mbr_process_design_description_gc_equipment_K2.pdf

MOINHOS AGUA E AMBIENTE, Lda.
Zona Industrial Alto da Cruz | Rua B, nº 66- Apartado 165 | 4780-739 Santo Tirso | Portugal
Tel/fax| Fax.: +351 252 857 925 |Tlm.: +351 91 868 91 17 | geral@moinhosambiente.com | www.moinhosambiente.com
owner: A.A.W.S.A. Addis Ababa Water and Sanitation Authority
project: Package waste water treatment plant supply and civil work construction for
Lot 1 -Kilinto, Mekenisa Korari, Kara Kore 1 Bole Bulbula, Deginet condominiums
local Addis Ababa; Ethiopia
description Waste water treatment plants with MBR technology
project phase: execution
document name Detail design description
document reference Lote 1 [detail design description]00
00 CF AT AM 2015-01-30 Release for approval. Note: Include just Mekenisa Site
rev. written by verified approved date remark

PROJECT DESIGN DESCRIPTION 2
INDEX
INTRODUCTION..................................................................................................................5
1 DESIGN DATA .............................................................................................................6
1.1 GENERAL CONSIDERATIONS.................................................................................................................6
1.2 DESIGN WASTEWATER FLOWS.............................................................................................................6
1.3 DESIGN WASTEWATER LOADS .............................................................................................................7
1.4 EFFLUENT LIMITS .....................................................................................................................................8
1.5 TREATMENT DEMANDS...........................................................................................................................8
1.6 DESIGN ALTITUDE, AIR TEMPERATURE AND HUMIDITY............................................................9
2 TREATMENT LINE ......................................................................................................10
3 PROCESS DESIGN .....................................................................................................12
3.1 LIQUID PHASE...........................................................................................................................................12
3.1.1 RECEPTION AND DESTRIBUTION OF RAW FLOW RATE..............................................................................12
3.1.2 THICK AND THIN SCREENING AND SAND SEPARATION .............................................................................12
3.1.3 EQUALIZATION AND BIOLOGICAL FEEDING................................................................................................13
3.1.4 BIOLOGICAL TREATMENT AND SOLID LIQUID SEPARATION BY MICROFILTRATION MEMBRANES
(MEMBRANE BIOREATOR MBR) ...............................................................................................................................13
3.2 SOLID PHASE .............................................................................................................................................19
3.2.1 DEWATERING .............................................................................................................................................19
3.3 BYPASS, OVERFLOWS, DISCHARGES EMERGENCY AND DRAINAGES...................................20
3.4 HIDRAULIC CIRCUITS ............................................................................................................................20
4 IMPLEMENTATION FHILOSOPHY AND CONSIDERATIONS...............................................21
5 PROCESS DESIGN CRITERIA AND DESIGN CALCULATIONS............................................22
6 EQUIPMENTS ............................................................................................................23
7 ELECTRICAL INSTALLATIONS, ELECTRICAL PANEL, AUTOMATION AND CONTROL ..........24
7.1 POWER SUPPLY ........................................................................................................................................24
7.2................................................................................................................................................................................24
7.2.1 DISTRIBUTION OF ENERGY AND ELECTRICAL PANEL (EP).........................................................................24
CABLE DISTRIBUTION..............................................................................................................................................24
GENERAL ELECTRIC PANEL ....................................................................................................................................24
7.3 AUTOMATION AND CONTROL.............................................................................................................25
7.4 HIERARCHY OF COMMAND OPERATION ........................................................................................25
7.5 ALARMS ......................................................................................................................................................25
8 CONTACTS ...............................................................................................................26
9 ANNEX 1 - PROCESS DESIGN CRITERIA AND DESIGN CALCULATIONS ............................27
9.1 LIQUID PHASE...........................................................................................................................................27
9.1.1 WASTE WATER LIFTING STATION...............................................................................................................27
9.1.2 THICK AND THIN SCREENING AND SAND SEPARATION .............................................................................27
9.1.3 EQUALIZATION ...........................................................................................................................................27
9.1.4 BIOLOGICAL TREATMENT AND SOLID LIQUID SEPARATION BY MICROFILTRATION MEMBRANES
(MEMBRANE BIOREATOR MBR) ...............................................................................................................................28

9.1.5 MEMBRANES AND FILTRATION DESIGN .....................................................................................................28
9.1.6 TANKS AND RECIRCULATION DESIGN........................................................................................................29
9.1.7 ACTUAL OXYGEN REQUIREMENTS (AOR) ..................................................................................................31
9.1.8 MBR AERATION SYSTEM ............................................................................................................................32
9.1.9 ADICIONAL AERATION SYSTEM..................................................................................................................33
9.1.10 MBR CLEANING IN PLACE ......................................................................................................................34
9.1.11 GLOBAL PARAMETERS OF THE BIOLOGICAL TREATMENT ....................................................................34
9.2 SOLID PHASE .............................................................................................................................................35
9.2.1 DEWATERING .............................................................................................................................................35
ANNEX 2 – EQUIPAMENT LIST OF MEKANISA KOTARI ..........................................................36
ANNEX 3 TECHNICAL DOCUMENTATION ............................................................................50

TABLE INDEX
TABLE 1 DESIGN WASTEWATER FLOWS TOTAL AND PER LINE. ............................................................................6
TABLE 2 DESIGN RAW WASTE WATER LOADS. ...................................................................................................7
TABLE 3 EFFLUENT LIMITS................................................................................................................................8
TABLE 4 TREATMENT DEMANDS .......................................................................................................................8
TABLE 5 DESIGN ALTITUDE, AIR, TEMPERATURE AND HUMIDITY..........................................................................9
FIGURE INDEX
FIGURE 1 TREATMENT LINE FOR KARA KORE, MEKANISA, BOLE AND KILINITO. ...............................................................10
FIGURE 2 SCHEME OF THE OPERATING PRINCIPLE OF A MBR REACTOR..........................................................................14
FIGURE 3 SCHEME TYPE OF A MBR REACTOR........................................................................................................................14
FIGURE 4 STRUCTURE OF THE MEMBRANE MODULE FOR ONE FLOOR AND TWO FLOORS............................................15
FIGURE 5 STRUCTURE OF CARTRIDGE MEMBRANES............................................................................................................16
FIGURE 6 FILTRATION..................................................................................................................................................................17
FIGURE 7 CHEMICAL CLEANING METHOD IN SITU ..................................................................................................................18
FIGURE 8 IMAGES OF EXTRACTING MODULES........................................................................................................................18
FIGURE 9 E 10 IMAGES OF TOUCH MONITOR. ........................................................................................................................25

INTRODUCTION
Addis Ababa Water and Sanitation Authority launch the Package waste water treatment plant supply and Civil work
construction for Lot 1 -Kilinto, Mekenisa Korari, Kara Kore 1 Bole Bulbula, Deginet condominiums
The tender was granted to the consortium Tsemex Global Enterprise and Moinhos Água e Ambiente lda.
The present document has the intention to describe all the criteria and design calculations of the Waste Water treatment plant
hydraulic process.

1 DESIGN DATA
1.1 GENERAL CONSIDERATIONS
The treatment solution was designed to meet the following assumptions:
 Meet the design load and waste water flows and effluent limits
 Absence of unpleasant odors
 Avoid the proliferation of mosquitoes, which can contribute to disease transmission
 Negligible noise and vibrations
 Install safety solutions (reduce risks of intrusion).
 Design compact solutions (more free space for social areas)
 Minimum visual and environmental impact
 Find the Appropriate construction solutions for each Site
 Easy and quick installation
 High mechanical and chemical resistance due to the construction material
 Simplicity of operation and maintenance
 Automatic operation
 standardization of processes and equipment for the 5 WWTP
 The solution was preconized to be as possible in a gravitical way ˃ avoid the construction of pumping station that
would lead in a solution with higher investment cost, and higher operational cost because of the energy consumption
and maintenance.
1.2 DESIGN WASTEWATER FLOWS
The table 1 describes the design waste water flows used in the actual project.
Table 1 Design wastewater flows total and per line.
Legend: * from tender; ** estimated by Moinhos Ambiente.
Parameters notes units Value
SITE Deginet Kara Kore 1 Mekenisa Kotari Bole Bulubla Kilinito
Lines of treatment * un 1 2 2 2 2
Type of efluente * domestic
Daily medium flow rate * m3/day 400 =400x1 1000= 500x2 1700 = 850x2 3000=1500 x 2 4000 = 2000 x2
Daily medium flow rate
24 h
* m3/h 16,7= 16,7x1 41,67=20,83 x2 70,83=35,42x2 125,00= 62,5x2 166,67 = 83x2
Coefficient Peak Flow ** 2 2 2 2 2
Peak Flow * m3/h 33,33 = 33,33x1 83,33 = 41,67x2 141,67=70,83x2 250 = 125,00x2 333 = 166,67x2

1.3 DESIGN WASTEWATER LOADS
In table 2 the pollutant loads and their concentration are presented:
Table 2 Design Raw waste water loads.
Legend * from tender; ** estimated by Moinhos Ambiente.
Parameters Notes Symbol units
SITE Deginet Kara Kore 1
Mekenisa
Kotari
Bole Bulubla Kilinito
Chemical Oxygen Demand * COD
mg/l 750,00
kg/day 300 750 1275
2250
3000
Biochemical Oxygen
Demand
* CBO
mg/l 300,00
Kg/day 120 300 510 900 1200
Total Suspended solids ª SST
mg/l 350
kg/day 140 350 595 1050 1400
Total Nitrogen ** TN
mg/l 42,00
Kg/day 16,80 42,00 71,40 126,00 168,00
Kjeldah Nitrogen * TKN mg/l 42
Kg/day 16,80 42,00 71,40 126,00 168,00
Total Phosphorous *
mg/l 22,00
kg/day 8,80 22,00 37,40 66,00 88,00
Oil and fats **
mg/l 50,00
kg/day
pH *
Escala
Sorensen
7-7,5
Fecal Coliforms ** nº/100 ml 10^8 (**)

