DETAILED PROJECT ON CONSTRUCTION OF COMMON EFFLUENT TREATMENT PLANT FOR PHASE-III & IV AND UP-

GRADATION OF EXISTING CETP OF 15 MLD TO 30 MLD OF PHASE I & II, IMT- MANESAR

THE REPORT

1.0

Manesar was a small village in the foothills of Aravali in Gurgaon District of

Haryana, until Govt. of Haryana decided to develop it as Industrial Modern

Township. It is located at a distance of about 15 Kms. from Gurgaon on

National Highway No.8 i.e. Delhi-Jaipur. It has now come up as a beautifully

laid and maintained modern Industrial Modal Township. It is located at the

longitude of 76

GENERAL

° 55' and latitude of 28°

2.0

22'. In Phase-I, Industrial activities have

been taken in about 1544 acres of land with a residential Sector of about 256

acres. In all under I to IV, 3464 acres of land stand acquired and majority of

same stands developed. This modern industrial township shall be fully equipped

with modern infrastructure facilities like roads, water supply, sewerage, storm

water drainage, electrification and horticulture etc.

This Industrial Township is in great demand now. Many multinational groups

like Maruti-Suzuki, Honda and Munjal Shoewa etc. have already started

functioning in this township. Internal services have already been planned and

laid. Phase I and II with about an area of 1922 acres has already been developed.

The water supply, sewerage and storm water channel systems are functional. A

common effluent treatment plant is operative with a capacity of 15 MLD. There

is partial and defunct system of recycling of treated waste water with PCV pipe

and, therefore, is allowed to dispose of through a katcha drain excavated for

disposal of storm water during monsoon. The length of this channel is about

PRESENT SCENARIO

11900-m, before it terminates into Badshahpur nallah near railway culvert no.61 for final disposal into Najafgarh Drain. Out of this about 1000-m already stands lined with vertical wall section of 2.40m x 1.50m and with a depth of about 2.40-m below ground level, work for construction of this pucca channel is in progress.

3.0

An estimate amounting to Rs. 2027.71 Lacs was approved by the competent authority vide its letter no. HSIIDC-IA-2009/4788 dt. 22.01.2009 for construction of 25 MLD CETP with laying of 1000 Metre long 1000 mm RCC NP-3 pipe sewer connecting existing laid sewer lines up to disposal work. This connecting sewer stands laid up to disposal work, but the CETP is yet to be constructed.

NECESSITY

Another estimate amounting to Rs. 1365.28 Lacs was approved by competent authority vide its letter no HSITDC/IA/2009/4789 dt. 22.01.2009, for up-gradation of existing capacity of 15 MLD CETP to 30 MLD for phase I & II of IMT Manesar.

Necessary steps were taken for inviting bids and awarding the work. In the mean

time some offers were received from associations/ NGO/Firms with different

technological options. Process of finalizing invitation of bid was held up for

finalising the offers so received. Finally it was decided to go ahead with the

same technology option as earlier with giving a option to bidder to quote for

different technology also, if he so desires, with technical data for satisfaction of

the employer. In the mean time market prices of the relevant items of the work,

have improved by about 44%, as worked out in the accompany pages of this

project, thus necessitating preparation of this revised project for combined

CETP of 25 MLD and up-gradation of existing CETP from 15 MLD to 30 MID

capacity. Besides this it was also decided to include operation and maintenance

charges for in this project. But as desired this revised io_r_oiect for

combined CETP has be framed excluding operation and maintenance _charges,

for which estimate shall be separately processed, as and when required.

4.0 4.1

PROPOSAL

Keeping in view, the fast development of industrial area of IMT Manesar, the

DGM H.S.I.I.D.C. Manesar discussed and desired to have a project on

construction of common effluent treatment plant and requested Sh. V.K.Gupta

consulting engineer cum arbitrator to prepare the same. Hence this project is

framed. A master sewer has been laid almost upto Technology Park of 1MT

Manesar with a total discharge of 10.6 cusecs. As the technology park will have

higher wastewater discharge than normally assumed discharge for any industrial

area, hence it was desired that remaining leg of master sewer with total

discharge, including that from technology park and transport hub, be designed

along with the design of this C.E.T.P. The area going to contribute wastewater is

detailed below:

25 MLD Common Effluent Treatment Plant

Sr. No. Description Area in acres Remarks

1 Phase-I 1750 Acres To existing CETP

2 Phase-II 172 Acres To existing CETP

3 . P h a s e - I V 650 Acres Covered under this estimate.

4 . Transport Hub 466 Acres Covered under this estimate.

Hence under this project it is proposed to construct CETP to cater to the

requirement of ph- IV, transport hub, having area of 466 acres and 4 nos villages

viz village Basharia Baskushal, Dhana and Kankraula with designed population

of 10168 persons only. As,M/s Maruti

be contributing zero discharge towards waste water generation and its treatment,

Uclyoglid_has conveyed that they will

its requirement has not been considered. Capacity of CETP has been worked out

taking into account discharge from above areas/village and the present scope of

this estimate is limited to providing CETP for 510 acres falling under Phase-IV,

140 acres falling under Technology Park, 466 acres falling under transport hub

and waste water generation from aforesaid 4 Nos villages.

= 13.30 MLD

= 4.43 MLD

= 6.00 MLD

= 0.84 MLD

= 24.57 MILD Say 25 MLD '

4.1.1

Common Effluent Treatment Plant has been designed for average flow of

25MLD capacity on extended aeration process as worked out below :

Capacity Computation

a) Total area of phase IV = 650 acres b) Less area under Technology Park = (-) c) Net area under phase IV = 510 acres

140 acres

d) Net area under Transport hub = Total area = 976 acres

466 acres

e) Waste water generation i) From fresh water supply @ 4000g1n/acr/day

with interception factor of 0.75 976 x

4000 x 0.75 = 29,28,000 gallons

ii) From recycling of treated waste water

@ 2000g1n/acr/day

with interception factor of 0.50 976 x 2000 x 0.50 = 9, 76,000 gAons

iii) From technology park with interception

factor of 0.60

10 MLD x 0.60

iv) From 4 Nos village viz, Bashariya, Baskushla,

Dhana & Kankraula having a combined

Prospective population of 10,168 persons

@ 110 LPCD water supply with 75% reaching

CETP

10168x 110 x 0.75

Therefore average flow capacity of CETP = 25 MLD

4.2

A master sewer has been laid almost upto existing CETP, but sewer for residential sector -1 and future pocket of 162 acre needs to be connected with this disposal cum CETP with a separate trunk sewer line. Estimate for the same

Up-gradation of 151VILD to 30 MLD Common Effluent Treatment Plant

shall be prepared and submitted separately. Therefore it is proposed that the

present CETP of 15 MLD capacity be upgraded to 30 MLD. There is no

provision of grease & oil chamber, inlet box, grit chamber, parshall flume, fine

screens, sludge digester and sludge drying beds at the existing STP, accordingly

the provision have been made for 30MLD of both the units. Remaining units

like PST, Aeration Tanks & SST have been kept for 15 MLD. The location for

recirculation tanks have been made in the drawings but not included in the

present project.

