Innovating Water Treatment Technologies in Managing Water-Energy Demand

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1 Innovating Water Treatment Technologies in Managing Water-Energy Demand L.Y. Lee, S.L. Ong, J.Y. Hu and H.Y. Ng Centre for Water Research, Department of Civil & Environmental Engineering; NUS Environmental Research Institute, National University of Singapore

2 Pictures taken from Wikimedia Commons Pictures taken from Wikimedia Commons 2

3 Singapore s Four National Taps: Water Demand & Supply Flow Catchment water Water Treatment Plants Domestic Use Industry use Water reclamation plants Reservoirs Imported water Desalinated water NEWater Indirect potable reuse

4 Growing needs of Industrial Water NEWater and Industrial Water Supply for non-domestic use can free up potable water for consumption

5 NEWater Process Domestic wastewater Wastewater Treatment Treated effluent RO Brine Discharge to Sea NEWater Factory NEWater Microfiltration/ Ultrafiltration Reverse Osmosis UV Disinfection 5

6 Water Quality Comparisons Water Quality Parameters Turbidity [NTU] Total Dissolved Solids [mg/l] Lead [mg/l] Local Reservoir Water < PUB Tap water < NEWater < < to USEPA / WHO Standards Mercury [mg/l] Hormones (Synthetic & Natural) [μg/l] PCBs [μg/l] Dioxin [pg/l] Total Organic Carbon [mg/l] Total Coliform [cfu/100 ml] Enterovirus < ND ND ND ND < ND ND ND ND ND < ND ND ND <0.1 ND ND Not Specified Not Specified ND ND ND Not Detected

7 Emphasis on Energy & Water Efficient Technologies Water Reclamation Process change Self Sufficient Treatment Plants Optimization of operating mode Energy & Water Efficient Processes Green Technology Optimizing energy management

8 PROCESS CHANGE & NEW TECHNOLOGIES in Wastewater Treatment & Water Reclamation Wastewater Treatment Anaerobic process Membrane Bioreactor (MBR) Lower energy consumption, biogas production, reduced GHGs emission High treated effluent quality free from suspended solids Water Reclamation Reverse Osmosis (RO) Process Forward Osmosis (FO) Process Capacitive Deionization (CDI) Process Lower energy for water reclamation Lower energy & increased water recovery

9 Wastewater Treatment Anaerobic Processes

10 Conventional Activated Sludge System Influent Preliminary Treatment Primary Sedimentatio n Tank Activated Sludge Effluent Biogas Thickene r Digester Dewatering Centrifuge Sludge Disposal Integrated Anaerobic and Aerobic System > 50% Increase Biogas Waste Sludge 10 to 30% Reduction Influent Preliminary Treatment Anaerobic Process (UASB) Activated Sludge Effluent Dewatering Centrifuge Sludge Disposal 30% Reduction

11 High Rate Anaerobic Treatment Designs Anaerobic filters Upflow Anaerobic Sludge Blanket (UASB) Sequencing Batch Anerobic Reactor (AnSBR) Advantages: Compact small footprint Low energy requirement Ability to withstand shock loading and treats from toxicants Bioenergy production Anaerobic Membrane Bioreactor (AnMBR)

12 Aerobic post-treatment system performance at HRT 4 h treating anaerobic effluents (HRT = 6 h) Influent WW UASB Effluent CAS Effluent MBR Effluent SS (mg/l) (440) (322) 4 41 (18) N.D. VSS (mg/l) (350) (134) 3 28 (12) N.D. tcod (mg/l) (562) (227) (42.7) scod (mg/l) (93) (57) (21.2) (23.2) tbod 5 (mg/l) (230) (79) (6.3) (0.8) sbod 5 (mg/l) (35) (19) 0.7 2,3 (1.3) NH 4+ -N (mg/l) (43) (41) N.D. N.D. NO 3- -N (mg/l) N.D. N.D (41.3) (33.9)

13 Estimation and Comparison of IAATP and AS Average Influent Flow = 325,000 m 3 /d; Average Influent total Chemical Oxygen Demand = 590 mg/l Discharge: BOD5 = 10 mg/l; SS = 20 mg/l Parameter IAATP AS Overall Plant Energy Consumption (kwh per 1000 m 3 of wastewater treated) Aeration Energy Consumption (kwh per 1000 m 3 of wastewater treated) Sludge Production (kg per 1000 m 3 of wastewater treated) (without nitrogen oxygen demand) 181 (without nitrogen oxygen demand) Total Reactor Footprint (m 2 ) 44,442 56,300

