WA2 Hybrid ceramic membrane filtration in water treatment Erwin WA2.pdf · WA2 Hybrid ceramic...

WA2 Hybrid ceramic membrane filtration in water treatment

This project has received funding from the European Union’s Seventh Programme for Research, Technological Development and Demonstration under Grant Agreement no. 308339.

Final meeting, June 17+18 2015 Erwin Beerendonk, Egbert Dubbelink, Thomas Wintgens, Arslan Ahmad, Andreas Nahtstedt, Jörg Gebhardt, Patrice

Nagtegaele and Marie-Pierre Denieul

• Introduction • Work packages • Conclusions • Success stories, leassons learned and

challenges

23.06.2015 2

23.06.2015 5

Introduction

• UF (poresize >5 nm - 0,1 μm) and MF (>0,1 μm) will not/partly remove emerging compounds and pathogens

• Hybrid systems – Coagulation to improve removal of NOM and viruses (MF)

and improve operation – Ion exchange to improve removal of NOM and operation – Activated carbon (PAC) or ozone to improve removal of

emerging pollutants

CMF = High investment costs!

WP21 Ceramac (RWB)

WP22 Hybrid Ceramic Membrane Systems (KWR)

WP23 Neural Net Control (IWW) WP24 Laser-Induced Breakdown Detection (Cordouan)

WP21 Ceramac (RWB)



•Innovation in reactor design (200 elements in 1 vessel, reduce footprint, piping etc)

•Further optimizing design

•Pilot testing and implementation full scale PWN

WP21 Ceramac (RWB)



•High potential (Techneau) •Optimizing performance HCMS

•Compare with state of the art

•Demonstration in Hamburg (HSE)

WP21 Ceramac (RWB)



•Developed in EU-Life “Purifast”

•Adapt to full scale

•Training neural net

•Pilot and full scale UF backwash water WAG

WP21 Ceramac (RWB)



•Demonstrate nanoparticles analyzer on lab, pilot and full scale

•LIBD prototype mobile system

•Field demonstration LIBD

23.06.2015 11

WP21 Optimisation Ceramac® concept (1)

• Design 192 membranes in one reactor • Tests, validation and development of the top

and bottom plate and hydraulic behavior • Validation tests May 2013 until September

2013 on the full scale pilot • The top and bottom carbon fiber plate

concept is tested in a separate test unit

23.06.2015 12

WP21 Optimisation Ceramac® concept (2)

• Test of 793 backwashes (critical) showed stable process and applicable to the full scale plant

• Successful implementation of the full scale CeraMac® in Andijk 3 (Capacity and quality meet design criteria)!

• Application of HCMS improved (footprint, costs, sustainability and full scale reference)

Pilot locations • WWTP Almelo

(The Netherlands) • WWTP Basel

(Switzerland)

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WP22 HCMS to increase application CMF (1)

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PAC-CMF pilot at WWTP Almelo


• Experiments: (1) OMP removal (2) Operational stability • WWTP effluent + OMPs = Feed pilot plant. • Cocktail of OMPs dosed, each ≈1µg/L. • PAC dose (mg/L): 0, 15, 30, 60 [precoat mode] • BW: pressurized (5 bar) with permeate and air • CEB: BW with permeate and NaOCl

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OMPs dosed µg/L metoprolol 0,936 gemfibrozil 0,953

sotalol 0,901 tramadol 0,951

carbamazepine 0,962 venlafaxine 0,881 diclofenac 1,027 atenolol 0,972

propranolol 0,849 trimethoprim 0,973

sulfamethoxazool 0,980 ketoprofen 0,999 bezafibraat 0,918

diatrizoic zuur 1,019 metronidazole 1,005

fenazon 0,996 cyclophosphamide 0,797

pentoxifylline 0,970

Filtration time 15 min Filtration flux 60,80,100, 120 L/(m2·h) BW frequency 4 times per hour BW time <5 sec CEB frequency 1 time per 6 hour Chemicals used NaOCl (12,5 wt%) Soaking time 5 min


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0 0,2 0,4 0,6 0,8

1 1,2 1,4 1,6 1,8

20 30 40 50 60 70 80 90 100

TMP

(bar

)

Time (hour)

TMP with 30mg/L PAC Flux=100 L/m2.h

TMP


Removal of OMPs

23.06.2015 17


Pilot tests in Basel (double HCMP) • Combination of PAC sorption and UF-filtration in one process:

HCMP (Hybrid ceramic membrane process)

• Two parallel systems

Double HCMP system

Membrane ITN Nanovation

Membrane area 0.8 m2

Contact zone 35 L

Filtration tank 150 L

PAC dosage 20 mg/L

Fe dosage 4 mg/L

Feed per line Ca 20 L/h


Experimental set-up (double HCMP)

