MBR basics have not changed in the last 10 years but the industry landscape is nearly unrecognizable. With so many manufacturers flooding the market what will 2025 look like?
9. Hydraulics, hydrodynamics & fouling/clogging
• All interlinked:
• increasing flux increases fouling/clogging
• increasing crossflow (promoting turbulence)
increases flux – but increases energy demand
• Fouling also determined by:
• biomass characteristics
• This is in turn influenced by
• feedwater quality
• retention times (hydraulic and solids)
• Key design parameter is
• critical/ sustainable flux
• There is a limit to how far the design flux can be
pushed
14. Membrane pore size trends
• The seven PES membranes are offered exclusively
as FS and are all 150 kDa rated (~0.03 µm)
• The two PE FS membranes are 0.4 µm and
hydrophilicised (by chemical oxidation)
• The PP membranes are offered exclusively as HF
and have various pore sizes
• The PVDF membranes cover a pore sizes of 0.01-0.4
µm and a range of HF diameters
• Ceramic FS membranes are offered predominantly in
the 0.1-0.5 µm range
16. Flat sheet MBR membrane panels:
• all vertically-oriented
• almost all rectangular in shape
• 1-1.5 m in height
• 0.4-1 m in width
• separated by 6-9 mm
• single permeate extraction point
Membrane module dimensions:
FS panels
19. HF modules and
cassettes
Hollow fibre MBR membranes are almost all:
•vertically-oriented
•outside diameter 0.4-2.8mm
•predominantly PVDF
•around 2 m high
20. MBR system suppliers
FS
• Ovivo
• ADI
• Busse
• Kruger
• Smith and Loveless
• Sanitherm
• Wigen
• Hitachi
• Memcon
HF
• Layne
• Aquabio
• Berghof
• Dynatec
• Triqua
• Wehrle
MT
23. Process components
Category Component(s) ID Description/purpose
Tanks Raw water T1 Storage tank for inlet wastewater
Primary sedimentation T2 Removal of gross, settleable solids
Equalisation (EQ) T3 Equalisation of flow
Anoxic (Ax) T4 Denitrification
Aeration (Ae) T5 Nitrification and biological oxidation
Membrane T6 Membrane separation
Treated water T7 Storage of permeate water
Sludge T8 Storage of wasted sludge
Chemicals storage T9,10
Pumps Settled sludge transfer P1 Submerged, settled sludge to sludge storage
tank
Feed P2 EQ tank through rotary screen
Permeate P3 Self-priming, membrane suction filtration
Sludge return/discharge P4 Submerged, sludge recirculation and excess
Sludge transfer P5 WAS to dewatering
Chemicals P6,7 Cleaning chemicals transfer to membrane, x2
Blower Process B1 Biological process aeration
Membrane B2 Membrane scouring
Mixer EQ tank mixer X1 High speed, equalisation tank
Ax tank mixer X2 Low speed, anoxic tank
Screen Rotary screen S1 Fine screening of feed
Membrane Membrane module M1 FS membrane plus frame with built-in aerator
Diffusers Fine bubble diffuser D1 Process aeration
Coarse bubble diffuser D2 Membrane aeration
32. Capital cost
Young et al, 2012
• MBR CAPEX lower
for enhanced
nutrient removal
and water reuse
applications
• Result is the same
for cold climates,
warm climates,
with primary
clarification, and
for plants with
high peaking
factors
TSS < 20
BOD < 20
NH3-N < 1
Temp
12°C
Peak 2X
Case 1 &
TN < 10
TSS < 10
BOD < 10
NH3-N < 1
TN < 10
TP < 0.2
Temp 12°C
Peak 2X
Case 3
with
Primary
Clarifier
Case 3
with
Tmin 25°C
Case 3
with
Peak 4X
Case 1 Case 2 Case 3 Case 4 Case 5 Case 6
by kind permission of GE
36. Specific energy demand, Japan
Itokawa et al, 2014 (Japanese Sewage Works Agency)
0
1
2
3
4
5
6
7
8
9
10
0 10 20 30 40 50 60 70 80 90 100
Inflow/capacity ratio [%]
Specificenergyconsumption[kWh/m3
]
Moryama
intermittent
operation
37. Moryama plant, JSWA
Itokawa et al, 2011*
• System configuration
• UCT process with FS membrane units submerged in the aerobic tank.
• Several energy saving measures incorporated.
*Original figure taken from “Guidelines for Introducing Membrane, Technology in Sewage Works: The 2nd Edition”, MLIT, 2011.
Membrane units for
large-scale MBRs.
Siphon
filtration
Air-lift pumps for
internal circulation.
Low speed mixers.