4.2.1

The details are given as below

Capacity Computation

4.2.1.1

The area going to contribute wastewater is detailed below:

Contributing Area

Sr. No. Description Area in acres Remarks

1 Phase-I 1750 Acres To existing CETP

2 Phase-II 172 Acres To existing CETP

3. Sector-1 (Res.) 264 Acres To existing CETP

4. Sector-2 (Comm.) 50 Acres To existing CETP

5. New land 162 Acres To existing CETP Total 2348 Acres

4.2.2

The total discharge reaching CETP site has been worked out as detailed below:

Waste water generation

Sr. No. Description Discharge Remarks

1 Phase-I & II 22.00 MLD From DPR

2. Sector-1 (Res.) 4 MLD Detail attached.

3. Sector-2 (Comm.) 2.26 MLD Detail attached.

4. New land 2.20 MLD Detail attached. Total 30.46 MLD Say 30 MLD

4.3

The present day status report is detailed out here as under:

4.3.1

Status Report

Connecting sewer of 1000 mm i/d RCC NP-3 pipe stands laid up to the site

reserved for disposal works of this CETP. The connection for existing sewer line

to screening chamber needs to be made.

25 MLD Common Effluent Treatment Plant

4.3.2

The status reports of existing structure constructed at site for existing CETP are

detailed below:

Up-gradation of 15 MLD to 30 MLD Common Effluent Treatment Plant

Sr. No. Description No./Size of existing b

Structure at site

1. Grease & oil trap -

2. Screening chamber 1 No — 40 Sqm

3. Main Pump machinery

Chamber with 1 No.

4. Inlet Box -

5. Chemical House -

6. Flash Mixer -

7. Grit Chamber -

8. Parshall flume -

9. Fine Screen -

10. P.S.T 3 Nos.

11. Aeration tank - 48.20 x 24.10 2 Nos. (1152 M2)

12. S.S.T. -: 12.50 M i/d 3 Nos. (1470 M2)

13. Return Sludge arrangement -

14. Sludge Digester -

15. Centrifuge -

16. Sludge Drying beds — 6 x 7.4 x 7.2 213.12 sqm

17. Sludge Platform -

18. Effluent Channel 1 No.

19. Gas burner, gas meter etc -

4.4

Sr. No.

Pumping Machinery

Description of structure

Description of machinery Qty. Remarks

(A) Collecting tank 1. Non clog sewage submersible pump set 25HP

2. Non clog sewage submersible pump set

12.5HP .7 /

3. Horizontal centrifugal pump set 12.5 HP (S-P- 4L)

6 Nos

1 No /

11 No

/

In working condition.

In working condition.

In working condition.

-

(B) Primary settling tank 2 Nos. working N 1-l-(one lleinused-as: Sludge sump )—

X

1. Clarifier 0.50HP 2 Nos. motor each tank.

. .. _ _ ..., . __., ___

2. Horizontal---cOlifugal-- ,.,.-_. pump set 1-0 HP (SP-4L)

(----- 4 Nos

..

2/Nos

In working condition.

-In working condition.

(D) Aeration tanks — 2

Nos 1. Fixed type aerator 30

HP( Surface aerator) 4 Nos In working condition.

(E) Secondary settling tank - 3 Nos (2 Nos. working)

1. Clarifier 0.51-1P 1 motor each tank

2. Non clog sewage pump set 12.5HP

7 . ;,-.. -

2 Nos

2 Nos

In working condition.

In working condition.

(F) Sludge drying beds 1. Horizontal centrifugal'pump (SP-4L) 12.50 HP

, 1 No. In working condition.

(G) Treated water tank '"1. Horizontal centrifugal pump (SP-6L) 25 HP

2 Nos In working condition.

(H) Panel room 1. Electric panel for above said pumps

2. Main panel

3 Nos

2 Nos

In working condition.

In working condition.

(I) Open area DG set 400 KVA 1 No. In working condition.

(J) Open area Transformer 500 KVA 1 No. In working condition.

(K) Chemical dozing Complete set 1 No. In working condition.

4.5

A double storey laboratory building exists at existing C.E.T.P. site. It is

practically sufficient for housing laboratory cum office block, but needs minor

repairs or modifications. The list of available equipment and glassware is given

below.

Buildings

4.6

1.

List of available equipment and glassware

Jar test apparatus 1 No.

2. Heating mantle 1 No.

3. Hot air oven 1 No.

4. Conductivity meter 1 No.

5. Dissolved oxygen meter 1 No.

6. Magnetic stirrers 1 No.

7. B.O.D. incubator 1 No.

8. Laboratory balance 1 No.

9. PH meter 1 No.

10. Precision thermometer 2 Nos

11. Water distillation apparatus 1 No.

12. Manual pipette controller 1 No.

13. Hot plate 1 No.

14. Burette 10 Nos

18. Reagent bottle (PVC)

i ) 1000 ml . i i ) 500 ml .

i i i ) 250 ml . iv) 100 ml .

6 Nos.

6 Nos.

-

10 Nos. 19. Indicator Drop bottle (600m1) 2 Nos

20. Wash bottle 500 ml. 5 Nos

21. Measuring Cylinder

i ) 10 l i t e r . i i ) 5 l i t e r .

1 No.

-

22. Bucket PVC with tap 1 No.

23. Tripod stand -

24. Retort ring -

25. Retort stand -

26. Tongs (stainless steel)

6 inch

12 inch 1 Nos 2 Nos

27. Water path rectangular with 6 holes -

28. Aquarium air supply pump 1 No

29. Breaker

i) 1000 ml.

i i) 500 ml .

i i i ) 250 ml . iv) 100 ml .

5 No.

5 Nos.

5 Nos.

5 Nos.

30. Flask

i ) 500 ml . i i ) 2 5 0 m l

11 Nos.

10 Nos.

machinery, connection with sewers construction of boundary wall, office & lab, staff quarter, DG set and transformer etc for new CETP. Similarly, for existing CETP of 15 MILD, necessary provisions have been made for up gradation of existing CETP from 15 MLD to 30 MLD capacity and for provision of missing units up to 30 MLD.