• HCMP (Hybrid ceramic membrane process)

• Two parallel systems

Double HCMP at pilot hall Top view on flat sheet ceramic membranes


Experimental setup

Experiment

• HCMP operation on WWTP effluent as reference (without PAC)

• PAC addition

• PAC/Fe3+ addition

• Optimization for stable operation (filtration flux)

• Investigate chemical cleaning strategy


Membrane performance

• Filtration of WWTP effluent

• Comparability of the 2 HCMPs (same operational parameters)

Operational parameters Flux: 25 LMH CEB frequency 2.5 d PAC: 0 Fe3+: 0


Operational parameters Flux: 25 LMH CEB frequency 2.5 d PAC: 20 mg/L Fe3+: 0

Micropollutants- concentration and removal with PAC addition

• Good reduction of non-polar substances

n=11


Membrane performance with PAC + Fe3+ addition

• PAC dose: 20 mg/L in both HCMP

• Fe dose: 4 mg/L - in one HCMP only

• 1st experiment: little difference between the two HCMPs until problems with aeration in HCMP 1

Operational parameters Flux: 25 LMH CEB frequency 2.5 d PAC: 20 mg/L Fe3+: 4 mg/L (only HCMP 1)

(with Fe3+) (no Fe3+)

wrong flux setting

uneven aeration in HCMP1


Membrane performance with PAC + Fe3+ addition

• PAC dose: 20 mg/L in both HCMP

• Fe dose: 4 mg/L - in one HCMP only

• 2nd experiment: little difference between the two HCMPs, until the dosing point of Fe3+ moved

from contact zone into the membrane tank

Operational parameters Flux: 18 LMH CEB frequency 1 d PAC: 20 mg/L Fe3+: 4 mg/L (only HCMP 2)

(with Fe3+) (no Fe3+)

Point of Fe3+ dosing changed


• Removal increases with PAC dose, as expected

• At 30mg/L PAC dose and flux=100 lmh, HCMF process remained stable

• PAC-CMF applicable on waste water (calculation of costs and sustainability to be checked (WA5))

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Conclusions


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WAG Wassergewinnungs- und -aufbereitungsgesellschaft Nordeifel (treatment plant Roetgen)

Pilot UF treating backwash water process (Sept. 2014 – Feb.

2015) Two treatment lines :

- UF-modules Lab 1.5 MB 1.0 (Multibore®)

- Membrane area 1m² (small area / full length)

- Capillaries per fiber 7 - Inner diameter 1.5 mm - Outer diameter 6.0 mm - Pore size ca. 0.02 µm - Material: PESM

WP23 Process control with ANCS (2)

27

Pre-Filtration

Kalkstein-Filtration

Disinfection

Storage

Flocculation (in-line)

Ultrafiltration 1st stage

PAK (if necessary)

NaOH / CO2

Al2(SO4)3

CO2

NaOH (if necessary)

Backwash Water

Recycling Ultrafiltration

2nd stage without

chemicals

River

Neutralization

with chemicals

Raw water: Dreilägerbach Reservoir

with chemicals


23.06.2015 WP2.3 28

ANCS-Structure: − Clustering of input data with similar patterns

(feed water quality, parameter settings) − Weighting input channels for single ANCS

neurons to link data clusters with their effect on treatment efficiency


UF100 UF200

Gemessen Optimiert Einsparung/ Verbesserung

Gemessen Optimiert Einsparung/ Verbesserung

Elektrische Energie Kosten [€/m³]

1,901 1,671 0,23 2,521 2,053 0,467

Erlös [€/m³] 0,642 0,649 0,006 0,653 0,659 0,006

Energieeinsparung von 12,10% und eine Verbesserung der Produktivität um 0,98%

Energie Einsparung von 18,55% und Verbesserung der produktivität um 0,97% .

Optimisation results

Ergebnisse im Überblick

• Modelling of permeabilility after/before backwash • Improving permeability results in reduction of energy

use • May result in decrease of production optimise to

find the best compromise


Conclusions • Succesfull modelling of start- and end-permeabibility

after/before backwash • ANCS results in cost reduction of 4 - 25 %

• ANCS proven on membrane application (full scale to be

done), before already on coagulation/flocculation and distribution


Context & Objectives • Context:

• Current tests for checking UF membrane integrity (PDT / DAF) involve: • Reuse of produced water • Interruption of operation of membrane units • Loss in production + Costs $

• Objectives: Evaluation of potentials of the LIBD technology at lab- & pilot scale • Online semi-quantitative detection of nano particles (NP) in water to

ensure early monitoring of loss of integrity of UF membranes (skid or module)

23.06.2015 WA2.4 progress - Process monitoring with LIBD 32

Need for online monitoring of the integrity of UF membranes designed for the Drinking Water treatment market

