all detail about Design of Sewage Treatment Plant

1. 1
CHAPTER 1
1.1 INTRODUCTION
Wastewater treatment refers to the process of removing pollutants from water
previously employed for industrial, agricultural, or municipal uses. The techniques used to
remove the present in wastewater can be broken into biological, chemical, physical and
energetic.
Sewage is a major carrier of disease (from human wastes) and toxins (from industrial
wastes). The safe treatment of sewage is thus crucial to the health of any community. This
article focuses on the complex physical and biological treatments used to render sewage
both biologically and chemically harmless.
The waste treated is a mixture of domestic and industrial waste, with the domestic
accounting for slightly more than half of the total. Some storm water also enters the system
through leaks and illegal connections.
1.2 WASTE WATER CHARACTERISTICS
An understanding of the nature of wastewater is essential in the design and operation of
collection, treatment and disposal facilities and in the engineering management of
environmental quality. To promote this understanding, some of the wastewater
characteristics are discuss below.
 Temperature
 PH
 Colour
 Odour (ton)
 Solids
 Nitrogen
 Phosphorus
 Chloride
 Toxic metals and compounds
 Effluent discharge standards
 Biochemical oxygen demand (BOD)
 Chemical oxygen demand (COD)
 Objectives treatment
 Unit operation and process and flow sheet
 Treatment systems
 Preliminary treatment system
 Primary treatment system
 Secondary treatment system
 Tertiary and Advanced treatment system

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1.3 NEED OF THE PROJECT
In recent years, with increasing awareness of sewage system effect on the
environment, technology has advanced with the introduction of reticulated pipework
systems collecting swage from both domestic and industrial sources, transfer of collected
sewerage to a central treatment facility, and state of the art treatment technology to ensure
that discharge to streams and disposal of byproduct wastes do not threaten the environment.
Everyone generates west water. Typical residential water usage is from 75 to 100 gallons
per days. Seventy-three percent of the population is connected to a centralized (municipal)
waste water collection and treatment system, while the remaining 27 percent uses on-site
septic systems.
Water is not used up. When people are through with water it becomes wastewater-
better known as sewage-that must be cleaned up before it is returned to the environment for
reuse. In one way or another, all water is recycled. In the past, people had the idea that
wastewater was something that could be disposed of – it would just disappear. This idea has
caused many people to assume that when they dispose of the waste water they also dispose
of any problems or hazards related to it.
Today we recognize that we must recycle water to maintain sustainable supplies of
safe drinking water for future generations. In order to clean up or treat wastewater for
recycling, it is important to understand what waste water contains, what problems it may
cause, and what to take to clean it up.
This project also suit objectives of “Ganga Action Plan” which is executed by
Central Government of India for decreasing pollution level in holly river Ganga.
1.4 OBJECTIVES
This plant, based on up flow anaerobic sludge blanket process, was constructed and
commissioned in January 2010. This plant is designed introduction Sewage is generated by
residential, institutional, commercial and industrial establishments. It includes household
waste liquid from toilet, baths, showers, kitchens, sins and so forth that is disposed of via
sewers. In many areas, sewage also includes liquid waste from industry and commerce. The
separation and draining of household waste into grey water and black water is becoming
more common in the developed world, with grey water being permitted to be used for
watering plants or recycled for flushing toilets.
Sewage may include storm water run-off. Sewage systems capable of handling
storm water are known as combined sewer systems. This design was common when urban
Sewerage systems were first developed, in the late 19th
and early 20th
centuries. Combined
sewers require much larger and more expensive treatment facilities than sanitary sewers.
Heavy volumes of storm runoff may overwhelm the sewage treatment system, causing a
spill or overflow.
Sanitary sewers are typically much smaller than combined sewers, and they are not
designed to transport storm water. Backups of raw sewage can occur if excessive
infiltration/inflow (dilution by storm water and/or ground water is allowed into a sanitary
sewer system. Communities that have urbanized in the mid-20th
century or later generally

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have built separate systems for sewage (sanitary sewers) and storm water, because
precipitation causes widely varying flows, reducing sewage treatment plant efficiency.
As rainfall travels over roofs and the ground, it may pick up various contaminants
including soil particles and other sediment, heavy metals, organic compounds, animal
waste, and oil and grease. Some jurisdictions require storm water to receive some level of
treatment before being discharged directly into waterways. Examples of treatment processes
used for storm water include retention basin, wetlands, and buried vaults with various kinds
of media filters, and vortex separators (to remove coarse solids). For treatment of 130 MLD
of domestic waste water.
Since its commission illegal discharge from tanneries and industrial waste water
from various industries situated in city areas is being discharged regularly to 90 outfall
sewers reaching the main pumping station from where sewerage is pumped to this plant.
The tannery waste water and industrial waste water contains leather flushing, chromium
sulphides and other toxic elements for which the STP has not been designed. Consequently
the components of the equipment are corroded.
The plant is now running at 1-/3rd
of its capacity. The treated effluent from two STPs
(36 MLD and 13 MLD) is pumped into a channel that transports water to the sewerage farm
with a total area of about 2200 hectare. From the channel, irrigation water is fed to the farm
lands. With even 100 percent efficiency in system, there is surplus sewage, which gets
discharged in Pandu or Ganges River without treatment. Comprehensive 210 MLD
sewerage treatment for old city area of Kanpur has been approved by CSMC with Project
cost of Rs. 127 cr.
The project will provide Sewerage facility in Kanpur city in Comprehensive manner
and to the present population of 42 lakhs of Kanpur city, the largest commercial center in
U.P, which is located on the river Ganges and currently discharges 426 MLD sewage
against which the installed capacity for sewage treatment in the city currently is 162 MLD.
Out of 23 Nallas in Kanpur, 19 Nallas have been intercepted.
There is hence a need to provide a sewage treatment facility otherwise this network
would keep polluting the river Ganga. The project under JNNURM will utilize this existing
gravity sewerage network under construction and the intermediate pumping stations at
Rakhimandi, Munshipurwa and Gandanala will pump the combined swaged to the main
pumping station at Bingwan rough drunk sewer along COD nala which will be treated in the
two modular units of 105 MLD each. This will benefit District II which discharges 210
MLD but does not have any treatment capacity at present.

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CHAPTER 2
2.1 HISTORICAL DEVELOPMENTS OF UASB TECHNOLOGY
Worldwide presently over 200 full-scale UASB plants are in operation for the
treatment of both domestic and industrial waste waters. However, in India the UASB
Process is being widely adopted for domestic waste water and it can be claimed that 80% of
total UASB reactors worldwide for domestic waste water treatment is in India. The basic
approach towards selection of technology for sewage was low capital costs, low energy
requirement, low O&M costs and sustainability aspect. This was derived from the
experience of Ganga Action Plan (Kanpur-Mirzapur). Based on the successful results of 5
mld demonstration plant was constructed at Kanpur, Uttar Pradesh.
The experience GAP was mixed in terms of efficiency of treatment versus energy
consumption and cost of operation and maintenance. Drawing lessons from GAP, the YAP
opted for energy neutral and energy recover technologies like anaerobic processes for the
sewage treatment. Conventionally, anaerobic processes are to be used for the treatment of
high strength organic waste waters. However, typical hydro-dynamics of UASB coupled
with its unique characteristics of holding high granular biomass (Sunny et al, 2005), made it
possible to apply the anaerobic processes for the treatment of low strength waste waters.
After studying the performance of the demonstration plant for a few years, a full
scale UASB plant of 14 MLD was constructed at Mirzapur for treating he domestic waste
water (Draijer et al, 1992) In view of the fact that the USAB effluent does not meet
discharge standards, the plants were used in consumption with a settling pond called „final
polishing unit‟ to achieve desired BOD and suspended solids reduction. These being pilots
and experimental plants, their performance were varied.
However they were found to be promising in terms of energy consumption, biogas
yield and reduced requirements, for sludge disposal. The key factors that influenced
selection process against the conventional aerobic systems were their high energy
requirements, unreliable power supply situation in the state, and higher O&M costs; while
those in favors of UASB were their robustness, low or no dependence on electricity, low
cost of O&M Moreover, the possibility of resource recovery form biogas and aquaculture
respectively also influenced the selection process. Among the large capacity plants under
YAP, in all 28 STPs comprising 16 UASBs, 10 Waste Stabilization Ponds (WSPs) and 2
BIOFOR technology STPs with aggregate capacity of 722 MLD were constructed. UASBs
accounted for an overwhelmingly high 83% of the total created capacity.
The state of Haryana almost entirely opted for UASB technology where 10 out of
the 11 large plants were based on this. On the other hand in the state of UP there was a
balance in terms of numbers of STPs based on UASB and WSP technologies. Generally for
larger flows UASBs were considered while for smaller flows WSPs were adopted.

