Cloneqal W T W ATTACHMENT C1

The existing WWTP had been built in 1985 for an estimated capacity of 200 pe. The WWTP is currently receiving a load of 400pe. In spire of this the existing WWTP is performing in a reasonable manner particularly with regard to BOD and Suspended Solids.

There is no nutrient removal at the WWTP so the WWTP would not be reducing P levels down to lmg/l.

There is also no storm water facilities at the WWTP and currently storm water discharges directly and untreated to the River Derry.

During the economic upturn of the 2000s Clonegal began to come under Development pressures and Carlow County Council saw Clonegal as a suitable location to develop as a settlement town.

Carlow County Council moved to the procurement of a new WWTP at Clonegal with a proposed capacity of 1,000pe to satisfy its requirements in line with :

Q National Development Plan Q Water Framework Directive

Q Habitats Directive Q Drinking Water Directive

’ Q Urban Waste Water Regulations

Carlow County Council progressed the new Clonegal WWTP to tender stage during 2004. Funding was obtained under the Small Schemes. In the Small Schemes the Government funds 75% of the scheme with the remaining 25% ffom Development Levies.

The Clonegal WWTP upgrade was tendered as a DBO bundle with the Rathoe WWTP project. Tenders were received during May 2008 and the Tender was awarded to E.P.S. Ltd.

The new works at Clonegal will consists of the following:

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Inlet 6mm screening and de-gritting on all flows, including storm flows. Storm water holding of 3DWF for 2 hours, providing settlement and a baffled outlet for overflow to the River Derry, with held storm water returned for treatment. Flow measurement of flow to full treatment and storm overflow. Secondary treatment using aeration and settlement working in a process known as a Sequence Batch Reactor. Tertiary treatment using a sand filtration system. Phosphorous reduction using ferric dosing. Sludge holding and thickening tank with flow measurement for sludge removed fi-om site.

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EPA Export 26-07-2013:15:04:21

The treatment standards for the new works are :

BOD IOmg/l 95%ile TSS 1 Omg/l 95%ile AmmN 5mg/l 95%ile Total P lmg/l 95%ile

The proposed Clonegal WWTP is designed to receive a DWF of 230m3 per day. The WWTP can cater for a peak flow of 45Vs.

The WWTP will treat flows up to 3 DWF, 690m3 a day.

The Existing Works

The flows enter the WWTP via a 225mm diameter sewer at the north eastern end of the site.

The manhole within the site boundary contains a storm overflow which consists of a 225mm pipe to the river. The storm water currently receives no screening at this location.

I t then enters a forward feed pump sump. There is a duty and standby pump in the forward feed chamber.

It then is pumped to the Aeration Tank, a concrete tank 6.8m by 6.8m in area and 3.5m deep. Here the effluent receives aeration via a 2.8 kw Venturi Aerator sitting on the floor of the tank. There is a screening mechanism on the pipe incoming into the aeration.

From the Aeration Basin the effluent flows into the clarifier. The clarifier is a concrete tank 4.6m by 4.6m in area and with a hopper at the centre. The hopper at the centre collects sludge. Sludge is then returned to the aeration tank or drawn off by a sludge tanker and transferred to Tullow WWTP.

There is a sludge drying bed on the site but this has not been used for a long period due to issues with smells and odours.

From the Clarifier the effluent discharges into an outlet chamber. There is a measuring device in the outlet chamber but this is not working.

From the outlet chamber effluent then discharges to the River Derry via a 225mm diameter outlet pipe.

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EPA Export 26-07-2013:15:04:21

Clonegal WWTW c2 -

There are no pumping stations in the Clonegal catchment and there are no overflows in the drainage network other than .at the new wastewater treatment works. At the treatment works there are two discharges, that of the final effluent and that for the overflow fi-om the storm water holding and settlement tank.

The final effluent (3DWF) is tertiary treated to the following standard.