4 . 8 C E T P

To treat the Industrial Effluent of Industrial Modal Township Manesar and to bring it to standard norms of disposal, fully automatic CETPs of 30 /25 MLD capacity, for phase- I & II and phase- ill & IV respectively are proposed to be constructed on earmarked sites in the Industrial Modal Township Manesar. The corporation has decided to develop this CETP which can meet the eventuality of receiving 750 BOD in the influent. Accordingly the requisite design has been carried out. It has been proposed to treat the effluent being generated by industrial estate reuse it for horticulture, washing, plumbing and air-conditioning. Presently dispose of the total/ surplus treated waste water in the adjacent storm water drain (Nalla), under construction up to Badshahpur nallah, till such time that a proper recirculation network is provided and the treated waste water is taken use of in horticulture, washing and flushing needs etc.

4.9

As desired by HSIIDC, provision for annual maintenance of bo of theyeETP making total capacity of 55 MLD has been provisioned for ,120- months for in this project as a separate component of this project. As per directions of the Corporation the estimation for annual maintenance has been carried out with assumption that BOD of the influent is 350 only.

Annual Maintenance

5.0

The methods for treatment of sewer effluent ranges from physico, chemicals and biological as depicted below:

TREATMENT OPTIONS

A) Physico- Chemicals

I ) Screen & gr i t r emova l

I I ) S e d i m e n t a t i o n I I I ) S l u d g e T h i c k e n e r s IV) V a c u u m F i l t e r s V) C e n t r i f u g e s

31. Flask volumetric

i ) 1000 ml .

i i ) 500 ml .

i i i ) 250 ml . iv) 100 ml .

-

-

-

-

32. Round bottom flask (500 ml) -

33. Measuring Cylinders

i ) 1000 ml . i i ) 500 ml .

i i i ) 250 ml .

iv) 100 ml . v) 5 0 m l .

1 No.

4 Nos. 4 Nos. 4 Nos. 4 Nos.

34. B.O.D. bottle with inter changeable stopper

capacity 300 ml.

45 Nos.

35. Pipette

i ) 1 m l .

i i ) 2 m l .

i i i ) 5 m l . i v ) 1 0 ml .

3 Nos.

-

3 Nos. 4 Nos.

36. Crucible silica capacity 100 ml 6 Nos

37. Funnel plain 60° - angle long stem

38. Desiccators large with top dia. 150mm, height

330mm

1 No.

39. Steel almirah 2 Nos

40. Office table 2 Nos

41. Chairs 6 Nos

42. Ceiling fans 3 Nos

43 Exhaust fan 1 No.

4 .7

Provision has been made for construction of 25 MLD MPS consisting of coarse screens, equalization cum collecting tank, pump chamber and pumping

Main Pumping Station (MPS)

B) Biological 1) Anaerobic

a) Contact beds b) U A S B c) Sludge Digesters

d) Anaerobic Ponds ID Aerobic a) Attached

i) Moving bed bio reactor ii) Plasma treatment

b) Suspended i) Activated Sludge ii) Extended Aeration iii) Aerated Lagoons iv) Waste Stabilization Ponds (WSP)

5.1

The following alternatives of sewage treatment have been considered for evaluation of performance characteristics, land requirement, energy input, equipment requirement and operational characteristics.

Evaluation of Treatment Processes

i) Conventional Activated Sludge Process (ASP) ii) Up flow Anaerobic Sludge Blanket (UASB) iii) Extended Aeration iv) Waste Stabilization Ponds v) Facultative Aerated Lagoon

vi) Moving bed bio reactor technology (MBBR)

The advantages and disadvantages of various processes are as under:-a) Advantages:-

Facultative / Aerated Lagoon

i) Aerated lagoons are easy to run

ii) In operating Aerated Lagoons less skilled labour is required. Disadvantages:-

i) Area requirement is large.

ii) Facultative aerated lagoons have higher civil works cost and lower mechanical and electrical works cost.

iii) Can pollute underground water unless adequate precautions are taken in construction to prevent seepage.

iv) Low BOD removal efficiency. Only about 80-85% of BOD removal could be expected.

v) Bad odour spoils the surrounding environment. Consultants' Observations:-

Due to large area requirement, cost of this treatment plant would increase abnormally and other disadvantages of this option make this process unsuitable for the STP to be established in sector 37 at Karnal.

b) Advantages:-

UASB

i) Being anaerobic process required lesser power consumption.

ii) Methane gas which is generated @ 0.08 to 0.1 cum. Per kg.of BOD load can be profitably used, if the effluent BOD loads are high.

iii) In this system, reduction of BOD up to 70-75% is achieved. Disadvantages:-

i) Being anaerobic in nature, it is susceptible to be able to have the bacteria are more susceptible to change. Raw effluent will have heavy materials and toxic compounds, which will inhabit the growth of bacteria.

ii) Moreover as the process in is the development stage and has not been widely adopted.

iii) Very careful maintenance is required, any small mistake can reduce the efficiency very low and plant has to be close down for making it normal in treatment.

iv) No significant operating data is available.

v) UASB is not suitable for industrial wastes, due to high temperature variation in North India.

vi) Treated effluent from this process needs aeration before its final disposal, thus making it costlier then the aerobic treatment.

Consultants' Observation:-

Not suitable for the present case.

c) Advantage

Activated Sludge Process

i ) E a s y t o r u n

i i ) More suitable for any modification, if required in future.

i i i ) As this is aerobic in nature, thus bacteria are easy to maintain.

i v ) Can achieve desired values of efficiency.

v ) Process is dependent on power and will stop in case of power failure. Disadvantages:-

i) Only drawback is high power requirement for supply of oxygen as compared to any other system suggested.

ii) Improved version of this process is available. Consultants' Observation:-

Not suitable for the present case, as better option is available. d) Extended Aeration

The conventional system represents early development of activated sludge process. Over the years, several modifications to this system have been developed to meet specific treatment objectives by modifying the process variables like loading rates, the mixing regime and flow scheme. A better alternate is the modified version of this process in shape of extended aeration process detailed below.

Advantage:-

i) High degree of treatment-Efficiency 95 to 98% BOD removal

ii) The excess sludge does not require separate digestion and can be directly dried on beds.

iii) Sludge production is minimum.