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2.2 MATERIAL OF CONSTRUCTION OF UASB REACTORS
From the time of introduction of UASB concept in India in late 1980s and till date,
there have been significant modifications in the material of construction of UASB reactors,
which has significantly resulted in lowering capital costs.
The modifications incorporated in the 14 MLD UASB plant at Kanpur under GAP
were in the selection & introduction of Fibre Reinforced Plastic (FRP) (bisphenol resin) to
rectify corrosion problems and resulting in longer durability. Simpler waste water feed inlet
system in the UASB reactors is adopted to take care of choking, operation and maintenance
problems surfaced at 5 MLD plant. But, in the ten UASB STPs designed for YAP in
Haryana and recently in other UASBs, further necessary improvements were incorporated,
such as, improvements in fixing of FRP Fed inlet boxes, Gas Liquid Solids Separator
(GLSS), change in design of deflector beam, selection of most appropriate material with
respect to durability and costs etc.
In the present scenario, the main structure of UASB reactor being constructed at
various places in India is with RCC (Reinforced Cement Concrete) since concrete is easily
available and has been used in most of the developing counties for construction works. The
inside surface was coated with epoxy paint as a protective layer to avoid corrosion due to
formation of H2S and CO2. FRP of Isothelic resin class gas hoods and domes have been
providing in the GLSS (Gas-Liquid-Sold Separation). The purpose of use of FRP because of
easy construction, light weight, anti-corrosion and simple maintenance.
The feeding boxes, effluent gutters, baffle plates and gas collection pipes are also
constructed with FRP material. For feeding pipes, HDPE (High Density Polyethylene) pipes
are being used to distribute the waste water uniformly over the surface of the reactor. For
sludge discharge, CI (Cast Iron) pipe is being generally used. However, further R& D shows
that the reactors can be constructed fully in FRP using Isothelic resin instead of RCC for
small flows provided modular approach is adopted.

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2.3 POTENTIAL OF UASB TECHNOLOGY IN OTHER DEVELOPING
COUNTRIES
In most of the developing countries, sewage treatment technologies that can provide
effluent standards at minimum cost are generally preferred. The concept of centralized
sewage treatment methods is very common in these countries. The most widely used
treatment systems are stabilization ponds, activated sludge process, trickling filters,
extended aeration system etc.
The performance of waste water stabilization ponds in achieving the goals for
developing countries appears to be satisfactory in many cases. Conventional sewage
treatment processes (like the activated sludge process) require high capital investment,
excessive consumption of energy, and high maintenance costs.
As a result, efforts to implement these methods in developing countries for water
pollution control have been seriously impeded. During the last two decades, the use of
anaerobic treatment systems particularly the UASB process in outstanding position has
increased significantly for sewage treatment in countries having warm climatic conditions
like in Brazil, India, and Columbia (C.A.L. Chernicharo, 2006).
In spite of their grate advantages, anaerobic reactors hardly produce effluents that
comply with usual discharge standards established by environmental agencies. Therefore,
the effluents from anaerobic reactors (UASB) usually require a post-treatment step as a
means of adapt the treated effluent to the requirements of the environmental legislation and
protect the receiving water bodies.
In contrast to developed countries, emphasis is given more in developing countries
to remove organic pollutants, solids and pathogens to some extent only. The ideal situation
for sewage treatment in these counties would be the complete removal of pathogens (health
protection) and the highest removal of COD (environmental protection) with recovery of
energy (methane or hydrogen) and compounds of interest: nitrogen (as NH+, NO2 and
NO3), phosphorus (as phosphate) and sulfur (as S0). As such, in terms of sustainability the
use of UASB reactors as the core unit of sewage treatment facility is most suited for this
purpose.
In addition to the removal of organic matter with low energy consumption and with
a net production of methane as, the presence of phosphate, nitrogen and sulfur reduced
compounds in the effluent opens the opportunity for the development of economically
feasible processes to recover these compounds of interest. In fact, the development of post-
treatment units of anaerobic reactors is not only important to improve the effluent quality
for environmental protection, but also to achieve the recovery of resources.

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CHAPTER: 3
3.1 SEWAGE WATER:
Sewage water is any water household waste water with the exception of waste water
from sinks, dishwashers, laundry/wash machine, bathroom sinks, tubs, and showers which
is known as gray water. Typically, Black water, which is water contaminated by sewage,
comes from your toilet. If you use a composting toilet, 100% of your water household waste
water is black (sewage water).
3.2 SEWAGE WATER REUSE OPTIONS:
• Gardening
• Fire sprinklers
• Agricultural use
• Industrial use
• Construction Use
3.3 SEWAGE WATER CONTAMINATION:
Various sources of contamination are -
• Biological
‐ Microorganisms
• Chemical
‐ Dissolved salts – sodium, nitrogen, phosphates, chloride
‐ Chemicals – oils, fats, milk, soap, detergents
• Physical
‐ Soil
‐ Food
‐ Lint
Sewage Water
Fig. 1

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3.4 HEALTH EFFECTS OF SEWAGE
The public health and environmental implications of sewage overflows are
tremendous. Sewage pollutes our waters with pathogens, excess nutrients, heavy metals, and
other toxins. It kills aquatic life and creates algal blooms that can suffocate fisheries.
Even worse, sewage carries pathogens that can end up in our drinking water supplies
and swimming areas. These disease-causing microorganisms cause diarrhea, vomiting,
respiratory, and other infections, hepatitis, dysentery, and other diseases. Common illnesses
caused by swimming in and drinking untreated or partially treated sewage include
gastroenteritis, but sewage is also linked to long term, chronic illnesses such as cancer, heart
disease, and arthritis.
Experts estimate that there are 7.1 million mild-to-moderate cases and 560,000
moderate-to-severe cases of infectious waterborne disease in the United States each year
and the Environmental Protection Agency estimates that between 1.8 and 3.5 million people
are estimated to get sick from recreational contact with sewage from sanitary sewer
overflows annually. While most people recover from these diseases, they can be deadly for
children, the elderly, and other patients with weakened immune systems who comprise
approximately 30% of our population at any one time.
3.5 ECONOMIC LOSS:
Debris associated with sewage probably has the highest monetary cost associated with
its presence on our beaches due to the resulting loss of tourism in addition to blockage
removal. The closing of commercial shellfish beds due to sewage contamination can lead to
high income loss.
Clean beaches have many advantages for humans and commercial seafood farms as well
as for the wildlife.
 They are safer for the public.
 They encourage people to come and use them, which will improve local economy.
 They benefit everyone now and in the future.
These reasons prove the necessity for a solution.

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3.6 WHAT IS THE SOLUTION?
It used to be said that “the solution to pollution is dilution.” When small amounts of
sewage are discharged into a flowing body of water, a natural process of stream self-
purification occurs. However, densely populated communities generate such large
quantities of sewage that dilution alone does not prevent pollution. Instead of discharging
sewage directly into a nearby body of water, it‟s better to let it pass through a combination
of physical, biological, and chemical processes that remove some or most of the pollutants.
This takes place in sewage treatment plants.
3.7 TREATMENT PLANT:
Sewage treatment plants neutralize and deactivate the chemicals found in the sewage
water. They work by relying on the bacteria that is found in our colons, which eat away the
nitrates, phosphates and organic matter that is found in sewage. These plants can be
expensive to build and operate for many governments, but there are cheaper alternative
which rely on nature to do most of the work. This is done by rebuilding or restoring
wetlands, because the plants and bacteria found in the wetlands will do the same thing that
bacteria in standard sewage treatment plants do. This helps the environment in two ways:
restoring wetlands and treating human waste water before it pollutes the natural waterways.