14 Wastewater Treatment Membrane Bioreactors

15 MBR Demonstration Plant at Ulu Pandan WRP - Capacity: 23,000 m 3 /d - Feed: Primary settled domestic sewage effluent - Energy requirement: designed less than 0.7 kwh/m 3 system optimization enabled the plant to be operated at 0.4 kwh/m 3 Reference: G. Tao: Large Scale Membrane Bioreactor Plant Design (Retrofit) and Optimisation, Conference Proceedings IWA MTC Pictures from:

16 Anaerobic MBR for Domestic Wastewater Treatment Effect of SRT (30, 60 and 90 d) Parameter Feed (Concentration/Value) COD, mg/l ± TOC, mg/l 56.99± Ammonium, mg/l 57.43± TN, mg/l 50.3± 9.20 ph ~ 7.0 Temperature, o C 25 ~ 30 COD Removal Efficiency of ~85% Effluent COD: 62 to 69 mg/l TMP Increase, (kpa) R30 R60 R90 Huang et al. (2013) J. of Biotechnology; Huang et al. (2011) Water Research time (d)

17 Main Challenge in MBR Process Optimization Energy demand Aeration requirement Biofouling control

18 CWR SRT Impact on MBR Fouling ESE Submerged MBR operated at less than 5 days experienced rapid fouling. Fouling rate dependent on the amount of SMP (particularly the carbohydrates) and NOT the concentration of MLSS. Normalized membrane suction pressure days SRT 5 days SRT 10 days SRT 20 days SRT 3d SRT 5d SRT Days 10d SRT 20d SRT Reference: Ng et al. (2006) Environ Sci. & Tech., 40 (8),

19 Effect of Membrane Pore Size on MBR Fouling R80 On off Control Level sensor Ceramic Membrane TMP (kpa) R100 R200 R300 Feed pump P Pressure Gauge On off Control Day The biggest pore-sized ceramic membrane had the highest fouling potential, while the ceramic membrane with the smallest pore size encountered least fouling. Rougher membrane fouled faster. Flow Meter F Aeration Permeat e Parameters Material α Al2O3 /TiO2/ZrO2 Support layer α Al2O3 Permeability 3300/1450/1450/260 L/m2*h*bar Pore size 300/200/100/80nm Jin et al. (2013) J. of Membrane Sci.; Jin et al. (2010) Water Research

20 Enhancing Water Reclamation Process: Integrating MBR-RO for NEWater Production Integrating Membrane Bioreactor with Reverse Osmosis (MBR-RO) provides a new option for NEWater production Activated sludge process Primary Sedimentation tanks Aeration Basin Secondary clarifier MF/UF UV disinfection Domestic wastewater NEWater Primary Sedimentation tanks Membrane Biorector UV disinfection Qin et al. (2006). New option of MBR-RO process for production of NEWater from domestic sewage. Journal of Membrane Science, 272,

21 Integrating MBR-RO for NEWater Production MBR operated at a SRT : 20 days and HRT : 5.5 h Overall recovery efficiency : 80%.

22 Water Reclamation Membrane Processes

23 Fouling Management

24 Fouling Measurement Traditionally membrane fouling can be indicated by: Flux decline under constant pressure, or Pressure increase for constant permeate flux Are these suitable for full-scale RO? Flux TMP Time Time

25 Observations from Full-Scale RO System Cannot detect initial fouling Flux 1m 6m Cannot explain cleaning efficiency Flux Time Time

26 Laboratory and Full-Scale System Fouling behavior can be very different between lab and full-scale RO processes Full-scale RO is less sensitive to initial fouling

27 Effect of Channel Length Short channel has high average flux 2.5x x10-5 Constant average flux does not appear for 1 m The period of constant flux increases with channel length Permeate Flux (m/s) 1.5x x x m 3 m 6 m Fouling cannot be seen in the initial stage x x x x10 1 Membrane Resistance (Pa.s/m) Flux decline is not a good indicator for fouling

28 Flux Controlling Mechanisms 8.0x x Permeate flux (m/s) 4.0x x Thermodynamic 2. Mass transfer 3. Combined Pressure (kpa)

29 Fouling Development Flux F 0 F 2 F 1 a b Pressure P1

30 Effect of Water Fouling Potential Average permeate flux is strongly affected by feed water quality The figure shows: Effectiveness of pretreatment can be assessed by fouling potential Water quality is linked to performance of fullscale RO Average Permeate Flux (m/s) 1x10-5 8x10-6 6x10-6 4x10-6 2x10-6 k-values: [1] Pa s/m 2, [2] Pa s/m 2, [3] Pa s/m 2,[4] Pa s/m 2, [5] Pa s/m 2 [4] [5] Time Period (day) [1] [2] [3]