1.4 EFFLUENT LIMITS
The reclaimed (treated) water is to be used for gardening, car washing at the condominium sites.
The table 3 indicates the limits characteristics of the treated effluent.
Table 3 Effluent limits.
Legend * from tender; ** estimated by Moinhos Ambiente.
Design Guarantee
Chemical Oxygen Demand * COD mg/l <50
Biochemical Oxygen Demand * CBO mg/l <5
Total Suspended solids * SST mg/l <5 < 1
Total Phosphorous * mg/l 5
pH * Sorensen 6,5-8
Fecal Coliforms * nº/100 ml <100 <10
Virus * % 99,99999
1.5 TREATMENT DEMANDS
According the above, the efficiency of the WWTP for each parameter is presented at the following table:
Table 4 Treatment demands
legend* from tender; ** estimated by Moinhos Ambiente.
Parameters Notes Symbol units Efficiency
Chemical Oxygen Demand COD mg/l
Biochemical Oxygen Demand CBO mg/l
Total Suspended solids SST mg/l
Total Phosphorous * mg/l 77
Fecal Coliforms nº/100 ml
Virus % 99,999

1.6 DESIGN ALTITUDE, AIR TEMPERATURE AND HUMIDITY
Adding to the flow and waste water loads there are more design parameters that have high impact in the WWTP design.
In the next table it is described the assumed air temperature and humidity, with higher importance to the altitude of the
installations, that once is very high has enormous impact in the oxygen demand.
Table 5 Design altitude, air, temperature and humidity.
Legend * from survey; ** estimated by Moinhos Ambiente.
SITE Deginet Kara Kore 1
Mekenisa
Kotari
Bole Bulubla Kilinito
Altitude *
m above
sea level
2304 2384 2222 2185 2103
mbar 765 758 773 777 785
Air temperature ** T ºC 20
Relative humidity ** RH % 60

2 TREATMENT LINE
The sequence of wastewater treatment plant, which comprise the steps and associated systems corresponding to the design to
implement, are shown below:
Figure 1 Treatment line for Kara Kore, Mekanisa, Bole and Kilinito.
Equalization Tank
Treated waste water tank for
reuse with CIP compartiment
Irrigation/ washing streets /
citernes/ construction works
Manhole
Raw Waste Water
MBR tank
Atmosferic
Air
Deposition in appropiate
destination
(ex.Agriculture)
Environnement
Sludge dewatering equipment
Pumping Station
Pré- areation Tank
Automatic Sieve /sand
separator
Solids, sand
Atmosferic
Air
Distribution chanel
Overflow for Septic tanks
Thik manual sreen
Equalization Tank
MBR tank
Atmosferic
Air
Atmosféric
Air
Pré- areation Tank
Automatic Sieve /sand
separator
Thik manual sreen
Atmosferic
Air
Solids
Solids, sand
Solids
Sludge dewatering equipment
Deposition in appropiate
destination
(ex.Agriculture)
PRELIMINARY
TREATMENT
EFFLUENT
RECEPTION
AND
REPARTITION
THIK
SCREENING
THIN
SCREENING
SAND
SEPARATION
PRE-TREATMENT
EQUALIZATION
BIOLOGICAL
TREATMENT
FEEDING
SECONDARY
TREATMENT
AND
TERCEARY
TREATMENT
-
COMBINED
PROCESS
BIOLOGICAL
TREATMENT
SLUDGE
SEPARATION
BY
MICROFILTRATION
MEMBRANES
EFFLUENT
REUSE
TREATED
EFFLUENT
STORAGE
PUMPING
STATION
SLUDGE
TREATMENT
DEWATERING

The waste water treatment plant for Kara Kore, Mekenisa, Bole and Kilinito are done in two parallel treatment lines, for Deginet in
one line.
The WWTP comprises the treatment of the liquid phase and the solid phase. There is no need to treat the gas phase, since there
is no treatment stage which could causes unpleasant odors.
Following a brief description of each stage of treatment for Kara Kore, Mekenisa, Bole and Kilinito:
a) LIQUID PHASE TREATMENT
 Preliminary treatment:
o Effluent reception and repartition, by gravity from manhole to a concrete box (1 for 100%)
o Thick screening, in a contiguous concrete channel with a thick manual screen (1 50% + 1 50%)
o Thin screening an Sand separation, in an automatic combined equipment (1 50% + 1 50%) installed in a
common dry concrete box
 Pre-treatment:
o Convergence and repartition of flow rates to feed equalization tank, in a concrete box (1 for 100%)
o Equalization, in concrete tanks (1 50% + 1 50%) with air aeration systems (1 100%)
o Biological treatment feeding and flow rate measurement , by pump and flow meter (1 50% + 1 50% + 1
50% spare store)
 Secondary treatment and tertiary treatment
o Aerobic biological treatment, developed in a concrete pre-aeration tank with aeration by fine bubble
diffuser (1 50% + 1 50%)
o sludge separation and disinfection by microfiltration membranes developed in a concrete MBR
tank (1 50% + 1 50%), with filtration pumps with flow meter, cleaning aeration system,
o Effluent recirculation between MBR tank and pre-aeration tank, by pump (1 50% + 1 50%)
o Membranes cleaning in place (1 for 50%)
 Treated effluent reuse
o Treated waste water storage in a concrete storage tank (1 for 100%)
o Internal reuse by a pumping station (1 for 100%)
b) SOLID PHASE TREATMENT
 sludge treatment
 Dewatering, in a screw dewatering system (1 50% + 1 50%)
c) BY PASS, EMERGENCY DICHARGES, AND DRAINAGES
 General Bypass of the WWTP that is made in last manhole which also feeds septic tanks
 Local drainage of combined units box through a submersible pump to the final discharge box
 MBR Overflow tank to the pre-aeration tank
 Overflow of pre-aeration tank to the equalization tank
 Overflow of equalization tank to the final discharge box

3 PROCESS DESIGN
In this chapter the detail process design is described.
3.1 LIQUID PHASE
3.1.1 RECEPTION AND DESTRIBUTION OF RAW FLOW RATE
Once that WWTP will have two lines of treatment, it exist the need to establish an organ to allow the reception and distribution of
effluent to each treatment line.
So it will be built a common concrete box where it will arrives the pipe from the last manhole (same feeding septic tanks).
This concrete box will bifurcating into the two channels that will be used for the thick screen as it will be described in the next
chapter.
3.1.2 THICK AND THIN SCREENING AND SAND SEPARATION
The pre-treatment is composed by the following steps:
 A manual screening, for bigger solids retention;
 And an automatic screening and grit removal system;
The raw effluent arrives to a concrete channel next to distribution box, where is installed a manual thick screening for retention
solids bigger than 50 mm. This manual screening will protect the automatic screening unit against big solids. In each screen it
will be installed a perforated box to receive the screen solids, that will be manually take out by an operator.
From the concrete channel the sewage will flow by gravity, for the combined unit with a thin screening system and a grit
removing system, both totally automatics.
In this combined unit, the solids bigger than 3 mm are retained and removed to the solids container, through a screening screw.
The effluent is received in first input unit tank, where it is installed a screen that removes the larger solids than 3 mm washing,
pressing and drying it. The sieve consists of a sieving area and a spiral screw without a shaft. During operation of the equipment
solids are retained in the sieving and gradually gets filled. The upstream liquid level rises to a predetermined maximum level,
which starts running gear motor driving the spiral. A set of brushes fixed peripherally to the bottom of the spiral will be
responsible for cleaning the mesh sieving, as well as to promote the transport of solids to the discharge area. Solids or harrowing
are slightly compressed and dehydrated by moving the auger to the discharge area for a container.
After screening, the sand are separated by sedimentation, in a proper compartment, and is removed to the sand container, first
by a horizontal screw and after by an inclined screw.
The unit also has a bagging system that continues collect the extracted solids and sands, avoiding the direct contact of operators
the release of odors. When necessary, these solids must be transported to a local authorized and deposited there.
The container will be normalized, with castors for easy movement
The pre-treated sewage flows by gravity to the equalization tank, more precisely to the equalization distribution box, by individual
pipe.
Each unit is fitted by pipes with cut off valves in the inlet and outlet.

The combined unit is installed in a concrete dry box, depth enough to allow gravitational inflow of effluent. The box will have
access to the interior by stairs.
Each screening and grit unit works automatically, controlled by level sensors installed in each unit. The command of this
equipment will be done by the general electrical panel of the WWTP
3.1.3 EQUALIZATION AND BIOLOGICAL FEEDING
The waste water that arrives to the WWTP has peaks and distinct quality parameters along the day. So is important to have a
buffer tank to equalize and amortize the peaks, in order to turn possible to feed the biological process at a constant flow and
regular characteristics 24 hours a day. The equalization tank capacities permit to achieve these objectives.
There will exist 2 concrete equalization tanks. The effluent arrives to them by a convergence and distribution box.
If necessary, in case of maintenance, it is possible to keep one out of service during one or two days, for example, by closing
one entrance with a blind flange, without affecting the normal running of the WWTP.
The mix and oxygenation of the sewage in the equalization tanks, are made through air, introduced in the liquid by membrane
disc diffusers (fine bubble diffusers). The air is supplied by a common blower. The blower works continuously and/or with timer.
The oxygen (air) dissolved in the liquid does not allow to develop inconvenient odors in the equalization tank.
The equalized sewage is elevated, to a pre-aeration tank, at constant flow, by self-priming centrifugal pumps.
There are installed 2 self-priming pumps. Each pump feeds the correspondent MBR tank.
Each self-priming pump works always automatically (on-off), controlled by the level sensors installed into the equalization tank
and in the MBR tanks.
In the suction pipe of the electric pump groups will be installed one stainless pre-filter with a mesh of 6 mm, easy to remove for
cleaning (once a week).
3.1.4 BIOLOGICAL TREATMENT AND SOLID LIQUID SEPARATION BY MICROFILTRATION
MEMBRANES (MEMBRANE BIOREATOR MBR)
3.1.4.1 General Principle of Operation
This step is a biological process that uses a broad range of microorganisms which convert organic matter into simpler
substances dissolved and biomass.
To develop these microorganisms is necessary to provide food that is present in the effluent, sufficient residence time in the
bioreactor, so that the microorganisms grow and to fulfill their function, and supplying oxygen to the breathing process.
This reaction results in a liquid phase process (treated effluent) and a solid phase (biological sludge), which need to be
separated. In this project, the solid-liquid separation process will be made microfiltration membranes submerged in the MBR
tank.