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CHAPTER 4: METHODOLOGY
4.1 PROCESS
 Primary treatment
 Screening
 Grit removal
 Flow equalization
 Fat and grease removal
 Secondary treatment
 Activated sludge
 Aerobic granular sludge
 Surface-aerated basins (lagoons)
 Filter beds (oxidizing beds)
 Constructed wetlands
 Soil bio-technology
 Biological aerated filters
 Rotating biological contactors
 Membrane bioreactors
 Secondary sedimentation
 Tertiary treatment
 Filtration
 Lagooning
 Nutrient removal
 Nitrogen removal
 Phosphorous removal
 Disinfection
 Odor control
 Sludge treatment and disposal
 Anaerobic digestion
 Aerobic digestion
 Composting
 Incineration
 Sludge disposal

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4.1.1 PRIMARY TREATMENT
The primary treatment system includes all the units of the preliminary treatment
system and the Primary Sedimentation Tank (PST), also known as the primary clarifier.
When only these units are provided for treatment it is called primary treatment of
wastewater. Fig. shows a schematic diagram of a typical primary treatment system.
Bar screen Grit chamber Skimming tank Disposal
s
Parshall PST
Approach Flume or
Channel other velocity
Control device Primary
Sump and Screening Grits Oil and sludge for
Pump house grease treatment
Schematic diagram of a typical primary treatment system
In the primary treatment system, the removal of the most of the large floating
materials takes place in the screen chamber; the most of the heavy suspended solids are
separated in the grit chamber. The primary clarifier (PST) then reduces about 60-70% of
fine settable suspended solids, which includes about 30-32% of organic suspended solids. It
should be noted that colloidal and soluble (dissolved) organic content of waste water is not
removed in the system.

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4.1.2 SECONDARY TREATMENT
After primary treatment, if wastewater is further treated for the removal of colloidal
and soluble organic matter present in wastewater, then it is called secondary treatment of
wastewater. Normally, biological processes are employed to remove the remaining colloidal
and soluble organic as shown in figure.
PST Aeration Reactor SST Effluent
For disposal
or reuse
Influent from
Preliminary Return sludge line Secondary Sludge
Treatment
Sludge to
Treatment
Primary Sludge
(a) Secondary treatment system with activated sludge process
PST Tricking filter SST
Influent Secondary sludge
From (Humus)
Preliminary
Treatment Sludge to treatment
Primary sludge
(b) Secondary treatment system with tricking filter
Schematic diagram of biological secondary treatment system
Other biological treatment units usually provided for secondary treatment to cater to
specific needs, particularly for a small volume of wastewater, include:
 Waste stabilization ponds (also known as oxidation ponds)
 Oxidation lagoons (Aerated lagoons)
 Oxidation ditches (Extended Aeration System)
 Rotating Biological Contractor (RBC)
 Up-flow Anaerobic Filter (UAF)
 Up-flow Anaerobic Sludge Blanket (UASB)

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4.1.3 TERTIARY TREATMENT
This treatment is sometimes called final or advanced treatment, and consists in
removing the organic load left after the secondary treatment, and particularly to kill the
pathogenic bacteria.
This treatment, which is normally carried out by chlorination, is generally not
carried out for disposal of sewage in water, but is carried out, while using the river stream
for collecting water for re-use or for water supplies. It may, however, sometimes be
adopted, when the outfall of sewage is very near to the water intake of some nearby town.
The different techniques available for the tertiary treatment are given in table.
Different techniques for tertiary treatment
Techniques For Complete removal
1. Granular media filtration,
ultrafiltration and micro-strainers.
Residual suspended solids.
2. Biological nitrification de-
nitrification , ion exchange and air
stripping
Removal of nitrogen, chlorine and dissolved
gases.
3. Biological and chemical process. Residual nitrogen and phosphorus.
4. Ion exchanges Reverse Osmosis,
Electro dialysis, Chemical
Precipitation, Adsorption.
Residual dissolved inorganic solids, toxic
and complex organic compounds.

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4.1.4 SLUDGE TREATMENT AND DISPOSAL
The residue that accumulates in sewage treatment plants is called sludge (or bio-
solids). Treatment and disposal of sewage sludge are major factors in the design and
operation of all wastewater treatment plants. Two basic goals of treating sludge before final
disposal are to reduce its volume and to stabilize the organic materials. Stabilized sludge
does not have an offensive odour and can be handled without causing a nuisance or health
hazard. Smaller sludge volume reduces the costs of pumping and storage.
It involves the process of sludge treatment and disposals are:-
 Anaerobic digestion
 Aerobic digestion
 Composting
 Incineration
 Sludge disposal
 Sludge dewatering
 Sludge drying

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4.2 WORK PLAN:
DURATION
Graph between activity and duration
D
C
B
A
ACTIVITY

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4.3 PROCESS DESIGN CALCULATIONS
1 PROCESS DESIGN CALCULATIONS
A BASIC DATA ON FLOW
Total flow to plant 210 mld
8750 cum/hr
2.431 cum/sec
Peak flow 420 mld
17500 cum/hr
4.861 cum/sec
Minimum design flow 84 mld
3500 cum/hr
0.972 cum/sec
B SITE INFORMATION
General ground level at site 118.5-120.0 m above msl
H.F.L of river Pandu 119.610 m
R.L of top of rising main at inlet chamber 127.640 m
R.L of bottom of treated effluent channel 119.900 m
F.G.L at STP site 121.0-119.9 m
Sub soil water level 6.000 m
C BASIC DATA ON INFLUENT
CHARACTERISTICS
Average inlet bod (5 days@20 c) 322 mg/l
Average inlet bod load 67620 kg/day
Average inlet cod 523 mg/l
Average inlet suspended solids 418 mg/l
PH of influent 7.7
Sulphate 52.3 mg/l
Sulphides 25 mg/l
D DESIRED TREATED EFFULUENT QUALITY
Desired effluent bod to be less than 30 mg/l
Desired effluent suspended solids to be less than 50 mg/l
Desired effluent Sulphides to be less than 2 mg/l
Fecal coliform count after chlorination 10000 mpn/100 ml

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E UNTI SIZE OF SEWAGE TREATMENT PLANT
Design of inlet chamber 4.861 cum/sec
Design peak flow 1
No. Of chambers 30 sec
Retention period 146 cum
Volume required 15.44 m
Length of chamber 2.25 m
Area of chamber 34.74 sq.-m
Depth required 4.2 m
Hence size of inlet chamber provided 15.44m × 2.25m × 4.2m
swd + 0.5 m fb
2 DESIGN OF SCREEN CHAMBER
Design avg peak flow 210 mld
Design peak flow 420 mld
2A MANUAL SCREEN CHANNEL
No. Of manual screen 2
Angle of inclination 60 deg.
Size of MS bars 50 mm wide
Thickness 10 mm
Width of clear opening 10 mm
Inclined depth 1.68 m
Total width of opening required with inclination 1.68 m
Total width of opening required with inclination 168 nos.
Nos of bars required 167 nos.
Size of channel provided 3.36m × 1.25m × ld + 0.5
m
Fb
Velocity through channel at avg flow 0.3 m/sec
2B DESIGN OF MECHANICAL SCREEN CHAMBER
Nos of mechanical screen channel 3 nos.
Angle of inclination 40 deg.
Size of ss bas 40 mm wide
Thickness 2 mm thick
Width of clear opening between bars 3 mm
Clear surface area of opening at peak flow 1.620 sq.-m
Inclined depth 1.69 m

