WASTE WATER TREATMENT USING MBRUSING MBR - … -WASTE WATER TREATMENT USING MBR... · WASTE WATER...

WASTE WATER TREATMENT WASTE WATER TREATMENT USING MBRUSING MBRUSING MBRUSING MBR

Peter Brechtelsbauer, Managing Director,

&

Vikrant SarinVikrant Sarin

Huber Tecnology Middle East (FZE), SAIF Zone, Sharjah, UAE

The QualityCompany -Worldwide

, j ,

The HUBERThe HUBERM b Cl BM b Cl B ®®MembraneClearBoxMembraneClearBox®®


New module design – Why?

Experience during the last years:Different standards in different countries regarding geometry and water cosumption (e.g.:geometry and water cosumption (e.g.: USA: low level tanks, high per capita consumption; Sweden: round veryconsumption; Sweden: round, very deep tanks


MembraneClearBox® - Installation Kit

MCB Design Advantages

permeat discharge connection

Holder for float swithes

• no blocking (8 mm plate distance)

• Adapted to different tank sizesVUMmodule

connection

scouring air connection

• homogenous permeate outlet

• Plug in Unit

aeration bl

connection g

• Backwash – Possible

• robust stainless steel designblower connection

robust stainless steel design

• Module + Aeration + Floatswitches = 1 Piece

ipipe aeratorsupplying the

• lower investment cost

• Suitable for up to 500 PE


scouring box

supplying the microorganismswith oxygen

p

Module - Connection Scheme


MCB® – Aggregates/Control Unit

aggregates unit

MCB Aggregates/Control Unit

with control panel

control box incl. monitoring unit permeate outlet,

for discharge or infiltration …

Sample taking valve

scouring blower

flow meter with limit

contact

aeration

contact

aeration blower

permeatepump


MCB-Control Unit

Start-up menu for easy and fast setting of plant parametersEl t i l ti j lElectronical operation journal

Client dataParametersParametersOperating hoursFault signalingOperating mode

PC-interface for automatic data logging of key plant data G hi l l i f ti j lGraphical analysis of operation journalBattery backed alarm system

optical


opticalacoustical

Optional remote control with automatic fault signaling (e.g. via SMS)

HUBER Membrane ClearBox®

For any installation situation

As a retrofit kit:E d i k fi f i iEasy and quick retrofit of existing septic tanks, whether angular or round, irrespective of the tank , pshape.

For installation into new tanks:The equipment can also be installed into new tanks or supplied pre-assembled with


supplied pre assembled witha tank (plastic or concrete).

Advantages of Huber MCB module design

The module combines for the first time the advantages of submerged hollow fiber and flat modulesHigh packing density due to self-supporting

b h tmembrane sheetsOptimal plate distanceResistant to clogging e.g. with hairs and fibers or sludgeor sludgeCompact, space-saving, robust stainless steel designReady to plug in unit for quick and easyReady to plug in unit for quick and easy installationGeometry is adapted to all standard septic tanksseptic tanksEfficient use of surface area by a hydrodynamically optimized designEffective membrane cleaning with permeate


Effective membrane cleaning with permeate possible

Membrane technology for any connection size

HUBER MembraneClearBoxHUBER MembraneClearBoxfor up to 50 PESmall wastewater treatment plantf i di id l hfor individual houses

HUBER MembraneClarBoxHUBER MembraneClarBoxfor up to 500 PESmall wastewater treatment plant fori di id l h di t i t d h l tindividual houses, districts and hamlets. The modular design allows adaptation on almost every plant size.

HUBER VRM technologyFor any flow rate from small to


For any flow rate, from small to very big wastewater treatment plants

HUBER TECHNOLGY COHUBER TECHNOLGY CO--OPERATION WITHOPERATION WITHHUBER TECHNOLGY COHUBER TECHNOLGY CO OPERATION WITH OPERATION WITH UNIVERSITIESUNIVERSITIES

H b T h l R h & D l t WiH b T h l R h & D l t WiHuber Technology, Reserch & Devlopment WingHuber Technology, Reserch & Devlopment Wing ––In coIn co--operation with the following institutes in operation with the following institutes in --

GERMANYGERMANY

11. University of Berlin.. University of Berlin.22. University of Applied Sciences, Amberg, Sulzbach.. University of Applied Sciences, Amberg, Sulzbach.y pp , g,y pp , g,33. University of Karlrlsruhe.. University of Karlrlsruhe.

INDIAINDIA11. Indian Institute of Technology, Mumbai.. Indian Institute of Technology, Mumbai.


