that the plant will be able to feed steam and power

requirements entire Sugar Complex. The capacity of the boiler will be 110 TPH at 108 ata and

540ºC. The turbine capacity would be 19 MW at 110 TPH at 108 ata and 540ºC steam parameters.

The turbine will have 3 extractions and condensing mode. The two numbers of HP extractions will

be uncontrolled and one no. of LP extraction controlled. The first HP extraction (higher pressure) will

feed HP heater – II and second HP extraction will feed HP heater – I and process HP steam

requirement of Sugar and Distillery. The controlled LP extraction will feed the requirements of LP

steam of Sugar process Dearator and Distillery.

For off-season operation, we have to utilize the purchased biomass fuel and imported coal. The

season period will be 5 to 6 months and off-season will be 3 to 4 months depending on the

availability of fuels at economical price.

3.5.2.3 Fuel Balance:

Cane crushing per hr 315 TPH

Bagasse % on cane is 30%

Bagacillo consumption 1.0% on cane

Net bagasse available for cogeneration 29%

Steam fuel ratio for bagasse is 2.50 for new Boiler of 110 TPH @ 108 ata

Steam generation from mill bagasse is 110 TPH and Procured Bagasse.

For off season we have to procure biomass fuels and imported coal to ensure 25% of the total fuel

consumption is from coal and other biomass in a year.

3.5.3 Manufacturing Process (Rectified Spirit/Ethanol/ENA)

Yeast propagation:

Yeast seed material is prepared in water-cooled yeast vessels by inoculating molasses with yeast.

The contents of the yeast vessel are then transferred to the Yeast activation vessel. The purpose of

aerated yeast activation in the yeast activation vessel is to allow time for the yeast cell multiplication.




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Fermentation:

The fermentation technology adopted in the industry is of continuous fermentation with yeast

recycle with this technology the total spent wash generation will be restricted to a max. of 10 kl/kl of

R.S. (As per latest CPCB recommendation).

The purpose of fermentation is to convert the fermentable sugars into alcohol. During fermentation,

sugars are broken down into alcohol and carbon-di-oxide. Significant heat release takes place

during fermentation. However the fermentation temperature is maintained at 32 – 35 0C by forced

recirculation heat exchangers.

At the end of fermentation, the wash is fed through a yeast separator where the yeast cream is

separated, acidified in the yeast treatment tank and returned to the yeast activation vessel for

activation. Sludge is separated in a sludge decanter. The clear wash from both the yeast separator

and sludge separator flows to the clarified wash tank. The wash is then pumped to distillation.

Distillation:

Fermented Wash about 8% v/v alcohol is preheated in two stages i.e. in the beer heater using the

Rectifier vapours and then in the Fermented wash PHE using the effluent. The preheated wash is

then fed the Degasifying Column to remove residual CO2 and volatiles.

The wash then flows down to Analyser Column, which acts as a total stripper. The alcohol water

vapour mixture which rises upward in this column is fed to the Rectifier Column. The spent wash,

which is devoid of alcohol, flows down the Analyser Column for suitable treatment.

The lower boiling impurities are concentrated in the Aldehyde Column where about 5% spirit is

drawn off as impure spirit with a minimum strength of 660 OP.

The alcohol vapours are concentrated in the Rectifier Column to produce Rectified Spirit of 95% v/v

strength. Higher boiling impurities, which are formed during fermentation, are removed by taking

side draw purges to a decanter from the Rectifier Column. A trace stream of spirit is drawn off as

impure spirit (about 2% of plant capacity) to remove the concentrated volatile compounds. The high

grade Rectified Spirit is taken as a draw from the upper trays of the Rectifier Column.

The Rectified spirit is fed to the purification column. Dilution water is fed on the top most tray of the

column with a dilution ratio of 1: 9. This column serves to remove the impurities based on the

principle of HYDROEXTRACTION. The water is fed to the column in such a way that it selects the

higher alcohols and other impurities to move upwards and extracts ethanol down. The purifier

bottom alcohol composition is maintained at 12 % v/v. At this composition there is an inversion in




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relative volatiles of higher alcohols as compared to ethanol and these alcohols get separated in the

top distillate. Top draw for volatiles is fed to the Fusel oil concentration column.

The purified dilute ethanol is removed from the bottom of the purification column and fed to the

rectification column, which concentrates the ethanol to 96% v/v. The high grade spirit is drawn from

one of the upper trays of the rectification column. A small heads cut is removed from the overhead

stream as technical alcohol (T.A.) cut to with draw impurities and is fed to the heads concentration

column. The lees from the exhaust column is recycled as dilution water after a part of it is purged.

The purged spentlees is used to preheat the make-up dilution water.

Lower side draw streams are taken from rectification column to avoid fusel oil build up in the

column. These streams are then taken to the fusel oil column. This column concentrates the dilute

streams of ethanol containing esters and fusel oils to approximately 95% v/v of ethanol. The

concentrated ethanol is removed as T.A. cut from the top of the column. T.A. cut is removed out of

the system in order to remove propanol and remaining is fed to the heads concentration column

where the heads from the purification column and rectification are fed to the static mixer. Soft

water, which has been preheated, is used for diluting the high proof ethanol. An impure spirit cut of

about 5% of the rectified spirit feed is drawn from the top of the column. The dilute ethanol solution

at the bottom of this column is pumped back to the purification column for repurification.

Carbon Dioxide Recovery System (By Product): Carbon dioxide produced during fermentation will be recovered by means of scrubbing

arrangement, chemical treatment drying process and finally liquefaction. The water utilized for

scrubbing will be recycled back into the fermentor.

CO2 gas will pass through scrubbing tower, where the gas is scrubbed with water. From the

scrubber after washing the gas will pass through air compressor and then the gas will pass through

a tower containing sodium dichromate to eliminate the impurities, if any and then to drying

arrangement with sulphuric acid. Subsequently it passes through a tower containing coke coated

with washing soda to eliminate odour. Finally it goes to the chilling unit to cool the gas before

passing through different cylinders, where the cooled gas will be filled into the cylinders under

pressure. The scrubber blowdown will be recycled into the fermenters.

Total CO2 production : 45.6 T/day

This carbon dioxide in cylinders will be sold to industries like soft drink manufacturing units, etc.




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Ethanol Production:

This plant is filled with imported 3A grade Molecular Sieve. It is operated with vaporized Alcohol and

removes water completely. Then Molecular sieves are regenerated under vacuum of 710 mm Hg.

Feed Alcohol comes to this Plant in a Day Tank continuously from bulk storage tank. From this tank

alcohol is pumped to a steam vaporizer at 4 Kg/cm2 pressure. This is vaporized in a steam heater

and then vapor is super heated to 160oC in a super heater and taken to Molecular Sieve Unit. This

super heated vapor now pressure through one Molecular Sieve column for moisture removal. There

are 2 Molecular Sieve columns. At a time one column remain in drying cycle while other columns

under goes vacuum regeneration. Each column remains in cycle for 6 minutes. Here drying process

takes place at 3.0 Kg/cm2 pressure and dry alcohol vapor of 99.8% purity comes out as final

product. This alcohol vapor is condensed in a water cooler and then collected in another day tank.

From this tank dry alcohol is continuously pumped to bulk day storage tank through a level

controller and a control valve. In the regeneration process some left over alcohol also comes out

which is condensed in regeneration condenser. This alcohol is around 95% strength and is re-

cycled in to rectifier column continuously.

The other Molecular Sieves column under goes regeneration by a vacuum pump. In this column

vacuum pumps pulls and creates vacuum of 710 mm Hg. At this vacuum the moisture from

Molecular Sieve pores comes out and along with 30% pure alcohol from on line Mole Sieve bed is

sprayed. Thereafter during vacuum process, some left over alcohol and water from Molecular

Sieves comes out and is condensed. Concentration of this lean alcohol is around 70% alcohol,

which can be recycled to the Rectifying Column. From Rectifier the pure water will be sent out

automatically.