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Total width of opening required with inclination 1.43 m
Nos of bars required 478 nos
Nos of opening required 477 nos
Width of channel required 2.64 m
Size of channel provided 2.64m × 1.25m × ld + 0.5
m
Fb
Velocity through channel at avg flow 0.25 m/sec
Ok
3 DESIGN OF GRIT CHAMBERS
3A MANUAL GRIT CHAMBER
Nos of tank 6 nos.
Nos pf working channel 5 nos.
Design peak flow for each unit 84 mld
84000 cum/day
0.972 cum/day
3.889 m2
Effective depth provided 0.90 m
Width of channel required 4.32 m
Surface loading rate 958 cum/m2
/day
Surface area 87.68 m2
Length of channel required 20.29 m2
Length if channel adopted 21.00 m
Width 4.32 m
Total depth including 0.2 m for grit storage 1.10 m
Size provided 21.0 m × 4.32m×1.10m
ld + 0.5 m
Fb
3B MECHANICALLY OPERATED GRIT CHAMBER
Nos of tanks 4
Each mechanically operated grit chamber design flow 105 mld
Surface loading rate as per cpheeo manual 959 cum/day
Surface area of grit chamber required 109.489 m2
Size of square tank provided 10.5 m × m
Size of square tank required 10.5 m × m
Liquid depth provided in grit chamber 0.80 m

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Volume of grit chamber 88 cum
Hydraulic attention period at peak flow 1.2 minute
Free board provided 0.5 m
Size of mechanically operated grit chamber provided 10.5 m × 10.5m×0.8m ld
+ 0.5 m
Fb
4 PARSHALL FLUME WITH ULTRASONIC FLOW
METER
Nos of channel with parshall flume 1
Design peak flow 420.0 mld
4.861 cum/sec
Velocity in channel considered 1 m/sec
Width of channel considered 4.000 m
Depth of flow 1.2 m
Throat width of parshall flume provide 900 mm
5 DESIGN OF UASB REACTORS
Design capacity or peak flow 420 mld
17500 mld
Design capacity or average flow 210 mld
8750 cum/hr
Nos. Of unit for 210 mld 16 nos.
Minimum design flow 84 mld
3500 cum/hr
0.972 cum/sec
Upflow velocity recommended for peak flow as per nit 1.5 m/hr
Considering the upflow velocity on peak flow 1.15 m/sec
The surface area of each UASB reactor required 951.09 m2
Spacing of gas collection beams considered 4 m
Length of UASB reactor required in multiple of 4 m 32 m
Width of each reactor required 29.7 m
Width of reactor considered 30.00 m
Surface area of each UASB reactor 960.00 m2
Width of glass considered 3.0 m
Area of aperture 240.00 m2
Velocity through aperture on peak flow 4.6 m/hr
Upflow velocity at dry weather flow 0.228 m/hr

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6 SLUDGE PRODUCTION IN UASB REACTOR
Design inlet BOD (5 days @ 20 C) 322 mg/l
Design inlet BOD load 4224.64 kg/day
Avg inlet COD 523 mg/l
Design inlet COD load 6861.76 kg/day
COD removal efficiency 65 %
COD removal in reactor 339.95 mg/l
Design temperature 20 c
Total bacterial yield factor 0.007 kg vss/kg cod
removed
7 BIOLOGICAL SLUDGE PRODUCTION
Vss production in reactor due to cod 23.8 mg/l
Degradation of organic compound 50 %
Solids in digested sludge 11.9 mg/l
Biological sludge production 11.9 mg/l
Biological sludge production per reactor 156.1 kg/day
Tss in influent given iv nit 418.0 mg/l
Min. Tss reduction in reactor 65 %
TSS in effluent 146.3 mg/l
VSS in influent given in nit 178.0 mg/l
VSS in effluent 57.9 mg/l
VSS in digested sludge 60.10 mg/l
Ash content 57 %
Sludge production due to ash content 156. Mg/l
Sludge production due to tss per reactor 216.1 mg/l
Total sludge production per reactor per day 2991 kg/day
Sludge concentration 65 kg/cum
Sludge volume production per reactor per day 46.0 cum
Sludge retention time 38 days
Total sludge mass in reactor 113658 kg
Sludge volume 1749 cum
Area of one reactor 960.0 m2
Maximum sludge bed height % of height up to gas
collector
80%
Height of deflector beam 2.28 m
Height of glass from edge of deflector beam 0.87 m
Height of glass 1.49 m
Total sludge in UASB reactor required 5.04 m
Total sludge in UASB reactor provided 5.20 m
Volume of each reactor 4992 cum
HRT on average flow 9.13 hrs

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COD loading per day 6862 kg
COD loading per cum per day on each reactor 1.37 cod/cum/day
8 DESIGN OF COMPONENTS OF UASB REACTOR
Angle of gas collector 50 deg
Min: hood width 0.44 m
Min. Settling zone detention time 1.20 hr
Max. Feed inlet pipe distance 2.00 m
Angle of deflector beam 45 deg
Minimum overlap 0.15 m
C/c distance of gas collector 4.00 m
Max. Weir loading 5.00 m/hr
Min. bio gas 0.08 mg/l
Min. Sulphides at reactor outlets 22.00 mg/l
22.00 mg/l
Min. Methane content in bio gas 70%
H2s content in bio gas 1%
Min. Nos. Of sludge withdrawal pits in one reactor 4
Min. Sludge withdrawal points per sw pits 2
Total no. Of reactor provided for 210 mld avg. Flow 16
Area of first 8 nos. UASB reactor provided 32 m × 28 m = 896.0 m2
Area of second set of 8 nos. UASB reactor provided 32 m × 32 m = 1024 m2
Total area of all 16 reactor 15360 m2
Hence size of each of 8 nos UASB reactor provided 32.0m × 28.0m × 5.2m ld
+0.5m fb
Size of each of other 8 nos UASB reactor provided 32.0 m x 32 m x 5.20 ld
+ 0.5 m fb
Reactor size 32 m × 28 m
Design peak flow to each reactor 24.5 mld
Length of one reactor 32.0 m
Reactor width provided 28.0 m
Distance of gas collector 4.0 m
Nos. Of gas collector beam in one reactor 8
Area covered by one feed point 4.0 m2
No. Of feeding points in one reactor 224
No. Of feed inlet box provided in one reactor 16
Nos. Of feed pipes in one feed inlet box 14
Size of pipe provided (hdpe pipe) 110
Nos of feed boxes per distribution box 8
Nos of distribution box per reactor 2
Size of pipe provided 180 mm
Width of gloss at bottom 3.00 m
Weir loading at peak flow 448.0 m

22. 22
9 DESIGN OF FEED INLET BOX(FRP)
Size of one outflow chamber 0.2m × 0.2 m × 0.2 m
Length of feed inlet box 2.04 m
Width of central chamber 0.4 m
Width of feed inlet box 1.12 m
Depth in central chamber 0.5 m
10 DESIGN OF NOTCH WEIR PLATE OF FEED
INLET BOX (FRP)
Nos of feed pipes in one feed box 14
Peak flow in one reactor 24.5 mld
Peak flow in one feed inlet box .01772 vum/sec
Flow through 90' v notch .00127 cum/sec
Depth of flow in v notch 0.055 m
Peak flow in one reactor 24.5 mld
0.289 cum/sec
Peak flow in one effluent gutter 0.0181 cum/sec
Avg. flow of each gutter 0.0090 cum/sec
Assuming width of each gutter 0.2 m
Velocity in gutter 0.8 m/sec
Depth of flow at discharge end 0.08 m
Depth of flow at mid-point 0.100 m
Avg. Depth of flow in one effluent gutter 0.100 m
11 DESIGN OF V NOTCH N WEIR PLATE FOR
EFFLUENT GUTTER
Peak flow in one effluent gutter 0.0181 cum/sec
Provided triangular v notch with an angle 90 degree
Assuming depth of flow in notch 0.03 m
Flow through v notch 0.00022 cum/sec
Nos of v notch per gutter 82
Reactor size 32 m x 32 m
Design peak flow to each reactor 28.00 mld
Design average flow to each reactor 14.00 mld
Length of one reactor 32.0 m
Reactor width provided 32.0 m
Distance of gas collector 4.0 m
Nos if gas collector beam in one reactor 8
Area covered by one feed point 4 sq-m
No of feeding points in one reactor 256