WP24 Process monitoring with LIBD (1)


The challenge

A perfect method for low-pressure membrane integrity test should be:

on-line, continuous, easy to handle, reliable, highly

sensitive & low cost

Magellan Technology - LIBD


+ Robustness


The MAGELLAN analyzer is compact, transportable and robust

Test performed in Magellan Vial trials

• SYNTHETIC WATERS spiked in Flow though cell (MQ UPW) • Validate the field of measuring range , check the repeatability of the measurement, validate the detection of different

natures particles ORGANIC: PS 20 nm / 40 nm / 100 nm (concentration range : 103 – 107 part/mL) INORGANIC: AG 20 nm / 100 nm (concentration range : 103 – 107 part/mL) BIOLOGIC: MS2 phages 27 nm (concentration range : 104 – 108 part/mL) * SCREENING EFFECT : Mix PS 20nm + 40nm * NATURE EFFECT Mix PS 20nm + AG 20nm * TEMPERATURE EFFECT

• NATURAL WATERS in Flow though cell => Verify the feasibility of the measurement of a real water

Membrane pilot


Description Concentration of nanoparticles spiked Aim

Trial 1 Reference blank test with ultrapure water (UPW)

No Reference blank for each type of membrane

Trial2 MS2 phages in UPW 108 PFU/ml MS2 phages

To compare the results done by LIBD technology with the Plaque Forming Unit counting method.

Trial 3 Synthetic water spiked 6. 108 part/ml PS 20 nm and PS 40 nm 6.107 part/ml PS 100 nm and 6.108 PFU/ml MS2

phages

To test different size of nanoparticles. Evaluate the membrane cut-off.

Trial 4 Natural water No Study of effect of the water matrix

Trial 5 Natural water spiked PS 20 nm 1010 part/ml PS 20 nm

+ Repeatability


ORGANIC (PS)

UPW INORGANIC (Ag)

BIOLOGIC (MS2 phages)

Good repeatability regardless

the nanoparticle type

+ Reproducibility


UPW ORGANIC (PS)

Good reproductibility regardless the nanoparticle type

+ Sensitivity (concentration range)


• Organic (PS 20 nm) • Organic (PS 40 nm)

Order of magnitude for: • Detection: 103 part./mL • Quantification: > 106 - 107 part./mL

ZOOM IN

ZOOM IN

+ Detection of different types of particles • Biologic (MS2 phages 27 nm) • Inorganic (Ag 20 nm)


The LIBD is able to detect different types of nanoparticles with more or less sensitivity (no differentiation according the nature of particles)

+ Capacity to detect a loss of membrane integrity: evaluation of screening effect


Conclusions


Advantages

Repeatability

Reproductibility

No temperature effect

Integrity monitoring

Cut-off evaluation

Detection mode

Limits of technolgy

Quantification concentration

limit

Screening effect

Flow though cell fouling

Software

No Log removal quantification

LIBD : Demonstrates good repeatability and reproductibility Allows to detect different nature of particles but without differentiation Detects nanoparticles down to 103 part./mL but able to quantify

concentrations from 106 - 107 part./mL only Is not influenced by temperature effect and transport Can detect losses of integrity as well as damage levels Cannot monitor the log removal (screening effet & concentration level) Can be used to detect nanometric breaches in permeates in detection

mode No operational analysis software for small sizes up to now

Online trials should allow to check: Possible contamination of the flow through cell Influence of bubbles or flow rate variations Robustness in the harsh environment of water works (vibrations, noise,

temperature, hymidity,…) By-pass or pipeline implementation during the cleaning or backwashs

NEW TECHNOLOGY NEW WAY OF WORKING

• WA4: Evaluating toxicity before and after PAC-CMF (testing Almelo)

• WA5: Evaluating drivers and barriers of HCMS and ANCS (workshop Roetgen, June 11)

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Synergy with other WA’s

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Success stories (1)

– Ceramac • Improved footprint, costs and sustainability • Full scale reference PWN • Demo plant PUB Singapore • Pilot + demo plant SWW (UK) • Pilot Cairns (Australia) • Pilot Manitowoc (USA)

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Success stories (2)

– HCMS: PAC-CMF increased performance and removal of emerging compounds in waste water treatment

– ANCS • Reduce costs ultrafiltration (full scale UF Roetgen to be

finished) • Other drinking water plants and treatment

processes(coagulation, distribution)

Thank you for your attention!

This project has received funding from the European Union’s Seventh Programme for Research, Technological Development and Demonstration under Grant Agreement no. 308339.

WA2 Hybrid ceramic membrane filtration in water treatment Erwin WA2.pdf · WA2 Hybrid ceramic...

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