Disadvantage:-

i) Long aeration time

ii) Higher power consumption iii) Less F /M ra t io

Consultants' Observation:-

Extended aeration process is advantageous over other sewage treatment methods as its results give very high efficiency, to the extent of 98%, cost effective with clear, sparkling and odourless effluent and low pump head

requirement, its operation is simple and requires no skilled manpower. Hence is recommended for adopting in this project.

e) Moving Bed Bio Reactor (MBBR) Advantage:-

i) Sensitivity to small power breakdowns is low

ii) Sludge re-circulation not needed and the system is self sustaining. iii) Land requirement is about 60% of conventional system. iv) Low power consumption v) High degree of treatment vi) High degree of coli form removal

vii) Less chlorine dosing required Disadvantage:-

i) Installation cost is quite high.

ii) It requires highly skilled technical manpower for its operation and maintenance.

iii) Presently being tried for smaller units upto 1 MLD as prefabricated treatment plant for individual industry or group housing.

Consultants' Observation:-

It is a new technique, not much of experience and performance is available on larger plants at present. Needs highly skilled staff to operate and maintain. Further no significant operating data is available towards its performance and costing. Hence is not recommended.

5.2

After detailed discussions on various technical options available for treatment of waste water reaching disposal works of Manesar, the final recommendations of the consultant zeros down to extended aeration process. Recommendations have been made keeping in view the capacity of treatment plant, its location, cost economics, environmental impact, technical capacity of manpower available for maintenance and other technological restrictions and options. Accordingly, the proposed common effluent treatment plants for phase- I & II and for phase- III & IV of this Industrial Modal Township, Manesar, has been designed and enclosed in this project on extended aeration process only.

Final Recommendations

While coarse screens are provided at main pumping station before collecting tank. Another mechanically operated medium/fine bar screen is proposed to be

6.0

The design of common effluent treatment plant has been based on extended

aeration process. Activated sludge process is advantageous over other sew\age

treatment methods as its results give very high efficiency, over 92-95% removal

of BOD and total solids, its initial cost is lower, require smaller area of land as

compared to trickling filter method, effluent is clear, sparkling and odourless

and head required for operation is very small as compared to trickling filter. The

design is carried out as per standards and formulae given in the manual for

sewer and sewerage treatment published by Central Public Health Engineering

& Environmental Organization, a wing of Ministry of Urban Development,

Govt. of India, New Delhi. The treatment flow sheet will consist of inlet

chamber, screens, grit chamber/channel, flow measuring flume, Primary settling

tanks, aeration tanks, secondary settling tanks, sludge drying beds and effluent

channel etc.

DESIGN OF COMMON EFFLUENT TREATMENT PLANT UNITS

6.1

Various instruments required for functioning of individual units of CETP or

installed for recording of performance thereof, should be so provided that the

common effluent treatment plant is fully automatic in its operation.

General

6.2

Inlet chamber is provided to act as a wastewater receiving structures from the

terminal pumping station (TPS), which comprises of screening chamber — cum-

collecting tank, pump chamber and pumping machinery to pump the sewage

effluent into CETP. It also has a bye pass arrangement in case the treatment

plant cannot accept the flow. It will have hydraulic retention time (HRT) of 60

— 90 seconds at peak flow. It is proposed to provide an inlet chamber of size 3m

x 3m to receive sewage from the pump chamber for onward distribution to

CETP units.

Inlet Chamber

6.3 Screening Chamber

provided after the inlet chamber to arrest any matter which may have escaped initial screening at the main pumping station. It is proposed to provide:-

a) Screening chamber XD with coarse screen at main pumping station with width of screens = 1.8Mtr.

b) Screening chamber with medium/fine screen at CETP with width of screens = 2.30Mtr.

6.4

In order to decrease the inert suspended solids load on aeration reactor and to avoid settling the large size inorganic particles in the reactor, which cannot be withdrawn under hydraulic pressure (thereby reducing effective volume of reactor), grit will be removed from the waste water after screening. Grit can be removed either in a channel of suitable cross section with a flow control device to maintain a horizontal scouring velocity between 0.15 - 0.3 m/s at all flow rates to re-suspend any settled organic matter, or in channels and tanks without flow control device in which case it becomes necessary to wash the settled solids to remove the settled organic matter. This is achieved through a mechanical scraping, lifting and washing or aeration system. The former type of grit channels can be cleaned manually and do not require any mechanization. Both the types of devices will be designed for surface overflow rate of 1500 m

Grit Chamber

3/m2/day at the maximum flow to remove grit particles of 0.15 mm size or higher. A suitable allowance for non-ideal flow conditions will be given. It is expected that .025 - .075 m3 of grit will be collected per 1000m3

Despite the regulation for allottees to construct their own effluent treatment plants, provision of grit chamber is necessitated on account of Indian conditions where, grit finds access into the sewer through road, washing etc. Presence of grit in the effluent adversely affects the performance of reactors. A small cost of construction of grit chamber improves functioning and therefore efficiency of plant and thus has been proposed to be provided.

of wastewater treated.

6.5

Provision of oil and grease trap should be made mandatory as part of the

treatment plant of each industrial unit before disposing off its effluent into

master sewers. However, no provision of grease and oil trap has been made in

this project, as the test report indicate that level of grease and oil in the raw

sewage is well within the prescribed limits.

Oil and Grease tray

6.6

A Parshall flume is an open constricted channel which can be used both as a

measuring and also as a velocity control device, more commonly used for the

latter purpose in grit chambers. The flume has a distinct advantage over the

proportional flow weir, as it involves negligible head loss and can work under

submerged condition upto certain limits. The limit of submergence is 50% in

case of 150-mm throat width and 70% for wider throat width upto 1 m. Another

advantage is that one control section can be installed for 2 to 3 grit chambers.

The flume is also self cleansing and there is no problem of clogging. As the

Parshall flume is a rectangular control section, the grit chamber above it must be

designed to approach a parabolic cross section. However, a rectangular section

with a trapezoidal bottom may be used with a Parshall flume in which case the

variations in velocity, at maximum and minimum flow conditions, from the

designed velocity of flow should be within permissible limits as per norms. It is

proposed to provide a parshall flume suitable for flow range of 5-30MLD with

following dimensions:-

Parshall flume

Range 5-

30 MLD W

150

A

610

B

600 C 315

D 391

F 300

GK

600 75

Z 113

6.7

Primary sedimentation of sewerage also reduces the organic load on secondary treatment units. While inorganic suspended solids are removed in grit chamber, the organic and residual solids, free oil and grease and other floating material are removed in primary settling tanks, which are located after screens and grit

Primary Settling Tank

chambers. The efficiency of primary settling tank is nearly 30% and the specific gravity of organic suspended solid vary from 1.01 to 1.20.

6.8

An activated sludge plant essentially consists of the following:

Aeration Tank

i) Aeration Tank- containing microorganisms in suspension, in which the reaction takes place.

ii) Activated sludge- recirculation system. iii) Excess sludge wasting and disposal facilities. iv) Aeration systems to transfer oxygen.

v) Secondary sedimentation tank to separate and thicken activated sludge.