23. 23
Nos of feed inlet box provided in one reactor 16
Nos of feed pipes in one feed inlet box 16
Size of pipe provided (D of hdpe pipe) 110 mm
Nos of feed boxes per distribution box 8
Nos of distribution box per reactor 2
Size of pipe provided 180 mm
Width of glass at bottom 3.00 m
Total weir loading in one reactor 512.0 m
Weir loading at peak flow 2.279 cu/sec
12 DESIGN OF FEED INLET BOX (FRP)
Size of one outflow chamber 0.2 m× 0.2 m × 0.2 m
swd
Length of feed inlet box 02.24 m
Width of central chamber 0.4 m
Width of feed inlet box 1.12 m
Depth in central chamber 0.5 m
13 DESIGN OF V NOTCH WEIR PLATE OF FEED
INLET BOX (FRP)
Nos of feed pipes in one feed box 16
Peak flow in one reactor 28.0 mld
0.324 cum/sec
Peak flow in one feed inlet box 0.02025 cum/sec
Peak flow in one feed inlet pipe 0.00127 cum/sec
Flow through 90 degree v notch 0.00127 cum/sec
Depth of flow in v notch 0.055 m
14 DESIGN OF EFFLUENT GUTTER INSIDE
REACTOR
Peak flow in one rector 28 mld
Peak flow in one effluent gutter 0.0181 cum/sec
Avg. Flow in one effluent gutter 0.009 cum/sec
Assuming width of each gutter 0.2 m
Velocity of flow in gutter 0.8 m/sec
Depth of flow at discharging end 0.08 cum/sec
Depth of flow at mid-point 0.100 m
Avg. Depth of flow in one effluent gutter 0.100 m

24. 24
15 DESIGN OF V NOTCH IN WEIR PLATE FOR
EFFLUENT GUTTER
Peak flow in one effluent gutter 0.0181 cum/sec
Provided triangular notch with an angle 90 deg
Assuming depth of flow in notch 0.03 m
Flow through v notch 0.00022 cum/sec
Nos of v notch per gutter 82
Design of division box
Nos of outlets from box 32
Nos of division box for 32 x 28 m reactor 16
Peak flow to each compartment 6.125 mld
Retention period for each chamber 10 sec
Volume of each compartment 0.729 cum
Liquid depth considered 1.000 m
Width of weir considered 1.870 m
Width of chamber provided 0.90 m
Nos of division box for 32 x 32 m 16
Peak flow to each compartment 7.000 mld
Retention period for each chamber 10 sec
Volume of each compartment 0.810 cum
Liquid depth considered 1.0 m
16 DESIGN OF DISTRIBUTION BOX
Design flow 7.000 mld
Retention time for common chamber 15 sec.
Volume of common chamber 1.215 cum
Nos of outlets from distribution box 8
Width of each outlet box 0.50 m
Length of common chamber 2.60 m
Depth of common chamber 1.20 m
Width of common chamber 0.39 m
Width of distribution box 1.798 mm
Size of distribution box 2.60 m× 2.163 m × 1.20
ld + 0.5 m fb
17 BIO GAS PRODUCTION
Influent COD 523 mg/l
COD reduction in reactor 65%
COD reduction in reactor 340 mg/l
Bio gas production per reactor 356.81 cum
Bio gas by all reactor 5708.98 cum

25. 25
18 DESIGN OF FACULTATIVE AREATED
LAGOONS
Design flow
Nos of units 2
Retention period 12 hrs
Volume required 52500 cum
Depth of lagoons provided 4 m
Area of aerated lagoons required 13125 m2
Size of each aerated lagoons provided 13125 m2
× 4.0m ld + 0.5
m fb
Capacity of aerated 39.38 kw
Sulphides in effluent of FPU 22 mg/lit.
Oxygen requirement 19.3 kg/hr
Total capacity of aerator‟s 74.31 hp
19 DESIGN OF CHLORINE CONTACT TANK
Design flow 210 mld
Numbers of tank 1
Retention time 30 min
Volume of each tank required 4375 cum
Liquid depth provided 3 m
Area of tank provided 1458.3 m2
Width of tank taken 30.0 m
Length of tank 48.6 m
Size of chlorine tank provided 48.6 m × 30.0 m × 3.0 ld
+ 0.5 m fb
Chlorine design rate 5. Mg/l
Consumption of chlorine per day 1050 kg
20 DESIGN OF SLUDGE SUMP AND PUMP HOUSES
Sludge produced by one reactor per day 46.02 cum
Capacity of wet well provided 184.1 cum
Depth of wet well provided 5.0 m
Area of wet well required 36.8 m2
Length of wet well required 8.0 m
Width of wet well 4.6 m
Sludge pump required 3
Nos of working pump 2
Capacity of each pump provided 23 cum/hr
Power required with 50 % efficiency of pump 5.0 kw
Hence size of sludge sump 8.0 m × 4.6 m × 5.0 swd
+ 0.5 m fb

26. 26
4.4 HYDRAULIC DESGN CALCULATIONS
1 HYDRAULLIC DESIGN CALCULATIONS
Flow to STP 210 mld
210000 cum/day
8750.0 cum/hrs
145.833 cum/min
2.431 cum/sec
Peak factor 2
Peak flow (q peak ) 420 mld
42000 cum/day
17500.00 cum/hr
291.667 cum/min
4.861 cum/sec
2 GENERAL INFORMATION OF LEVELS
General ground level at site 118.5-120.0m above
MSL
H.F.L of river Pandu 119.61 m
R.L of top rising main inlet chamber 127.64 m
R.L of bottom treated effluent channel 119.90 m
F.G.L at STP site 122.00 m
Sub soil water level 6.00 m
Twl at inlet chamber 127.215 m
Total head loss in STP 6.115 m
3 HYDRAULIC LOSSES CALCULATIONS AND
SIZING OF CONDUIT
IL of conduit at discharge point 119.90 m
Length of final effluent channel 250.0 m
Width of channel considered 4.10 m
Critical depth in channel considering free fall in
river(Dc)
Dc =(q/b*Og) )^2/3
0.523 m
Depth of flow in the final effluent channel is
provided
1.2 m
Twl of flow in the effluent channel is provided 121.100 m
Peak flow in final effluent channel 4.8611 cum/sec
Velocity in channel assumed 1.00 m/s

27. 27
Liquid depth in channel 1.186 m
Using manning‟s equation (V) 1/n × r^2/3×s^1/2
For concerts surface (N) 0.012 m
Hydraulic radius (R) 0.757 m
Slope in channel required (S) 0.000209
Slope in channel provided (1 in 4600) 0.000217
Depth of flow at peak flow at the end 1.200 m
Critical velocity at the end at peak flow 0.988 m/s
Depth of flow provided in final effluent channel
outside (CCT)
119.954 m
Twl in final effluent near CCT 121.154m
Free fall in channel from CCT 0.125 m
Crest level of CCT outlet weir 121.275
Nos. Of CCT units 1
Flow through 1 CCT 4.8611 cum/sec
Total length of weir 3000 mm
Clear length of weir (B) 30 m
Width of weir 150 mm
Head over rectangular weir=(q/1.77b)^2/3 0.205 m
Twl of CCT 121.481
CCT received the flow from final polishing pond-ii
through treated effluent
Channel. The open channel receive the 50%flow
from land compartment of
FPU-ii and balance 50% from is compartment of
FPU-ii
Considering losses in entry point of CCT 0.049 m
Twl of channel at inlet of CCT 121.530 m
Peak flow in effluent channel 100% 4.8611 cum/sec
Width of channel considered 4.10m
Depth of flow considered as above 1.2m
Velocity in channel 0.99m/sec
Il of channel at outlet FOU-ii 120.33m
Twl of channel at channel at outlet of FPU-ii 121.530 m
Free fall in effluent channel from FPU-ii 0.1 m
Level of crest of weir at FPU-ii outlet 121.630
Nos of FPU units 2.000
Flow through one FPU 2.4306
Total length of wire 30000mm
Total width of end supports (2x500) 1000 mm
Clear length of wire b 29m
Head over rectangular wire=(q/1.77b) 2/3
0.1336m