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3.6 Raw Materials

The following will be the raw material requirement for the for the existing and proposed expansion project

S.NO RAW MATERIAL SOURCE QUANTITY ( TPD)

METHOD OF TRANSPORT Existing Expansion Total

Sugar plant :

1 Sugar Cane From Bagalkot 4750 2750 7500 By trucks

2 Lime Local area 11.875 6.875 18.75 Through covered trucks by Road

3 Sulphur Local area 3.325 1.925 5.25 Through covered trucks by Road

4 Phosphoric Acid Local area 0.285 0.165 0.45 Through covered trucks by Road

Co-gen power plant :

1 Fuel

Bagasse From Sugar plant 1050 1200 2250 Conveyor

(or)

Coal Imported 395 495 890 By Sea/ Rail/Road Covered trucks

Distillery :

1 Molasses From Sugar plant &

External

--- 230 230 Through Pipeline/Tanker

2. FUEL For 25 TPH Boiler

Concentrated Spent wash From Distillery Unit --- 166 166 Through Pipeline

Coal (100%) Karnataka --- 116 116 Through covered trucks by Road




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3.7 Resource Optimization / recycling and reuse: Sugar Plant

Condensate from the Sugar Plant will be utilized for Cooling tower make up

Power Plant

The effluent generated from the Plant will be treated in Neutralization pits and will be utilized for

dust suppression, ash conditioning and Greenbelt development after ensuring compliance with

stipulation for on land irrigation by MoEF / CPCB

Distillery

Spent wash generated during the process of Fermentation, will be treated in Multiple Effective

Evaporators to concentrate the solids content up to 55% and concentrated spent wash will be

incinerated in the Boiler along with Coal.

The condensate generated during the process of Multiple Effective Evaporators will be reused in the

Process thus decreasing the net water requirement.

3.8 Availability of Water:

Water requirement for the existing Plant is being met form the Krishna River. For the proposed

expansion also, water required will be met from the Krishna River.

Water requirement for the existing plant 406 KLD and for proposed expansion will be 1504 KLD.

Hence after proposed expansion the total water requirement will be 1910 KLD.

Prior permission from Irrigation Department will be for enhanced water requirement in due course.

WATER CONSUMPTION (in KLD)

Section

Sugar Co-gen Total after

expansion Existing

(4750 TCD) Expansion (2750 TCD)

Existing (15 MW)

Expansion (19 MW)

a)Domestic 10 10 10 10 40

b)Industrial purpose

1. Process water 23 14 -- -- 37

2. Boiler feed

234 270 504

3. DM plant regeneration

30 40 70

4. Cooling water make up

89 100 189

5. Service water 10 10 20 Total 33 24 373 430 860




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WATER REQUIREMENT FOR 60 KLPD DISTILLERY PLANT & 3 MW CO-GEN. POWER PLANT

SECTION Water requirement

Process water 560

Make up water for Boiler 40

DM water for RS dilution 190

Cooling tower make up 220

DM plant regeneration 30

Domestic water 10

Net water Requirement 1050

Water requirement for Sugar (Existing) : 33.00

Water requirement for Sugar (Expansion) : 24.00

Water requirement for Co-gen power (existing) : 373.00

Water requirement for Co-gen power (expansion) : 430.00

Water requirement for Distillery : 1050.00

Total water requirement for after proposed expansion will be : 1910 cum/day

3.9 Power Requirement:

The power required for the existing and expansion project will be met from the Co-generation Power

plant and proposed 3 MW Captive power plants.

3.10 Quantity of wastes generated:

3.10.1 Waste water generation

Waste water generation from the existing Plant 596 KLD. Waste water generation from the

proposed expansion will be 1083 KLD. Hence total waste water generation after proposed

expansion will be 1679 KLD

SECTION

SUGAR CO-GEN Total after proposed expansion

Existing (4750 TCD)

Expansion (2750 TCD)

Existing

(15 MW)

Expansion (19 MW)

a)Domestic 8 8 8 8 32

b)Industrial purpose

1. Process & Washings

82 48 -- -- 130

2. Boiler Blow down -- -- 24 28 52

3. Tube cleaning 218 122 340

4. DM plant regeneration

-- -- 30 40 70

5. Cooling tower blow down

176 104 40 45 365

6. Service water -- -- 10 10 20 Total 484 282 112 131 1009




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WASTE WATER GENERATION FROM

60 KLPD DISTILLERY PLANT & 3 MW CO-GEN. POWER PLANT

SECTION Water requirement

Spent wash 600

Cooling tower blow down 23

Boiler blow down 9

DM water regeneration 30

Domestic water 8

Total 670

Waste water generation from Sugar (Existing) : 484.00 KLD

Waste water generation from Sugar (Expansion) : 282.00 KLD

Waste water generation from Co-gen power (existing) : 112.00 KLD

Waste water generation from Co-gen power (expansion) : 131.00 KLD

Waste water generation from Distillery : 670.00 KLD

Total waste water generation for after proposed expansion will be : 1679 KLD

3.10.2 Waste water Treatment: Sugar Plant

Total wastewater generation will be 750 cum/day. Effluent generation per ton of cane crushed will

be below 100 lit/ton of cane crushed as per CREP recommendations.

Capacity of the existing ETP is 1000 KLD. Hence existing ETP is adequate for proposed expansion

also.. The following is the ETP description.

Design Data & Performance Projections

This Wastewater Treatment plant is designed for following parameters & shall perform as under

upon reaching steady state of its operation:

PARAMETER RAW WASTEWATER TREATED WASTEWATER

Flow (KLD) 750 750

pH (S U) 5.0 – 6.5 6.5 – 8.0

BOD (mg/l) 3000 < 30

COD (mg/l) 6000 < 250

TDS mg/L 2000 < 2100

TSS mg/L 500 < 100

Oil & Grease mg/L 100 < 10

Note: The Sugar ETP has been designed for 1000 KLD, to treat 750 KLD of trade effluent from

Sugar plant with a cushion of 25% in order to treat the non process effluent like cooling tower blow

down and tube cleaning. However necessary provision shall be made to operate the ETP with a

minimum flow of 750 KLD of trade effluent in the Digester and Aeration tank.




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PROCESS DESCRIPTION

The proposed wastewater treatment plant shall consist of following treatment units.

PRIMARY TREATMENT

Screen

Oil & Grease trap

pH adjustment

Equalization Tank

SECONDARY TREATMENT

UASB Anaerobic reactor

Aeration Tank

Secondary Clarifier

Sludge Drying Beds

Screen Chamber:

Screen chamber constructed in RCC shall be provided with SS 304 fabricated bar screen for

removal of free and floating material. The screen shall be inclined at 45 Deg with horizontal.

Oil & Grease Trap:

Oil and grease trap constructed in RCC shall be provided for removal of free and floating oil from

the Wastewater. The oil trap shall of gravity type and shall be provided with Belt type oil Skimmer.

Lime Preparation Tank:

A lime preparation tank constructed in RCC. In this tank is used for lime solution preparation and

continuous mixing of lime. Lime solution is then feed to equalization tank for pH correction in a

required proportion. 1 HP agitator shall be provided for mixing in the tank content.

Equalization:

Wastewater emanating from sugar has fluctuations in wastewater quality and quantity. Equalization

tank shall be provided for dampening these fluctuations. In equalization tank the raw effluent is

collected and equalized for adequate time. An equalization tank shall be provided with an agitator to

mix the tank content thoroughly. The equalized effluent from equalization tank shall then be pumped

to buffer tank. A stand by floating mixer shall also be provided for equalization tank




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Buffer Tank:

Buffer tank constructed in RCC shall be provided for preconditioning / pre-acidification of the raw

effluent. In buffer tank the Raw Effluent is mixed with treated effluent form UASB Reactor. The

nutrient required for the process will also be added to the effluent in Buffer tank. The content of

buffer tank shall be mixed hydraulically using UASB Reactor feed pumps. The tank content will

then be pumped to UASB Reactor for first stage biological treatment.

UASB Reactor:

Upflow Anaerobic Sludge Blanket reactor is provided for anaerobic treatment of dairy effluent. The

UASB reactor shall be constructed in RCC M-25. The reactor consists of three zones viz. Influent

distribution zone, Reaction zone, Gas solid liquid separation zone.

Influent Distribution zone: The raw wastewater enters into the at the bottom through influent

distribution zone. A sophisticatedly designed piping net work is provided for uniform distribution of

the effluent in the tank. The effluent then travels upward in the reactor.

Reaction Zone: In the reaction zone the anaerobic bacteria are maintained in the form of sludge

blanket. The organic matter in the wastewater comes in contact with the bacterial population and is

degraded anaerobically to methane rich biogas, the end product of anaerobic digestion. The

process of conversion of organic matter in to the biogas is a two-stage process. In the first stage the

organic matter in the raw effluent is converted in to the volatile acids by acid forming bacteria. In the

second stage the acid produced in the first stage are converted in to methane by another group of

bacteria i.e. methane formers. In UASB process both the stages are completed in single reactor.

The biogas so produced is bubbled through the effluent and is separated out in the third section i.e.

Gas-Solid-Liquid separation zone. The suspended solids are also separated to prevent escape of

solids from the reactor.

