industrial waste water ikea application example turkey
TRANSCRIPT
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Application example:Application example:
INDUSTRIAL WASTE WATER REINDUSTRIAL WASTE WATER RE --USEUSE
MEMBRANA GmbHWuppertal, GermanyNorbert Selzer
www.liqui-flux.com
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Content
Introduction of MembranaIntroduction of Membrana
Initial position of the ProjectInitial position of the ProjectPilot trialsPilot trials
Plant designPlant designOperating experienceOperating experience
Summary and previewSummary and preview
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ENERGY STORAGE
Ion Exchange Membranes
TRANSPORTATION& INDUSTRIAL
Lead acid batteryseparators
Polypore separator
ELECTRONICS
Rechargeable andDisposablelithium batteryseparators
SEPARATIONS MEDIA
High Performance Filtration
HEALTHCARE
- Hemodialysis- Plasmapheresis- Blood
oxygenation
INDUSTRIAL& SPECIALTY
- Liquid filtration- Degasification- Gasification- Debubbling
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Membranas core business
Dialysis membranes Oxygenation membranes
Membrane Contactors Filtration Modules
H e al
t h c ar e
I n d u s t r i a
l S e p ar a
t i onFlat sheet membranes
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Part of Polypore-Group since 2002
Plant in Wuppertal, Obernburg(Germany) and Charlotte,North Carolina (USA)
Leading manufacturer ofmembranes for medical andindustrial application
~ 480 employees
Turnover > 100 Mio /a
Start of dialysis membraneproduction
Start of CUPROPHAN membraneworldwide leader in dialysis
Start of industrialmembrane (ACCUREL )
J. P. Bemberg, Vereinigte Glanzstoff Fabriken 1925
BU Membrana, Enka Glanzstoff 1960
Enka Glanzstoff 1950
BU Membrana, Akzo 1988
History and status:
Start ofMicroPES -membrane
Introduction of UltraPEScapillary membrane
J.P. Bemberg 1792
Membrana GmbH, Polypore 2002
Product launchLiqui-Flux
1965
1974
2000
1980
1995
2005
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Initial situation of the Project
200 - 500Alkalinity [mg/l]
7-30Temperature [C]
300-650Color [Co-Pt]
1200-2800Conductivity [S/cm]
400-800CSB [mg/l]
500-750TSS [mg/l]
RangeParameterMix of waste water
from open sewer,
with sewage from
chemical, metal and
textile industry.
In winter diluted by rainwater.
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Existing Waste Water Treatment Plant
Incl. tertiary treatment: Precipitation/Flocculation/Sedimentation/Sand filter
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Clean water quality
After existing WWTP
7,1-7,8pH
7-30
10-60
1200-2800
20-60
8-30
2-10
Range
Temperature [C]
Color [Co-Pt]
Conductivity [S/cm]
CSB [mg/l]
TSS [mg/l]
Turbidity [NTU]
Parameter
7-8pH
-Temperature [C]
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Pilot trials in 2 phases
Mechanicalcleaning
Biological cleaning Chemical treatmentSand filter
Pilot Chemical Treatment
UF Pilot system
Pilot RO
Phase APhase B
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> 12 barBurst Pressure
1,25 / 0,8 mmOuter / Inner Diameter
80 kDaNominal Cut-off
PolyethersulfoneMembrane Material
Hollow Fiber, Inside - OutMembrane Type
Membrane Characteristics
UltraPES Membrane
Cross-section of the 3-layer structure
SeparationlayerSupport layer
Protectivelayer
MultifiberP.E.T. Technology
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1-13pH-Range During Cleaning
40 CMax. Working Temperature
4 barMax. Working Pressure
61 m 2Membrane Surface Area
135 kgWeight Filled With Liquid
40 kgShipping Weight
Victaulic (76.1 mm)ConnectorsEPDM, O-RingSealing Material
PolyurethanePotting Material
Glass Fiber Reinforced PlasticHousing Material
Liqui-Flux UF Module W02
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Pilot system in the field
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Phase A: Start of pilot trial
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Pilot trial - waste water Turkey 90 lmh; BW every 59 min; PAC 0,5 mg Al/l; CEB H 2SO 4
0
100
200
300
400
500
600
700
800
900
1000
07.04.2007 09.04.2007 11.04.2007 13.04.2007 15.04.2007 17.04.2007
T M F [ l / h / m / b a r ]
0
1
2
3
4
5
6
7
8
9
10
T u r b
i d i t y
[ N T U ]
Phase A: Stable operation achieved
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Simulation of overdosing in pilot sedimentation - UF 65 lmh; BW every 39 min; PAC 0,5 mg Al/l