28. 28
Twl at outlet of FPU-ii 121.764m
Twl at inlet of FPU-ii 121.764m
Level crest of wire of FPU-ii inlet 121.764m
Total length of wire 36000m
Clear length of wire 36 m
Width of wire 150mm
Head loss over wire (H) Qa/(1.65×b)2/3
0.1213m
Head over wire 0.121m
Head loss in pipe from collection channel of aerated lagoon to overflow
chamber in FPU-ii
Nos of pipe for each aerated lagoons 1
Peak flow through each conduit 2.431 cum/sec
Size of RCC NP3 pipe provided 1.8m
Velocity through sever 0.95563m/sec
Velocity head (v2
/2g) 0.0465m
Head loss at entry and exist [1.5x (v2
/2g)] 0.0698m
Length of pipe from collection chamber to FPU-i 25.0m
Conduit material Rcc
Cr value for modified h-w formula 1.00
Frictional losses in pipe using modified Hazen-
Williams formula,
HF= (l*(Q/CR)1.81
/994.62*D4.81
0.07 m
Total head loss in pipe 0.07724m
Twl in collection channel 121.842m
Considering free fall in collection channel of aerated
lagoon
0.13m
Level at crest of channel 121.000m
Head over the weir 0.035m
Twl at outlet of aerated lagoon 122.007
Considering losses in lagoon 0.3m
Twl at aerated lagoon considered 122.037
Aerated lagoon receives flow from common
collection channel of UASB
Reactors through 1800 mm RCC pipe. The flow is
further divided in three
Parts for better distribution in
Aerated lagoon
Size of each overflow chamber 4m×4m
Level of crest of overflow channel 122.050
Length of weir crest 12.000m
Flow to each chamber 0.810 cum/sec

29. 29
Head over the weir 100m
Twl in distribution overflow chamber 122.150 m
HEAD LOSS THROUGH PIPE FROM COLLECTION CHAMBER TO
AERATED LAGOON
Nos. Pipe for each aerated lag through lagoons 1
Peak flow through each conduct Q 2.431 cum/sec
Size of rcc np3 pipe provided 1.8 m
Velocity through sewer 0.95563m/sec
Velocity head (V2
/2g) 0.0465m
Head loss 0.0
Head loss in bend 0.0233 m
Length of pipe from collection chamber to FPU-i 25.0 m
Conduit material RCC
CR value for rcc pipe for modified h-w formula 1.00
WORK VALUE MEASURED in
Critical losses in pipe .using modified Hazen-
Williams formula.
HF = (l*(q/cr1.81
)/99.62*d4.81
0.007 m
Total head loss in pipe 0.10051 m
Twl in collection chamber effluent chamber 122.251 m
Consider the topography of the area and head
available the twl in collection can be increased
123.266 m
Losses in the effluent outside UASB reactor
considered (maximum)
0.300 m
Width of channel 1.200 m
Velocity of flow 1.000 m
Depth of flow during flow 0.608 m
Il of channel 0.506 m
Free fall in channel effluent channel considered 122.760 m
Il of frp in the UASB reactors 0.100 m
Nos. Of gutter in the one reactor 123.666 m
Peak flow to each reactor 16 m
Peak flow to each frp reactor 0.30382 m
Width of each frp gutter 0.00949 m
Width of each gutter 0.2 m
Critical depth in the gutter considering free fall
in the
m
Depth of the starting point (at middle of gutter ) 0.106 m

30. 30
Average depth of flow in gutter 0.084 m
Depth of flow in the gutters considered 0.110 m
Twl in the frp gutter provided 123.776 m
V- notch provided in frp gutters@ 250 m
Nos of v-notch in 1 gutter 83 m
Flow through each v-notch 0.000057 cum/sec
Head over weir in v-notch(q/1.48)2/5 0.026 m
Free fall in gutter 0.054 m
Twl in UASB reactors 123.856 m
Nos of feed inlet pipes in one reactor 224 m
Flow through each pipe 0.00136 m
Size(outer dia)of feed inlet pipe 90 m
Velocity through pipe (id=0.098m) 0.26997 cum/sec
Velocity head 0.00371 m
Losses through pipe 0.012 m
Water level in outlet box of feed inlet box 123.868 m
For proper distribution each outlet box receive
flow through v-notch
Flow through v-notch q=8/5 cd 2g h tan 0/2 0.001356337 cum/sec
Head over v-notch h (q/1.40)2/5 m
0.061 m
Total depth of v-notch provided 65 cum/sec
Fee fall after the v-notch considered 0.1 m
Twl center chamber required 124.033 m
Difference between twl in reactor and in feed
intent
0.177 m
This head shall be helpful to clear in feeding
Each feed box will receive the flow distribution
box through 180 mm hdpe pipe
Consider id of hdpe pipe 0.019 cum/sec
Consider id of hdpe pipe 0.155 m
Velocity through pipe 1.00684 m/sec
Velocity head V2
/2g .0517 m
Head loss at enter and exit 0.775 m
Head loss in 3 nos bends (max) 0.0775 m
Strength of one pipe considered (max) 23.0 m
Material Hdpe m
Value of hdpe pipe for modified h-w formula 1.0 m
Friction losses pipe using modified Hazen
Williams formula
HF=(l*(q/cr1.81
)/994.62*d4.81
0.139 m

31. 31
Total head in pipe at peak flow 0.2939 m
Total head loss in pipe at average flow 0.0714 m
Twl in outlet box of distribution box 124.327 m
Free fall considered in outlet box at peak low 0.1 m
Level of edge wire 124.427 m
Width of wire 0.6 m
Head over rectangular wire (q/1.77b)2/3
0.0702 m
Twl at center chamber of distribution 124.497 m
Each distribution box will the flow division
through 450 mm id/di pipe
m
Flow through each 450 mm id pipe 0.154 m
Size of pipe 0.45 m
Velocity through pipe 0.95563 m
Velocity head v2
/2g 0.0465 m
Lead loss at entry exit 0.0698 m
Lead loss in 4nos bends (max) 0.0931 m
Length of one pipe considered (max) 135.0 m
Pipe material Cl m
Value for ci pe for modifier h-w formula 0.85 m
Considering same twl in connecting as
manual grit chamber
126.765 m
Width of connecting channel 6.0 m
Peak flow in channel 1.620 m
Velocity in channel assumed 1.0 m
Liquid depth in channel 0.27 m
Using manning equation 1/n*r2/3*s1/2 m
For concrete surface 0.012 m
Hydraulic radius 0.248 m
Slop in channel provided (1 in 1700) 0.000924 m
Depth of flow at peck flow 1.25 m
Of connecting channel 125.515 m
Twl at d/s of fine bar screen same as u/s of
manual grit chamber
126.7635 m
Considering maximum head loss across
screen
0 m
Twl at u/s of bar screen 127.065 m
Depth of flow at screen 1.25 m
Of screen channel 125.815 m
Considering head loss across the open
channel gates
0.15 m
Twl inlet chamber of STP 127.215 m

32. 32
CHAPTER 5
DESCRIPTION OF UNITS
5.1 MAIN PUMPING STATION ( M.P.S)
Pumping stations are facilities including pumps and equipment for pumping fluids
from one place to another. They are used for a variety of infrastructure systems, such as the
supply of water to canals, the drainage of low-lying land, and the removal of sewage to
processing sites.
A pumping station is, by definition, an integral part of a pumped-storage
hydroelectricity installation.
Sewage treatment plant at Bingawan main pumping station detail’s:---
Delivery pipe 1200 mm
Suck pipe 800 mm
Cost of M.P.S 26 crore‟s approx.
Total number of pumps 12 pumps
Working at a time 6 pumps
 After the treatment of sewage water, treated water delivered to the Pandu River.
 Total cost of the full plant approx. 150-170 corer‟s.
Pumping station is the most important part of any treatment plant or sewage
treatment plants. It transfers the fluids of water one place to another place for treatment
process or supply purpose of fluids of water.
OUTLET PIPE OF M.P.S
(During Construction)
Figure-2