The MBR is a combination of activated sludge processes for
biological treatment of dissolved organic matter in the effluent,
with solid-liquid separation processes by membranes.
The membrane bioreactor works in similar conditions to
bioreactor of activated sludge. However, the solid-liquid
separation instead of settling is realized by submerged
microfiltration membranes.
⇒ Biodegradation of organic matter+ solid-liquid separation +
Physical Disinfection
Tertiary effluent quality in a single system
The following figure illustrates an example a type of an MBR reactor.
Figure 3 Scheme type of a MBR reactor.
3.1.4.2 Biological reactors and recirculation
The biological treatment will be carry out in two distinct concrete tanks per line:
 MBR tank, with tight dimensions to be installed the submerged membranes Units (SMU)
 Pre-aeration tank, that add the necessary volumetric require for the biological degradation
Between these two tanks will be exist a recirculation which will allow maintain the desired concentration of solids therein.
The recirculation is done by a self-priming pump one per line, from MBR tank to pre-aeration tank. The effluent returns to MBR
tank by an overflow.
These pump will works continuously or/and with timer and protected by a level sensor in the MBR tank.
Figure 2 Scheme of the operating principle of an MBR reactor.

3.1.4.3 Submerged Membrane Units (SMU)
The SMU are installed inside the MBR tank.
The submerged membrane modules are used for solid-liquid separation, for filtering a high-quality liqueur water. The membranes
serve as a physical barrier preventing the passage of particles with daymeters greater than its pours while allowing free passage
of the treated water.
The number of modules depends on the design flux and the flow to be filtered.
The installation are prepared with one more space in the MBR tank for the implementation of one more SMU for future
necessities. The diffuser case will be by now installed.
Structure of the submerged membrane module
Each membrane module consist in a membrane compartment and a diffuser compartment.
The membrane compartment includes multiple cartridges, which are connected to a common permeate pipe by several
transparent tubes.
It is possible to remove each interior membrane cartridge for maintenance,
The diffusers compartment has diffusers pipes inside.
The SMUs can be of one deck (lower deck) of membranes, or two decks having also the upper deck, as discriminates the
following figure.
Figure 4 Structure of the membrane module for one floor and two floors.

Structure of the membrane cartridge
Figure 5 Structure of cartridge membranes.
3.1.4.4 Aeration system / cleaning of the membranes
The membrane aeration system has a cleaning function once the air continuously remove retained sludge, wiping the walls of the
membranes, to prevent the clogging, and at the same time provide a big amount of the oxygen needed to the biological
treatment.
The membrane aeration system is constituted by the diffuser case of the membrane and one blower per line.
Each line will have and inlet head piper and an outlet head piper. The SMU is fitted to the head piper by vertical pipes.
The blower feeds the inlet head piper that is design to distribute the air equally for all SMUs in this line. In the outlet pipe will be
installed an automatic cut off valve to purging condensate.
The blower’s works in a fixed flow rate, by timer.
The valve will also open by timer set.
3.1.4.5 Supplementary aeration System
The homogenization and oxygenation of the entire biological mass produced at this stage, necessary for depuration of dissolved
organic matter in the effluent, will be promoted for dissolution of oxygen (atmospheric air) through porous diffusers of the MBR
modules and complemented with a system of fine bubble diffusers, fed from another blower for each pre-aeration tank.
The diffusers will be installed in sets. From the blower the air will run by a unique head pipe per line doing the distribution of air of
each set by a vertical pipe.
Each set of diffusers will have a vertical pipe in the opposite side of the feed, ending in a cut-off manual valve, for the
condensate purge.
In each head pipe will be installed a fitting for the maintenance clean. The maintenance should be done once a year without
taking out the diffusers neither empty the tank.
In each pre-aeration tank will be installed a O2 sensor and controller.

The flow rate of the blower will be proportional to the read of the O2 controller. In this way the process control and energy saving
will be effective.
3.1.4.6 Filtration - Vacuum permeate in cross flow
The separation between treated effluent (purified) and biological sludge, which are the liquor mix of MBR bioreactor will be
promoted through flat microfiltration membranes by Kubota (Japan), which will act as a filter between the biological mass
formed and the liquid.
The liquor flows on the membrane surface at the same time the water permeates the
membranes. This cross-flow prevents the occurrence of fouling.
The extraction of water through the microfiltration membranes is held by suction by means of a
self-priming pump by establishing a depression necessary to force the passage of water
between 0.1- 0.4 bar
The pump suck the effluent from the MBR reactor, making it pass through the membranes,
filtering it, getting the biological sludge retained on the outer walls of the membranes.
The treated effluent will be directed conducted to the storage water tank to reuse.
On the installations that uses SMU of one deck, it will be installed one head piper per line. On the installations that uses SMU of
two decks it will be installed two head piper per line - one will connect the lowers decks and the second the upper deck.
The SMUs fits the head pipe by vertical pipes.
It will be installed one pump per head pipe.
It will be installed a pressure indicator in the pump suction, to control the transmembrane pressure.
It will be installed in the discharge the pump an electromagnetic flow meter and a flow control valve.
The operation of this electric pump is protected by level sensor to be installed in the biological reactor and by controlling the
negative pressure in the suction pipe.
Whenever the filtration process is running the blower of the membranes should be operating, because in this way it generates an
upward air flow that cleans the surface of the membrane reducing the clogging.
When the depression generated by the pump overcome 0.3 bar, will be activate an alarm signal indicating the need for cleaning
the membranes.
3.1.4.7 Membrane Cleaning System
The cleaning solution consists of a sodium hypochlorite solution at a concentration of 0.5%.
The cleaning solution is transferred by gravity to the membrane cartridge by the permeate manifold.
So in each permeate head pipe it will be left a fitting with a blind flange. In the opposite side it will be installed another fit with a
manual cut of valve to purge the air during the solution injection.
Figure 6 Filtration

In this project the cleaning solution will be performed in a small tank within the
treated water tank.
The rise of the solution to the injection point will be performed by a portable
submersible pump.
In the injection point the pipe have a cut off valve which allows the operator to
regulate the solution flow rate to be injected in each collector.
The injection time is about 10-15 min.
This system allows various cleaning membrane modules, without the need to
empty the tank, extracting modules, or stopping of the plant.
The frequency of cleaning is estimated to be 1-2 times a year, each lasting 2-3
hours where the hand labor is minimal.
3.1.4.8 System of membrane extraction and modules
Each membrane module is mounted on a guide tubes that facilitate extraction by any actions of maintenance and
cleaning without emptying the tank membranes. If necessary, each cartridge can be extracted from the module for
individually inspection or replacement.
Figure 8 Images of extracting modules.
Whenever necessary the modules can be extracted from the tank, by using a lifting tool with and a crane.
Chemical
Tank
Figure 7 chemical cleaning method in situ

3.1.4.9 EFFLUENT STORAGE AND PUMPING REUSE STATION
The treated effluent will be storage in one common tank for both lines.
The water, from the permeate pump flows to the water storage tank and is discharged into the final box by an overflow.
Since the water is continuously filing and discharge, the water is maintained “fresh”.
A pressurization pump will be implemented for reuse treated waste water into the following application points:
 Combined unit
 Dewatering system.
 Faucet(s) for hose connection which can be used for floor cleaning and irrigating
3.2 SOLID PHASE
3.2.1 DEWATERING
When the concentration of MLSS overcome the maximum value, the biomass should be removed from the WWTP, restoring
acceptable levels of MLSS in the MBR reactor.
Once the MBR sludge reactor will meet higher concentrated sludge, of about 1.5%, it is possible to extract it directly to
dewatering unit.
The dewatering system will consist of the following elements per line:
 Eccentric screw pump, which pump MBR sludge from the reactor for flocculation tank
 Polyelectrolyte Preparation unit
 Polyelectrolyte Dosing pump
 Sludge dewatering equipment consists of eccentric screw reduced speed, free noise, low energy consumption, easy
operation and maintenance to reach a dehydration level of about 15-20%.
The dewatered sludge will be stored in big bags, and then transported by truck self-cistern, to an appropriate and authorized
location deposition, which may be in agriculture as fertilizer.
The resulting effluent from the dewatering, as well as drained from the big-bag , will be collected in on point and discharge into
equalization tank.

3.3 BYPASS, OVERFLOWS, DISCHARGES EMERGENCY AND DRAINAGES
The following bypass circuits and emergency discharges will be included:
 General by pass of the WWTP is made in the last manhole which also feed the septic tanks
This bypass works when:
o WWTP is not in service because of maintenance issues or electric failure, etc.
o The flow rate is higher than the project, normally it happens in case of high rain and storms. This by pass
safeguards the "biomass laundering" from the reactors that compromise the efficiency of the biodegradation
of organic matter.
 Local drainage of combined units through submersible pump to the discharge end box.
This drainage becomes necessary, since there is no gravity flow for general discharge box WWTP.
Will be used in times of rainfall and when it needs to carry out washing of floors.
 MBR overflow tank to the pre-aeration tank.
Usually works as a process.
 Pre-aeration tank Overflow to the equalization tank
Works in case of any failure of equipment or electric power
 Equalization tank overflows to the final discharge box.
Works in case of any failure of equipment or electric power
 Overflow of water storage tank treated for final discharge box.
Normal operation process
 All bypass circuits and emergency overflow will have installed an input detection system in operation of the bypass
which sent an alarm for supervision
3.4 HIDRAULIC CIRCUITS
Networks and hydraulic circuits are sized according to the legal requirements and depending on manufactures indications.
For air pipe were used velocity below 20 Nm/s and for liquid below 3 m/s.
The entire visible pipe will be in Stainless steel AISI 304.
The entire buried or submersible pipe (non visible) will be in PVC and PEAD.
The stainless steel pipe will be used under the ISO standards.