BOD 10mg/l 95%ile TSS 10mg/l 95%ile AmmN 5mg/l 95%ile TotalP lmg/l 95%ile

The storm water is treated in the following manner:

All flows are screened(6mm) and de-gritted and then any storm water flow above 3DWF(43m3/hr) is overflowed 1.0 the storm water holding tank. This tank has a storage capacity of 2 hours at 3DWF. If the tank fills up then settled, screened and de-gritted storm water is overflowed to the: river, via a baflled overflow pipe, this flow is measured and recorded. The held storm water in the tank is returned to the forward feed pumping station and provided with secondary treatment, as inlet flows permit, this is managed by the operator.

The new Clonegal WWTP with a capacity of 1,000pe will cater for development in the Clonegal area up to 2020 and ensure a good quality effluent to the Clonegal.

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EPA Export 26-07-2013:15:04:22

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i i L

9 % $3

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EPA Export 26-07-2013:15:04:22

Clonepal WWTP: SBR CvcPe Justification

SBR No.1 Fill & Anoxic Fill & Aerale Fill & Aerale Fill & Aerale

Aerate Settle Settle

Decant

The SBRs at Clonegal are designed to accept 3 DWF + all re-circulated flow at all times during their cycle. The design is based upon a 4-hour cycle which is broken down into the following 30 minute periods;:

Time SBR No.2 30 mins Aerate 30 mins Settle 30 mins Settle 30 mins Decant 30 mins Fill & Anoxic 30 mins Fill & Aerate 30 mins Fill & Aerate 30 mins Fill & Aerate

Regardless of the flow entering the plant, the 4-hour cycle remains at a constant, i.e., if flows are low the tank will only partially f i l l before the aeration stage is initiated. At maximum flow the SBRs will hlave enough capacity to continuously receive 3 DWF + all re-circulated flows:

1. FFT @ Clonegal = 3 DWF = 720m3/day = 30m3/hr

2. Total re-circulation flows (supernatant, wash water, etc.) = 1 .3m3/hour

3. Total flow sent to SBR at 3 DWF = 75 1.2m3/day = 3 1.3m3/hr

4. Maximum volume received by each SBR in a 2 hour cycle = 62.6m3

5. Maximum SBR Decant Volume (including all re-circulated flows):

= 6.75m x 5.0m x I .9m Decant Depth = 64.125m3 / SBR

6. A 4 hour cycle will be as follows at 3 DWF: m m l 0 5 0.5 0.5 0.5 0.5 0.5 0.5 0.5

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EPA Export 26-07-2013:15:04:22

7. 4 hour cycle = 6 cycles/day x 2 tanks = 769.5m3/day. This is the maximum volume that can be drawn off by the decant arm every day and includes all re- circulated flows (supernatant, filter backwash, screen wash water)

Stream SBR1 SBR2

8. At 1 DWF (=10m3/hr), the cycle time remains the same:

2 hours 2 hours FX FA A S I D A S I D FX FA 0.5 0.5 I 0.5 I 0.5 0.5 0.5 I 0.5 I 0.5

- _ _ SBR1 SBR2

9. At 2 DWF (= 20m3/hr), the cycle time remains the same:

~

FX FA A S I D A S I D FX FA 0.5 0.5 I 0.5 I 0.5 0.5 0.5 1 0.5 I 0.5

I Stream I 2 hours I . 2hours I

I I I I I I I

10. As the cycle time does not change (i.e. six cycledday is a constant) the only variant is the decant depth. For example, at 1 DWF the maximum decant depth

. will be 0.67m and at 3 DWF the maximum decant depth will be 1.9m.

Because sufficient capacity has been allowed in the Decant Volume for 2 hours storage of 3DWF + re-circulated flows, and due to the fill cycle switching between tanks every 2 hours, there will never be a need to spill to storm as long as the incoming flow does not exceed 3 DWF.

Enough capacity has been provided in the SBRs to accommodate an instantaneous increase in flow from 1 DWF to 3 DWF at any stage during the f i l l cycle. Since there is always a f i l l cycle in progress, no balancing is required before the SBRs.

In the case of 6 DWF being reached (3 DWF to treatment, 3 DWF to storm), the storm tanks are appropriately sized for 2 hours storage as per the specification.