33. 33
5.1.1 WORKING OF MAIN PUMPING STATION
Main pumping station in sewage collection system also called lift stations, are
normally designed to handle raw sewage system that is fed from underground gravity
pipelines (pipes that are sloped so that a liquid can flow in one direction under gravity).
Sewage is fed into and stored in an underground pit commonly known as a wet well.
Sewage pumping stations are typically designed so that one pump or one set of
pumps will handle normally peak flow condition. And in this pumping station there are too
set of 6-6 pumps on the both adjacent side of MPS and three- three pumps are running from
both side at a working hours (4 hours from 8 hours).
Fig. 3- Main Pumping Station
(During Construction)

34. 34
Fig. 4-Main Pumping Station
(After Construction)
Fig.5
Main pumping station one side pipes

35. 35
 During working hours, in this pumping station there are to set of 6-6 pumps on the
both adjacent side of MPS and three- three pumps are running from both side at a
working hours (4 hours from 8 hours). Three pumps are working only four hours
continuously from both side, after that remained all six pumps are worked.
Fig. 6
Main pumping stations both side pipes

36. 36
5.2 INLET CHAMBER (Receiving Chamber)
The raw sewage will be delivered through 2200mm diameter RCC pipe into the inlet
chamber. The function of the inlet chamber is to reduce the incoming velocity which is
constructed in RCC M30 concrete. Fig2 Inlet Chamber. The chamber is provided with
coarse screen for screening the coarse particulars coming through the inlet pipe which
reduce the choking of pump and to ensure smooth running. All internal surfaces are finished
with smooth cement plaster with water proofing compound. All outside surface above
ground level are finished with thick sand faced plaster.
Figure-7
Inlet Tank

37. 37
5.3 SCREENING CHANNEL
5.3.1 Mechanical Screening Channel
Fine screen channels are provided to remove still finer suspended/floating particles
like leaves, paper, weeds etc. that is escaping coarse screen. They may escape from primary
clarifier and attach themselves to the weir of clarifier thereby preventing uniform over flow.
Sometimes the screening might choke sludge pipe line and also sludge pumps. The screens
installed are mechanical whereby the cleaning is done by means of a mechanical lift and
removed by using belt conveyor. This prevents any manual handling of the screen and is an
added advantage. The numbers of mechanical screens installed in the plant are three which
further allowed the flow into grit channel.
5.3.2 Manual Screening Channel
Two manual screen channels are provided with dimensions of 6×3.36×1.25m + 0.5m
FB to overcome any mechanical problem or any power failure situations at R.L. of 125.815
m. At the entrance of these channels fine screens are installed to prevent the entrance of
coarser particles into channel that may affect the further process of treatment.
Screening Channel
Figure-8

38. 38
5.4 SETTLING TANK
5.4.1 Detroiter Tank
Four Detroiter tanks two manual screen channels are provided with dimensions of 10.5
× 10.5 × 0.8m + 0.5 FB at R.L. of 125.565 m. The grit removal consists of two essential
elements-grit collecting mechanism and grit washing mechanism. Each operates separately
but in hydraulic communication with one another. The removal of grit is essential to protect
moving mechanical equipment from abrasion and accompanying abnormal wear.
 Reduce formation of heavy deposits in pipeline, channels and conduits.
Fig. 9 - Detroiters Tank

39. 39
Mechanism
The Detroiter is a continuous flow tank in which the grit settles due to gravity and
the water overflows though the outlet weir on the opposite side. The settled grit is scraped
by means of a scraper mechanism towards the openings on the classifier sidewall at the
bottom. The collection chamber works on velocity principal and is so designed that only grit
settles down and organic matter overflows. The classifier mechanism consists of a
reciprocating rake driven by a gear drive fitted with a motor. The grit collected is given a
thorough washing and is delivered from the top of the classifier through a Parshall Flume
for further disposal.
5.4 .2 Manual Grit Chamber
Grit chambers are nothing but like sedimentation tanks, designed to separate the
intended heavier inorganic materials) (specific gravity about 2.65) and to pass forward the
lighter organic materials. Hence, the flow velocity should neither be too low as to cause the
settling of lighter organic matter, nor should it too high as not to cause the settlement of the
silt and grit present in the sewage. Six chambers, each with the dimensions of 21.0 4.32 1.1
m + 0.5 m FB at R.L of 125.565 m are provided. A center of these chambers a hole of 30
cm diameter is made to remove the settled grit manually.
Generally grit channels are designed to remove all particles of higher specific
gravity of 2.65 or so with a nominal diameter of 0.20 mm and more, having settling velocity
of about 21 mm/sec at 100
/C, although some grit removal channels are designed to remove
particles above 0.15 mm size, having settling velocity of about 15 mm/sec at 100
/C. It is not
at all desirable to remove any organic matter in the grid chambers because no further
treatment of removed grit is provided.
Fig. 10- Manual grit chamber

40. 40
5.5 PARSHALL FLUME
A Parshall flume is a fixed hydraulic structure (104.5m) used in measuring
volumetric flow rate in surface water and waste water treatment plant. The Parshall flume,
R.L. 123.965m, accelerates flow though a contraction of both the parallel sidewalls and a
drop in the floor at the flume throat. Under free-flow conditions the depth of water at
specified location upstream of the flume throat can be converted to a rate of flow.
The Weirs, in which the discharge is proportional to head, are known as
Proportional Weirs. By float-regulated dosing devices the flow over a proportional weir
can be determined, e.g. in the case of a rectangular notch it is proportional to 3h/2 and in the
case of a triangular V-notch) the discharge is proportional to 5h/2, etc., where h is the head
over weir. The inverse problem is for a known head-discharge relationship finding the shape
of a weir constitutes the design of proportional weirs.
Fig. 11- PARSHAL FLUME

41. 41
5.6 DIVISION BOX
Division box is a long distributing channel which is dividing into 32 blocks to
distribute the sewage flow into different distribution boxes. It consists of a baffle wall
through which the sewage is uniformly distributed throughout the channel. Each box has a
dimension of 2.2×1×1.75 m with a R.L. of 123.665 m. 32 Densities iron pipes of diameter
450 mm are used to carry sewage from division box to distribution box to feed the reactors.
Each pipe has a flow regulating valve at the entrance of the plant.
Fig.12 - Division Box after Construction

42. 42
5.7 DISTRIBUTION BOX
Distribution box is the structural unit which is installed just before the UASB
reactors. The main function of the distribution box is to receive the flow from the division
box and feeds to reactors. At its bottom, flow from division box is stored and stabilized and
flow is further fed to reactors using 8 outlets of FRD pipes at the side of distribution box.
Fig. 9- Distribution Box
Fig.13 - Distribution Box

43. 43
5.8 UPFLOW ANAEROBIC SLUDGE BLANKET (USAB) REACTORS
Up flow Anaerobic Sludge Blanket (UASB) reactors are anaerobic centralized or
decentralized industrial wastewater or block water treatment system achieving high removal
of organic pollutants. The wastewater flows upwards in a vertical reactor through a blanket
of granulated sludge.
Bacteria living in the sludge break down organic matter by anaerobic digestion,
transforming it into biogas. Solids are also retained by a filtration effect of the blanket. The
upflow regime and the motion of the gas bubbles allow mixing without mechanical
assistance. Baffles at the top of the reactor allow gases to escape and prevent an outflow of
the sludge blanket. As all aerobic treatments, UASB require a post-treatment to remove
pathogens, but due to a low removal of nutrients, the effluent water as well as the stabilized
sludge can be used in agriculture. UASB reactor (Under construction) in the UASB process,
the whole waste is passed through the anaerobic reactor in an upflow
Mode, with a hydraulic retention time (HRT) of only about 8-10 hours at average
flow. No prior sedimentation is required. The anaerobic unit does not need to be filled with
stones or any other media; the up flowing sewage itself forms millions of small “granules”
or particles of sludge which or held in suspension and provide a large surface area on which
Organic matter can attach and undergo biodegradation. The gas produced is collected
through gas hood. Anaerobic systems function satisfactorily when temperatures inside the
reactor re above 18-200
C .Excess sludge is remove from time to time through a separate
pipe and sent to sludge sump under the action of gravity.
There are 16 UASB Reactors (32x28x5.2m) in 4rows each having 4 reactors. Each
reactor is subdivided into 8 parts each having a deflector beam, and is fed by two
distribution boxes from both sides. Sludge generated in reactors flows into sludge sump
under the action of gravity through three valves at different height.
These valves are operated on the basis of amount of sludge formed in the reactor.
Sewage coming upward through sludge blanket flows into gutter made of FRP. This
effluent is carried in a channel and conveyed to AERATION LAGOON. After this stage
contaminations are removed approximately 50-60% from sewage.