4 IMPLEMENTATION FHILOSOPHY AND CONSIDERATIONS
The follow considerations are done for all the WWTP taking into account the technical, environmental and social concerns:
 Cover the equalization tanks.
Reduce the risk of falling into the treatment tanks. Less visual impact to the residents
 The semi-underground tanks (pre-aerated and MBR tanks) will be about 1 m outside
Allow the safe visual inspection of the inside of the tank without protection grades. Facilitates the installation of the
equipment and piping in a safe way.
 Utilization of the equalization bottom slab to be the base of the technical area
This made the solution very compact, with robust floor to implement equipment and prevent displacement
 Construction of just one technical area subdivide in the necessary areas:
1- Guardhouse, office, toilets, Electric and Automation Panel, will be accommodate in a civil building.
2- The equipment, blowers, pumps, dewatering equipment will be installed in an open space with cover with a
lightweight structure. In this technical area the sludge equipment will be separated by the others by a delimitation
area with a wall
3- Functional simple and compact solution
 It was preconize continuous concrete tanks
Facilitates the civil work and made a compact solution.
 The contiguous concrete tanks have the background slabs all in the same level
Facilitate the civil work
 It was predicted a fence at the perimeter of the entire WWTP
Prevent the entire safeguard the security of all the installation
 This fence shall be accompanied with green spaces with trees and shrubs.
To minimize the visual and environmental impact
 It will exist a compacted ground floors around the tanks, so that the whole area could be a local to entry and exit of
vehicles.

5 PROCESS DESIGN CRITERIA AND DESIGN CALCULATIONS
In Annex 1 the design criteria and the design of the solution will be presented for the five WWTP
In the first column indicates the followed:
DB: Data base
DC: Design criteria
PD: Predesign
D: Design

6 EQUIPMENTS
Annex 2 provides a list of equipment which are presented by each unitary process of the waste water treatment
plant.
For each equipment is presented:
 The tag concerning the process and instrument diagram (P&I) (shown in the drawing documents). The
nomenclature used is the follow:
 The main features
 Number of units: in service, spare installed and spare warehouse
 Installed power
 Some observations on the command and other relevant.
 It also described the technical documentation available for each equipment
The naming of each document follows the following logic: Brand_model_equipment [type of document]
Either in digital form or in paper documentation will be organized alphabetically. Digitally was also done a
direct link to the documentation.

7 ELECTRICAL INSTALLATIONS, ELECTRICAL PANEL, AUTOMATION AND CONTROL
7.1 POWER SUPPLY
The customer will be responsible for the supply of electricity to the General Electric Panel (EP) WWTP.
This QEG must be installed in the technical area of the WWTP, closed and covered
7.1.1 DISTRIBUTION OF ENERGY AND ELECTRICAL PANEL (EP)
CABLE DISTRIBUTION
The power cords or power command of the various equipments will be installed in plastic PVC mats. This distribution should be
performed taking into account the statutory provisions relating to crossings, intersections and neighborhood cable voltages and
different services.
The circuit will consist of sight running cables XVH1, fixed to walls or ceilings by clamps, threaded tubes installed in PVC
perforated plastic gutters.
The cables that constitute the distribution channels, will be protected in the HP by electromagnetic circuit breakers
GENERAL ELECTRIC PANEL
The framework will be industrial type, equipped with door for surface mounting, cabinet construction, containing
cutting equipment and circuit protection, switches, circuit breakers and switchgear signaling, and binding measure.
The framework should be electrified and fitted as unifilar respective scheme.
The bus bars generally will comprise copper-section sized to meet the current carrying capacity of 2 A/mm2, applied on supports
of insulating material. The input circuit will be equipped with:
 a main switch of tetrapolar omnipolar;
 a set of dischargers voltages on class B;
 a relay fault voltage (phase sequence);
The power circuits for different electromechanical equipment will be equipped with:
 switch tetrapolar general differential;
 breaker engine;
 contactor;
 respective commands on the touch panel from Siemens;
The starter motor should be straightforward to 5.5 kW.
The signaling and control circuits are fitted with circuit breakers. One of these circuits will have a single-phase transformer
230/24 V AC and another power source with 230/24 V DC.

7.2 AUTOMATION AND CONTROL
Will use a system (SIEMENS) automation with touch monitor for visualization and control of processes and equipment
installation, as the examples presented below:
Figure 9 e 10 Images of touch monitor.
7.3 HIERARCHY OF COMMAND OPERATION
The chain of command working in any facility is of utmost importance. In the case of this installation is intended that the hierarchy
for controlling the operation on the following principles:
 Automation
 Manual Command
This chain of command has the principle, that it is always up to the operator or responsible for installing decide the mode of
operation of equipment. The way this is achieved is simple, ie, for each device exists on the touch panel, that feeds it, a
specifique command menu.
In the AUTO position of the equipment is controlled according to the automatic provided. (being able to change its operating
parameter).
7.4 ALARMS
At installation the alarm indication will be made as follows:
 Indication of each individual alarm panel process.
 Acoustic Signalling general alarm
 General alarm signaling devices
There will be an audible alarm and flashing general that should be played by the cabinet.
In the table there will be a push button electric to recognize and cancel the alarm. The alarm is always active in red until
acknowledged.

9 ANNEX 1 - PROCESS DESIGN CRITERIA AND DESIGN CALCULATIONS
9.1 LIQUID PHASE
9.1.1 WASTE WATER LIFTING STATION
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Pumping well and lifting station
DB Peak Flow m3/h 33,33 83,33 141,67 250,00 333,33
CD Minimum residence time min 15,00 15,00 15,00 15,00 15,00
PD Minimum useful volume m3 8,33 20,83 35,42 62,50 83,33
D Amount of pumps un 2 --- --- --- ---
D Unitary pump flow rate % 100,00 --- -- --- ---
D Head elevation m 10
9.1.2 THICK AND THIN SCREENING AND SAND SEPARATION
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Thin and thick screen
DB Peak Flow m3/h 33,33 83,33 141,67 250,00 333,33
DC Number of main channel un 1 2 2 2 2
DC Flow rate per channel % 100 50 50 50 50
CD/D Mesh type of thick screen
bars
CD/D Mesh size of thick screen mm To protect the thin screen
10
CD/D Mesh type of thin screen
hole
CD/D Mesh size of thin screen mm
Minimum of 3 mm to protect
membranes
3
9.1.3 EQUALIZATION
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Volumes and residence time
DB Daily medium flow rate m3/day 400,00 1000,00 1700,00 3000,00 4000,00
DB Daily medium flow rate (24h) m3/h 16,67 41,67 70,83 125,00 166,67
DB Peak Flow m3/h 33,33 83,33 141,67 250,00 333,33
DB
Real filtration flow for membrane design
flux
m3/h 23,56 47,13 78,54 125,67 188,50
DB Excess volume to buffer m3/h 9,77 36,21 63,13 124,33 144,83
D Number of parallel tanks un 2,00 2,00 2,00 2,00 2,00
D Length m 4,500 9,800 10,300 11,400 14,600
D With m 4,400 5,000 7,700 7,700 7,700
D Water level m 2,500 2,500 2,500 4,000 4,000
D Effective water level m Less 500 mm 2,000 2,000 2,000 3,500 3,500

D Effective real volume per tank m3 39,600 98,000 158,620 307,230 393,470
D Useful real volume per tank m3 49,500 122,500 198,275 351,120 449,680
D Retention time h 5,940 5,880 5,598 5,618 5,396
D
Buffering capacity in terms of h of peak
flow rate
h 4,05 2,71 2,51 2,47 2,72
Deginet
Kara Kore
1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Aeration of equalization tank
D Type Fine bubble diffusers
Minimum flow rate
CD Ratio of air per area Sm3/h/m2 1,5-2 1,50
CD Ratio of air per area Sm3/h/m3 0,6-1 0,60
PD Flow rate resulted from ratio area Sm3/h 59,40 147,00 237,93 263,34 337,26
PD Flow rate resulted from volume ratio Sm3/h 59,40 147,00 237,93 421,34 539,62
Diffusers
DB Diffusers model
PIK 300
DB Unitary minimum flow rate Sm3/h 20ºC, 1 atm 2,5
DB Unitary maximum flow rate Sm3/h 20ºC, 1 atm 8
D Unitary design flow rate Sm3/h 20ºC, 1 atm 2,7 3,7 3,3 3,7 2,7
D Number of diffusers un 24 48 84 120 144
Blower
DB Quantity of blowers for equalization un 1,00 1,00 1,00 1,00 1,00
DB Unitary design flow rate
Sm3/h 20ºC, 1 atm 60,00 147,36 257,88 422,40 540,00
Nm3/h 0ºC, 1 atm 55,91 137,31 240,29 393,58 503,16
D Blower real flow rate Nm3/h
0ºC, 1 atm; related to the
specifications of the selected
blower
61,00 155,00 256,00 449,00 540,00
PD/D Total head loss mbar 350,00 350,00 350,00 500,00 500,00
Hydrostatic pressure mbar 250,00 250,00 250,00 400,00 400,00
Head loss in diffusers mbar 50,00 50,00 50,00 50,00 50,00
Head loss in pipe mbar 30,00 30,00 30,00 30,00 30,00
Head loss in valves mbar 20,00 20,00 20,00 20,00 20,00
9.1.4 BIOLOGICAL TREATMENT AND SOLID LIQUID SEPARATION BY MICROFILTRATION
MEMBRANES (MEMBRANE BIOREATOR MBR)
9.1.5 MEMBRANES AND FILTRATION DESIGN
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
SMU (Submerged membrane units)
DB Inlet flow rate to biological tanks m3/day 400,00 1000,00 1700,00 3000,00 4000,00
DB Design temperature ºC
15,00
CD Design flux
m3/
(m2.day)
Depends on temperature
0,65
D SMU model
RM200 RW400
RW400