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EPA Export 26-07-2013:15:04:22

Clonegal

C l

Plant

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EPA Export 26-07-2013:15:04:22

Index

3 1 Introduction ................................................................................................ 2 General Plant Description .......................................................................... 3 3 Particular Plant Description ....................................................................... 4

3.1 Inlet Works 4 3.2 Biological Treatment ........................................................................... 4

3.2.1 Sequential Batch Reactor (SBR) 4

..........................................................................................

.................................................. 3.3 Sludge treatment and storage ............................................................. 8

3.3.1 Sludge Holding Tank .........................................................~........~ 8 3.4 Phosphorous Removal ........................................................................ 8

3.4.1 Chemical treatment ..................................................................... 8 3.5 Tertiary Treatment .............................................................................. 8 3.6 Final Effluent ...................................................................................... g 3.7 Instrumentation .................................................................................. 9

3.7.1 Flow Metering .............................................................................. g 3.7.2 Dissolved Oxygen (DO) Metering.. 9 3.7.3 Automatic Sampler 9

.............................................. ......................................................................

Clonegal WWTP Page 2 of 9

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1 Introduction

1 Suspended Solids (mg/l)

The E.P.S. design herein for Clonegal Waste Water Treatment Plant designed in accordance with BATBJEEC and the EPS design standards.

10

The treated effluent will comply with the standards shown in the following table:

Ammonia (mg,’l) 5

TP(mg/l) - 1

Table 1 - Effluent Limits tdischarge

2 General Plant Description

The new Wastewater Treatment Works shall have an ultimate design of Population Equivalent of 1,000 PE.

(Please read in conjunction with Flow Diagram rev o and GA Drawing which are submitted)

The E.P.S. proposal shall be based on Sequential Batch Reactors.

The following provisions shall be incorporated in the design:

- Automatic inlet screenings and grit removal including screenings and grit washing, dewatering and disposal facility

CIonegai WWTP Page 3 of 9

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- The Biological Treatment includes 2 No. SBR

- Provision for biological nitrogen removal

- Provision for Aeration System

- Phosphorous removal based on chemical dosing including dosing pumps and chemical storage

Provision of 1 No. on site Sludge Holding Tank - - Provision for Tertiary treatment based on 1 no. mechanical sand filter

3 Particular Plant Description

3.1 Inlet Works

The inlet works shall consists of:

- inlet screening and grit removal arrangement that will remove solids in excess of 6 mm

3.2 Biological Treatment

E.P.S. proposes a Sequential Batch Reactor Process.

3.2.1 Sequential Batch Reactor (SER)

The flow shall be pumped into the SBR tanks for treatment after preliminary treatment.

Flow to each SBR shall be measured and monitoring.

Provision shall be made within each SBR for DO meter.

The system shall be based around two reaction vessels. SBR tanks act as a

balance tank, anoxic, aeration chamber, and settlement tank. Following

Clonegal WWTP Page 4 of 9

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EPA Export 26-07-2013:15:04:22

. . . . . . . . . . . .. . . . . . . - . . . . . . . - . . . . - . . . . . . . . . . . - . .. . . .. . - . . . . . .. . - . - ..

preliminary treatment, the wastewater enters a distribution chamber. An

actuated valve on the inlet to each SBR dictates which SBR receives flow.

Provision shall be made for air blowers to serve the SBR as required. Air blowers shall be controlled by an individual D.O. meter per SBR.

The system shall be design to allow fill, anoxic, aerate for a preset time (refer to SBR cycle chart). Once the preset time for fill, anoxic, aeration is complete, settlement stage starts. IOnce the preset settlement time expires the decanted supernatant shall be discharged by a floating arm draw-off assembly, which shall be connected to a winch at the top of the tank. Once the decant cycle is complete, the floating arm draw off shall be returned to the park position by the electric winch, and tlhe cycle shall be repeated.