Gas-Solid – Liquid Separation: In gas solid liquid separation a hood fabricated in M S and duly

painted with corrosion resistant paint is provided. The hood separates the solid from the overflowing

reactor content. Gas collectors are provided for collection and conveyance of gas. The treated

effluent overflows through a launder and will take to a secondary treatment.

Aeration tank:

The partially treated effluent from UASB shall then be subject to activated sludge process for further

reduction of organic matter. Aeration tanks are provided for degradation of organic matter through

biological process. Microorganism in the controlled environment carries out the biodegradation

process. The container i.e aeration tank of requisite capacity is provided for this purpose. The tank

shall be provided with an aeration mechanism to transfer the oxygen from air to tank content for

survival for microorganisms. Slow speed fixed type surface aerators shall be provided for this




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purpose. The content in the aeration tank is kept under constant aeration and mixing. The aeration

thank shall be constructed in RCC.

Secondary Clarifier:

A secondary Clarifier in the form of circular tank shall be provided for settlement of fully aerated

Effluent from the aeration tank. The tank shall be provided with centrally driven fixed bridge type

clarifier mechanism. Part of the settled sludge at the bottom of the settling tank will be pumped to

the aeration tank and part of it will be discharged on sludge drying beds as per operational

requirement. This sludge being fully mineralized is suitable for sun drying on sand drying beds.

Sludge Drying Beds: In aeration system the sludge is sufficiently mineralized and does not need

any further treatment before dewatering and disposal. Sand filtration drying beds will be provided,

where sludge will be dewatered by filtration through sand bed and sun drying of the dewatered

sludge is scraped & may be used as manure after composting.

Note: All the civil structures in the ETP except sludge drying beds will be constructed with

RCC M20 grade to make them impervious. Sludge drying beds will be constructed with brick

masonry. Sugar ETP diagram shown below




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B) Cogeneration Power Plant

Total wastewater generation from power plant will be 227 Cum/day. The effluent generated from

power plant will be sent to Sugar plant ETP. The treated effluent will be utilized for Greenbelt

development, Dust suppression and ash conditioning.

Sanitary waste water will be treated in septic tank followed by soak pit. Hence there will not be any

adverse impact on environment due to the proposed activities. ETP diagram shown in below.

C) Distillery Plant:

With Molasses:

As per CPCB recommendations the spent wash quantity will be restricted to a maximum of 10 kl/kl

of R.S. for Molasses by adopting continuous fermentation technology with yeast recycle. The

Maximum Spent wash generation from the proposed Ethanol plant with Molasses as raw material

will be 600 KL/day.

The spent wash will be concentrated to 60% solids in Multiple Effect Evaporators and then will be

incinerated in exclusive 25 TPH Boiler. This is a ZERO discharge system already approved by

Central Pollution Control Board.

EVAPORATION SYSTEM

The objective of Evaporation is to concentrate a solution consisting of a volatile solute and a volatile

solvent. Evaporation is conducted by vaporizing a portion of the solvent to produce a concentrated

solution of thick liquor with 60% solids and 40 % moisture content.

The evaporation system consists of 5 evaporators, which are connected, in series. The spent wash

will be pumped from distillation section, which will be fed to the evaporator by using feed pump. Gas

Liquid separator (5 Nos.) will be used to separate the vapor and liquid. Both Vapor & Spent wash

will be fed to the next evaporation effect so it is called as feed forward effect evaporation. The vapor

from last evaporator will be condensed in condenser and transferred to the dryer while the

condensate from the evaporators is first utilized for heat recovery. While vacuum pump maintains

vacuum in the entire system. Product final thick spent wash with 60% solids will be used in boiler for

incineration.

INCINERATION OF CONCENTRATED SPENT WASH

The final concentrate from the Evaporators (60% solids w/w) will be incinerated in the Boiler by

mixing with coal. The condensate from the Evaporation system will be reused in the plant operation.

Zero discharge will be implemented as per CREP recommendations. ETP diagram shown below

Figure – 10.1




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Non Process Effluent Treatment & Disposal:

The boiler blow down & DM Plant & Softener regeneration water will be treated in a neutralization

tank and after treatment it will be mixed with CT Blow down. All these treated effluent streams will

be stored in a Central Monitoring Basin (CMB). The treated effluent will be used for dust

suppression / ash conditioning and onland for irrigation within the premises after ensuring

compliance with CPCB / KSPCB standards. The scrubbed water from CO2 Scrubber will be

consumed in the Fermentation section. The effluent will be used for greenbelt development within

the plant premises after ensuring the compliance with CPCB / KSPCB standards.

Storage Lagoon:

A Spent wash storage lagoon of storage capacity of 5 days which is less than 30 days will be

provided as per CPCB protocol. Closed storage tank will be provided.




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3.11 Solid Waste:

The following are the solid waste generation & disposal.

S.No Solid waste Quantity (TPD)

Disposal Existing Expansion Total

Sugar Plant

1. 1.

Bagasse 1425 825 2250 Will be used as fuel in Co-gen Boiler

2. 2.

Molasses 213.75 123.75 337.5 Will be used in the proposed Distillery

3. 2.

Filter cake 190 110 300 Will be given to the farmers to use as manure in the Agricultural fields

4. ETP Sludge 0.19 0.11 0.3 Will be used as manure Cogeneration Power plant

5.

When Bagasse used as fuel in Boiler 24.25 26.25 50.5

Will be disposed to farmers to use as manure in Agricultural lands

When Coal used as fuel in Boiler 18.8 24 42.8

Will be given to cement plants/brick manufactures

Distillery

6. Yeast Sludge -- 2.2 2.2 Mixed with spent wash and incinerated in the boiler.

25 TPH Incineration Boiler

7.

When concentrated spent wash used as fuel in Boiler

-- 10 10

Ash generated will be used as

manure

When Bagasse used as fuel in Boiler

-- 3.5 3.5 Ash Will be disposed to farmers to use as manure in Agricultural lands




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4.0 SITE ANALYSIS

4.1 Connectivity:

Component Description

Road The site can be well approached by a NH # 13

Rail Nearest Railway station located at 27 Km South west

Air port Nearest Airport located at Belgaum which is at distance of 145 Kms

from the Plant site

Sea Port Goa port is at a distance of 230 Kms from the Plant site

4.2 Land form, Land use and Land ownership:

The present use of the land is Industrial as Sugar and Co-generation power plant is under

operation. Now the proposed expansion of Sugar and Co-gen power plant and new Distillery plant

activities will be taken in the existing plant premises only.

4.3 Topography:

The topography of the land is more or less flat without undulations.

4.4 Existing land use pattern:

The present use of the land is Industrial

4.5 Existing Infrastructure:

The infrastructure required for operating the 3500 TCD of Sugar Plant and 15 MW Co-gen Power

plants exists at the Plant site

4.6 Soil classification:

The soil at the site is Black soil.

4.7 Climatologically data: GEOGRAPHICAL LOCATION:

Bagalkot district is located in the northern part of Karnataka state. The district lies between 15º46¹

and 16º46¹ north latitude and 74º59¹ and 76º20¹ east longitude. The district has boundaries with

Bijapur district in north and Belgaum district in west and Raichur & Koppal in east and Gadag in

south directions. Bagalkot district has an area of 6593 sq.km. The total Population of Bagalkot

district according of 2001 census is 1.65 million.




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CLIMATE:

The climate of the district is generally dry and hot. The hot weather season begins by middle of

February reaches peak during April / May and slowly temperature declines. From beginning of June

followed by the southwest monsoon season extending to the end of middle of September and last

up to November end. The cold season starts from December, end by the middle of February. The

season from December to February is a period of generally fine cool weather.

TEMPERATURE & RELATIVE HUMIDITY:

The highest mean daily maximum temperature in the district is in the month of May which ranges

between 38ºc which is the warmest month, Over major part of the district with the onset of monsoon

early in June here is appreciable drop in the day‟s temperature, January is generally the coolest

month with mean daily minimum temperature ranges between 15ºc to 18ºc.

The average relative humidity in July and August month is about 60 to 80% over major part of the

district. The lowest relative humidity is in April / May months which is about 30% and even as low as

10% on individual days.

RAINFALL:

The average rainfall in the district is 562 mm. The actual rainfall for the last year is 228 mm. The

district receives 40% of the total rainfall in the south west monsoon period from June to September.