22. Indian Institute of Technology, Delhi.. Indian Institute of Technology, Delhi.

Various factors involved for optimization design Various factors involved for optimization design

conditionsconditions

Optimum Operational Cost – Cost estimation of Sludge Treatment & Aeration and determination of MLSS & corresponding HRT.

Prediction of CRITICAL FLUX VALUE – using CFV model.

FACTORS AFFECTING CFV -

- MLSS determined from optimized sludge treatment vs.MLSS determined from optimized sludge treatment vs. aeration.

- Activated Sludge Properties.- Air Sparging – Size of bubble and its cross flow velocity- Air Sparging – Size of bubble and its cross flow velocity.- Membrane Material and Module configuration.- Cleaning Regime.


Algorithm for optimization of design conditions Algorithm for optimization of design conditions g p gg p gfor MBRfor MBR

Influent Parameters, COD, Amm Nitrogen, pH TSS Type of effluent Temp etc

Determination of MLSS build up Against diff HRT

MLSS

Membrane material

pH, TSS, Type of effluent, Temp etc

build up Against diff HRT yielding SRT, Yobs etc

Sludge productionC f Sl d Di l

SOTE, η

Membrane material,Module configuration

Plate & Frame, Hollow Fibre,Tubular, etc

- Cost of Sludge Disposal

AerationRequirement

-Cost of AerationOPTIMIZED

Identification of ASPMlSS, PSD, EPS, Soluble

Microbial Products, R Hydrophobicity,D Viscosity, SS, Zeta potential on

MLSS, HRT, SRT, Yobs, etc

CRITCAL FLUXVALUE, MODEL

membrane fouling

AIR Scouring,Size of bubble,

Scouring VelocityVALUE, MODEL Scouring Velocity

OPTIMIZED MBR DESIGN CONDITIONSMLSS, SRT, HRT, AERATION LOAD,

Cleaning Regime


REACTOR TANK SIZE, CFV, MEMBRANE SURFACE AREA, TMP, CLEANING REGIME,

TREATED EFFLUENT PARAMETER

Determination of MLSS build upDetermination of MLSS build upDetermination of MLSS build up Determination of MLSS build up against various HRT & timeagainst various HRT & time

Determination of MLSS build up against various HRT & time



• Microbial growth is expressed by Monod equation, and the endogenous respiration,by first-order kinetic equation.

d /dt (( S ) / (K + S ) ) k (1)dx /dt = ((µmSe) / (Ks + Se) ) x - kd .x

• Balance of organic substrate consumed by microorganisms and that discharged i h ffl

(1)

with effluent.

dSe /dt = (Q/V) (Si – Se) – (1/Y)((µm.Se)/(Ks + Se)) .x (2)

Where µm, is a maximum specific growth rate, day-1, Ks is half saturation constant, mg/L-1, kd is a endogenous decay Constant, day-1, Se is substrate constant in mixed liquor mg/L-1, x is an MLSS in bioreactor, mg/L-1, t is time in daysV is aeration tank volume, m3, Q is influent flow rate L day-1



• Time Curve of Sludge concentration in theconcentration in the reactor as a function of HRT


Determination of SRT YobsDetermination of SRT, Yobs against various HRT & target

MLSSMLSSThe SRT and the observed yield coefficient, Yobs are expressed as

SRT = x / (dx/dt) x= xtarget Yobs = (V (dx/dt) x= xtarget) / (Q.Si)

•SRT and observed yield ycoefficient, Yobs are functions of HRT and target MLSS iMLSS in bioreactor


Sludge Production in MBRSludge Production in MBR

Total Sludge Cake production rate when MLSS is target value in MBR

Є – Water content in the cake.X – Total cake production rate.

• Amount of cake production as function of HRT and Target MLSS

• Water content of the cake has been assumed to be 0.8


A ti R i tA ti R i tAeration RequirementAeration Requirement

Total oxygen consumption rate

• First term on the right side describes the COD balance between influent and effluent.

• Second term describes the amount of COD converted to biomass

.O d O / dt (Q/V) (S S ) β (dx/dt)

Where β is a conversion factor of biomass to CODO2 = d O2 / dt = (Q/V) .(Si - Se) - β.(dx/dt) factor of biomass to COD.

• Aeration requirement (Qair) is calculated from the oxygen consumption rate O2 considering thespecific oxygen transfer efficiency (η) and reactor depth as (m).specific oxygen transfer efficiency (η) and reactor depth as (m).

.Qair = O2 / (4.0 * η.m)

• The power requirement, P P = 0.7 * (Qair )


Aeration RequirementAeration RequirementAeration RequirementAeration Requirement

• Oxygen requirement during Waste Water Treatment as a function of HRT and Target MLSS

• In MBR process, sludge production is suppressed by long HRT and/or highby long HRT and/or high MLSS.