31 Fouling Characterization Index A effective fouling characterization index can be defined by the following equation: where F L 0 R m I f 1 dx ( x) F 0 F F 0 t F 0 F t : Initial filtration coefficient : Measured filtration coefficient at time t EXAMPLES Case 1: No fouling, F t = F 0, so that I f = 0 Case 2: Most serious fouling, F t = 0, so that I f = 1

32 Effectiveness of Cleaning Protocols Flux F 2 F 0 F 2 F 1 Thermodynamic Equilibrium a d c d e b Pressure P2 P1

33 Configuration Management

34 Performance Enhancement Demo-scale study (16- inch RO system) Modeling of flow distributor using CFD and reverse osmosis process Membrane fouling study

35 Forward Osmosis (FO)

36 FORWARD OSMOSIS (FO) PROCESS Natural phenomenon using osmotic driving force 1.5M (117,000 ppm) Na 2 SO 4 solution 74 bar OP Main advantage: Low pumping energy requirement Estimated energy requirement is ~ 15 28% of the current desalination technologies Concentrated draw solution Diluted draw solution Membrane Cell Draw solution channel Feed solution channel FO MEMBRANE Seawater/Brackish water Concentrated brine

37 FO-MBR CONCEPT

38 FO MBR : LAB SCALE SYSTEM

39 NORMALIZED FLUX A FOULING INDICATOR 0.25 water flux (Lm 2 h 1 bar 1 ) d MCRT 5 d MCRT 10 d MCRT Time (day) Normalized water flux indicated insignificant flux decline, flux decline by fouling was minimal. 3 MCRTs normalized water flux were similar fouling similar

40 NF PERMEATE QUALITY MCRT TOC COD TDS TN NO - 3 -N (day) (mg/l) (mg/l) (mg/l) (mg/l) (mg/l) 3 < ± ± ± ± < ± ± ± ± < ± ± ± ± 10.5 TOC and COD removal above 97.6% for all MCRTs studied. High TN (NO 3 N) in permeates suggests requirement to include anoxic mode in FO MBR operation.

41 Water Reclamation Capacitive Deionization (CDI) Process

42 RO Reject Treatment & Recovery Cost effective technology in treatment and recovery Reduce brine volume for handling and disposal Meet regulatory requirements Technology for RO reject treatment & recovery needs to address two major pollutants in RO reject: 1. Recalcitrant organics 2. Salts retained by RO membrane

43 RO Reject Treatment & Recovery Treated effluent MF/UF NEWater Factory RO UV NEWater 75% to 95% 25% to 5% RO Reject Harnessing more water with RO reject treatment

44 Pilot Scale RO reject Pilot-Scale Study treatment & recovery system Stage 1 Stage 2 RO Reject BAC Column CDI Treated RO Brine or Disposal BAC was able to achieve ~ 24% TOC removal from RO brine. Capacitive Deionization (CDI) process was able to generate a product water more than 80% ions removal. Additional breakdown of recalcitrant organics using ozone increased removal with subsequent BAC by 3 times. Ozone-BAC pretreatment has the potential of reducing fouling in the CDI process. Removal of recalcitrant organics Removal of salts

45 Pilot CDI Unit Description Power source Flow rate 230 V AC, 50Hz,9 Amps Up to 4,800 L/d CDI cell Electrode surface area Power supply 20 m 2 (2 cells, each 10 m 2 ) 2.58 VDC Power consumption is estimated at 0.85 kwh/m 3 Lower than the target of 1 kwh/m 3 computed based on a pressuredriven membrane process

46 Water Quality (BAC Pretreatment) Parameter Water quality RO brine BAC effluent CDI effluent CDI permeate Conductivity (ms/cm) TDS (mg/l) TOC (mg/l) <0.1 COD (mg/l) <2 - SiO 2 (m/l) Anions (mg/l Cl NO PO <0.08 SO Cations (mg/l) Na K Mg <0.027 Ca

47 A Search for Energy Efficient Technologies

48 Singapore s National Research Foundation - Environment and Water Industry (NRF-EWI) Roadmap includes: Water Reclamation Systems Energy Self-sufficiency in Wastewater Treatment - To reduce the energy consumption in municipal wastewater treatment by 80% or less than 0.1 kwh/m 3 Seawater Desalination To achieve System energy efficient desalination system < 0.75 kwh/m 3

49 Thank you

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