4.8 Social Infrastructure Available:

The following are the educational and other infrastructural facilities in the district

S. No Particulars Numbers / Values

01 Educational facilities

a) Pre-primary NA

b) Primary

LPS 608

HPS 1035

Others 22

c) Middle NA

d) High 349

e) Higher- secondary NA

02 Professional colleges

a) Medical 1

b) Engineering 1

c) Agriculture / Horticulture 1




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d) Veterinary / Fisheries -

e) Others (Please specify) -

03 Number of Arts and Science Colleges 88

04 Institutional Credit Facility

a) Name of the Lead Bank Syndicate Bank

b) Number of branches of lead bank in the

district

182

c) Other Commercial Banks 88

d) Primary Land Development Bank 6

e) District Central Co-operative Banks 1

f) Urban Banks 14

g) Primary Agricultural Co-operative Credit

Society

207

h) Housing Co-operative Societies 20

i) Employees Co-operative Societies 58

j) Weavers Co-operative Society 111

k) Industrial Co-operative Society -

l) Khadi and Village Industries Societies -

m) Industrial Co-operative Societies 07

n) Primary Co-operative Stores 2

o) Co-operative Sugar mills 1

q) Other Marketing Society (please specify) 6




37

5.0 PLANNING BRIEF

5.1 Planning Concept:

The integrated complex will be of Sugar, Co-gen, & Distillery. Project at SSL will integrate sugar mill

operations with enhanced energy efficiency measures and optimum usage of Molasses and

Bagasse. During season, the Co-gen Plant will operate on procured bagasse, other bio-mass fuels

and coal.

All excess available power is exported to the KPTCL grid. During off-season procured Bagasse /

biomass from nearby sugar mills will be used in the Co-gen plant and power generated, less

auxiliary consumption will be pumped to the KPTCL grid. KPTCL has an attractive policy on the

guidelines of MNES, to buy power from sugar cogenerations. Molasses generated from the Sugar

Plant will be utilized for Distillery plant operation.

Further, the integrated Sugar, Co-gen, and Distillery projects will improve the overall profitability of

SSL, through its additional revenue generation. This will enable SSL to give higher dividend to

promoters & higher price per ton of cane to its cane growers. Also the project will help to improve

Karnataka State‟s power situation apart from providing ethanol for use.

5.2 Population Projection:

Unskilled Man Power required for the proposed expansion Project will be met from the local villages

completely. Qualified semi skilled man power require will be met from local villages if available.

Hence there will not be much population increase in the area.

5.3 Land use Planning:

The following is the Land use Planning of the area

ITEM EXTENT OF LAND (ACRES)

Existing Expansion After expansion

Built-up area 57 25 82

Internal roads 5 5 10

Storage areas 15 5 20

Parking area 5 0 5

Greenbelt 60

Vacant area 0.2

Total 177.2

5.4 Amenities / Facilities:

Facilities like canteen, rest rooms and recreation facilities will be provided in the proposed

expansion project. No other additional facilities are proposed.




38

6.0 PROPOSED INFRASTRUCTURE:

6.1 Industrial area

The following Plant and machinery will be installed in the Industrial processing area

List of Plant and Machinery for proposed expansion

Sugar Plant

SUGAR PLANT MASTER EQUIPMENT SCHEDULE

Item

No. Item Description Nos. Type/Capacity

0100 Cane Weighment

0101 Cane weighbridges 2 1 #60 T capacity

1 #10 T capacity

0200 Cane Unloading

0201 Cane unloader 2

Sling Type cane unloaders 7.5T

SWL Capacity,

0201.1 Gantry and structure 1

0202 Feeder table 2 1 # 7 m X 7 m

0300 Cane handling & Preparation

0301 Feed Cane Carrier 1

Head end shall be suitable to 2200

mm swing dia. Fibrazor.

Chain strength should be 60 T

breaking load. Head end

Sprocket is 16 teeth.

0302 Prepared cane carrier 1

0303 Chopper 1

2 #250 HP HP motor will run in

reverse direction at 300 rpm

through gear box having 1.95:1 ratio

0304 Leveler 1

2 #350 HP HP motor will run in

forward direction at 585 rpm

0305 Fibrazor 1

2200 mm swing dia, 144 nos.

hammers of 23kg with new

Pocketed type anvil.

0305.1 Cane pusher 1

1400 mm dia pusher driven by 30

HP/1440 rpm through

speed reducer and open spur gear

0306 Auto cane feed control Lot

0400 Juice Extraction Plant

0401 Donnelly chute 2

0402 Mills 2

2 # Mills 42" x 84" with pressure

feeding system.

First and last mill s to be provided

with GRPF

0402.1 Under feed roller 2 UFR of 1100 mm PCD

0403 Mill drive 2

2# 1250 HP AC /Planetary drives




39

0404 Inter carrier 2

Rake carrier with 50 HP drive carrier

speed shall be

25m/min

JUICE HANDLING

EQUIPMENT

0406 Juice Screen 1 Rotary screen with 0.35 slit opening.

0406.1 Cush - Cush conveyor 1

Double scroll type 410 mm dia x

7000. The screw

conveyor is driven by 10 HP / 1440

rpm

0407

Mass flow meter for imbibition

water 1 150 cu.m/hr capacity, 50 m head

JUICE PUMPS

0408.1 Unscreened juice pump 2 350 cu.m/hr, 12 m head 960 rpm

0408.2 Screened Juice pump 3 400 cu.m/hr, 12 m head 960 rpm

0408.3 Imbibition juice pump 2

350 cu.m/hr, 12 m head, 30 HP/960

rpm - 2 nos.

0408.4 Imbibition water pump 2

200 cu.m/hr, 50 m head, 50

HP/1440 rpm

0409 Mill house crane 1 Install 1# 40 t EOT crane

0409.1 Mill house gantry Lot

0410 Millhouse lathe 1

Install 1# lathe to be procured to

suit 1200 x 5000 mm rollers

grooving

0500 JUICE TREATMENT

0501 Water flow meter 1 0-200 t/h, volumetric flow meter

0502 Water weighing scale 1

0503 Juice flow meter 1

Install 1 # volumetric flow meter with

density compensation

in parallel with the flow meter.

Capacity 200 t/h

0504 Juice weighing scale 1

0505 Driver trough 1

0506 Check weighing scale

0507 Weighed juice receiving tank

0508 Weighed juice pumps

0509 Phosphate addition system

0509-A Preparation tank

Install 1 # phosphoric acid

preparation tank.

Capacity 1 cu.m

0509-B Storage tank

0509-C Dosing pump

Install 1 # dosing pump of capacity

100 lph

0510 Juice flow stabilization system 1

Install common control system

suitable for 400 t/h

for both the flow meters.

0511-A Juice sulphitor 1 250 HL capacity




40

0511-B Prelimer 1

0512

pH control system for juice

sulphitor 1 pH control system

0513 Sulphured juice receiving tank 1 Cylindrical tank, Cap : 12.5 cu.m

0514 Sulphured juice pumps 3

Install 2 # 400 cu.m/h, 60 m head

pumps.

0600 CLARIFIER & FILTERATION

0601 Flash tank 1

Install 1# flash tank suitable for

clarifier

Install 1# volumetric flow meter &

control

valve to control flow to the clarifier

0602 Clarifier 1

Install 1 # clarifier of 36' dia or

Install 1# short retention time

Clarifier suitable for 2750 TCD.

0603 Polyelectrolyte preparation tank 1 Install along SRT clarifier

0604

Polyelectrolyte storage / dosing

tank 1 Install along SRT clarifier

0605 Polyelectrolyte dosing tank 1 Install along SRT clarifier

0606 Rotary vacuum filters 2

2 # Dia 3600 x Long 7200 mm (12' x

24')

0607

Vacuum filtrate Pick-up

receivers 3 2 # Dia 600 x Long 1200 mm MS

1 # Dia 900 x Long 1500 mm MS

0608 Vacuum filtrate wash receivers 3 2 # Dia 600 x Long 1200 mm MS


0609 Filtrate collection tank 1 SS make dia 1100 x 2490 long

0610 Filtrate pumps 2 Cap : 70 cu.m/h, 21.5 m head

0611 Filter condenser 3 2 # Dia 600 x Long 2400 mm MS


0612 Entrainment separator 3 2 # Dia 450 x Long 900 mm MS


0613 Vacuum pump 2

2# 1200 cu.m/hr with 30 hp motor,

motor rpm 1460

pump rpm 1250

1# 300 mm size water jet air

extractor for both filters

0614 Mud overflow circulation tank 1 Dia 2235 x 1500 long

0615 Mud recirculation pump 3 Cap : 70 cum/hr, 21.5 m head

0616 Cake wash water pump 1

Install 1# pump Cap : 10 cum/h,

55.6m

head.