1. SBR Sequence of Operation:

a. Fill/Anoxic - incoming screened and de-gritted raw sewage with the biological mass in to SBR.

b. Aeration -- Aeration shall be supplied by fine bubble diffused aeration system. The oxygen brings the biological mass from a latent state to a food-consuming active state

c. React Cyc1.e - during this phase the raw sewage flow ceases and is transferred to the second SBR. The biological mass now breaks down the remaining sewage and consumes it as food

d. Settle - Aleration is inhibited, and the biological mass begins to settle. The biological mass continues to use oxygen and goes to a

latent statle when all the oxygen is consumed

e. Draw/Decant - After settling occurs, a clear liquid shall form at the top of the tank. This liquid shall be through the decant arm

f. Sludge Wasting - At the end of the process cycle a percentage of

the biological mass shall be pumped from the SBRs to the

Clonegal WWTP Page 5 of g

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EPA Export 26-07-2013:15:04:22

sludge holding tank. This shall maintain the correct concentration of biomass within the SBR.

Provision shall be made within SBR for a fine bubble diffused aeration system.

Scum shall be removed using a surface scum scraper, into box into sludge holding tank.

Sludge draw off from the each SBR will include 1 no. Waste Activated Sludge (WAS) duty per SBR and 1 no. common standby.

The supernatant from the sludge holding tank shall flow by gravity back to the works to the splitter chamber for recycling through the works.

Each SBR tank will contain the following mechanical and electrical equipment:

1 No. Ultrasonic level sensor 1 Floating arm draw off c/w actuated winch 1 No.uPVC lateral pipework grids c/w diffuser network 1 No. Dissolved oxygen monitor 1 No. Sludge wasting pump 1 No. Anoxic Mixer

Clonegal WWTP Page 6 of 9

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EPA Export 26-07-2013:15:04:23

3.3 Sludge treatment and storage

3.3.1 Sludge Holding Tank

Wasted sludge shall have a solids content of 0.75% DS and shall be pumped from each SBR into the sludge holding tank to be thickened to 3 %DS.

3.4 Phosphorous Removal

3.4.1 Chemical treatment

Phosphorous exists in three main forms in wastewater; ortho-phosphate, polyphosphate and organic phosphate. During aerobic treatment, the latter two forms are converted to ortho-phosphate, which is the easiest form to precipitate using chemical addition.

E.P.S. proposes to remove phosphorous using chemical dosing of Ferric Sulphate (Fe2S04). It is proposed to dose Fe2S04 directly into splitter chamber.

3.5 Tertiary 'Ikeatment

Water shall be fed into an area below the entire sand bed. As the water rises to the surface, the particles if dirt remain between the grains of sand. Once the water is above the sand bed, shall be treated.

The cleaning of the filter shall be performed by the sand washer, which continuously flushes the sand grains in the filter. An airlift sucks up sand from the bottom, where the grains are dirtiest, and feeds them into the sand washer. In the washer the dirt shall be separated from the grains of sand, partly through flushing, partly through fiction. The clean sand shall then returned to the sand bed in an even layer at the surface.

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EPA Export 26-07-2013:15:04:23

3.6 Final Effluent

Final effluent prior to discharge to an outfall shall be subject to outflow measurement and sampling. A composite flow proportional wastewater sampler shall provide sampling.

3.7 Instrumentation

3.7.1 Flow Metering

1 no. Inlet flow 0 1 no. Outlet flow

1 no. Row to treatment

3.7.2 Dissolved Oxyipen (DO) Metering

0 1 no. each SBRTiank

3.7.3 Automatic Sampler

I no. on inlet f low 1 no. on outlet flow

Clonegal WWTP Page g of g

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

1

EPS Dual SBR Cycle SBR No.1 Time SBR No.2

Fill & Anoxic 30 mins Aerate Fill & Aerate 30 mins Settle Fill & Aerate 30 mins Settle Fill & Aerate 30 mins Decant --

Aerate 30 mins Fill & Anoxic Settle 30 mins Fill & Aerate Settle 30 mins Fill & Aerate

Decant 30 mins Fill & Aerate

Clonepal WWTP: SBR Cvcle Justification

Stream

I D 0.5 I 0.5 I 0.5

The SBRs at Clonegal are designed to accept 3 DWF + all re-circulated flow at all times during their cycle. The design is lbased upon a 4-hour cycle which is broken down into the following 30 minute periods:

2 hours A S I D

FX FA 0.5 0.5 I 0.5 I 0.5

Regardless of the flow entering the plant, the 4-hour cycle remains at a constant, i.e., if flows are low the tank will only lpartially f i l l before the aeration stage is initiated. At maximum flow the SBRs will have enough capacity to continuously receive 3 DWF + all re-circulated flows:

I . FFT @ Clonegal = 3 DWF = 720m3/day = 30m3/hr

2. Total re-circulation flows (supernatant, wash water, etc.) = 1 .3m3/hour

3. Total flow sent to SBR ait 3 DWF = 75 1.2m3/day = 3 1.3m3/hr

4. Maximum volume received by each SBR in a 2 hour cycle = 62.6m3

5. Maximum SBR Decant Volume (including all recirculated flows):

= 6.75m x 5.0m x 1.9m Decant Depth = 64.125m3 / SBR

6. A 4 hour cycle will be as follows at 3 DWF:

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EPA Export 26-07-2013:15:04:23

7. 4 hour cycle = 6 cycles/day x 2 tanks = 769.5m3/day. This is the maximum volume that can be drawn off by the decant arm every day and includes all re- circulated flows (supernatant, filter backwash, screen wash water)

Stream SBRI S B R 2

8. At I DWF (=10m3/hr), the cycle time remains the same:

2 hours 2 hours FX FA A S I D A S D FX FA 0.5 0.5 [ 0.5 0.5 0.5 0.5 I 0.5 I 0.5

Stream I 2 hours I 2 hours SBR 1 I FX L... FA \ A \ S I D SBR2 I A 1 S I D I F X I FA

I 0.5 I 0.5 1 0.5 I 0.5 I 0.5 I 0.5 I 0.5 I 0.5 I I I I I I I I I I

9. At 2 DWF (= 20m3/hr), the cycle time remains the same:

I O . A s the cycle time does not change (i.e. six cycles/day is a constant) the only variant is the decant depth. For example, at 1 DWF the maximum decant depth wil l be 0.67m and at 3 DWF the maximum decant depth will be 1.9m.

Because sufficient capacity has been allowed in the Decant Volume for 2 hours storage of 3DWF + re-circulated flows, and due to the f i l l cycle switching between tanks every 2 hours, there will never be a need to spill to storm as long as the incoming flow does not exceed 3 DWF.

Enough capacity has been provided in the SBRs to accommodate an instantaneous increase in flow from 1 DWF to 3 DWF at any stage during the fill cycle. Since there is always a f i l l cycle in progress, no balancing is required before the SBRs.

In the case of 6 DWF being reached (3 DWF to treatment, 3 DWF to storm), the storm tanks are appropriately sized for 2 hours storage as per the specification.

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EPA Export 26-07-2013:15:04:23

Population Equivalent Flow DWF Running hours DWF FFl- Peak flow Supernatant return now -

3 DWF

31.3 m3h Foul pumps No.

1:OOO PE 240 1ffE.d 240 m3/d 24 h/d 10 m3/h 3 DWF 1 1 DWF

31.3 m 3 h (Duty/Standby)

m3/h 1.3 m 3 h

Influent Characteristies

Ammonia

Screenings - (FIOW rate @ stom FIOWS

Screens Screens aperture Screenings storage Screenings storage type Screen Min capacity Screen wash water Screen wash water frequency Screen wash water flow rate -

11 DWF I No. 6 mm 2 No.

105 m 3 h 1 I/S

I min/h 0.06 m3h

whee I ie bin

105 m3/h

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EPA Export 26-07-2013:15:04:23

Storm Flows I Storm Flow 11 DWF Storm Storage @ Peak Flow Storm Tank Volume req Storm Tank Volume offered Storm return pumps Storm return pumps flow rate No. Tanks each Tank Length each Tank Width each Tank Depth each Water Depth

Biological Treatment 3 DWF Supernatant Return Flow Total Flow to Treatment No. SBR Tanks each Working Volume Retention Time each Tank Length each Tank Width each Tank Depth each Water Depth No. of cyclesJSBR Fill volumelcycle MLSS MLVSS Max Decant depth Decant time Decant flow rate Denitrification rate FM ratio BOD loading Sludge age Min Temperature Max Temperature

2.40 h 72 m3 82 m3 2 No.