The main variables of the activated sludge process are the loading rate, the mixing regime and the flow scheme. The extended aeration process employs low organic loading, long aeration time, high MLSS concentration and low F/M ratio. The BOD removal efficiency is high. Because of long detention time in aeration tank, the mixed liquor solids undergo considerable endogenous respiration and get well stabilized. The excess sludge does not require separate digestion and can .be directly dried on sand beds. The excess sludge production is a minimum.

The volume of aeration tank is calculated for selected value of sludge retention time (SRT), by assuming a suitable value of MLSS concentration Tank can also be designed from F/M and MLSS concentration according to equation given as below F/M = Q So

It is seen that economy in reactor volume can be achieved by assuming a large value for X. However, it is seldom taken to be more than 5000 g/m

/ X.V

3. A common range is between 1000 and 4000 g/m3 Considerations which govern the upper limit are initial and running cost of sludge recalculation system to maintain a high value of MLSS, limitations of oxygen transfer equipment to supply oxygen at required rate in a small reactor volume, increased solids loading on secondary clarifier which may necessitate a larger surface area to meet limiting solid flux, design criteria for the tank and minimum 1MT for the aeration tank for stable operation under hydraulic surges.

Except in the case of extended aeration plants and completely mixed plants, the aeration tanks are designed as long narrow channels. This configuration is achieved by the provision of round-the-end baffles in small plants when only one or two tank units are proposed and by construction as long and narrow rectangular tanks with common intermediate walls in large plants when several units are proposed. In extended aeration plants other than oxidation ditches and in complete mix plants the tank shape may be circular or square when the plant capacity is small or rectangular with several side inlets and equal number of side outlets, when the plant capacity is large.

The width and depth of the aeration channel depends on the type of aeration equipment employed. The depth controls the aeration efficiency and usually ranges from 3 to 4.5 m, the latter depth being found to be more economical for installations treating more than 50 MLD. Beyond 70 MLD duplicate units are preferred. The width controls the mixing and is usually kept between 5 and 10 m. Width-depth ratio should be adjusted to be between 1.2 to 2.2. The length should not be less than 30 or not ordinarily longer than 100 m in a single section length before doubling back. The horizontal velocity should be around 1.5 m/min. Excessive width may lead to settlement of solids in the tank. Triangular baffles and fillets are used to eliminate dead spots and induce spiral flow in the tanks. Tank freeboard is generally kept between 0.3 and 0.5 m.

Due consideration must be given in the design of aeration tanks to the need for emptying them for maintenance and repair of the aeration equipment. Intermediate walls should be designed for empty conditions on either side. The method of dewatering should be considered in the design and provided for during construction.

The inlet and outlet channels of the aeration tanks should be designed to maintain a minimum velocity of 0.2-meter per second to avoid deposition of solids. The channels or conduits and their appurtenances should be sized to carry the maximum hydraulic load to the remaining aeration tank units when any one unit is out of operation.

The inlet should provide for free fall into aeration tank when more than one tank unit or more than one inlet is proposed. The free fall will enable positive control of the flows through the different inlets. Outlets usually consist of free fall

weirs. The weir length should be sufficient to maintain a reasonably constant water level in the tank. When multiple inlets or multiple tanks are involved, the inlets should be provided with valves, gates or stop planks to enable regulation of flow through each inlet. Salient details of proposed aeration tanks are as under :-

a) Efficiency of activated sludge plant = 90%

b) F / M r a t i o = 0 . 1 8

c) MLSS = 5000 mg/L d) Volumetric loading = 0.70 Kg BOD/M

6.9

3

Secondary settling assumes considerable importance in the activated sludge

process as the efficient separation of the biological sludge is necessary not only

for ensuring final effluent quality but also for return of adequate sludge to

maintain the MLSS level in the aeration tank. The secondary settling tank of the

activated sludge process is particularly sensitive to fluctuations in flow rate and

on this account it is recommended that the units be designed not only for

average overflow rate but also for peak overflow rates. The high concentration

of suspended solids in the effluent requires that the solids loading rate should

also be considered. Salient features of proposed SST are as under:-

Secondary Settling Tanks

a) Solid loading rate = 120 Kg/day/Sqm

b) Surface loading rate at peak flow = 25-35 cum/day/sqm

6.10

As it is proposed to use the treated effluent for meeting out demands of

horticulture, washing, air conditioning, flashing and other Industrial uses,

tertiary treatment has to be given so as to make the effluent worthy of the

proposed use. For this purpose, it is proposed to have deep bed rapid sand

filtration units. These filters shall be supplied clarified effluent from SST and

shall have top level as that of the feeding pipe to avoid overflow in the filters.

Dual Filter (Deep Bed Rapid Sand Filter)

Filtration through these units is by gravity down wards, through a bed of filtering media consisting of coarse material of crushed coconut shell / charcoal, anthracite and final silica sand over hard durable grains of silica. The under

lying gravel media consists of hard rounded stones free from clay, sand, loam and organic impurities of any kind. The under drainage system consist of piped grit system, comprising of central pipe / channel with lateral system of pipes having nozzles. The system should conform to IS 8419 (part-2). The dual filter is complete with filter operation gallery, pipe gallery, back wash arrangement with storage, pumps, blowers etc.

6.11

Sludge thickening is resorted to for minimizing the volume content of sludge as detailed below:

Sludge Thickening

a) By installing sludge digester Assuming reduction in moisture content as 2%

Reduction in volume of sludge = Vi

100-P (100-P)

= 50% of original volume 2

6.12

The principal purposes of sludge digester is to reduce its putrecibility or offensive odour, pathogenic contents and to improve its dewatering characteristics. This can be achieved through any of the following biological processes.

Sludge Digester.

i ) Anaerobic digest ion. i i ) A e r o b i c d i g e s t i o n

6.12.1

Anaerobic digestion is the biological degradation of organic matter in the absence of tree oxygen. During this process, much of the organic matter is converted to methane, carbon-di-oxide and water and therefore the anaerobic digestion is a net energy producer. Since little carbon and energy remain available, to sustain further biological activity, the remaining solids in the sludge's are rendered stable.

Anaerobic digestion

6.12.2

Anaerobic digestion involves several successive biochemical reactions carried out by a mixed culture of microorganisms. There are three degradation stages viz. hydrolysis, acid formation and methane formation.

Microbiolozv of the process

In the first stage of digestion, the complex organic matter like proteins, cellulose, lipids are converted by extra cellular enzymes into simple soluble organic matter.

In the second stage, the soluble organic matter is converted by acetogenic bacteria into acetic acid, hydrogen, carbon dioxides and other low molecular weight organic acids.