0
200
400
600
800
1000
1200
1400
1600
27.08.200700:00
27.08.200712:00
28.08.200700:00
28.08.200712:00
29.08.200700:00
29.08.200712:00
30.08.200700:00
30.08.200712:00
31.08.200700:00
31.08.200712:00
01.09.200700:00
T M F [ l / h m
b a r ]
CEB NaOH + NaOCl,10 min
CEB NaOH + NaOCl,10 min
Phase B: Adjusting with the treatment of the WWTP
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Filtrate quality in pilot trial
RO elements with high packaging ( 28 mil-Spacer )were in stable operation without performance loss for weeks
~0 (detection limit)TSS [mg/l]
10-30COD [mg/l]
22,5SDI-15 [%/min]
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System design of UF&RO
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System design of Ultrafiltration
Feed tank for approx. 30 min (nominal operation)Dosing of coagulant and dynamic mixer
Coagulation pipe (inside feed tank) forapprox. 60 sec residence time
7 feed pumps for 7 UF-racks
Sieve basket filter, 200m, automatic backwash,synchronized with UF backwash
7 UF-Racks each with 76 modules , 4636 mmembrane surface per rack
Backwash with UF-filtrateCEB with RO-permeate
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From August until September 2007 the 7 UF and RO racks were started one afteranother, one UF rack then one RO rack and so on.
At this point in time a good basis from the piloting was available to increase the fluxof the UF up to the scheduled value of 75 l/h/m within a few weeks. At the beginningthe backwash interval was adjusted to 30 minutes and in several steps increased to60 minutes. Transmembrane pressure (tmp) during filtration stayed below 0.2 bar(2.9 psi).
The chemical enhanced backwash was adjusted several times to fit to the raw waterquality. The standard procedure now is cleaning with NaOH at pH >12 with additionof 200ppm chlorine. After a backwash an acid step at pH 2 for rinsing out the causticfollows.
During the start-up it was examined by sampling that all modules get the sameconcentration of chemicals.
Operating experience I
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Two events during the last 3 years required special activities.
In December 2007 the performance of the biological treatment in the WWTPdecreased and also a part of sludge came into the feed to the UF. Within a shorttime the tmp increased to 0.8 bar and the system was stopped automatically.Several backwashing steps could recover the flux only partially. Therefore thecaustic CEB was done two times at pH of 12.5 with a soaking time of 20 minutes,which increased permeability to >500 l/h/m.
One year later, around New Year 2008/2009 an increase of the tmp took placeduring several weeks until 0.6-0.7 bar were reached. The caustic CEB did not workwell. After checking the water analyses from the WWTP, which is done regularly bythe operating company, high values of metals (Al, Mn, 0.4-0.5 ppm) were obvious. ACIP with citric acid for 1h at 38C recovered the flux to a value in the range of thestart value.
Operating experience II
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During 9 of 12 month in a year one CEB per day is satisfying. In case of highcontamination in the raw water the operator switches the CEB to every 12h and insingle cases to every 8h.
The filtrate quality is checked continuously regarding SDI-15 (
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Summary and previewSummary and previewBy the combination of Inline-coagulation, Ultrafiltration and Reverse osmosis asystem design has been installed which works safely and economically despite thechanging load in the waste water from the different industrial companies.
The used Ultrafiltration membranes have been demonstrating their suitability by alow fouling tendency and favorable cleaning properties.
In combination with a sophisticated module and system design, and an operationadapted to the local situation, this process system obtains central importance inindustrial waste water recycling.
Alternatively to the pre-treatment from the existing system in this project(sedimentation, gravel filter) for new systems, depending on the load of the water,other process steps like flotation and sieve filter should be tested and considered.
UF system costs may be reduced by usage of modules with increased membrane
surface: 75sqm