. 15 m3h 2 No.

5.4 rn 2.7 m 3.1 m 2.8 m

30 m 3 h . 1.3 m3h

31.3 m3h 2 No.

125 m3 25 h 5 m

6.75 rn 4 m

3.7 m 6 No.

62.6 ni3 3,000 mgll 2,768 mgll 1.90 m 0.50 h 128 m3h 0.02 0.09 0.24 kdm3.d

. 19.4 d IO c 20 c

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EPA Export 26-07-2013:15:04:23

I

- Ixygen Requirements - 'arbonaceow ,pecific oxygen consumption 'eak factor Ixygen Transfer Rate (a) 3xygen Transfer Rate (0) 3xygen Requirement

TP

qutrients 4mmonia oxygen consumption 3xygen required (nibification) Safety factor 3xygen required (nitrification)

Total oxygen requirement Dissolved oxygen concentration at 20C Dissolved oxygen concentration Aeration Time Total oxygen requirement Safety factor Oxygen transfer rate Specific oxygen input Air capacity per diffuser

No. of Blowers Blowers min capacity No. of diffusers Oxygen transfer efficiency -

I .2 1.2

0.65 0.9 I23

4.3 43 1.2

5 I .60

174.6 9.08

2 12

7.28 1.5

10.91 15 5

2 191.4

38

kg 02kg BOD

kg 02/d

kg02/kg N Kg02/d

KgO2/d

Kg02/d mgfl mg/l h Kg02h.SBR

kg/h.SBR g O2Mm3 x msd Nm3h.diffUser

NO. (Duty/Standby)

N m 3 h No.

2.5 kg 02ikW.h

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EPA Export 26-07-2013:15:04:23

Ferric Dosing Phosphorous to be removed Rat io Solution strenght Weight of ferric sulphate P Volume of Ferric required safety factor Volume of Ferric required No. of dosing pumps Each flow rate Storage tank Storage tank capacity Storage tank capacity

3.26 kgfd I .25 45 Yo

58.42 kg I .56

37.45 Vd I .4

52.43 Vd 2 No. (Duty/Standby)

2.2 I i h IBC 1.0 m3

26.7 d I 1

Sludge Production Waste activated sludge production Sludge yield Sludge age Quantity of waste activated sludge

Chemical sludge production Quantity of phosphorous to be removed Quantity of sludge production Quantity of chemical sludge

Total sludge production Sludge volume (@ 0.75YoDS Wasting time Sludge volume (@ 0.75%DS WAS pumps WAS pumps flow rate + 20%

1.1 23.1 d 68.7 kg DS/d

3 kg/d

16.296 kg DSld 5 kg/kg

. 85.0 kgDS/d 11.3 m3/d 10 min/cycle.SBR

5.65 m3h 2 No. (Duty/Stand by)

6.8 m 3 h

For

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EPA Export 26-07-2013:15:04:23

Sludge Holding Tank No. Tanks Design DS Working Volume required Storage capacity required Working Volume offered Expected outlet DS Tank Length Tank Width Tank Depth Water Depth Floor slope supernatant

1 No. 1.5 %DS 171 m3 30 d

236 m3 2.5 % D S 10 m 6.2 m 4 m

3.8 m 7.5 degrees 7.9 m3ld

Balance Tank No. of Balance Tanks each Balance tank working volume Total working Volume each Decant Volume at 3 DWF no. Forward pumps Flow rate Balance Tank capacity required @ 3DWF

2 No. 34 m3 68 m3

64.12 m3 2 No. (Duty/Standby) 60 m3h 2 h

Tertiary Treatment No. of Sand filters Flow rate Filter bed SA Max Washwater consumption Max supernatant Length Width Height