In the third stage, two groups of methanogenic bacteria, strictly anaerobic, are active. While one group converts acetate into methane and bicarbonate, the other group hydrogen and carbon-di-oxide into methane.

For satisfactory performance of an anaerobic digester, the second and third

degradation should be in dynamic equilibrium i.e. the volatile organic acids

should be converted into methane at the same rate as they produced. However,

methanogenic microorganisms are inherently slow-growing compared to the

volatile acid formers and they are adversely affected by fluctuations in PH

concentration of substrates and temperature. Hence, the anaerobic process is

essentially controlled by the methanogenic microorganisms. It is proposed to

provide sludge digester of 24mtr

6.13

The sludge from the primary chemical and excess secondary sludge sump duly blended shall be taken in to sludge thickener.

Sludge Thickener

The same shall be designed as per the following parameters: -

Thickeners: -

General.

T y p e . : Circular with mechanical scrapper. ....

Quantity. : One Unit each

Design.

Chemical + Secondary Sludge Solids : < 30

loading, Kg s/ MA2/ Day

Surface loading, M^3/ MA2/ day : 12000

Side water depth, mm. : > 4000.

Sludge drain pipe mm 0 : > 200

Slope : 1 in 8 towards center.

Thickeners Mechanism

Type : Central driven.

Width, M. : 1.2

There shall be 1.2 M wide platform all around the thickener with stair for approach with CI posts & 40 mm 0 MS PVC coated railing & encapsulated PVC footrests of size 35 mm x 35mm shall be fixed inside the thickener.

The supernatants shall be collected in the launders outside / inside the periphery of the tank & Thickened sludge shall be collected in a sludge tank of suitable size.

The Thickener Mechanism shall be suitable for installation in RCC tank of specified size. The mechanism shall comprise of the following main components:

Thickener Mechanism (Central Driven Fixed Full Bridge Type): -

> Bridge Superstructure spanning the tank diameter

> Drive assembly complete with drive head, chain & sprocket, geared motor etc. > Feed Well > Center Shaft

> Cone scraper > Rake arms > Tie rods for rake arms

> Plow blades & squeegees > Weir plate

Brief Technical Specifications : -

The bridge shall span the entire diameter of the tank. The width of the walkway shall be minimum 1.2 M. The bridge shall rest on the thickeners wall at both the end. The bridge shall be of truss type welded steel construction with walkway of gratings / chequerred

Bridge Superstructure: -

plates for full of the bridge and center platform. The truss bridge shall be provided with one row of handrail.

The central drive head shall rest on the bridge at the center. The drive head shall be coupled to a geared motor through chain & sprocket and shall support the center shaft at the bottom for rotating the rake arms.

Drive Assembly with Drive Head: -

A fixed feed well shall be hung from the bridge superstructure. The inlet feed pipe shall run under the bridge up to the feed well.

Feed Well: -

The center shaft shall be of SS welded ERW pipe and shall be attached to the output shaft of the drive head. The center shaft shall be bolted to the drive head at the top and shall support the rake arms at the bottom through a torque frame.

Centre Shaft: -

A cone scraper shall be attached to the bottom of the center shaft and shall serve to stir the sludge in the bottom hopper.

Cone Scraper: -

Two sets of rake arms shall be attached to the center shaft torque cage in diametrically opposite direction through a hinged connection. The rake arms shall be attached to the center shaft through tie rods with provision for adjustment of inclination of the rake arms. Each rake arm shall be provided with plow blades at the bottom and adjustable renewable squeegees for scraping of sludge.

Rake Arms & Tie Rods: -

V-notch weirs of size 5mm thick x 150mm wide shall be provided along the periphery of thickener for uniform draw-off of the overflow. The weir plate shall be fixed to the tank wall by means of plate washers.

Weir Plate: -

All civil works along with anchor bolts, inserts etc. Inclusions

All electrical, instrumentation & cabling including motor starters.

Inlet piping and sludge outlet piping

Material of Construction

Tank RCC- M30

Feed Well SS-304

Bridge MSEP

Rake Arm SS-304

Vertical shaft / Center Cage SS-304

Blades SS-304

V-notch weir SS- 304

Squeegees Neoprene

Walkway MS Chequerred Plate / Grating

Handrail 40 NB MSPVC Coated

Vertical Post CI

Scum skimmer SS-304

Scum box SS-304

Scum baffle SS- 304

Anchor Bolt

Fasteners — Under Water SS-304

Fasteners — Above Water SS- 304

6.14

This method can be used in all places where adequate land is available and dried sludge can be used for soil conditioning. Where digested sludge is deposited on well-drained bed of sand and gravel, the dissolved gases tend to buoy up and float the solids leaving a clear liquid at the bottom, which drains through the sand rapidly. The major portion of the liquid drains off in a few hours, after which drying commences by evaporation. The sludge cake shrinks producing cracks which accelerates evaporation from the sludge surface. The areas having greater sunshine, lower rain fall and lesser relative humidity, the drying time may be about two weeks while in other areas, it could be four weeks or more. Covered beds are not generally necessary. With the provision of sludge digester & sludge thickener, the number of drying days reduces from 7-2 and accordingly area of sludge drying beds gets reduced to 15-20%.

Sludge Drying Beds

6.14.1

The sludge drying process is affected by weather, sludge characteristics, system design (including depth of bed) and length of time between scraping and lifting of sludge material. High temperature and high wind velocity improve drying while high relative humidity and precipitation retard drying.

Design Criteria

6.14.2

The area needed for dewatering and drying the sludge is dependent on the volume of the sludge, cycle time required to retain sludge for dewatering, drying and removal of sludge and making the sand bed ready for next cycle of application and depth of application of sludge on drying bed. The cycle time between two drying of sludge on drying beds primarily depends on the characteristics of sludge including factors affecting its ability to allow drainage and evaporation of water, the climatic parameters that influence evaporation of water from sludge and the moisture content allowed in dried sludge. The cycle time may vary widely, lesser time required for aerobically stabilized sludge than for anaerobically digested sludge and for hot and dry weather conditions than for cold and/or wet weather conditions. The area of land required for sludge can be quite substantial with value of 0.1 — 0.25 m

Area of Beds

2

6.14.3

/capita. The average cycle time for drying may range from few days to two weeks in warmer climate and upto 3 to 6 weeks in unfavorable conditions. By the provision of sludge digester bed, the no of sludge drying beds gets reduced by 50%.

A sludge drying bed usually consists of a bottom layer of gravel of uniform size over, which is laid a bed of clean sand. Open jointed tiles under drains are laid in the gravel layer to provide positive drainage as the liquid passes through the sand and gravel.