0617 Feed mixer 1

1 # Dia 1000 x 3500 mm long for

both filters, U shaped.

0618 Bagacillo blower and chute 2 Connected with 20 hp motor

0619 Bagacillo piping 2 1 # pipe of 500 mm dia

1 # pipe of 350 mm dia




41

0620 Cyclone separator 2 1 # MS make dia 1500 x 3150

1 # MS make dia 1340 x 2700

0621 Mud belt conveyor 1

650 mm width troughed, 36000 mm

long

0622 Cake collection bin 1 MS make 2500 x 2500 x 1100

0623

Vibratory screen or filtrate

1

80 mesh screen vibratory type with

rectangular

screen of 1075 x 1000 x 30

Filtrate Clarification System

0624 Filtrate buffer tank 1

Cap : 20 cu.m, dia 2.5 m x 4.0 m

height, steam coil

is installed inside to maintain

temperature of filtrate

0625 Untreated filtrate pumps 2 Cap : 45 cu.m/h, 15 m head

0626 Flow meter 1 Cap : 0-50 cum/h, Magnetic type

0627 Lime sucrate preparation tank 1 Cap : 4 cu.m, dia 1.5 m x 2.25 m Ht

0628 Lime sucrate dosing tank 1 Cap : 4 cu.m, dia 1.5 m x 2.25 m Ht

0629 Lime sucrate dosing pump 2

Cap : 800 lph, 1.5 bar discharge

pressure

0630 Phosphoric acid storage tank 1 Cap : 1 cum

0631 Phosphoric acid dosage pumps 2


pressure

0632 Flocculent preparation tank 1 Cap : 4 cum, dia 1.5 m x 2.25 m Ht

0633 Flocculent dosing tank 1 Cap : 4 cu.m, dia 1.5 m x 2.25 m Ht

0634 Flocculent dosing pumps 2


pressure

0635 Reaction tank 1

Cap : 2 cum, Dia 1.1 m x 2.25 m Ht.,

Impeller

speed 48 rpm

0636 Aeration pumps 2 Cap : 20 cu.m/h, 15 m head

0637 Filtrate floatation clarifier 1 Cap : 13 cu.m, Dia 3.0 m x 1.8 m Ht.

0638 Automation Set Total system is automated

0700

Milk of Lime and SO2

Prepartion

0701 Quick lime elevators 1

Electric hoist for bag lifting with 0.5

hp motor

0702 Lime slaker 1

Cap : 1200 Kg/h, 5.5 KW, 12 final

rpm

0703 Lime clarifier 1

Koran, 3.7 KW, perforation dia 0.5

mm

0704 Vibratory screen 1

Circular, 60 mesh size, 3.7 KW, 1.5

m dia

0705

0706 Milk of lime storage tanks 2

Dia 3000 x 3150 mm height, 20 cum

each, 5 KW

0707 Milk of lime pumps 2

Install 1 # new pump cap: 10 cu.m/h,

20 M head.




42

0708

Sulphur burners for juice,

Continuous type 2 200 kg./h. Film Type Burners

0709

Sulphur burner for syrup,

continuous 2 Cap. 70 kg/h one working

0710 Air compressor 4

Install 1# 1000 cum/h air

compressor

0711 Air receiver 1

air receiver for compressor suitable

for two compressors

0800

Juice heating and

Evaporation

0801

Raw Juice Heater (Tubular

type) 2 300 sq. m heating surface

0802 Condensate Receiver for JH 2

Collect juice condensate to common

receiver for both

juice heaters

0803 Condensate pump 2

Use both pumps for common

receiver. One working and

one stand by

0804

Sulphured Juice heater

(Tubular type) 3 300 sq. m heating surfaces.

0805 Condensate Receiver for JH 3

Use only 2# condensate receivers

one each for each

effect bleeding

0806 Condensate Pump 3

20 cum/h capacity, 30 m head

condensate

pumps for SJ1 & SJ2

0807 Clear juice Heater 2 2 # Direct contact Heaters

0808 Condensate Receiver for JH

0809 Condensate pump

0810 Clear juice column 1 Dia 3000 x 5000 height

0810 A Clear juice filters

Install 2 # leaf filter for clear juice

filtering suitable for 4000

TCD with all accessories

0811 Clear juice pump 2

Capacity 250 cum/h and 60 m

head to CJ pumping

0812

Intermediate juice receiving

tank

0813

Evaporator Set Quintuple

0814 Quint I 1

2500 sq. m body as Quintuple 1st

effect.

0815 Quint II 1

2700 sq. m body as Quintuple 2nd

effect.

0816 Quint III 1

1250 sq. m body as Quintuple 3rd

effect




43

0817 Quint IV 1

600 sq. m body as quintuple 4th

effect.

0818 Quint V 1

600 sq. m body as quintuple 4th

effect.

0820

Condensate receiver for Quint -

1st effect 1

Install 1# 1.2 mtr dia and 2.0 mtr

height mound

0821

Condensate pump for Quint-1st

effect 2

Install 1# 130 cu.m/hr, 30 m head

condensing pump as

common standby for quintuple 1 & 2

bodies

0822

Condensate receiver for Quint-

2nd effect 1

Install 1# 1.2 mtr dia and 2.0 mtr

height mound

0823

Condensate pump for Quint -

2nd effet 1

100 cum/h, 30 M head pump for this

duty pump

0824


3rd effect 1

Quintuple 3rd effect condensate

receiver

0825

Condensate pump for Quint -3rd

effect 1 Cap : 50 cum/h, 30 m head

0826


4th effect 1

Quintuple 5th effect condensate

receiver

0827

Condensate pump for Quint -4th


0828


5th effect 1

Quintuple 5th effect condensate

receiver

0829

Condensate pump for Quint -5th


0830

Common condensate flash tank

for 2nd Condensate 1

2.5 meter dia and 5.0 meter length

receiver

0831

Common condensate flash tank

for pan and JH Condensate 1

2.5 meter dia and 5.0 meter length

receiver

0832 Syrup receiving tank 1 Dia 1000 x 1500 mm height

0833 Syrup Extraction Pump 2 Cap : 70 cu.m/hr, 30 m head

Syrup Clarification System

0834 Buffer tank 1 Cap : 32 cum, Dia 3.89 m x 2.5 m Ht

0835 Untreated syrup pumps 2 Cap : 70 cum/h, 30 m head

0836 Syrup heaters 2

HAS 77.5 sq. m, 144 tubes, 45

OD/18 SWG/4 m length, 9

tubes / pass, 16 passes

0837

Color precipitant preparation

tank 1 Cap : 1 cum

0838 Color precipitant dosing tank 1 Cap : 1 cum

0839 Color precipitant dosing pumps 2


pressure

0840 Phosphoric acid storage tank 1 Cap : 1 cum

0841 Phosphoric acid dosage pumps 2


pressure




44

0842 Flocculent preparation tank 1 Cap : 4 cum, dia 1.5 m x 2.25 m Ht

0843 Flocculent dosing tank 1 Cap : 4 cum, dia 1.5 m x 2.25 m Ht

0844 Flocculent dosing pumps 2


pressure

0845 Reaction tank 1 Cap : 32 cum, Dia 1.465 m x 1.72 m

0846 Aeration tank 1 Dia 0.45 m x 2.0 m Ht.

0847 Syrup floatation clarifier 1 Cap : 32 cum, Dia 4.5 x 1.8 m Ht

0848 Clear syrup tank 1 Cap : 14 cum, Dia 2.1 x 4.0 m Ht

0849 Clear syrup pumps 2 Cap : 50 cum/hr, 35 m head

0850 Automation Set Total system is automated

0850A Leaf filters for syrup filtration

Install 2 # leaf filters to filter syrup

before going to pan floor

0851 Syrup sulphitor 1 Sulphitor of 15 cum working capacity

0852 Caustic Soda Tank 1

Cap : 19.4 cum, Rectangular type,

2900 x 2200 x 3000 mm

0853 Caustic Soda pumps 1 Cap : 100 cum/h, 20 m head

0854

Pressure reducing valve no.1

(PRV-1) P1 to P2 1

kg/sq.cm (g)

0855


(PRV-2) P2 to P3 1

Cap : NA, 150 mm size from 7

kg/sq.cm to 1.5 kg/sq.cm

kg/sq.cm (g)

0856


(PRV-3) P2 to P3 1

kg/sq.cm (g)

0857


(PRV-3) P4 to P2 1

Cap : 5 t/h, from 13 kg/sq.cm to 7

kg/sq.cm

kg/sq.cm (g)

0858

Overflow surplus valve for

exhaust (OSV-1)

One exhaust over flow surplus valve

of capacity 30t/hr

0859 Overflow surplus valve (OSV-2)

2# OSV's on two Quntiple two

bodies, Cap : 1# 20 t/h

and 1# 40 t/h

0860 Overflow surplus valve (OSV-3) 1#OSV as relief valve. Cap : 20 t/h

0863 Desuperheater No.1 Dia 1500 x 3000 mm height

0864 Desuperheater No.2 Install desuperheater for PRV

0900 Graining and Crystallization

0901

Syrup & Molasses storage

tanks 17 Each capacity 20 cum

5 # syrup, 2 # Melt, 1 # AL, 4 # AH,

3 # BH & 2 # CL

0902 Molasses conditioner 3

Continuous type, between runoff

storage tank and pan

supply tank

1 # Cap : 2.58 cum for AH

1 # Cap : 2.0 cum for BH




45

1 # Cap : 1.3 cum for CL

0903 A Vacuum Pan - Batch 4

80 t with mechanical circulator. With

Pan automation.