• Along the sludge reduction, more oxygen is needed to oxidize the

i t i lorganic materials contained in wastewater.


Aeration RequirementAeration Requirement

Relationship between MLSS and SOTE is as follows

η = 9.00 – 8.63 * 10-4 MLSS + 2.56 * 10-8 * MLSS 2

• With increase in MLSS SOTE reduces and requirement of Dissolvedrequirement of Dissolved oxygen by increased MLSS increases.


Aeration Requirement

• Aeration Demand for biodegradation of organic matter as gfunction of target MLSS and HRT.


P ti f ti t d l d ff tiP ti f ti t d l d ff tiProperties of activated sludge affecting Properties of activated sludge affecting membrane foulingmembrane foulinggg

Activated sludge properties varies - With different types ofsubstrates present in the effluent.

Membrane fouling is influenced by the activated sludge properties -

• The mixed liquid of suspended solids (MLSS) concentration.• Sludge particle size distribution (PSD).• Extra cellular polymeric substances (EPS).p y ( )• Soluble microbial products (SMP).• Suspended solids in supernatant (SSs).• Dynamic viscosity (μ),

Relative hydrophobicity (RH)• Relative hydrophobicity (RH).• Zeta potential


P ti f ti t d l d ff tiP ti f ti t d l d ff tiProperties of activated sludge affecting Properties of activated sludge affecting membrane foulingmembrane foulinggg

Influence of – MLSS concentration, Particle size Distribution & EPS on the fouling resistance value RFEPS on the fouling resistance value RF

Rf = 2.250 eMLSS × 9 × 10−5 + 0.111 EPS + 1.99 × 10−2 PSD − 3.201

Unit of Rf , MLSS, EPS and PSD are 1011 m−1 mg/LPSD are 10 m , mg/L,mg/g MLSS and m, respectively.


Relationship between membrane fouling factors and membrane fouling resistance.

Critical Flux ModelCritical Flux ModelCritical Flux ModelCritical Flux Model

Change of filtration area• Change of filtration area and permeate local flux and consequences on fouling mechanismfouling mechanism.


Critical Flux ModelCritical Flux Model

The initial porous environment is comparable to a set of homogeneous pores np defined by astraight section Sp and a length Zp. Permeate flow expressed as Q, whose value is heldconstant throughout the operation, may be expressed in function of the flow rate Jp through theg p , y p p gpore, as the following relationship:

Q = J n p SI st Case (1)Q = J p.n p. S pI st Case (1)

At a sub-critical flux and during period 1, fouling is assumed to be due to different types ofsoluble particle membrane interaction Thus it is assumed that the mass of particles msoluble particle–membrane interaction. Thus it is assumed that the mass of particles minteracting at each moment with the membrane material and susceptible to being retained inthe pores is proportionate to the flow of matter through the membrane, where

II nd Case dm /dt = k 1. C solutes .Q (2)



The instantaneous variation in the number of open pores n p is taken as directlyproportionate to the mass of particles interacting with the membrane material and/orThe instantaneous variation in the number of open pores n p is taken as directlyproportionate to the mass of particles interacting with the membrane material and/ordeposited at moment t in a pore, wheredeposited at moment t in a pore, where

dn p/dt = −k2 m (3)III rd Case

k k constant in proportionality

ΔP = µRp Jp (4)

k1, k2 constant in proportionality

d(ΔP)/dt = µRp (d(Jp) / dt)

d(ΔP)/d ΔP 2

(5)

(6)

Variation in the number of open pores np over time induces instantaneous variations of Jp and P such that

where taking account of Eqs. (1)–(5): d(ΔP)/dt =α ΔP 2 t (6)

(7)α = (k1k2SpCsolutes/μRp) (LM−1) Where α is


μ is permeate viscosity Rp open pore hydraulic resistance


In fixed biological conditions (defined sludge age and

ΔP = ΔP0 / (1 − ((α ΔP0t 2)/2)) (8)hydraulic retention time), Csolutes

may be considered constant and this equation easily integrated as

Jp =J p0 / (1 − ((αJp0 μRpt 2)/2)) (9)p p0 ( (( p0 μ p ) ))

(10)Initial J value defined J p0 =Q/A (10)Initial Jp0 value definedsuch as

J p0 Q/A


HUBER Membrane TechnologyHUBER Membrane TechnologyHUBER Membrane Technology Products

VacuumRotationMembrane (VRM®)

Permeate discharge, additional pump or hydrostatic submersion


y

VRM membrane moduleScouring air intake

29

HUBER Membrane TechnologyHUBER Membrane Technology

Advantage of HUBER VRM, Rotary Module.