D Type of membrane
flat
D Membrane material
chlorinated polyethylene
D Porosity micros
0,40
D Membrane effective surface area
m2/cartri
dge
1,45
D Nº of membrane cartridge per unit un
200,00
400,00
D Number of SMUs un 3,00 6,00 10,00 8,00 12,00
D Number of cartridge un 600,00 1.200,00 2.000,00 3.200,00 4.800,00
D Module area m2 290,00 580
D Total area m2 870 1.740,00 2.900,00 4.640,00 6.960,00
D Real flux for average inlet flow m3/(m2/day) 0,460 0,575 0,586 0,647 0,575
D
Real Flow rate for design flux
m3/day 565,50 1.131,00 1.885,00 3.016,00 4.524,00
D m3/h 23,56 47,13 78,54 125,67 188,50
DB Maximum allowed flux
m3/(m2/d
ay)
just four hours per day
1,30
D
Flow rate for maximum flux
m3/day 659,75 1319,5 2199,17 3518,67 5278
D m3/h 47,13 94,25 157,08 251,33 377,00
DC Maximum transmembrane pressure mbar 500
D Number of SMUs per line SMU/ line Maximum of 10 3,00 3,00 5,00 4,00 6,00
DB Number of lines un 1,00 2,00 2,00 2,00 2,00
Calculation of suction pipes and
pump
DB Filtration time h 21,00 21,00 21,00 21,00 21,00
DB Quantity of modules per line un 3,00 3,00 5,00 4,00 6,00
DB Quantity of permeate main pipe per line un 1,00 1,00 1,00 2,00 2,00
DB Number of the permeate piping to the
permeate header
un 3,00 3,00 5,00 2,00 3,00
PD Flow rate per line instantaneous m3/h 19,05 23,81 40,48 71,43 95,24
PD Flow rate per permeate main pipe
instantaneous
m3/h 19,05 23,81 40,48 35,71 47,62
9.1.6 TANKS AND RECIRCULATION DESIGN
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
BOD5 removal in the preliminary
treatment
DB Inlet BOD5 kg/day 120,00 300,00 510,00 900,00 1200,00
CD
BOD5 removal in preliminary treatment
% 10 10 10 10 10
DB
kgDBO5/
day
12 30 51 90 120
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
MBR Tank
CD Notes:
The dimensions are done tight
for the installation of
membranes

D Number of tanks un 1,00 2,00 2,00 2,00 2,00
D Internal with tank m 4,300 4,300 4,300 4,300 4,300
D Internal length tank m 3,500 4,600 6,800 5,700 7,900
D Water level m 3,800 3,800 3,800 5,300 5,300
D Useful volume per tank m3 57 75 111 130 180
D Total useful volume m3 57 150 222 260 360
D
Retention time
days 0,14 0,15 0,13 0,09 0,09
D h 3,43 3,61 3,14 2,08 2,16
BOD removal in MBR tank
DB Total useful volume m3 57,19 150,328 222,224 259,806 360,082
CD SST concentration in MBR tank mgSST /l 12000
CD Food to microorganism
kgCBO5
/kgSS
/day
0,1
D Volumetric organic load
kgCBO5
/m3 /day
1,20
D CBO elimination
kgCBO/d
ay
68,63 180,39 266,67 311,77 432,10
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Pre-aeration tank
Volumetric
DB
BOD5 removal need in the pre-aeration
tank
kg/day 39,372 89,606 192,331 498,233 647,902
CD
Recirculation Factor between MBR and
pre-aeration tank
R 3
D SSTs concentration mgSST/l 9000,000 9000,000 9000,000 9000,000 9000,000
DB Food to microorganism
kgCBO5
/kgSS
/day
0,100 0,100 0,100 0,100 0,100
DB Volumetric load
kgDBO5/
m3/day
0,900 0,900 0,900 0,900 0,900
PD Minimum volume m3 43,747 99,563 213,701 553,592 719,891
PD
Minimum hydraulic retention
day 0,109 0,100 0,126 0,185 0,180
PD h 2,625 2,390 3,017 4,429 4,319
D Real retention tank h 3,591 4,363 4,159 5,027 5,024
D Number of parallel tanks un 1,000 2,000 2,000 2,000 2,000
PD Minimum volume per tank m3 43,747 49,781 106,851 276,796 359,945
D Real volume per tank m3 59,850 90,896 147,288 314,184 418,700
PD Real area per tank m2 11,512 26,201 56,237 104,451 135,828
D Real with per tank m 3,500 4,600 6,800 5,700 7,900
PD Minimum length per tank m 3,289 2,848 4,135 9,162 8,597
D Real length per tank m 4,500 5,200 5,700 10,400 10,000
D Water level m 3,800 3,800 3,800 5,300 5,300

9.1.7 ACTUAL OXYGEN REQUIREMENTS (AOR)
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Actual oxygen requirement (AOR)
AOR for DBO oxidation
PD Total KgO2/day 54,000 135,000 229,500 405,000 540,000
CD Substrate respiration rate kgO2/kgCBO5 0,5 0,5 0,5 0,5 0,5
DB
Variation in BOD5 load on
the MBR volume
kgCBO/day 68,628 180,3936 266,6688 311,7672 432,0984
PD AOR in MBR tank KgO2/day 34,314 90,197 133,334 155,884 216,049
DB CBO5 load in pre-aeration kg/day 39,372 89,6064 192,3312 498,2328 647,9016
PD AOR in pre areation tank KgO2/day 19,686 44,803 96,166 249,116 323,951
AOR for endogenous respiration
PD Total kgCBO/day 91,800 229,500 390,150 688,500 918,000
CD SSV/SST ratio % 85,000 85,000 85,000 85,000 85,000
CD
Endogenous respiration
Ratio
kgO2/kgVSS 0,100 0,100 0,100 0,100 0,100
DB Total MBR usefful volume m3 57,19 150,328 222,224 259,806 360,082
DB
SST concentration in MBR
tank
mgSST /l 12000 12000 12000 12000 12000
CD MLVSS concentration mg/l
10200,00
0
10200,00
0
10200,00
0
10200,00
0
10200,00
0
PD MBR AOR KgO2/day 58,334 153,335 226,668 265,002 367,284
DB
Minimum pre-aeration
volume
m3
43,74666
667
99,56266
667
213,7013
333
553,592
719,8906
667
DB MLSST concentration mgSST/l 9000 9000 9000 9000 9000
PD MLVSS concentration mg/l 7650,000 7650,000 7650,000 7650,000 7650,000
PD Pre-aeration AOR KgO2/d 33,466 76,165 163,482 423,498 550,716
AOR for nitrification Preventive action
D Total KgO2/day 51,855 129,637 220,383 388,911 518,548
CD Nitrification % 81,7 81,7 81,7 81,7 81,7
DB Variation of load NH4 kg/day 11,343 28,358 48,209 85,074 113,432
CD
Coefficient for the stoichiometric
oxidation of ammoniac nitrogen
kgO2/kgNH4-N 64/14 4,571 4,571 4,571 4,571 4,571
PD AOR for nitrification KgO2/day 51,855 129,637 220,383 388,911 518,548
TOTAL AOR
PD Total kgO2/day 197,655 494,137 840,033 1482,411 1976,548

9.1.8 MBR AERATION SYSTEM
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Airflows for Standard and Normal
Conditions
DB
Air volume of one membrane cartridge
min
Nl/min/cartridge Normal, 0ºC e 1 atm 10,000
7,000
DB
max
Nl/min/cartridge Normal, 0ºC e 1 atm
15,000 10,000
CD
of project
Nl/min/cartridge Normal, 0ºC e 1 atm
10,000 7,000
DB number of membrane cartridge per unit pcs/module
200,000 400,000
DB Number of diffusers case module 3,000 8,000 12,000 10,000 14,000
PD Minimum air supply per SMU Nl/min/module Normal, 0ºC e 1 atm
2000,000 2800,000
PD Maximum air supply per SMU Nl/min/module Normal, 0ºC e 1 atm
3000,000 4000,000
PD Design air supply per SMU Nl/min/module Normal, 0ºC e 1 atm
2000,000 2800,000
PD Minimum total air supply Nm3/h Normal, 0ºC e 1 atm 360,000 960,000 1440,000 1680,000 2352,000
PD Maximum total air supply Nm3/h Normal, 0ºC e 1 atm 540,000 1440,000 2160,000 2400,000 3360,000
PD Total design air supply Nm3/h Normal, 0ºC e 1 atm 360,000 960,000 1440,000 1680,000 2352,000
PD Total design air supply Sm3/h
Standard 20ºC 1013
mbar
386,359 1030,291 1545,437 1803,009 2524,213
MBR Blower
DB Quantity of blowers un 1,000 2,000 2,000 2,000 2,000
PD Unitary design flow rate Nm3/h 0 ºC 1013 mbar 386,359 515,146 772,718 901,505 1262,107
D Real blower flow rate Nm3/h 0 ºC 1013 mbar 394,000 524,000 812,000 913,000 1297,000
D ∆P Total head loss mbar 440,000 440,000 440,000 590,000 590,000
D Hydrostatic pressure mbar Water level 380,000 380,000 380,000 530,000 530,000
D head loss in diffusers mbar 20,000 20,000 20,000 20,000 20,000
D Head loss in pipe mbar 40,000 40,000 40,000 40,000 40,000
D head loss in valves mbar 0,000 0,000 0,000 0,000 0,000
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Standard Oxygen Transfer Rate
(SOTR)
20ºC and 1013 mbar
CD
Alpha coefficient α
admi 0,60
CD Beta coefficient β admi
0,97
CD Temperature correction factor θ adim
1,024
DB Altitude m 2.304 2.384 2.222 2.185 2.103
DB Depth of the tank m 3,8 3,8 3,8 5,3 5,3
DB Submergence of diffusers m 3,5 3,5 3,5 5,0 5,0
D Overall efficiency factor AOTR/SOTR 0,30 0,30 0,31 0,32 0,32
D Standard efficiency transfer % 5,25 5,25 5,25 7,5 7,5