Bed Specifications

6.14.4

Graded gravel is placed around the under drains in layers up to 30 cm with a minimum of 15 cm above the top of the under drains. At least 3 cm of the top layer shall consist of gravel of 3 to 6 mm sizes.

Gravel

6.14.5 Sand

Clean sand of effective size of 0.5 to 0.75 mm and uniform coefficient not greater than 4.0 is used. The depth of sand may vary from 20 to 30 cm. The finished sand surface shall be level.

6.14.6

Under drains are made of vitrified clay pipes or tiles of at least 10-cm dia. laid with open joints. However, other suitable materials may also be used. Under drains shall be placed not more than 6 m apart.

Under drains

6.14.7 Walls

Walls shall preferably be of masonry and extend at least 40 cm above and 15 cm below sand surface. Outer walls should be kerbed to prevent washing outside soil on to beds.

6.14.8

Drying beds are commonly 6 to 8 m wide and 30 to 45 m long. A length of 30 m away from the inlet should not be exceeded with a single point of wet sludge discharge, when the bed slope is about 0,5%. Multiple discharge points may be used with large sludge beds to reduce the length of wet sludge travel.

Dimensions

6.14.9

All sludge pipes and sludge inlets are so arranged to easily drain and have a minimum of 200 mm dia terminating at least 30 cm above the sand surface. Splash plates should be provided at discharge points to spread the sludge uniformly over the bed and to prevent erosion of the sand.

Sludge inlet

6.14.10

Drainage from beds should be returned to the primary settling units, if it can not be satisfactorily disposed of otherwise.

Drainage

6.14.11

Sludge is usually disposed of on land as manure to soil, or as a soil conditioner, or barged into sea. Burial is generally resorted to for small quantities of putriscible sludge. The most common method is to utilize it as a fertilizer. Ash

Sludge Disposal

,a) One set of Dual Fuel type Generating set capacity to match with 0=3 generation comprising of Engine make = Greaves/Cummins/Catterpillar - water cooled at

1500 RPM with kirloskar/ Crompton/ GEC/ NGEF take alternator to match Engine HP at 1500 RPM, Class “F” insulation with base plate, Fule Tank,

from incinerated sludge is used as a land fill. In some cases, wet sludge, raw or digested, as

well as supernatant from digester can be lagooned as a temporary measure, but it can

create problem of odour nuisance, ground water pollution and other public health

hazards. Wet or digested sludge can be used as a sanitary land fill or for mechanized

composting with city refuse. It proposed that the authorised agency HELMS shall be

contacted for disposal of hazardous waste as per directions of State Pollution Control

Board. Necessary provision of carriage of sludge up to village Palli, the disposal point

and security deposit has been made in the maintenance estimate.

6.15

In addition to the pumping machinery of MPS, various pumping machinery

required for CETP unit is as under:-

Pumping Machinery .

a) For mechanica l screens

b) F o r a e r a t o r s

c) Moving bridges at SST and PST

d) Sludge & supernatant recirculation pumps

e) Miscellaneous pumps for handling waste water and sludge of different

structures

f ) Street lighting of area pump chamber etc

6.16

Provision has also been made for Bye passing the sewerage flow from inlet box

to effluent sump should there be any repair/defect required in the treatment

plant.

Bye Pass Arrangement

6.17 Dual Fuel Generating Set

control panel, Batteries with leads (2 Nos.) AVM pads, cooling tower, fresh

water pump, raw water pump, heat exchanger, standard tools and spares, all

accessories which are supplied by the manufacturer of engine & alternator. One

Gen. Set should be able to treat average flow of STP in the event of power

failure.

Dual Fuel engine will run by consuming bio-gas & diesel in the ratio of 65 % &

35 %. The bio-gas produced from digester, stored in gas holder and diesel as

pilon fuel shall be used to run the dual fuel engine.

Dual fuel engine which is basically a diesel engine shall be provided with a

conversion kit to run the engine with diesel and bio-gas. This shall work on the

diesel cycle. Gaseous fuel shall be added to the air at air intake manifold or

before Turbocharger. Thus mixture of air and gas shall be compressed in the

cylinder just as air is compressed in normal Internal combustion engine. At the

end of compression, diesel shall be injected through a conventional fuel system.

This hot injection shall act as a source of ignition. The power output of the

engine shall be mainly determined by the supply of gaseous fuel.

The engine shall be able to run either on diesel or with diesel & gas. This shall

be achieved by electrical change over system. Adequate control shall be

provided for dual fuel operation.

Make of Engine will be Volvo/Greaves/kirloskar/Cater pillar/Cummins/premier

colt with 4 stroke diesel engine having 10 % over load capacity at 1500 RPM

under NTP.

Conditions confirming to IS 5514/ IS : 10000, continuous rating, fitted with

following accessories:-

Fly wheel

Fly wheel housing

Air Cleaner

Gear type lubricating oil pump

Lubricating oil filter

Fuel injection system with injection pump, nozzles, governor and fuel filter.

a) MCCB of suitable rating with short circuit and over load protection. 1 No.

A. 24 volts electric starting equipment comprising of:-

Lead Acid Batteries

Starter gear ring

Starter motor 24 volts

Battery charger alternator with inbuilt regulator

Lubricating oil pressure gauge

Coolant temperature gauge

Battery charging ammeter

Stop button.

B. Cooling System comprising of:

Heat Exchanger

i ) H e a t E x c h a n g e r

i i ) F resh Water P ump

i i i ) Cooling Tower (dimension of cooling tower to be given by tenderer). i v ) Set o f s t andard tool s .

C. Alternator:

Any of NGEF/GEC/Siemens/Jyoti/Kirloskar/Crompton/Stanford makes rated

for 1500 RPM at 0.8 lagging power factor at 415 volts suitable for 50 Hz. 3

phase 4 wire system conforing to IS: 2613/1S4722.

D. Accessories:

Suitable base frame of sturdy design of MS channel with necessary

reinforcement to take the load of engine & alternator. Anti vibration mountings

will also be supplied to dampen the vibrations.

E. Alternator Control Panel

Fabricated sheet steel of 14 SWG with powder coating floor mounting type

totally enclosed, complete with internal wiring incorporating the following:-

b) Suitably sealed AC voltmeter 1 No.

c) Voltmeter selector switch 1 No.

d) AC Ammeter 1 No.

e) Ammeter selector switch 1 No.

f) Frequency meter 1 No.

g) KWH meter 1 No.

h) KW Meter 1 No.

i) Low lubricating oil pressure indicator 1 No.

j) High coolant temp. return indicator 1 No.

1) Indicating lamps supply on load on

The panel will be completed with internal wiring and leveling. In addition to the above items, 1 No:reverse power relay and 1 No. Neutral isolating switch be provided on the above control panel.