• Rotation of module reduces the concentration of solute on the membrane surface

• Optimized and equalized sco ring effect of the s rfacescouring effect of the surface of membrane.


HUBER Membrane TechnologyHUBER Membrane Technology Products

HUBER Membrane Technology

VRM 20 (for installation into concrete tanks)Drive motorDrive motor

Permeate discharge Scouring air lines

Support frame

The QualityCompany -Worldwide31

Membrane module (only one element shown here)


VRM Test Plant on WWTP Berching

Newly developed and patented permeate discharge systempermeate discharge system

New permeate collector,New permeate collector, increased throughput



Drive Scouring air ti

VRM 30

connection

Newly developed and patented permeate discharge system

Membrane module


Support frame33

HUBER Membrane TechnologyHUBER Membrane Technology Products

HUBER Membrane Technology

Specific data

Membrane filtration in industrial and municipal membranebioreactors (industrial after prior piloting!)Diameter of filtration units: 2 3m (VRM 20) 3 2 (VRM 30)Diameter of filtration units: 2.3m (VRM 20), 3.2 (VRM 30)Membrane area: up to 2880 m² per unitThroughput: up to 50 m³/h (cont.) or 90 m³/h (peak) per unitThroughput: up to 50 m /h (cont.) or 90 m /h (peak) per unitPeak flows of up to 60 lmh with an optimal biological systemFor installation into filtration chambers or directly into aeration tanksyMinimum tank depth: 2.7 m (VRM 20), 3.7 m (VRM 30)



VRM ceramic journal bearing

ADVANTAGES

High-strength ceramic bearingGlued on and polished ceramic platespVery good sliding properties

Minimised power consumptionR d d l lifReduced wear, long lifeAlso suitable for very abrasive media



VRM permeate collectorADVANTAGESADVANTAGES

Reduced pressure losses com-pared to the FESTO distributorpared to the FESTO distributor Higher throughputs(high flux up to 80 lmh)Easier and faster to mountEasier and faster to mountLower price Reduces the total membrane price

collector unitPlastic hose liner

collection hose Use of standard fabric hoses


collector unit

37


VRM permeate bearing and permeate discharge

ADVANTAGES

No permeate contamination The shaft can be emptiedThe shaft can be emptied

Automatic lubrication of the ball bearingSealing liquid on the permeate side for detection of leaksThe only wear parts are:The only wear parts are:sealings (approx. 2 years life)bearing (> 5 years life)

low life time costsThe QualityCompany -Worldwide38

low life-time costs


Further developments – Outlook

Tests with new membrane materialswhich can dry outfor higher continuous fluxesfor higher continuous fluxes

Development of new cleaning strategies Reduction of scouring air Energetic optimisationInternal chemical purification without evacuating the filtration chamber

Relation between biological performance and membrane filtrationusage of scouring air for biological removalsmaller tanks, higher sludge load, reduction of chemical cleaningslimitation of the system


limitation of the system

39


Compact MBR System BioMem® (here: filtration tank)

VRM Unit InletReturn

Permeate outlet

Permeate pump

Drive

Outlet

Stainless steel filtration tank

Scouring air blower

Return


In combination with the customer‘s biological systemAlternative: supply of a biological tank 40


Compact BioMem® Plant


BioMem® Plant for an administration building, Iran


Filtration plant in combination with the customer‘s aeration plant

Compact BioMem® Plant

Filtration plant in combination with the customer s aeration plant(max. 15 m³/h per unit)

The dry installed filtration tanks are fed with activated sludge from the end of the wastewater treatment process.Perfect dimensioning of the aeration tank required!!

Complete system with bio tank and filtration tank for up toComplete system with bio-tank and filtration tank for up to max. 82 m³/d

All VRM 20 sizes available as VRM Compact BioMem PlantsAll VRM 20 sizes available as VRM Compact BioMem Plants.Overloaded existing plants can be retrofitted.