CD O2 transfer efficiency in
clean water
%/m 1,5 1,5 1,5 1,5 1,5
D Efficiency field transfer % 1,59 1,57 1,62 2,37 2,40
D
Standard volume of O2 contributed by
membranes (SOTR)
Kg/h 20ºC, 1013 mbar 107,0 285,4 428,1 499,4 699,2
D
O2 volume (AOTR) provided by
membrane modules
kg/day 40,96 107,72 166,14 283,51 402,39
9.1.9 ADICIONAL AERATION SYSTEM
Deginet Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
AOR needed in additional aeration
system
DB Total AOR KgO2/day 197,65 494,14 840,03 1.482,41 1.976,55
DB MBR AOR by MBR kg O2/day 40,96 107,72 166,14 283,51 402,39
DB MBR adicional aeration system KgO2/day 156,70 386,42 673,89 1.198,90 1.574,16
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Additional aeration system SOTR
PD
Overall efficiency factor
The design parameters are the
same as MBR less alpha factor
0,23 0,23 0,23 0,24 0,24
CD
Alpha coefficient admi 0,45 0,45 0,45 0,45 0,45
PD Oxygen transfer efficiency % 24,50 24,50 24,50 35,00 35,00
CD
O2 transfer efficiency in clean water %/m Related to the diffuser system 7,00 7,00 7,00 7,00 7,00
DB Depth of diffusers m 3,5 3,5 3,5 5,0 5,0
PD Field transfer Efficiency % 5,67 5,59 5,75 8,41 8,53
PD
Additional aeration system SOTR
KgO2/da
y
2.763,29 6.908,87 11.717,81 14.253,11 18.459,69
PD
Air must be supplied by diffusers
Sm3/day 9.975,79 24.941,77 42.302,56 51.455,26 66.641,47
PD Sm3/h 415,66 1.039,24 1.762,61 2.143,97 2.776,73
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Diffusers
CD Diffuser model 0 PIK 300
DB Unitary minimum flow rate Sm3/h 20ºC, 1 atm 2,5
DB Unitary maximum flow rate Sm3/h 8
PD Unitary design flow rate Sm3/h 6,6 6,5 6,1 6 5,8
PD
Number of units required based on the
required flow
un 62,98 159,88 288,95 357,33 478,75
D Number of real units un 63,00 160,00 288,00 360,00 480,00
PD Total minimum flow rate Sm3/h 20ºC, 1 atm 157,45 399,71 722,38 893,32 1196,87
PD Total maximum flow rate Sm3/h 20ºC, 1 atm 503,83 1279,07 2311,62 2858,63 3829,97
PD Design flow rate Sm3/h 20ºC, 1 atm 415,66 1039,24 1762,61 2143,97 2776,73

Deginet Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Blower
DB Quantity of blowers un 0 1,00 2,00 2,00 2,00 2,00
DB
Unitary design flow rate
Sm3/h 20ºC, 1 atm 415,66 519,62 881,30 1071,98 1388,36
DB Nm3/h 0ºC, 1 atm
387,30 484,17 821,18 998,85 1293,64
D Real blower flow rate Nm3/h
Wither converter correspond on
the maximum point
453,6 590,4 899,4 1661 1472,4
D Total head loss mbar 480,00 480,00 480,00 630,00 630,00
D Hydrostatic pressure mbar Water level 380,00 380,00 380,00 530,00 530,00
D Head loss in diffusers mbar 50,00 50,00 50,00 50,00 50,00
D Head loss in pipe mbar 30,00 30,00 30,00 30,00 30,00
D Head loss in valves mbar 20,00 20,00 20,00 20,00 20,00
9.1.10 MBR CLEANING IN PLACE
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
MBR CLEANING IN PLACE
DB Number of cartridge per module 200,000 400,000
DB Number of modules 3,000 8,000 12,000 10,000 14,000
DB Number of lines 1,000 2,000 2,000 2,000 2,000
DB Permeate head piper per line 1,000 1,000 1,000 2,000 2,000
CD Ratio of solution per cartridge l/cartridge 4,5
D Solution cleaning volume per SMU l 900,000 900,000 900,000 1800,000 1800,000
D Total volume solution per line l 2700 3600 5400 9000 12600
D
Solution volume per permeate
head pipe
l 2700 3600 5400 4500 6300
CD Chemical product sodium hypochlorite
DB
Chemical concentration in terms of
active compound
% (m/V)
15,00
CD
Solution concentration in terms of
active compound
%
0,50
D
Active compound amount to add to
the given volume of water
kg 13,50 18,00 27,00 45,00 63,00
D
Quantity of pure solutions to add to
The volume of water
l 90,00 120,00 180,00 300,00 420,00
CD Injection time min 10 - 15 10,00 12,00 10,00 12,00 10,00
D Injection flow rate m3/h 16,20 18,00 32,40 22,50 37,80
CD Estimated Operation frequency times/year 2,00 2,00 2,00 2,00 2,00
9.1.11 GLOBAL PARAMETERS OF THE BIOLOGICAL TREATMENT
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
Resulted parameters of the
Biological treatment
PD Minimum resulted aerobic volume m3 100,937 249,891 435,925 813,398 1079,973
PD Minimum resulted aerobic
residence time
h 6,056 5,997 6,154 6,507 6,480
PD Global food to microorganisms kgBOD /kg-VSS/d 0,118 0,118 0,118 0,118 0,118

PD kgBOD /kg-MLSS/d 0,100 0,100 0,100 0,100 0,100
PD Minimum resulted sludge age day 12,00 12,00 12,00 12,00 12,00
9.2 SOLID PHASE
9.2.1 DEWATERING
Excess sludge produced as dry
residue
Deginet
Kara
Kore 1
Mekenisa
Kotari
Bole
Bulubla
Kilinito
DB
Effluent flow rate
m3/h 16,67 41,67 70,83 125,00 166,67
DB m3/day 400,00 1000,00 1700,00 3000,00 4000,00
DB
DBO load
mg/l 300,00 300,00 300,00 300,00 300,00
DB Kg/h 5,00 12,50 21,25 37,50 50,00
DB Kg/day 120,00 300,00 510,00 900,00 1200,00
CD Specific production of dried sludge KgMS/KgCBO 0,75 0,75 0,75 0,75 0,75
D
Dried sludge production
KgMS/h 3,75 9,38 15,94 28,13 37,50
D KgMS/day 90,00 225,00 382,50 675,00 900,00
Excess sludge to be extract on
biological reactor
CD Concentration of sludge to be
drawn from MBR tank
Kg/m3 15,00 15,00 15,00 15,00 15,00
CD % 1,50 1,50 1,50 1,50 1,50
D Flow rate of sludge to be drawn
from MBR tank
m3/h 0,25 0,63 1,06 1,88 2,50
D m3/day 6,00 15,00 25,50 45,00 60,00
Excess sludge produced in the
dewatering system
CD
Solid Capture rate in dewatering
system
% 95,00 95,00 95,00 95,00 95,00
CD
Concentration of dewatered water
Kg/m3 200,00 200,00 200,00 200,00 200,00
CD % 20,00 20,00 20,00 20,00 20,00
D
Dried sludge production
m3/h 0,02 0,04 0,08 0,13 0,18
D m3/day 0,43 1,07 1,82 3,21 4,28
D Kg/h 17,81 44,53 75,70 133,59 178,13
D Kg/day 427,50 1068,75 1816,88 3206,25 4275,00

ANNEX 2 – EQUIPAMENT LIST OF MEKANISA KOTARI

Cod. Name Main characteristics Notes UN. Quantity Installed
power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
LIQUID PHASE
PRELIMINARY AND PRE-TRETMENT
RECEPTION AND EFLUENTE DISTRIBUTION
Convergence box and flow distribution concrete un 1 0 0 1 0
SOLIDS SREENING AND SAND
SEPARATION
Thick screening
STK. L. Ch.1.1/2 Grid channel concrete Manual clean by operator un 2 0 0 2 0 0
STK.L.Sc.1.1/2 Manual Thick screen S.S AISI 304, 50 mm bars for solids retention un 2 0 0 2 0 0
STK.L.Bx.1.1/2 Thick screen waste box reception S.S AISI 304 un 2 0 0 2 0 0
D. S C. 1.c thin solids container PP, 160 l un 1 0 0 1 0 0
Sieve and separator Sands
STD.S.Bx.1.c Thin screening and dessandig unit box concrete un 1 0 0 1 0 0
STD.L.E.1.1/2 Thin screening and dessandig equipment Screw type; 3 mm; FLUITECO / WAU2-30; 108 m3/h
maximum Flow rate: 30 l / s (1); Inlet/outlet DN200
Attached documentation
Fluiteco_WAU_ScreenGrit [CTI]
Fluiteco_WAU2-30_ScreenGrit [DSI]
Controlled from the general
automaton
Works by signal of level sensor
and timer
un 2 0 0 2 0,92 1,84
Screen Cleaning system un 2 0 0 2 0 0
STD.L.VS.1.1/2 Clean Water supply solenoid valve 1" un 2 0 0 2 0 0
Clean water pipe and fittings SS AISI 304 1" set 2 0 0 0 0 0
STD.L.VBF.1.1/2 Inlet cut offvalve of the unit Butterfly; DN200_ allow put out service the unit un 2 0 0 2 0 0
STD.L.VBF.2.1/2 Outlet cut offvalve of the unit Butterfly; DN200_ allow put out service the unit un 2 0 0 2 0 0
STD.L.LS.1.12 Level Sensor indicates the level of start-up un 2 0 0 2 0 0
ST.S.C.1.1/2 Solids thin screen container PP, 160 l un 2 0 0 2 0 0