0904 Graining vacuum pans - Batch 1

60 Ton with Mechanical circulator

with automation

0905 B' Vacuum Pan - Continuous 1

Install 1 # 30 t/h continuous pan for

B massecuite

0906 C' Vacuum Pan - Continuous 1

Install 25 T /hr continuous pan for C

Boiling

0907 Pan Condensate Receiver 2

Dia 2600 x 3800 mm for 2nd vapor,

Dia 2000 x 2700 for 1st

Vapor

0908 Pan condensate pump 3 2 # Cap : 50 cum/h, 30 m head

1 # Cap : 70 cum/h, 30 m head

0909 Dry seed crystallizer 1 U Shaped Net Cap : 40 t

0910 B Seed crystallizer 1 U Shaped Net Cap : 40 t

0911 Grain Seed Crystallizer 2 U Shaped Net Cap : 90 t

0912 A Vacuum crystallizer 1 U Shaped Net cap: 40 t

0913 B Vacuum crystallizer 1 U Shaped Net cap: 40 t

0914 C Vacuum crystallizer 1 U Shaped Net cap: 40 t

0915 Crystallizer for `A' massecuite 5 U Shaped, Net Cap : 90 t

0916

Strike receiver for `B'

Massecuite 1 U Shaped, Net Cap : 90 t

0917 B' Massecuite transfer pump 1 9 „‟ x 9 “ PSP pump, 30 m Head

0918 Strike receiver for B Massecuite 1 U Shaped, Net Cap. 90 t

0919

Vertical crystallizer for B'

Massecuite 1

Install 1 # 300 t mono vertical

crystallizer for B massecuite

0920 Liquidation pump for Vert. Cry. 1

Rota type, 8" x 8", Cap : 35 t/h, 30 m

head

0921

Strike Receiver for `C'

Massecuite 1 U Shaped, Net Cap.90 t

0922 C' Massecuite transfer pump 1

0923

Strike Receiver for `C'

Massecuite 1 U shaped, Net Cap. 90T

0924

Vertical crystallizer for C'

Massecuite 1 set

Install 1 # 300 t mono vertical

crystallizer for C massecuite

0925 Liquidation pump for vert.Cry 1

Roto type, 8" x 8", Cap : 35 t/h, 30 m

head

0926 Cooler for hot water 1 Install 1# parallel heater

0927 Cold water surge tank

0928 Cold water circulation pumps 2 Cap : 36 cum/hr, 55 m head

0929 Hot water surge tank by gravity

0930 Hot water circulation pumps by gravity

0931

Hot & Cold water overhead

tank 3

1 # 7500 x 3750 x 2500 for hot

water

2 # 7500 x 4500 x 2500 for cold

water




46

0932 Service water tank 1

Concrete 40000 x 20000 x 2500, net

capacity 2000 cum

0933 Service water pump 3 1 # Cap : 450 cum/h, 22 m lead

2 # Cap : 300 cum/h, 40 m head

1000 Centrifugals

1001

A Massecuite centrifugal pug

mill 2

U shaped 5600 long x 1000 wide.

Each catering to 3

Machines

1002 A Massecutie Centrifugals 4

Install 4 # 1750 kg/charge fully

automatic DC drive

Centrifugal machines.

1003 AH molasses receiving tank 1 Dia 1900 x 1250 height

1004 AH molasses pump 2

Screw type pump of 30 t/h capacity,

25 m WC

1005 AL Molasses receiving tank 1 Dia 1900 x 1250 height

1006 AL Molasses pump 1 Screw type, Cap : 30 t/h, 25mWC

1007

Superheated wash water

system Set Suitable for 7 batch machines

1008 Superheated wash water pump 2 Cap : 20 cum/h, 55m head

1009 Air Compressor 2 Discharge pressure 6 kg/sq.cm(g)

1010 B Centrifugal pug mill 2

1 # U Shaped, 4600 long x 1000

wide, for batch machine

1 # U shaped, 6100 long x 1000

wide, for continuous m/c

1011 B Centrifugals 3

1 # Batch machines of 1250

kg/charge

2 # WK 1500, Cap : 15-18 t/h

continuous machines

1012 B-Magma mixer 2


wide for batch machine


wide for continuous m/c

1013 B Magma pump 2

1# Rota type, Cap : 20 t/h, 30 m

head

1 # Rota type, Cap : 20 t/h, 30 m

head

1014 B Molasses receiving tank 2

Dia 1500 x 1200 height, 1 # BL & 1 #

BH

1015 B Molasses pump 2

Screw type pump of 20 cum /h

capacity, 25 mWC

1016 CAW centrifugal pug mill 1 U shaped, 4600 long x 1000 wide

1017 C after Centrifugals 2

WK 1500, Cap : 10-12 t/h. 1 # B

curing machine is common

standby for CAW

1018 C After Magma mixer 1

U Shaped, 4900 long x 1000 wide

for B & CAW continuous

Machine




47

1019 C-After magma pump 1 Common for B & CAW

1020 CL Molasses receiving tank 1 Dia 1500 x 1200 height

1021 CL Molasses pump 2


capacity, 25 mWC

1022 CF centrifugal pug mill 1 6800+1000 long x 800 dia

1023 C Fore worker Centrifugals 3

wk - 1500 or equivalent machine for

C Fore curing

1024 C-Fore magma mixer 1 U Shaped

1 # 6000 long x 1000 wide, with

planetary

1025 C-Fore magma pump 3 Rota type, Cap : 20 t/h, 30 m head

1026

FM receiving tank (below

machines) 1 Dia 1500 x 1200 height

1027 FM Pump below machines 2


capacity, 25 mWC

1028 Final Molasses weighing scale 1

1029 Weighed FM Receiving tank 1 Rectangular type

1030 FM Pump below weighing scale 2


capacity, 25 mWC

1031 Final molasses storage tank 2

Cap : 7500 T each, 28 m dia x 9.50

m Ht

1032 Final molasses transfer pump 2


capacity, 25 mWC

1033 Sugar Melter 2 Cap :: 35 t/h vertical

1034 Melt pump 3

2 # Centrifugal, Cap 40 cum/hr, 30

m head

1 # screw type, Cap : 30 t/h, 25mWC

1100 Sugar Handling & Bagging

1101 Gross Hopper Conveyor 1

Single tray type, 2.0 m width, 12 m

long

1102 Fluidized bed dryer 1

1 # 40 t/h fluidized bed dryer along

with all accessories

1103

Sugar elevator from FBD to

grader 2 Cap : 40 t/h

1104

Sugar grader

2

1 # Cap : 35 t/h

1 # Cap : 35 t/h

1105

Sugar elevator from grader to

bin 2 Cap : 25 t/h

1106 Sugar Bins 3 125 t sugar bin

1107 Slat Conveyor 2 Width 400 mm, 1.5 KW

1108 Bag stitching machine 3 Cap : 300 bags/h

1109 Dry seed magma mixer 1 U Shape, Cap : 5 t

1110 Dry seed transfer pump 1

Rota type, 8" x 8", Cap : 300 t/h, 30

m head




48

Dust collector system Set

1111 Dust collector tank 2 1 # Dia 3.0m x 3.7m Ht

1 # Rectangular wet scrubber, 2.5 x

1.5 x 2.0m

1112 Dust melt pump 2 Cap : 35 cum/h, 25 m head

1113 Sugar bag belt conveyor 6 Width 600 mm

1114

Sugar bags mobile belt

conveyor 10 Width 600 mm

1115 Sugar Godowns 4

2 # 100m x 40m x 10m, Cap :

400000 bags

1200 Condensing Plant

1201 Evaporator condenser 1

1 #Single entry Vapor inlet dia :

1100 mm with automation

1202 Batch Pan condensers 5





1023 Continuous Pan condensers 2



1024

Ejector for pans & vacuum

crystallizer 1

Same system is to be followed for

new condensers also

1025 Automation Set

1026 Injection pump 4 1600 cum/h, 22 m head pumps

1027 Priming pump 1 Cap : 25 cum/h, 3.75 KW

1028 Cooling tower 3 Cap : 1600 cum/h, each cell

1029 Cooling tower water pump

1210 Priming pump 1 Cap : 25 cum/h, 3.75 KW

1400 Electricals

1401 Distribution transformers 3 2.5 MVA distribution transformer

1402 Bus ducts 4 4000 Amps,

1403 Power control centre (PCC) 3 4000 Amps,

1404 Motor Control Center (MCC) 12

1405 Distribution boards Lot

1406 Push button stations Lot

1407 Lighting Lot

1408 Earthing LOt

1409 APFC panel 2

1410 LT power and control cables Lot

1411

Miscellaneous work (cable tray,

danger baords, Lot

rail for transformer, gravel

spreading etc.)