Secondary clarifier shutdown Replaced by filtration chamber


Aeration tank operation with increased biomass concentration Increased capacity of existing plants

42


Projects



HUBER Membrane Technology Products

20.000 PE, WWTP in North Spain

Projects

Supply of preliminary treatment equipment, sludge treatment equipment, membrane filtrationMunicipal WWTP, Qd = 4000 m³/d (Qmax = 417 m³/h)Discharge into a river, downstream drinking water intake structure Supply of 4 nos. VRM 30/440 filtration units (membrane surface: 10.560 m²)( )Delivery date: week 46/2005Start-up date: July 2006

®Compact BioMem® Plant Compact ww treatment plant in two tanksFor an administration building (2000 PE) in Teheran/Iran


For an administration building (2000 PE) in Teheran/IranDelivery date: October 2005Start-up date: April 2005 44



Reference Installations

MunicipalMunicipalKnautnaundorf/Germany: in operation since 03/2002Schwägalp/Switzerland: in operation since 04/2002Ankara/Turkey: in operation since 03/2005La Santa/Spain: delivered 12/2004 (start-up 2006)NIOC/Teheran/Iran: delivered 10/2005 (start up 2006)NIOC/Teheran/Iran: delivered 10/2005 (start-up 2006)Arenas de Iguna/Spain: delivered 12/2005 (start-up 2006)

IndustrialRaisio/Veurne/Belgium: in operation since 04/2004TBA/L /S it l d d li d 06/2006 ( t t 2006)


TBA/Lyss/Switzerland: delivered 06/2006 (start-up 2006)



Successful pilot plant installationsMunicipalMunicipal

Cairo/Egypt (2003)Gran Canaria and Teneriffa/Spain (2004) Order “La Santa“University of Warsaw/Poland (2005)University of Warsaw/Poland (2005)Singapore (2005/2006)Greensboro/USA (2003)Hawaii/USA (2004)San Diego/USA (2005/2006) Title 22 – certificationTrento/Italy (2005/2006)y ( )

IndustrialSlaughterhouse/Germany (2003)B /G (2003)


Brewery/Germany (2003)Paper industry / Syria (2005)Meat processing industry / Germany (2006)


Pilot Plants

5 Pilot plants for demonstration or testing on customers‘ sitesTest plant for industrial applications (MCB)1 Plant with combined filtration/biology for demonstration purposes) 2 New plants with separate filtration/biology (also as a pilot plant)1 New plant according to US standards (presently installed in the US)

The QualityCompany -Worldwide47Pilot plant with 108 m² membrane surface, Q = 30 m³/d

NIOC, TEHRAN

NIOC NEW BUILDING

NIOC OLD BUILDING

NIOC NEW BUILDING


NIOC, TEHRAN

- Complete solution of Mechanical and BiologicalComplete solution of Mechanical and Biological treatment plants according to the latest

International standards.International standards.


NIOC, TEHRAN

Precise control over the biological and acceptable effluent even if in Hydraulic andeffluent even if in Hydraulic and Loading shock in the biological process with High b o og ca p ocess t gQuality Effluent.


NIOC, TEHRAN

NIOC Plant layoutNIOC Plant layout


NIOC, TEHRAN

NIOC BioMem® plant parameters

NIOC Plant

VRM 20/120Membrane Type

360 m2Membrane Area AM

51 m3Aeration Tank Volume VBB

35 m3/hThroughput Qh

120 m3/hScouring air amount Q Scouring

250 m3/hAeration Capacity QAeration

8 14 g/lDS biology


-8 -14 g/lDS biology

NIOC, TEHRAN

Plant start up and operating resultsPlant start-up and operating results

The plant was started up in early May 2006 and run in by feedingThe plant was started up in early May 2006 and run in by feeding the biological system with totally 60 m3 activated sludge from Shahrak-e-Gharb municipal WWTP Which is located in west of

Teheran.starting with a low flux of 10 lmh. Within only a few days the filtration, and thus the total throughput, was increased to the

design throughput of 120 m3/d.

15.5ImhDesign Flux vp, nom

g g p

30ImhPeak Flux vp, max

120m3/dThroughput Qd 120m3/dThroughput Qd

200 -- 250l/(m2*h*bar)Operating permeability LP


15 - -33°CTemperature T

NIOC, TEHRAN

Operating results of membrane filtration

outflowinflowunitparameter

12832mg/lCOD

6290mg/l BOD

<4>1000mg/lTSS

98.6%COD reduction

97.9%BOD reduction

<13MPN Index /100 mlTotal Coliform

<5MPN Index /100 mlFaecal Coliform


NIOC, TEHRAN

- Fewer process stages and Smaller plant footprints


DBU’s German Environmental Award 2006.


DBU’s German Environmental Award 2006.

Federal President Horst Koehler (3rd.f.r.) presented the German Environmental Award of the Deutsche Bundesstiftung Umwelt to Hans G Huber (4th f r )


Bundesstiftung Umwelt to Hans G. Huber (4th.f.r.)

ANY QUERIES, PLEASE?


THANK YOU, FOR YOUR ATTENTION!

SHUKARAN!SHUKARAN!


WASTE WATER TREATMENT USING MBRUSING MBR - … -WASTE WATER TREATMENT USING MBR... · WASTE WATER...

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