44. 44
Fig. 14 -USAB Reactor
(After Construction)

45. 45
5.9 AERATED LAGOON (FPU I)
Aerated lagoons are relatively shallow lagoons which wastewater is added at a single
point either at the edge or middle of the lagoon and the effluent is removed from another
point. The retention time is a function days as the removal of BOD. The retention time may
vary from 6 to 18 days as the removal of BOD from domestic wastewater varies from 75 to
90 percent.
Oxygen is supplied by means of surface aerators or by diffused aeration units. The
action of the aerators also maintains the solids of the lagoon in suspension. Sewage in this
units gets oxidized in increase in DO level of flow. Two aerated lagoons are used in this
plant, each having area of 13125 sq. m with 4.5 m depth. 9 aerators are installed in each
lagoon at slabs supported on columns. The aerators have the following advantages:
 High circulation and mixing capacity
 Virtually maintenance free
 No risk of clogging, even at intermittent operation or power failure
 No spray water.
Fig. 15-Aeration Lagoon

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5.10 FINAL POLISHING UNIT II
Polishing ponds are used to improve the quality of effluents from efficient anaerobic
sewage treatment plants like UASB reactors, so that the final effluent quality becomes
compatible with legal or desired standard. That residual organic material and suspended
solids concentrations in the digested sewage are reduced, but often the main objective of
polishing ponds is to improve the hygienic quality, measured by the concentration of two
indicator organisms: helminthes eggs and fecal coli forms (FC).
The FC removal is normally the slowest process and for that reason becomes the
main design criterion for a polishing pond. Final polishing unit is usually a shallow earthen
basin of controlled shape, which is designed for treating wastewaters. The ponds are usually
2 to 4 feet deep, although much deeper ponds shave been used quite successfully.
There are two final polishing units in the plant of area70, 000 sq. m with LD of
1.5m+0.5m FB. Base of this unite is made of Mud-Husk.
Fig. 16- Block Diagram of Final polishing unit

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5.11 CHLORINE COTACT TANK
The treated sewage is disinfected using gas chlorinator all the micro-organism that is
present in water/waste water is not harmful to human beings. Disinfection is the process
meant for removal of those microorganisms, which are harmful (disease causing) to human
beings. In disinfection process, the cell wall of micro-organism is punctured and
deactivation of the enzyme occurs.
A minimum contact time of 15 min is required for the chlorine to destroy the micro-
organism in the treated sewage. Free residual chlorine of 0.5 ppm should be maintained
after 15 min to ascertain complete destruction of the micro-organism.
Chlorine contact Tank Size of chlorine contact tank in the plant is 48.6x30x3.00 m
LD + 0.3 m FB. Maximum amount of micro-organism is removed in this tank and treated
sewage is carried by Final effluent channel to Pandu River.
Fig. 17-Chlorine Contact Tank

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5.12 GAS HOLDER
SEWAGE GAS TO POWER—
Flaring of Methane produced from the Sewage Treatment Plant is highly hazardous
and detrimental to the environment. Besides, it wastes of a precious source of renewable
energy that can be utilized to run the Sewage treatment plant. Envirex India is a pioneer in
India for indigenously designing, developing and implementing a qualitative system to
efficiently convert the methane from Sewage treatment plants into a renewable and
sustainable source of energy.
Fig. 18 – Gas holder
(During Construction)

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5.13 FINAL EFFLUENT CHANNEL
A 4.5 m wide channel carried final discharge to Pandu River. This channel is made
of M 25 concrete with the level depth of 1.25 m at RL of 117.41 m.
Fig. 19-Final Effluent Channel

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5.14 SLUDGE PUMPING STATION
Sludge extracted in reactors is collected in sludge pumping station through FRP
pipes of diameter 10 cm under the action of gravity. Sludge in this unit, is in semi-solid
form which necessitates proper slope of DI pipes from reactors to sludge pumping station.
Powerful pumps should be installed to pump the sludge into filter press building.
5.15 FILTER PRESS BUILDING
One of the most difficult problems today is the disposal of sludge in waste
treatment. Dewatered sludge form traditional dewatering equipment, (i.e. rotary vacuum
drum filters, centrifuges and belt presses), are less acceptable for disposal in landfills and
due to their high moisture content they are not economical feasible. Drying Beds are widely
used these days but they require a considerable amount of land which makes the project
costly. Apart from this it is time taking process and fails in cloudy or rainy weather. The
filter press process results in drier sludge that has proven to be an effective solution. Three
Filter press Machine are used in this project on top of the building (25×15×9m. Solid
particles are collected in trucks under the filter press building. Water separated from sludge
transported to reactors through underground pipes under gravity.
Fig.20 -Filter Press Building

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5.16 ADMINISTRATIVE CUM LABORATORY BUILDING
Final effluent of the plant should satisfy standards of CPCB. For frequent and
regular testing of influent and effluent, an advanced Laboratory of area 200m2
is present in
the plant for the analysis of BOD, DO, COD and various other characteristics.
Fig. 21-Administrative Cum Laboratory Building

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6. CONCLUSION
UASB technology used Sewage treatment plant, Bingawan will play very
important role to treat large amount of sewage. It will help in reducing pollution
level in the Ganga in Kanpur district. It is also economic when compared with other
sewage treatment technology like UASB. It will be 2nd
largest STP in India.
It will reduce pollution load on river the Ganga. Apart from this solid sludge
can be used as fertilizers. Many environmental aspect is also associated with this
treatment plants. Aquatic life of river Ganga can be improved.

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7. REFRENCES
1. Jane Cumberlidge (2009) in land waterways of Great Britain (8th edition
) - Imrey
Laurie Norie and Wilson.
2. Barcelona city history museum water pumping station casa del “aigua”
3. "Evaluation Of Operation And Maintenance Of Sewage Treatment Plants In
India-2007". CENTRAL POLLUTION CONTROL BOARD, Ministry of
Environment & Forests. 2008.
4. "Status of Sewage Treatment in India". Central Pollution Control Board,
Ministry of Environment & Forests, Govt of India. 2005.
5. “Agbar water museum”
6. Sewage disposal and environmental engineering by S.K Garg
7. www.wikipedia.com; www.google.com
8. Environmental engineering II by Saurabh Kumar Soni with KATSON books
9. Environmental engineering by Ardent Publications
10. Some details from the staff of Sewage Treatment Plant, Bingawan, Kanpur
11. Khopkar, S. M. (2004). Environmental Pollution Monitoring and Control. New
Delhi: New Age International.
12. Wastewater engineering: treatment and reuse (4th ed.). Metcalf & Eddy, Inc.,
McGraw Hill, USA. 2003.
13. Metcalf & Eddy, Inc. (1972). Wastewater Engineering. New York: McGraw-Hill
Book Company.
14. Wastewater engineering: treatment and reuse (4th ed.). Metcalf & Eddy, Inc.,
McGraw Hill, USA. 2003.
15. Sharma, Sanjay Kumar; Sanghi, Rashmi (2012). Advances in Water Treatment
and Pollution Prevention. Springer. Retrieved 2013-02-07.
16. EPA. Washington, DC (2000). "Package Plants. "Wastewater Technology Fact
Sheet. Document no. EPA 832-F-00-016.
17. EPA. Washington, DC (1999). "Sequencing Batch Reactors." Wastewater
Technology Fact Sheet. Document no. EPA 832-F-99-073.
18. Wastewater engineering: treatment and reuse (4th Ed.). Metcalf & Eddy, Inc.,
McGraw Hill, USA. 2003