Standard Set of Tools & Spares Double necked spanner Screw Driver

Feeler gauge

Joint-cylinder head to cover Joint-cylinder head to exhaust Joint ring-Lub-oil filter

`0' ring lub-oil filter `0' ring push rod

Other components of Dual Fuel Engine drives Generating set will be as follow:-

1. For the diesel storage facility, on steel diesel tank of 1000 litres capacity with hand pump and other accessories shall be provided.

2. Modified Air intake connection.

3. The control valve.

4. Adapter solenoid valves for diesel flow re-strictors 2 Fuel solenoid valve

for change over system.

5. 3-position electrical switch for change over system. 6. Linkage between fuel pump throttle and gas control valve. 7. Manual and electrical gas shut off-valves. 8. Frequency monitor for over speed. 9. Automatic gas shut-off valve 230V.

10. F l a m e a r r e s t o r

11. M o i s t u r e s e p a r a t o r

12. Heav y du t y a i r f i l t e r

13. Change over switch for diesel to gas.

6.18

Treated effluent will first be led in to recirculation tanks and surplus, if any, will

be disposed off in to adjoining open storm water drain (Nalla).

Effluent Channel

7.0 The salient features and sizes of various structures of proposed combined

common effluent treatment plant on extended aeration process are as under:

SALMNT FEATURES

(1)

(A)

30 MLD CETP

i) Coarse screens chamber

At MPS

ii) E q u a l i z a t i o n t a n k

iii) W e t s u m p

iv) Pumping machinery

= 1.40 m wide overall size 5M x 5M

= 1 No. tank of 700 sqm existing at site

= existing

= 6 Nos. — 175 LPS x 12M = 30 BBP each

(4 Nos. working and 2 Nos. stand bye)

(B)

i) Fine Screens = 1.80 M wide

At CETP

ii) Grit chamber = 2No. of size 30 x2.10x1.30M depth each

(C)

Total BHP 827 BHP

GENERATING SET

KVA of Gen set 965 KVA

It is proposed to provide 2 Nos. DG set of 500 KVA, to take care of

present load of 965 KVA for BOD 350

(11)

(A)

25 1VILD CETP

i) Coarse screens chamber = 1.80 m wide overall size 5M x 5M

At MPS

ii) Collecting tank = 1 No. of size 15M x 10M

iii) Wet sump = 1 No. of size 15M x 3M

iv) Pumping machinery = 6 NOS-145 LPS x 12M =25 BHP each

(4 Nos. working and 2 Nos. stand bye)

(B)

i ) Fine Screens = 2.30 M wide

At CETP

i i ) Grit chamber = 2 Nos. of size 15.25 x 1.75x 0.75 M each

i i i) Parshall flume = 1 No.300 mm throat width

iv) P . S . T = 2 Nos. of size 20M 4

v) Aeration tank = 4 Nos. of size 50 x12.50 x3.5M each

each

vi) S . S . T = 2 Nos. of size 18 M 4

vii) Sludge digester (optional) = 2 Nos. -30 M (I) - 10.30M depth

each

vii i) Cent r i fuge = 2 Nos. — 5M x 4M ( 1W + 1SB)

ix) Sludge drying beds = 2 Nos. of size 30M x 20M each

x) Dual f i l t e r = 2 No. - 13M x 8M (1W + 1 SB)

xi) Pumping Machinery:

a) Raw sewage pumps =100 BHP

b) Flash mixer = 7.5 BHP

c) Flocculation pump = 5 BHP

d) P.S.T = 12 BHP

e) S.S.T = 12 BHP

fj Aeration tank = 300 BHP

g) Sludge pumps =20BHP

h) Sludge recirculation pump =50 BHP

i) Treated water pump set = 125 BHP

j) Chemical house = 3 BHP

k) Thickener pump =10 BHP

1) Equalization pump = 50 BHP

m) General lighting & misc. Load =7.5 BHP

(C)

Total BHP of CETP = 702 BHP

Total BHP = 702 BHP

GENERATING SET

KVA of Gen set = 820 KVA

It is proposed to provide 1 No. DG set of 500 KVA and 1 No. DG set of 400 KVA, to take care of present load of 820 KVA for BOD 350

8.0

As per requirement given by the corporation, the design BOD of the influent has been kept as 750 against recommended BOD of 350 for designing various components of this CETP to meet any untoward emergencies. However, BOD for the maintenance estimate has been considered as 350 only. All other

STANDARDS

technical parameters have been kept same as in recommended list issued by C.P.C.B Delhi.

9.0

The standard of P.W.D. Public Health Engineering Department, Govt. of

Haryana and manual for sewerage and its treatment by C.P.H.E.E.O.

Government of India, shall be followed for construction of this common effluent

treatment plant. The overall specifications in this project shall be as per PWD,

Specifications of Govt. of Haryana. In absence of PWD specifications, the

specifications given in manual for sewerage and its treatment, a publication of

Central Public Health Engineering and Environment Organisation, Ministry of

Urban development, Government of India, New Delhi and provisions of IS:

4127-1983 and IS: 783-1985 have been followed.

SPECIFICATIONS

10.0

As desired, cost of civil structures of MPS and CETP have been worked out on

RATES AND ESTIMATES

schedule basis from HSR 1988, with latest premium applicable w.e.f 1st

February-2009 and as amended through. Govt Gazetted notification dated July

21, 2009, upgraded to present day cost as per enclosed price index computation,

and that of electrical, mechanical and instrumentation has been worked out on

the basis of quotation received from M/s Care Projects and Services, Faridabad,

Designer, Manufacturer and Supplier of E.T.P. Mechanical, Electrical

Equipment. Based on these inputs, sample cost of construction of 25 MLD

CETP per MLD has been accordingly worked out and incorporated here in this

project. Annual maintenance cost has been worked out, taking in to account

wages of staff, repair of structures, energy charges, consumable stores & cost of

transportation of sludge up to dumping site. Up-graded cost of maintenance for

next 10 year has been worked out with 10% increase in cost per year & with 10%

contractor Profit.

11.0 The total cost of following projects, including 3% contingencies and operation

& maintenance cost of 10 years has been worked out of various pages of the

enclosed projects and it works out as under:

COST

i) Cost of construction of 25 MLD CETP for phase —III & IV, IMT,

Manesar — Rs. 951220 Lacs, including maintenance cost for 10 years.

ii) Cost of up-gradation of existing CETP of phase-I & II of 15 MLD to 30

MLD at IMT, Manesar — Rs. 9232.85 Lacs, including maintenance cost

for 10 years.

(V.K. Gupta)