49

Co-generation Plant:

Machinery Details:

Equipment name Qty. Capacity

Boiler Capacity 1 110 T

Turbine Capacity 1 19 MW

Electro Static Precipitator 3 Fields

FD Fans 2

ID Fans 2

Air heaters 1

Feed water system 2 HP heater-1 with 16 ata extraction steam

HP heater-2 with 8 ata extraction steam

Feed water pumps 3 80tph capacity,110kg discharge pressure

HP LP dosing system 2 HP dosing pumps for steam drum dosing

2 LP dosing pumps for derator dosing

Dearator 1

Bagasse Handling system 1 90 TPH

Coal Handling System 1 45 TPH

Biomass preparatory system 1

Feed regulation station 1 Control valve station with manual by pass

station

Atemperation system 1 Spray between primary super heater and

secondary super heater

D M plants 2 each 400 OBR at 30TPH

Water clarifier 1 200 TPH

Cooling tower system

No. of cells 4 1600 Cum.Mtr/Hr

Cooling tower pumps 4 1600 Cum.Mtr/Hr, Discharge pressure -

3.25 KSC

Two pass surface condenser with

cooling water flow 4200 Cum.mtr/Hr

Condensate extraction system

Pumps 3 50TPH each at 6kg pressure

Gland steam condenser 1 100 TPH

Steam ejectors 2 Main

1 Hogging

Turbine lub oil system/control oil

system

1

package

ST switch gear- 11kv

Generator transformer - 36MVA-

11/110kv

Distribution transformers 3 2.50mva each, 11kv/415volt

1 3.15mva, 11kv/415v

Diesel generator set 1 1500 kva

PRDS system 1 75 tph,87/8 ata

1 80tph,8/2.5ata




50

Pumping station at Kali river & Piping

Pumps 3 100 tph each, Pressure-4kg

Priming pump 2 20 tph

Infiltration pump 3 100 tph

Electrical substation at Kali pump

hose with 11kv/415 v transformer,

MCC and 250 kva diesel set

Switch Yard

110kva breaker 2

11kv breaker 1

100kv Isolators 3

CTs and PTs as per the requirement

Double circuit 110kv line to Haliyal

substation

Bio mass storage yard area 20 acres with all Fire fighting system

Fire fighting system for complete

complex

Fire water pump motor driven 1 100 TPH at 10 KSC

Fire water pump diesel set driven 1 100 TPH at 10 KSC

Jacky pump 2 30 TPH at 10KSC

Distillery Plant:

SECTION I : FERMENTATION HOUSE :

MOLASSES WEIGHING SECTION :

1] Weighscale / Loadcell for Check : 1 No.

weighment. Capacity : 3 MT

2] Molasses feed tank : 1 No.

Material of construction : M.S

Capacity : 50 MT

- FERMENTATION EQUIPMENTS

1. PROCESS TANKS

A] Fermenter : 2 Nos

Material of construction : MS

Capacity : 500m3

Equipped with roof manholes, air sparger in stainless steel construction, sight and light

glass assemblies, level indicator, defoaming oil sensor, pressure relief device and required

nozzles and fittings.




51

All internal surface will be sand blasted and epoxy coated ( 1 primer coat followed by 2

finish coats - min. DFT (150 micron ).

B] Propagation Vessel I

Design code : ASME VIII, Div. 1

Material of construction : SS 304

Capacity : 180 L

Equipped with sight glass, air sparger, cooling jacket, relief valve and necessary nozzles and

fittings.

C] Propagation Vessel II

Design code : ASME VIII, Div. 1


Capacity : 2000 L

Equipped with sight glass, manhole, air sparger, relief valve and necessary nozzle and

fittings.

D] Propagation Vessel III

Geometric Capacity : 100,000 L

Design code : IS 803

Material of construction : MS (epoxy lined)

Equipped with shell and roof manholes, air sparger, sight and light glass assembly and

necessary nozzles and fittings.

All internal surfaces will be sand blasted and epoxy coated (1 primer coat followed by 2

finish coats - min. DFT 150 micron).

E] Defoaming Oil Day Tank.

Capacity : 1000 L

Material of construction : MS

2. PROCESS PUMPS :

A] Molasses feed pump : 1 + 1 standby.

Type : Positive displacement

Material of construction : CI with SS wetted parts.

Shaft sealing. : Gland packing.

Drive : Variable speed

-Molasses storage to feed : 1+1

-Weighing to diluter : 1+1

B] Fermenter Cooling Pump : 2 + 1 standby

Type : Centrifugal


C] Fermenter Discharge Pump : 1 + 1 standby

Type : Centrifugal




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D] Wash Transfer Pump : 1 + 1 No.

Type : Centrifugal


E] Sludge Pump : 1 + 1 No.

Type : Centrifugal


F] Recycle Pump : 1 + 1 standby

Type : Centrifugal


G] Propagation II Cooling Pump : 1 Nos.

Type : Centrifugal


H] Defoaming oil dosing Pump : 1

Type : Positive displacement.

Material of construction : GI

3. PLATE HEAT EXCHANGERS. [ Alfa Laval make ]

M.O.C of Qty

Plates Nos.

a] Prop II Temp. Control PHE SS 316 1

b] Fermenter Cooling PHE SS 316 2

(Min.AK 20 FMI 168 plates each with back flushing arrangement)

4. MISCELLANEOUS :

A] Positive Displacement Blowers : 1 + 1 standby

Type : Twin lobe

Material of construction : CI body, cast steel.

Braided with suction/discharge silencers, relief valve, non-return valve & suction filter.( water

cooled) OR

Alternatively Vacuum Pump may be considered for same duty.

Capacity : 1700nm3/hr+900nm3/hr

Head : 9 MWC

B] Carbon-di-oxide Scrubber : 2 Nos.

Type : Sieve plate column


Plate material : SS 304




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Diameter : 600mm

With water spraying arrangement in AISI 304, sight glass and packing support grid.

C] Strainers - : 3 Nos.

For : 1) Fermented wash

2) Recycle.

3) Diluted Molasses

Type : Basket

Material of construction : AISI 304

Hole size : 0.6 mm

D] Sterile Air filters : 2 Nos.

Capacity : 20 M3/Hr. & 120 M3/Hr

E] Water molasses static mixer in AISI 304 : 1 No.

F] Air Compressor for Instrumentation Air : 1No+1No (Common for entire

plant including Mol. Sieve plant)

5. YEAST RECYCLING SYSTEM :

A] Yeast Separator [Alfa Laval make] 2 + 1 Nos.

Indigenous model DX 409

B] Chain Pulley block with travelling trolley : 1 No.

Capacity 1 MT

C] Cleaning table for separator in MS : 1 No.

D] Yeast Cream Funnel : 3 Nos.

Material of construction : SS304

E] Hydrocyclones : 1 Set.

Material of construction :

- Body : AISI 304

- Cone : Ceramic

6. CIP SYSTEM :

I CIP tank/Hot water tank : 1 No each.

Capacity : 2000 L

Material of Construction : AISI 304

II CIP Pump : 1 No.