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
D.S.C.1.1/ 2 Sand container PP, 160 l un 2 0 0 2 0 0
EQUALIZATION / HOMOGENEIZATION AND BIOLOGICAL TREATMENT FEEDING
Tanks
EQ.L.Bx.1.c Flow distribution box concrete Allow the convergence of the
effluent from the thin and
dessandig equipment and
distribute for both equalization
tanks.
In case of maintenance (once per
six years) the inlet flow could be
stop by installing a blind flange in
the feeding pipe of the tank in
maintenance.
un 1 0 0 1 0 0
EQ.L.TK.1.1/2 Equalization tank concrete
Unitary Utile dimensions (W x L x H) (m): 10,3 x 7,7 x 3
Water level (m):2,5
Unitary Useful volume (m3): 198,275
Design flow rate per line (m3/day): 850
Residence time (h) : 5,60
un 2 0 0 2 0 0
Aeration and agitation system for
equalization
EQ.G.BL.1.c Blower for equalization tank Roots type; Kaeser BB89C, DN65, 7,5 kW, 400 V, 50 Hz,
fixed speed , for:
PP : 360 m3/h; 256 Nm3/h; 350 mbar; 4530 rpm; 5,00
kW; 2222 m
Kaeser_ BB – HB_blower [CT]
Kaeser_BB89C 7,5 kW [DS]
Kaeser [GER-CG-ISO 9001 Certificate]
un 1 0 0 1 7,5 7,5
Soundproofing included in blower un 1 0 0 1 0
EQ.G.TS.1.c Temperature Sensor included in blower un 1 0 0 1 0
Flexible sleeve included in blower un 1 0 0 1 0

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
Air filter included in blower un 1 0 0 1 0
filter pressure indicator included in blower un 1 0 0 1 0
EQ.G.VSP.1.c Pressure relief valve included in blower un 1 0 0 1 0
EQ.G.PI.1.c Blower pressure indicator included in blower un 1 0 0 1 0
EQ.G.VR.1.c Retention valve included in blower un 1 0 0 1 0
Feed head pipe to aeration system T SS AISI 304; DN65 to DN80 For total flow rate: 20 m/s 9
mbar For half flow rate 9 m/s 2 mbar until the WL
set 2 0 0 2 0 0
Piping supply to each set of diffusers (vertical
pipe)
PVC 3" D 90 For total flow rate: 20 m/s 9 mbar For half
flow rate 9 m/s 2 mbar
set 2 0 0 2 0
Porous diffusers network ABS / PIK 300, for 1,5 - 8 S m3/h
42 diffuser per set;
ABS Nopon_ DDS 041212 [Declaration of EC directives
validity]
ABS Nopon_ PIK 300 [Curves]
ABS Nopon_PIK 300 [specification]
ABS Nopon_PIK300 [CT.I]
set 2 0 0 0
EQ.G.FD.1.1/2 Fine porous diffusers un 84 0 0 84 0
Fixing brackets
Piping diffusers network
Accessories diffusers network
EQ.G.CD.1.1/2 Piece of condensates discharge
Condensates routing piping set 2 0 0 2 0
EQ.G.VB.3.1 Condensate purge valve ball , manual activated manually once a week un 2 0 0 2 0
EQ.G.VB.4.1 Valve /or other instrument for cleaning
diffusers
un 2 0 0 2 0
Feed to the biological treatment

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
Biological Treatment feed pump Suction pipe
and fittings
SS 304 3" DN80 (88,9x2) 2m/s set 2 0 0 2 0
BF.L.PC.1.1/2 Biological Treatment feed pump Centrifugal self-priming , Varisco, JE3-210G10ET40 4
kW; 3x400 V, 50 Hz, 1500 rpm for 40 m3/h 13 Hm NPSH 3
Hm
Varisco_J pump [CT I]
Varisco_J 3-210 G [Curve]
Varisco_J P-JE 3-210 ET0 [DIM]
automaton
Works by level sensor on
equalization tank
un 2 0 1 3 4 8
Pipe and fittings from biological feed pump to
tank
SS 304 3" DN80 (88,9x2) 2m/s set 2 0 0 2 0
BF.L.Vb.1.1/2 Sampling valve un 2 0 0 2 0
BF.L.PI.1.1/2 Pressure indicator range 0 a 25 bar un 2 0 0 2 0
BF.L.Vb.2.1/2 Sampling valve for pressure indicator un 2 0 0 2 0
BF.L.VR.1.1/2 pump retention valve included in pump un 2 0 0 2 0
BF.L.VBF.2.1/2 discharge pump cut offvalve butterfly un 2 0 0 2 0
BF.L.F.1.1/2 SS filter, to protect the MBR membranes SS. AISI 304 10 mm perforated holes Manual cleaning by operator, once
a week
un 2 0 0 2 0
BF.L.FM.1.1/2 Flow meter Electromagnetic; Siemens/ Sensor MAG 5100W +
Transmissor MAG 5000; 3" DN80 ; 2 m/s
Siemens_MAG5000 6000_trasmissor [CT]
Siemens_MAG5100W_sensor [CT]
With digital and analogue output
(4-20 mA)
un 2 0 0 2 0
EQ.L.LS.1.1/2 Level Sensors Indication of start, stop and alarm set 2 0 0 2 0

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
SECONDARY AND TERTIARY TREAMENT
AEROBIC BIOLOGICAL TREATMENT WITH SOLID-LIQUID SEPARATION BY MBR
Tanks
MBR.L.TK.1.1/2 MBR Biological Tank Material: Concrete
Internal dimensions (W x L x Wl) (m): 4,3 x 6,8 x 4,3
Water level (m): 3,8
Useful unitary volume (m3): 111
Caudal de project per line (m3/day): 850
Residence time (h): 3,14
un 2 0 0 2 0
PA.L.TK.1.1/2 Pre-aeration tank Material: Concrete
Useful unitary Volume (m3): 147,3
Flow rate per line per line (m3/day): 850
un 2 0 0 2 0 0
overflow pipe between MBR tank and
preareation tank
Membranes 0 0
MBR.L.SMU.1.1/ Membranes units Flat submerged membranes units (SMU), Kubota/ RM200,
290 m2 per unit, 120 Nm3/h of air per unit, for 0,586 m/day
Kubota [ISO14001 certificate_EN_2015]
Kubota [ISO9001 certificate_EN_2015]
Kubota_RM200 [Dim]
Kubota_ SMU [General Information]
Maintenance cleaning once or
twice a year, without take out the
modules neither empty the tank
un 10 0 0 10 0
MBR.G.DC.1.1/2 Extra diffuser case un 2 0 0 2 0
Installation and extraction membranes
units system
Lifting tool 75 un 1 0 0 1 0

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
Guide pipe
Stabilization pipe
Lifting chain
Chemical anchors and stars to fix the modules
to the ground
Stars to fix the modules to the walls
Fixing bar of the modules to the wall
Effluent Recirculation
Suction pipe and fittings of the recirculation
pump
S.S. AISI 304 4" DN100 (114,3x2) ; 3,22 m/s set 2 0 0 0 0
R.L.VBF.1.1/2 Suction cut offvalve R 4" un 2 0 0 0 0
R.L.PC.1.1/2 Recirculation pump Centrifugal self-priming , Varisco, JE4-220G10FT40 5,5
kW; 3x400 V, 50 Hz, 1450 rpm for 110 m3/h 9 Hm NPSH
3,5 Hm
Varisco_J 4-220 G [Curve].
automaton
Works continuously or by timer
un 2 0 1 3 5,5 11
discharge pipe and fittings to the tank set 2 0 0 2 0 0
R.L.Vb.1. Effluent sampling valve un 2 0 0 2 0 0
R.L.Vb.2. Sampling valve of the pressure gauge un 2 0 0 2 0 0
R.L.PI.1.1/2 Pressure gauge un 2 0 0 2 0 0
R.L.VR.1.1/2 Retention valve included in pump un 2 0 0 0 0 0
R.L.VBL2.1/2 discharge cut offvalve butterfly 4" un 2 0 0 0 0 0
Suction Filtration
Interconnecting piping of the main pipe to the
head pipe
Pipe PVC 2 1/2" D75 0,57 m/s set 10 0 0 10 0 0
Permeate header pipe S.S.AISI 304 8" DN200 ; 0,31 m/s
with fittings of 2 1/2" DN65
un 2 0 0 2 0 0

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
MBR.L.VB.2.1/2 Pressure relief valve of the permeate collector butterfly DN50 un 2 0 0 2 0 0
Gravity injection tool DN100 with blind flange un 0 0 2 2 0 2
MBR.L.VB.3.1/2 Filtration pump suction cut offvalve Butterfly, 3" un 2 0 0 2 0 0
MBR.L.PT.1.1/2 Pressure transmitter to estimate the transmembrane
pressure and protect the MBR
un 2 0 0 2 0 0
MBR.L.PC.1.1/2 Filtration pump Centrifugal self-priming , Varisco, JE3-210G10ET40 4
kW; 3x400 V, 50 Hz, 1450 rpm for 40 m3/h 13 Hm NPSH 3
Hm
Varisco_J 3-210 G [Curve].
automaton
Works by level sensor
Is protected by the alarm of the
pressure transmitter
un 2 0 1 3 4 8
piping and fittings to the flow meter SS 304 3" DN80 (88,9x2) ; 1,96 m/s set 2 0 0 2 0
MBR.L.FM.1.1/2 Electromagnetic flow meter Electromagnetic; Siemens/ Sensor MAG 5100W +
transmitter MAG 5000; 3" DN80 ; 1,96 m/s
Siemens_MAG5000 6000_trasmissor [CT]
Siemens_MAG5100W_sensor [CT]
un 2 0 0 2 0
MBR.L.V.4.1/2 Flow control valve Knife valve un 0 0
Piping from flow meter to permeate tank set 2 0 0 2 0
MBR.L.V.5.1/2 cut offvalve to feed permeate tank un 2 0 0 2 0 0
MBR.L.LS.1.1/2 Level sensor floater un 2 0 0 2 0
Membranes modules aeration system 0 0