1 No. 60 m3h

9.75 m2 IO to20 Vmin

0.9 m3h 4.3 m 2.7 m

2.02 m

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

Phosphobus :in rthe.Effluent 0.24 kg

2 mg/l 1 1 1 mg/l 1.25 1

0.5 mg/l 1.5 1

3.00 Amou 2.16 kg

4

Consent P Molar weight 1.806'15 1613 Ratio 1.25

Solution strength 415.0°/o Weight of Ferric Sulphate 38.71 kg

\ 9 %

Specific gravity 1.56 Volume of Ferric Sulphate 24.81 I/day

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

< < < < ' < < < < < < <

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

EPA Licence application

Clonegal WWTW

River BOD mgr'l Amm N mgh

Deny River

1.0 Effluent Dilution.

The Clonegal WWTW discharges t1irt:ctly into the Deny River. The Deny River had a 44 rating in 2003,.

Phosphorous mgA ORP mg/l

2 1

There is a staff gauge on the Deny River at Clonegal and the 95%ile flow is for the staff gauge at Clonegal

as measured by the EPA, the median ilow is an estimated flow.

95%ile Flow

50%ile Flow

0 Calculated long-term 95%ile :flow - 0.58m3/s

Estimated 50%ile flow > 2.0m3/s

0.016 0.002

0.004 0.001

WWTW Flows

The flow modelled for the discharge from the WWTW is 230 1Md for the average flow, with the dry

weather flow (DWF) being 180Vh/d. These correspond to a daily flow average flow of 230m3/d and a

DWF of 180 m3/d for a population equivalent of 1000pe. These flows are then modelled discharging into

the Deny River at 50Y0ile and 95%ile flows.

The parameters considered for assimilative capacity are BOD, Phosphorous and ammonia and the final

effluent concentrations for the future design loading are set out in the Table 1 below and the resulting

increases in the parameter concentrations in the receiving waters as a result of these discharges are set out in

Table 2 below. The model data for these tables is contained in Appendix A.

Table 3 - Increases in Parameter Concentrations in Receiving waters

I I River Flow I BOD mg/l I Amm N mg/l I ORP mg/l

BOD

A final effluent standard of 10mg/l was selected for Clonegal WWTW, this is a strict standard given the

dilutions provided by the Deny River, this was selected because the Deny river flows into the Slaney River

about 2 miles south of the wwtw disch:uge and the Slaney River is a Salmonid river. Carlow County Council 1 Wastewater Treatment

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:23

The BOD concentration of I O mg/l was used in the water dilution modelling as this is a worst case as the

WWTW is designed to achieve this for 95% of the time so on average it should be producing a BOD

concentration of less than 5mg/l. The BOD concentrations in the Deny River as a result of the WWTW

discharge are 0.1 mg/l at 95%ile low flow and 0.03 mg/l at median flow which are negligible concentrations

and would be consistent with a high water quality status or Q5 rating and is an improvement compared with

the loads discharged from the old works.

Ammonia

An Ammonia concentration of 5mg/l was used for the water quality modelling, this would be a worst case

as on average the ammonia in the effluent would be around 2 mg/l. The ammonia concentrations in the

Derry River as a result of the WWTW discharge are 0.016 mg/l at 95%ile low flow and 0.004 mg/l at

median flow. These are very low coricentrations and would have minimum impact on the water quality in

the receiving water and would be consistent with a Q5 water quality. They are also be a reduction of some

3-4 times that discharged by the old works.

Phosphorous, ORP

A phosphorous concentration of 1 mg/l was used for the dilution modelling this was modelled as an ORP

concentration of 0.5mg/l. The ORP concentrations in the Deny River as a result of the WWTW discharge

are 0.002 mg/l at 95%ile low flow and less than 0.001 mg/l at median flow. Given the dilutions available

the impact of the wwtw ORP discharge is minimal and would have little additional impact on receiving

water quality. The old works had P discharges of between 4 - 8 mg/l as there was no P reduction so with the

new WWTW at the future design loading of lOOOpe discharging at less than lmg/l, there would be 3-4

times less phosphorous being discharged into the river, thus improving the water quality.

Carlow County Council 2 Wastewater Treatment

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EPA Export 26-07-2013:15:04:23

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EPA Export 26-07-2013:15:04:24