Type : Centrifugal


7. Cooling Tower : 2 Nos. 400 Cu.m./ hr.




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SECTION II : Distillation

1 Analysing Column (Vacuum) Material of Construction : SS304

Type of Trays : Sieve

No. of trays : 50

Tray spacing : 750mm

Diameter : 1698mm / 2195mm

(min. diameters mentioned)

2 Rectifying Column (Under pressure) Material of Construction : SS304


No. of trays : 144

Tray spacing : 300

Diameter : 1790mm


3 Aldehyde Column Material of Construction : SS304


No. of Trays : 60

Tray spacing : 250mm

Diameter : 710mm


7 Beer Pre-heater : Shell & Tube type

Material of Construction : SS 304

Tube length : 3000mm

Tube thickness : 1.25mm

8 Analysing coloumn Reboiler : Shell & Tube type

Material of Construction : Shell: 304Tubes: SS316



Qty : 1+1

9 Stripper Rectifier Column Reboiler

Type: Shell & Tube

MOC: Tubes : SS304 Shell : CS, Ends : CS

Qty : 1 Nos.




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10 Final Condensor : Shell & Tube type

Material of Construction : Tube and tube sheet are in

SS 304, water side in CS



11 Aldehyde Condensor : Shell & Tube type




12 Aldehyde Vent Condensor : Shell & Tube type




13 Final Product Cooler : PHE

Material of Construction : SS 304 plates

Area : Suitable

14 Fusel Oil / Heads Spirit Cooler : Vertical type


15 Fusel Oil washer decanter : Vertical type


16 Steam Chest : 1 No.

Material of Construction : MS

17 Hot water tank

Capacity : 1 M3

Material of Construction : MS

18 Reflux Tanks : 2 Nos.

19 Plate Heat Exchangers:

Sr. Description M.O.C. (Plates) Qty.

I Wash Pre-heating PHE SS316 2

II Recycle Wash Cooler (Recycle) PHE SS316 1

III Spent Wash Cooler PHE SS316 1




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20 Pumps : With flame proof motors, mechanical seals & back pull out rotor design.

Sr. Description M.O.C. Qty.

IV Rectifier Reflux Pump SS316 1+1

V Weak Alcohol feed pump SS316 1+1

21. Cooling Tower : 2 Nos. 375 Cu.m. / hr.

SECTION III: Molecular Sieve Dehydration:

1 Mol Sieve Superheater

Type: Shell & Tube

MOC: Tubes: SS304 Shell: CS Bonnets: CS

Qty : 1 Nos

2 Mol Sieve Unit

Type: Dished ends; with packed bed of Molecular Sieves

MOC: SS

Qty: 2 Nos

3 Mol Sieve Condenser

Type : Shell & Tube

MOC: Tubes: SS304 Shell: CS Bonnets: CS

Qty : 1 Nos.

4 Mol Sieve Product Cooler

Type: PHE

Qty : 1 Nos.

5 Mol Sieve Regenerant Condenser

Type: Shell & Tube

MOC: Tubes : SS304 Shell : CS Ends : CS

Qty : 1 Nos.

6 Mol Sieve Regenerant Drum

Type: Dished top & bottom

MOC : SS

Qty: 1 Nos

7 Mol Sieve Vacuum Pump Drum

Type: Dished top & bottom

MOC : SS

Qty: 1 Nos. 1




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8 Mol Sieve Recirculation Cooler

Type: PHE

Qty : 1 Nos.

9 Mol Sieve Regenerant Pump

Type: Centrifugal

MOC: Impeller:SS Casing: CI

Qty: 1 + 1 No.

10 Mol Sieve Vacuum Pump

Type: Liquid Ring

Qty : 1 No+1No

11 Rectified Spirit Day Tanks: 2 Nos. MS , Capacity : 100 KL Each.

Additional Columns for ENA Production.

Extractive Distillation Column

Recovery Column

Polishing Column

6.2 Residential Area (Non Processing area):

Facilities like canteen, rest room and indoor games facilities will be provided in the proposed

expansion project.

6.3 Green Belt:

Total 1/3rd of the total area including existing will be developed in the Plant premises.

Greenbelt development plan

Local DFO will be consulted in developing the green belt.

Greenbelt of 60 acres will be developed in the plant premises as per CPCB guidelines.

15 m wide greenbelt will be developed all around the plant.

The tree species to be selected for the plantation are pollutant tolerant, fast growing, wind

firm, deep rooted. A three tier plantation is proposed comprising of an outer most belt of

taller trees which will act as barrier, middle core acting as air cleaner and the innermost core

which may be termed as absorptive layer consisting of trees which are known to be

particularly tolerant to pollutants.




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6.4 Social Infrastructure:

Social infrastructure will be developed as per need based in the nearby Villages.

6.5 Connectivity:

Component Description

Road The site can be well approached by a NH # 13

Rail Nearest Railway station located at 27 Km South west

Air port Nearest Airport located at Belgaum which is at distance of 145 Kms

from the Plant site

Sea Port Goa port is at a distance of 230 Kms from the Plant site

6.6 Drinking water management:

Drinking water required for the workers will be met from ground water resources.

6.7 Sewerage system:

Domestic waste water generated will be treated in septic tank followed by soak pit.

6.8 Industrial waste management: 6.8.1 Waste water management

Waste water generated from the proposed Project will be treated in Effluent Treatment proposed

which is furnished under paragraph 3.10.2

6.8.2 Solid waste management:

Details of Solid waste generation and disposal is furnished under 3.11

6.9 Power requirement & Supply / Source:

The portion of power requirements will be met through KPTCL. Balance Power requirement will be

met through in house generation through turbine.




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7.0 REHABILITATION AND RESETTLEMENT (R & R) PLAN

No rehabilitation or resettlement plan is proposed as there are no habitations in the in the Plant site.




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8.0 PROJECT SCHEDULE & COST ESTIMATES

The total cost of the project has been estimated at Rs. 351 Crores. The Project Cost estimates

include all expenses to be incurred towards the entire project development including Site

Development Expenses, Payments to EPC Contractor, Non EPC Expenses, Pre-Operating

Expenses, Start-Up Fuel & Commissioning Expenses, Contingency, Margin Money for Working

Capital and Financing Expenses including Interest During Construction (IDC).

Detailed breakup of the Cost is given below.

S.No. Particulars Cost in Crores

1. Land Development & Civil Works : 41.00

2. Plant & Machinery : 181.00

3. Packing, Forwarding and Taxes : 26.00

4. Erection, commissioning and structures 20.00

5.

Power connection, PCC, Cables, yard

lighting etc., : 30.00

6. Contingencies : 10.00

7. Preliminary & Pre-Operative Expenses : 3.00

8. Margin Money for Working Capital : 40.00

Total : 351.00

MEANS OF FINANCE

1 PROMOTERS (33%) : 115.83

2 TERM LOANS (67%) 235.17

Total : 351.00




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9.0 ANALYSIS OF PROPOSAL (FINAL RECOMMENDATIONS)

With the implementation of the proposed expansion project, the socio-economic status of the local

people will improve substantially. The land rates in the area will improve in the nearby areas due to

the proposed activity. This will help in upliftment of the social status of the people in the area.

Educational institutions will also come-up and will lead to improvement of educational status of the

people in the area. Primary health centre will also come-up and the medical facilities will certainly

improve due to the proposed project.

EMPLOYMENT POTENTIAL

The man power required for the industry is 500 Nos. which is inclusive of 275 nos. on permanent

basis and rest all will on Temporary or contract basis.

S.No. Particulars No. Employees

1. Technical & Administrative Staff 150

2. Skilled & Semi Skilled 275

3. Unskilled & Helpers 75

Total 500

OTHER TANGIBLE BENEFITS

The following are the other benefits to the area due to the proposed project.

Educational status will improve in the area

Medical standards will improve due to the proposed project.

Overall economic up-liftment of socio-economic status of people in the area.

Ancillary developmental activities like CO2 plant, Cattle feed plants will be created due to the

establishment of the proposed unit.

SOCIO-ECONOMIC DEVELOPMENTAL ACTIVITIES

The management is committed to uplift the standards of living of the villagers by undertaking

following activities / responsibilities.

Health & hygiene

Drinking water

Education for poor

Village roads

Lighting

Creating harmonious relationships




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Helping locals to conduct sports

Training to the unskilled manpower

HEALTH & HYGINE

1. Personal and domestic hygiene,

2. Maintaining clean neighborhood,

3. Weekly health camps offering free-check up & medicines

4. Ambulance services

5. Education & drug de-addiction, aids.

DRINKING WATER

Making drinking water available at centralized locations in the village,

SUPPORTING EDUCATION

1. Providing books to all poor children,

2. Conducting annual sports festival in the village schools,

3. Providing amenities like fans, lavatories,

4. Maintain play ground etc.

e.i.d. parry (india) limited -...

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