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
MBR.G.BL.1.1/2 Blower for SMU Roots type; Kaeser DB236C , DN100, 22 kW, 400 V, 50
Hz, fixed speed , for:
PM: 1141 m3/h (812 Nm3/h); 450 mbar; 4000 rpm; 18,4
kW, 2222 m, 60 %RH, 20ºC
Kaeser_DB236C 22 kW [DS]
automaton
un 2 0 0 2 22 44
Soundproofing included in blower un 2 0 0 2 0 0
MBR.G.TS.1.1/2 Temperature Sensor included in blower un 2 0 0 2 0 0
Flexible sleeve included in blower un 2 0 0 2 0 0
Air filter included in blower un 2 0 0 2 0 0
MBR.G.PI.1.1/2 filter pressure indicator included in blower un 2 0 0 2 0 0
MBR.G.VSP.1.1/2 Pressure relief valve included in blower un 2 0 0 2 0 0
MBR.G.PI.1.1/2 Blower pressure indicator included in blower un 2 0 0 2 0 0
MBR.G.VR.1.1/2 Retention valve included in blower un 2 0 0 2 0 0
feed main pipe to aeration system Pipe stainless steel 304 8" DN200 () 1 mbar 7 m/s set 2 0 0 2 0 0
Vertical pipeline inlet and outlet Pipe stainless steel 3" DN 80 1 mbar 7 m/s
Pipe PVC 3" D 90 1 mbar 7 m/s
MBR.G.VB.3.1/2 Condensates purge valve Butterfly automatic DN100 Controlled from the general
automaton
Works by time
un 2 0 0 0 0 0
Agitation and aeration system of the pre
aeration zone

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
PA.G.BL.1.1/2 Blower for pré- aeration Roots type; Kaeser DB236C V, DN100, 30 kW, 400 V, 50
Hz,driven by a VDF, for:
PM : 1265,4 m3/h (899 ,4 Nm3/h), 480 mbar, 4400 rpm,
21,6 kWh, 2222 m, 60%RH, 20ºC
Kaeser_DB236C V 30 kW [DS]
automaton
Works by the read of the oxygen
sensor, with variation on seep
un 2 0 0 2 30 60
Soundproofing included in blower un 2 0 0 2 0 0
PA.G.TS.1.1/2 Temperature Sensor included in blower un 2 0 0 2 0 0
Flexible sleeve included in blower un 2 0 0 2 0 0
Air filter included in blower un 2 0 0 2 0 0
PA.G.PI.1.1/2 filter pressure indicator included in blower un 2 0 0 2 0 0
PA.G.VSP.1.1/2 Pressure relief valve included in blower un 2 0 0 2 0 0
PA.G.PI.1.1/2 Blower pressure indicator included in blower un 2 0 0 2 0 0
PA.G.VR.1.1/2 Retention valve included in blower un 2 0 0 2 0 0
feed main pipe to aeration system S.S. AISI 304 6" DN150 (14 m/s 4 mbar) set 2 0 0 0 0 0
Piping supply to each set of diffusers (vertical
pipe)
S.S. AISI 304 4" DN100 (16 m/s ,7 mbar) 0 0
Porous diffusers network ABS / PIK 300, for 1,5 - 8 Sm3/h
144 diffuser per set; SOTE 25%
ABS Nopon_ DDS 041212 [Declaration of EC directives
validity]
ABS Nopon_ PIK 300 [Curves]
ABS Nopon_PIK 300 [specification]
ABS Nopon_PIK300 [CT.I]
maintenance cleaning once a
year, without remove the diffusers
neither empty the tank
set 2 0 0 0 0 0
PA.G.DF.1. Fine porous diffusers

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
Fixing brackets
Piping diffusers network
Accessories diffusers network
PA.G.CD.1. Piece of condensates discharge
Condensates routing piping
PA.G. Condensate purge valve un 4 0 0 4 0 0
PA.G.V.3. Valve /or other instrument for cleaning
diffusers
ball , manual un 2 0 0 2 0 0
PA.G. Measurement and dissolved oxygen control
system
reading by luminescence; HachLange, one controller with
two sensors with digital and analogic (4-20mA) output
HachLange LDO+sc100 [CT]
to be installed in the pre-aeration
tank, to command the operation of
respective blower
set 1 0 0 1 0
PA.G.O2C.1.c Controller un 1 0 0 1 0
PA.G.O2S.1.1/2 sensor un 2 0 0 2 0
Reuse
RS.L.TK.1.c treated effluent storage tank Material: Concrete
Useful unitary Volume (m3): 111
Total flow rate (m3/day): 1700
un 1 0 0 1 0
Overflow to the discharge box set 1 0 0 1 0 0
RS.L.P.1.c reuse pumping station Double booster set with two centrifugal pumps; Lowara
10SV06F022T 2,2 kw 3000 rpmin for 10 m3/h 5 bar
Lowara_10SV06F022T [DS]
un 2 0 0 2 2,2 4,4

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
Chemical cleaning of membranes set 1 0 0 0 0
MCIP.L.TK.1.c chemical cleaning tank Material: Concrete
Internal dimensions (W x L x H) (m): 1,3x1,3x4,3
Useful unitary Volume (m3): 6,422
un 1 0 0 0 0
MCIP.L.VBF.1.1/2 cut offvalve for feed CIP tank butterfly un 2 0 0 0 0
MCIP.L.P.1. Solution injection pump Portable submersible pump, Flight CS3057HT, curve 262
; 1,7kW 2730 rpmin; R2" for 27,1 m3/h 11,8 mca
FLYGT_CS 3057.181HT(262) [DS]
Xylem [ISO9001_14001]
just installed at the moment of the
procedure
twice a year
un 0 0 1 1 1,7 0
Feed piping and fittings to the permeate head
pipers
2 1/2" set 1 0 0 0 0
MCIP.L.Vb.1.c Sampling valve for cip un 1 0 0 0 0
MCIP.L.VB.4.c cut offvalve of the recirculation CIP line Flanged Butterfly 2 1/2" DN65 un 1 0 0 0 0
MCIP.L.VB.5.1/2 cut offvalve of the modules cip feed line Flanged Butterfly 2 1/2" DN65 un 2 0 0 0 0
Washing system of thin bubble diffusers un 0 0 1 0 0
SOLID PHASE
DEWATERING SLUDGE
Sludge dewatering system
composed of: Attached documentation
Fluiteco_SD 700_ Sludge screw press [DSI]
Fluiteco_SD700_
controlled by it own electric panel vg 2 0 0 2 0
SD.L.RS.1.1/2 Reservoir for polyelectrolyte preparation POLYPACK MS 2000, 2000L, with mixer and level switch un 2 0 0 2 0,37 0,74
SD.L.P.1.1/2 Dosing polyelectrolyte pump Progressive cavity type Seepex / 025-6L MD/A6-A7-A7-F0-
GA-X
un 2 0 0 2 1,5 3

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
SD.L.P.1.1/2 Eccentric screw pump Progressive cavity type; Seepex / BN 5-6L /A1-C1-C6-F0-
A; 1,5- 4 m3/h With: Monofasic frequency inverter 1.5Kw
IC5
un 2 0 0 2 1,5 3
SD.L.TK.1.1/2 Flocculation tank with stirrer DOSAPACKS 280 , 280 l; with Mixer - HR5A-
030/085/E0.37/A; inferior conexion w/ 2" for sludge inlet +
polyelectrolyte ; superior conexion w/ 2" for sludge outlet
A un 2 0 0 2 0,5 1
SD.L.E.1.1/2 Dewatering screw Screw, Fluiteco/ SD700
Fluiteco_SD_ Sludge screw press [CTI].
Fluiteco_SD_Sludge screw press [MOM_I]
un 2 0 0 2 0
SD.L.VS.1.1/2 Solenoid valve for internal washing system G1 25mm 2/2 NF 4W 24V50HZ un 2 0 0 2 0
SD.L.VS2.1/2 Solenoid valve for external washing system G2 50mm 2/2 NF 4W 24V50HZ un 2 0 0 2 0
SD.L.V. Pinch valve un 2 0 0 2 0
Power and control panel for the dewatering
system
0
Packing and Storage of dewatering sludge 0
Big bag type bag mounted on stainless steel
support structure
0
Overflows, emergency discharges, bypass,
drainage
Geral by pass of the waste water treatment
plant
done in the last main hole that feed the septic tanks done in the last main hole that
feed the septic tanks
0 0 0
Piping and fittings of the overflow of the
equalization tank to the discharge box
un 2 0 0 2 0 0
Piping and fittings of the overflow of the pre-
aeration tank to equalization tank
un 2 0 0 2 0 0
Drainage system of the combined unit box set 1 0 0 1 0 0

power (KW)
in
service
spare
installed
spare
warehouse
total
unit
total
box
concrete
un 1 0 0 1 0 0
drain pump Submersivel centrifugal, Lowara / DOMO S7VX , 0,55 kw
2900rpm, RP1"; for 2 7,2 m3/h at 6 m
Lowara_ DOMO S7VX_Drain Pump [DS]
un 1 0 0 1 0,55 0,55
fittings and piping to connect the
discharge box
set 1 0 0 1 0 0
Gravitical drainage of the technical area in the
sludge dewatering area , to the equalization
tank
set 1 0 0 1 0 0
155

ANNEX 3 TECHNICAL DOCUMENTATION

mbr_process_design_description_gc_equipment_K2.pdf

Recommended

Recommended

More Related Content

Similar to mbr_process_design_description_gc_equipment_K2.pdf

Similar to mbr_process_design_description_gc_equipment_K2.pdf (20)

Recently uploaded

Recently uploaded (20)

mbr_process_design_description_gc_equipment_K2.pdf