40. Operating cost
Young et al, 2013
• MBR OPEX is
higher for all
cases
• Differences mostly
attributed to
power, chemical,
and membrane
replacement
• Membrane
replacement is
responsible for a
relatively small
portion of the NPV
TSS < 20
BOD < 20
NH3-N < 1
Temp
12°C
Peak 2X
Case 1 &
TN < 10
TSS < 10
BOD < 10
NH3-N < 1
TN < 10
TP < 0.2
Temp 12°C
Peak 2X
Case 3
with
Primary
Clarifier
Case 3
with
Tmin 25°C
Case 3
with
Peak 4X
Case 1 Case 2 Case 3 Case 4 Case 5 Case 6
by kind permission of GE
41. Life cycle cost (CAPEX + OPEX)
Young et al, 2013
• Life cycle cost is
lower for MBR
compared to
CAS for
enhanced
nutrient removal
and water reuse
applications
• Lower CAPEX
for MBR is off-
set by higher
OPEX
TSS < 20
BOD < 20
NH3-N < 1
Temp
12°C
Peak 2X
Case 1 &
TN < 10
TSS < 10
BOD < 10
NH3-N < 1
TN < 10
TP < 0.2
Temp 12°C
Peak 2X
Case 3
with
Primary
Clarifier
Case 3
with
Tmin 25°C
Case 3
with
Peak 4X
Case 1 Case 2 Case 3 Case 4 Case 5 Case 6
by kind permission of GE
43. Costs: summary
• MBR can be more cost-effective than CAS
depending on design and treated water quality
required.
• MBR is more cost-effective than CAS when tertiary
treatment with membranes is required.
• Cost breakdown, based on same effluent WQ for
published studies:
• OPEX higher for MBR
• this isn’t always necessarily the case
• CAPEX lower for MBR
• Lower life cycle costs
• CAS usually more cost-effective than MBR if
tertiary treatment is not required, depending on
design
• Critical membrane life for cost neutrality for NPV
analysis
4
3GE Water & Process
Technologies
44.
45. The MBR Survey (186 responses)
• Q1What is the main technical problem that prevents
MBRs working as they should?
16%
16%
12%
11%
10%
8%
8%
6%
5%
4% 4% Screening/pre-treatment
Membrane surface fouling
Operator knowledge
Energy demand
Membrane/aerator clogging
Sludge/mixed liquor quality
Membrane chemical cleaning
Overloading/under-design
Uneven aeration
Other/Comments
Automation/control, or software
46. The MBR Survey (186 responses)
• Q1What is the main technical problem that prevents
MBRs working as they should?
16%
10%
6%16%
4%8%
11%
12%
8%
5%4%
Screening/pre-treatment
Membrane/aerator clogging
Overloading/under-design
Membrane surface fouling
Automation/control, or software
Membrane chemical cleaning
Energy demand
48. The MBR Survey, Q2
• Q2 How will
MBR technology
develop in the
future?
48
32
27
17
16
14
13
13
10
10
9
9
8
8
8
6
6
6
5
5
0 5 10 15 20 25 30 35 40 45 50
energy/power
cost
fouling
membrane materials
automation & control
potable/drinking
robustness
awareness/perception/acceptance
nutrient
pretreatment/screening/clogging
49. Survey of 214 plants (Ovivo)
• Electrical 6
• Membrane CIP 12
• Mechanical piping/design 14
• Fine screening 14
• Control valves 26
• Instrumentation 27
• Ancillary equipment 103
• Process condition 111
• Integration and controls 187
possibly membranes related
50. An academic’s view
• Word cloud of keywords of all published MBR wastewater papers,
1990-2009
• Analysis of the SCOPUS database using Wordle
• Common/generic words excluded
51.
52. Past, present ..
THAT WAS THEN: PORLOCK
First municipal MBR (1997)
• 1.9 MLD
Manual aerator flushing
No separate membrane tank
• coarse-bubble aeration only
Up to 14 years membrane
life
>2 kWh/m3 (MBR only)
THIS IS NOW
Bigger plants:
• 9 MBRs of >100 MLD peak
daily flow capacity
Better plants
• Improved membranes and
membrane technology
• Effective pretreatment
• More efficient membrane air
scouring
• Smarter, more holistic design
• <0.5 kWh/m3
53. … and future?
• Further improvements/cost reductions in design and operation:
• Aeration efficiencies improving
• Continued smart design and operation
• automation, real time data capture and processing
• Cinder blocks and ceramic membranes
• Direct potable reuse
• Technically possible and already happening in some places
• Game changers:
• Complete standardisation (as in RO and other crossflow systems)
• Complete energy and resource recovery
• immersed anaerobic MBRs with nutrient removal
Find out more (for free) at www.thembrsite.com